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A HANDBOOK
of

PETROLEUM ASPHALT

and

NATURAL GAS

Methods of Analysis, Specifications, Properties, Refining
Processes, Statistics, Tables and Bibliography

by
ROY CROSS

Member of American Chemical Society, American Society for Testing

Materials, American Association for Advancement of Science,

American Society for Municipal Improvements,

Kansas City Engineers Club "^^^

Published as -•'/'/''

BULLETIN NO. i6

I n M J "^ ^ -

by ~^'^-^'^'

KANSAS CITY TESTING LABORATORY
KANSAS CITY, MO.

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Digitized by Ifhe^l^t^Pliet Archive

in 2009 witiT'fQippEl^ng from

University of Toronto

littp://www.arcliive.org/details/liandbookofpetrolOOcros

Preface to Bulletin No. 16.

This handbook includes the following new matter, as well as ad-
dition to and revision of:

Universal gauging tables for horizontal cylindrical tanks.

Gauging tables for the bumped ends of horizontal cylindrical
tanks.

Methods for the determination of the capacity of oil pipe lines.

Detail cost on the refining and cracking of oil.

The laws and taxes governing the sale and transportation of re-
fined petroleum.

The detailed description of the decomposition of petroleum hydro-
carbons in the presence of aluminum chloride.

The most recent specifications for the quality of petroleum prod-
ucts as used by the trade.

Standard method of drilling oil wells.

Detailed and explicit methods of analysis of all types of petro-
leum products giving preference to accepted or standardized methods.

New developments in the decomposition of heavy hydrocarbons
for the production of gasoline.

Formulae for the calculation of the total gasoline obtainable by
any means from crude oil of different gravities and bases.

The properties of crude oils from all of the important fields.

New matter on the uses, properties and value of fuel oil.

Specific gravity and Baume' gravity correction tables for very
light petroleum oils and for very heavy petroleum oils.

Baume' gravity and Specific gravity equivalents for oils heavier
than water, but on the lighter than water scale.

The combustion of gasoline and the products of combustion of
internal combustion engines.

The properties of gasoline made by present methods of decom-
position.

The properties of average gasoline as now sold on the market.

The vapor volumes of petroleum distillates and different tem-
peratures and of different gravities.

Processes and U. S. patents issued to 1922.

The statistics of the production, transportation and refining of
petroleum up to 1922.

Preface to Bulletin No. 15.

The purpose of this publication is to set forth in con-
cise form for the petroleum producer, seller, refiner, and
technolo^st, scientific information and statistics on the
production, properties, handling, refining and methods of
valuation of petroleum and related products.

All matter formerly published in Bulletin No. 14 has
been revised and included in this publication. In addition
there has been added fifty-five new illustrations, complete
temperature — Baume' correction tables, extensive tank
gauging tables, refinery engineering formulae, complete
specifications for petroleum products, much additional data
on oil cracking, geology, lubricants and asphalt, a complete
set of methods of analysis of petroleum, asphalt and natural
gas and a fairly complete bibliography.

The sources of original information have been from the
research, commercial and engineering departments of the
Kansas City Testing Laboratory and from the bibliography
published at the end of the book.

November 1, 1919,
Kansas City, Missouri.

TABLE OF CONTENTS.

(General outline only. See index for detailed subject matter.)

1. Economics of Petroleum 2-112

Uses, statistics, geographical distribution, geology, produc-
tion, prices, depletion of wells, drilling methods.

2. Transportatio-n, Storage and jauging 113-183

Pipe lines, storage losses, tank specifications, fire regula-
tions, tank cars, loading, storage tanks, gauging, measurements.

3. Properties of Crude Petroleum 184-191

General and chemical constitution, distillation properties,
physical properties. Special commercial petroleums.

4. Refining of Petroleum, Including Cracking 192-246

Refinery practice. Refinery designs. Cost of refining.
Chemical nature of cracking. Properties of gasoline and naphtha
made by various processes of decomposition. Aluminum chlo-
ride process. Classification of oil cracking processes. Benton
process. Dewar & Redwood process. Burton process. Cross
process. Cracking and refinery engineering. Calculation of
cracking yields and refinery profits.
•5. Properties of Refined Petroleum 247-310

Gasoline. Benzol. Kerosene. Gas oil. Distillate oil. Straw
oil. Lubricating oil. Grease. Paraffin wax. Transformer oils.
Petroleum. Miscellaneous refined oils. Complete detailed speci-
fications. State laws.

6. Fuel Oil 311-347

Chemical and physical properties. Advantages over other
fuels. Comparison with other fuels. Sampling. Relative costs.
Specifications. Combustion.

7. Oil Shale, Shale Oil and Coal Naphtha 348-366

Occurrence, properties, distillation products, by-product
coal distillation plants, gas manufacturing.

8. Asphalt 367-392

Refining oil for road building and paying purposes. Prop
erties of asphaltic and bituminous materials. Various types of
asphalt pavements with their properties and specifications. Spe-
cifications for brick filler. Asphalt for water-proofing. Road oils.

9. Natural Gas 393-424

Occurrence of natural gas. Production. Prices. Composi-
tion. Manufacture. Gasoline by absorption method. Capacity
of absorption towers. Manufacture of carbon black. Properties
and production of helium. Explosions of natural gas. Measur-
ing the capacity of gas wells. Capacities of gas pipe lines.

10. Methods of Analysis of Petroleum, Asphalt, Natural Gas. .425-519

Standardized and commercial methods.

11. Tables 520-561

Gravity correction tables, temperature correction tables.
Mensuration conversion tables.

12. Bibliography 562-595

Publications and Patents.

13. Index 595-622

BULLETIN NUMBER SIXTEEN OF

PETROLEUM— GENERAL DESCRIPTION OF USES.

The word petroleum has its derivation from the Latin "petra,"
rock, and "oleum," oil. Synonymous terms are mineral oil, rock oil,
crude oil and crude naphtha. In the widest sense, the word embraces
the whole of the hydrocarbons, gases, liquids and solids occurring in
nature. In a commercial or practical sense, the word applies to
natural liquid hydrocarbons, and the term asphalt applies to the solid
forms, such as asphaltum, albertite, elaterite, gilsonite, ozokerite,
glance pitch and hatchettite.

The occurrence of petroleum has been recorded from the earliest
times and has been spoken of as oil springs, burning water and the
like. The first probable exploitation of petroleum in the way of dis-
tillation was by Jas. Young, an Englishman, in 1850. Petroleum
was obtained by well drilling first in 18-58 by E. L. Drake. The
depth of this well was 70 feet and the yield of oil was 25 barrel?
per day.

The original use of petroleum was in the preparation of illumi-
nating oil to replace coal oil. After the production of illuminating
oil from petroleum, it was soon shown that the heavy petroleum oil
had far superior lubricating properties to vegetable and animal fats
and oils so that at the present time, practically all lubricating oils
are obtained from petroleum.

The development of the gasoline engine is due principally to the
need of a commercial outlet for gasoline. Gasoline was originally
used for lighting purposes and domestic stoves. It is now the most
valuable and important product of petroleum, being approached in
value only by that of lubricating oil. There are 10,000,000 gasoline
automobiles in the United States at this time.

The following outlines some of the main uses of petroleum
products:

Gasoline and Naphtha — Gas lighting, laboratory solvents,
cleansing, gasoline stoves, automobiles, extraction of seed oils, metal
polishes, gasoline engines, paint vehicles, asphalt paint and road
binder solvent, refrigerant.

Kerosene and Illuminating Oils — Lamps, distillate engines, sig-
nal lights, gas washing and absorbents, portable stoves.

Gas Oil— Pintsch gas, Blaugas, town gas, straw oil, heating,
cracking, anti-corrosives.

Heavy Distillates — Lubricants, spindle oil, auto oil, machine oil,
engine oil, cylinder oil, greases, vaseline, wax, medicinal oil, water-
proofing for fabrics, candles, soap filler, paints, polishes.

Liquid Residua — Steam fuel, heating, concrete waterproofing,
road and macadam oils, dust prevention, cracking, cylinder oil.

Semi-solid Residua — Asphalt pavement, waterproofing, brick
filler, roofing, rubber filler or substitute.

Crude Oils — Diesel engines, dust prevention, waterproofing,
steam fuel.

The following statistics show the extent of the petroleum indus-
try at this time:

KANSAS CITY TESTING LABORATORY

PETROLEUM IN 1919, 1920 AND 1921.
CRUDE OIL BALANCE SHEET. (U. S.)

1919 1920 1921

Stocks on handJanuary 1st. 117,204,000 123,344,000 133,690,000

Crude oil produced during year . . 377,719,000 443,402,000 472,439,000

Crude oil imported 52,822,000 106,175,000 125,307,000

547,745,000 672,921,000 731,436,000

Stocks on hand December 31st. . . 123,344,000 133,690,000 197,089,000

Crude oil consumed during year. . 418,477,000 531,186,000 525,407,000

Crude oil exported 5,924,000 8,045,000 8,940,000

547,745,000 672,921,000 731,436,000

PRODUCTION BY STATES IN UNITED STATES.

1919 1920 1921

Oklahoma 87,000,000 105,725,700 115,680,000

California 101,564,000 105,668,000 114,900,000

Texas 85,900,000 96,000,000 105,200,000

Kansas 30,000,000 38,501,000 35,750,000

Louisiana 14,853,000 35,649,000 25,835,000

Wyoming 13,000,000 17,071,000 19,550,000

Kentucky 9,346,700 8,680,000 8,975,000

Illinois 10,165,000 10,772,000 10,000,000

Pennsylvania 7,500,000 7,454,000 7,425,000

West Virginia 7,900,000 8,173,000 7,990,000

Ohio 7,300,000 7,412,000 7,275,000

Indiana 9000,00 932,000 1,155,000

New York 890,000 906,000 970,000

Colorado 120,000 110,000 109,000

Arkansas 0,000 0,000 9,850,000

Montana 297,300 348,700 1,775,000

Total 377,719,000 443,400,700 472,439,000

PRODUCTION BY DISTRICTS IN UNITED STATES.

Mid Continent. . ." 115,897,000 144,226,000 258,885,000

California 101,764,000 105,668,000 114,709,000

Central and North Texas 67,419,000 70,952,000 Incl. Midco.

Gulf Coast 20,568,000 26,801,000 34,160,000

Appalachian 29,232,000 30,511,000 30,574,000

North Louisiana 13,575,000 33,896,000 Incl. Midco.

Illinois ■ 12,436,000 10,772,000 10,935,000

Lima-Indiana 3,444,000 3,059,000 2,411,000

Rocky Mountain 13,584,000 17,517,000 20,765,000

Total 377,919,000 443,402,700 472,439,000

BULLETIN NUMBER SIXTEEN OF

*

WORLD'S PRODUCTION OF PETROLEUM.

1919 1920 1921

United States 377,919,000 443,402,700 472,439,000

Mexico 87,359,000 163,039,000 191,418,000

Russia 34,284,000 34,284,000* 34,284,000*

Dutch East Indies 15,780,000 15,780,000* 16,000,000*

India 8,453,000 8,453,000* 8,500,000*

Roumania 6,353,000 7,200,000 7,500,000*

Galicia 6,255,000 6,255,000* 6,000,000*

Trinidad 2,780,000 2,780,000* 3,000,000*

Peru 2,561,000 2,561,000* 3,600,000

Japan 2,120,000 2,120,000* 2,000,000

Germany 1,000,000 1,000,000* 500,000*

Argentina, Egypt, Persia, Canada,

Italy, etc 14,028,000 14,028,000* 17,000,000

Total 558,892,000 700,902,700 762,241,000

*Estimated

PRODUCTS OF PETROLEUM. (U. S.)

1919 1920 1921
Total crude oil consumed

(all purposes) 418,477,000 bbl. 531,186,000 525,407,000

Crude oil refined 361,520,000 bbl. 433,915,000 443,363,000

Gasoline produced 94,210,000 bbl. 116,250,000 120,939,000

Kerosene produced 55,740,000 bbl. 55,240,000 46,300,000

Lubricating oils 20,160,000 bbl. 24,900,000 20,900,000

Gas oil, fuel oils, distillates,

road oils, flux oils 181,540,000 bbl. 246,500,000 230,100,000

Crude oil used for fuel 56,957,000 bbl. 97,271,000 82,044,000

Wax 467,235,000 lb. 541,404,000 433,887,000

Coke 603,460 ton 576,613 604,465

Asphalt 901,885 ton 1,290,614 1,214,536

Losses (cracking, etc.^ 15,000,000 bbl. 18,742,939 11,280,000'

FIELD OPERATIONS.

Wells drilled during the

year 28,512 33,385 21,152

Dry wells or gas 7,833 9,647 5,013

Per cent producing at end

of year 72.54% . 71.10% 76.30%

Producing wells in U. S.

December 31st 239,650 263,388 279,520

Average production per

well per day 4.41 bbl. 4.60 bbl. 4.63

KANSAS CITY TESTING LABORATORY

Geographical Distribution of Petroleum.
(U. S. Geological Survey.)

United States — The oil pools of the United States are grouped
in certain major areas or fields which originally were delimited
according to their geographical position alone. As the fields have
been extended areally, the geographic boundaries of some of them
have become in places less distinct and the gi-ouping has been deter-
mined more and more by commercial usage which in turn is in part
determined by the quality of the oils.

The Appalachian field embraces all the oil pools that lie east
of Central Ohio and north of Alabama, including those of New
York, Pennsylvania, West Virginia, Eastern Ohio, Kentucky and
Tennessee. Most of the strata that yield oil in this field are sand-
stones and conglomerates of Devonian and Carboniferous age. The
typical oils are of paraffin base, are free from asphalt and objection-
able sulphur, and yield by ordinary methods of refining, large per-
centages of gasoline and illuminating oil. They range in color from
black to light amber, but most of them are of some shade of green.
In gravity they range from 25° to 53° Baume' and average about
43° Be'.

The Lima-Indiana field embraces all the pools in Northwestern
Ohio and most of those in Indiana. The oil-bearing beds in this field
belong to the Ordovician, Silurian and Carboniferous systems, but
the most productive are lenses of porous dolomitic rock in the
"Trenton" limestone, a member of the Ordovician system and the old-
est known oil-bearing rock in the United States. The oil obtained
from the Carboniferous rocks in Southwestern Indiana properly
belongs to the Illinois field, next to be considered, for the formations
lie in the same structural basin and the two fields are continuous.
The oil in the pre-Carboniferous rocks of the Lima-Indiana field is
of lower grade than that from the pre-Carboniferous rocks of some
parts of the Appalachian field and contains sulphur compounds that
must be removed by special treatment. In color the oils obtained in
this field range from green to brown and their average gravity is
probably about 39° Baume', although some of them are much heavier.

The principal productive area in the Illinois field is in the south-
eastern part of the state, along the LaSalle anticlinal axis, but there
are also small scattered pools in Central and Western Illinois. Most
of the oil is obtained from beds of sandstone in the Pennsylvania and
Mississippian series of the Carboniferous system. The oils in the
northern part of the field are heavy, have an asphaltic base and
carry sulphur. The oils in the southern part of the field are of
be^'-er grade. In gravity the oils range from 27° to 37° Baume'.

The Mid-Continent field includes the oil-producing area in Kan-
sas, Oklahoma, Northern and Central Texas and Northern Louisiana.
Most of the oil produced in Kansas, Oklahoma and Northern Texas
i i obtained from beds of sandstone in formations of the Pennsyl-
vania series (upper Carboniferous). The oil produced in Southern
Oklahoma is obtained mainly from several pools in beds of sandstone
of the Pennsylvania series, though some oil is found in the "Red
Beds" of the Permian series (latest Carboniferous).

BULLETIN NUMBER SIXTEEN OF

Kjg 1 — .Map of the Tnited States Showing Refineri's. Production
Fields and Main Trunli Pipe Lin-es of Petroleum.

KANSAS CITY TESTING LABORATORY

The oil found in Northern Louisiana and Central Texas is ob-
tained from sandstones or other porous rocks of the Cretaceous and
Tertiary systems. In the Mid-Continent field the oil has accumulated
in anticlines, domes and terraces throughout an extensive region
where the strata have a general westerly dip. The oil grades in ap-
pearance and gravity from the thick, black oil of some of the
Louisiana fields, which have a gravity of 21° Baume', to the almost
colorless product of the so-called "gasoline well" near Cushing, Okla.,
which has a gravity that is reported to be above 55° Baume'. How-
ever, the average oil from the Mid-Continent field is light green and
has a gravity of about 35° Baume'.

The Gulf Coast field includes that part of the Gulf Coastal Plain
of Texas and Louisiana in which petroleum is associated with masses
of rock salt and gypsum in domes. The age of the oil bearing strata
ranges from Ci-etaceous to Quarternary, and the reservoir rock is
generally either sandstone or porous dolomitic limestone. The field
includes a great number of small, scattered pools, few of them more
than three miles in diameter, which produce oil having an asphaltic
base. The productivity of some of the wells is enormous but the pro-
duction of most of the pools soon reaches a maximum and then
steadily declines. The value of some of the oil is impaired by its
high content of sulphur, which may be as much as 2.3 per cent.
The gravity ranges from 15° to 30° Baume', and averages about 22°
Be'. Most of the oil is dark brown to black but some of it is green.
There is no apparent relation between color, gravity and content
of sulphur.

The Rocky Mountain field embraces all areas that produce pe-
troleum in Colorado, Wyoming and Montana as well as some areas
of prospective production in Utah and New Mexico. The petroleum
now obtained in this field is derived from strata of Pennsylvanian,
Permian, Triassic and Cretaceous age. Most of the oils from Paleo-
zoic and Mesozoic strata are dark and heavy with gravities averag-
ing about 23° Baume', although some of them have a gravity as low
as 11° Baume'. The Cretaceous oils are remarkably light in color
and their gravity ranges from 25° to 50° Baume'. "rhe average
gravity for the Rocky Mountain field is about 32° Baume'.

The California oil fields may be roughly divided into two geo-
graphic groups, one occupying two sides of San Joaquin Valley and
commonly knov/n as the Valley fields, and the other occupying a
large area along the coast and commonly known as the Coastal
fields. All the Valley fields, except one, lie on the west side of San
Joaquin Valley and the oil in most of them is obtained from porous
Tertiary sandstones that have been folded into anticlines and syn-
clines. The conditions in the Coastal fields are in many respects
similar to those in the Valley fields, but the structure is much more
varied. A very small part of the oil produced in California is
obtained from Cretaceous formations. The oils range in color from
black to honey-yellow and in gravity from 9.9° to 54° Baume'.
Heavy dark oils that contain little sulphur predominate. A fair
average gravity is about 21° Be'.

BULLETIN NUMBER SIXTEEN OF

FiSJ. -

lap .Sliowin.e Producins- .\rcas an.l Pipe Lines
in the Mid Continent and Gulf Fields.

for retroleum

KANSAS CITY TESTING LABORATORY

Nearly all the petroleum produced in the United States is carried
to refineries through buried pipes. Some pipe lines extend from the
fields in the interior of the country to the Gulf of Mexico and
to the Atlantic seaboai'd for the distances of many hundreds of
miles. The trunk pipe lines, that is, the main lines only, not the
subsidiary branches, now cover moi'e than 34,000 miles.

Canada — Indications of petroleum have been observed in many
parts of Canada but no fields have been much exploited, except
those in Ontario, vv^here the oil occurs in sandstones and limestones
of Silurian and Devonian age. Most of the Ontario oil has a paraf-
fin base but contains large quantities of sulphur. The Calgary
field in Alberta has produced only a small quantity of oil, but a
field in Northern Alberta, where the famous Tar sands of early
Cretaceous age occur, gives promise of commercial production

Mexico — The petroleum fields of Mexico that now seem to promise
the greatest production are in the eastern part of the country in
the Gulf Coastal Plain. There are two fields which are distinct
geographically and geologically and which produce different kinds
of petroleum.

The Tampico — Tuxpan field lies in the northern part of the State
of Vera Cruz and the southern part of the State of Tamaulipas.
In this field indications of oil are found in a region about 250 miles
long and 40 miles wide. The Tehuantepec field forms a similar long,
narrow area which extends along the Gulf coast from southern Vera
Cruz about 200 miles eastward to the eastern limit of Tabasco.

Most of the oil in both fields is found in porous limestone of
Cretaceous or Eocene age but some oil in the Tehuantepec field is
found in later Tertiary rocks. In the Tampico-Tuxpan field, the oil
accumulates either in anticlines or at underground dams formed by
intrusive necks and dikes of igneous rocks by which the oil pushed up
or along by salt water has been impounded. In the Tehuantepec field,
the oil is associated with rock salt and gypsum in domes similar to the
domes in the Coastal Plain of Texas and Louisiana. The oil gener-
ally becomes lighter from north to south through the two fields but
nearly all of it should be classed as heavy. Its gravity ranges from
about 10' to 43° Baume'.

Pronounced indications of oil are reported in western Mexico but
no development has yet been undertaken there.

Mexico, which has furnished the largest gushers known, is now
the second largest producer of petroleum in the world.

Central America — Oil seepages are reported to occur in Honduras,
Costa Rica, Guatemala and Panama but no oil has been developed
commercially in any of these countries.

South America — Much interest centers in the known and pros-
pective oil fields in South America along the Caribbean Sea. Exuda-
tions and seepages of oil and deposits of asphalt are scattered
through northern Columbia and Venezuela from the Gulf of Darien
to the delta of the Orinoco. The oil is found in porous sandstones
that afford good reservoirs at horizons extending through several
thousand feet of Cretaceous and Tertiary beds which are both folded
and faulted. Most of the oil has a heavy asphaltic base but some is
lighter. The production has been small but development has been
carried far enough to prove that both Colombia and Venezuela con-
tain large reserves of petroleum.

10

BULLETIN NUMBER SIXTEEN OF

Fig. 3 — Map Show-in;? Producing- Areas and Pipe Lines for Petroleum

in Eastern Urtited States.

KANSAS CITY TESTING LABORATORY 11

Peru is the only country on the Pacific coast of South America
that has contributed much petroleum to the world's supply. Most of
the indications of oil are. found in the broad promontory at the north
end of Peru in a belt that extends along the coast from the frontier
of Ecuador southward for about 200 miles to a point south of Payta.
The oil occurs at several horizons throughout 2,000 feet or more of
folded and faulted beds of rather soft sandstone and shale of early
Tertiary age. It escapes at numerous seeps and asphaltic outcrops
and is an excellent refining oil.

Bolivia, Ecuador, Argentina and Chile appear to contain con-
siderable reserves of petroleum which however are apparently not
comparable in extent to those of Colombia and Venezuela. Argen-
tina has produced oil since 1908 from the Comodoro Rivadavia field
on the coast of Patagonia where oil occurs in nearly horizontal sup-
posedly Cretaceous beds which are covered by Tertiary beds. The
oil is heavy, black and of asphaltic base. Indications cf oil have been
found at intervals in a belt that extends along the eastern flanks of
the Andes from Tierra del Fuego northward to Colombia. The whole
belt has produced only a few thousand tons of oil but probably con-
tains extensive reserves.

So far as known, Brazil contains no marked surface indications
of petroleum but it does contain extensive deposits of oil shale.

West Indies — Traces of petroleum are scattered through Cuba,
Porto Rico, Santo Domingo, Trinidad and Barbados but Trinidad is
the only one of these islands that has produced it in any considerable
quantity. The oil fields of Trinidad are mainly in its southern part
and the oil is obtained from lenses of sandstone of Tertiary age which
are closely folded into a series of parallel synclines and anticlines.
Trinidad gives promise of large future production.

Africa — In Africa, oil has so far been produced only in Egypt but
Algeria contains encouraging prospects. The Egyptian oil fields lie
along the Gulf of Suez. The oil occurs in sandstone and in cavernous
dolomitic limestone associated with thick beds of gypsum in Miocene
(Tertiary) age, accompanied in some places by thick beds of salt.
The underlying Nubian (Cretaceous) sandstone also contains some
oil. This field occupies a strategic position on a great trade route
and shows promise of considerable production.

Little work has been done in Algeria but some oil has been ob-
tained in the Cheliff River area, in the Oran province, northwestern
Algeria. The oil bearing formation is probably upper Miocene, and
its structure is complex.

Promising indications of petroleum have been reported in the
Tertiary coastal plain formations in Angola and Ashanti (Gold Coast)
and oil seepages are reported to extend over a large area in Western
Madagascar.

12

BULLETIN NUMBER SIXTEEN OF

Fig. 4— Mai) Showing r'r.,(hi(inf;- Aroas and Pipe Lines for Petroleum

111 Wyoming.

KANSAS CITY TESTING LABORATORY 13

Europe — Most of the known deposits of oil in Europe are in its
southeastern part. More than half of the oil thus far produced in
Europe has been taken from an area of not more than 50 square
miles in the Apsheron Peninsula, in southeastern Russia, on the Cas-
pian Sea, and a large part of the remainder from Rumania and
Galicia. A second reserve in the Caspian region, discovered only
recently but undoubtedly very large, lies in the Ural-Caspian area
along the north shore of the Caspian Sea east of the Volga. Most
of this area appears to lie east of the political boundary between
Asia and Europe but there is no insurmountable barrier to trans-
portation to Europe and the oil there will doubtless become of great
commercial value throughout southeastei'n Europe.

Probably more than 90 percent of the oil found in Europe occurs
in highly disturbed formations of comparatively recent age (Ter-
tiary) similar to those of California. Beds of this type offer great
difficulties to the driller and the average wells make a high initial
yield and decline rapidly in production.

The oil fields of Russia are scattered among ten provinces but
the field in the province of Baku has been by far the most productive.
This relatively small area has produced more than a quarter of the
world's total output of oil and though it reached a peak in its pro-
duction in 1901 when Russia furnished more than half the world's out-
put, its decline has been a decline in world rank rather than in
actual quantity of oil produced. Other highly productive oil fields
of Russia are the Grosny, Maikop, Ural-Caspian and Tcheleken fields.
A number of smaller fields also have excellent prospects. The Grosny
field lies on a sharp anticline of Miocene beds about 500 miles north-
west of Baku, north of the Caucasus range. The Maikop field is in
the province of Kuban, on the north flank of the Caucasus, northeast
of the Black Sea. The other fields of Russia have not produced large
quantities of oil but extensive showings of oil are found in the Ural-
Caspian and Tcheleken fekls of Asiatic Russia, the former covering a
large area in the Emba-Uralsk region and around the north end of
the Caspian Sea and the latter lying on the east shore of the Caspian
Sea in the Trans-Caspian province.

The oil fields of both Galicia and Rumania I'e in a narrow belt
that follows the northern, eastern and southern foothills of the Car-
pathian Mountains. Throughout this belt, oil is obtained from highly
disturbed Tertiary strata. In Rumania most of the oil is obtained
from Miocene and Pliocene beds but part of it is obtained from Eocene
and Oligocene and possibly from Cretaceous beds. In Galicia, the
largest output is obtained from Eocene beds The geology of this
zone is very complex, the rocks being sharply folded and in some
places faulted by overthrust In 1913 the chief producing area in
Rumania was the Prahova, although Buzeu and Bacau also produced
some oil. Promising indications of oil are also found in Bukowina,
Hungary which also lies in this productive belt.

The oil produced in Germany is obtained largely from fields in
Hanover where it occurs in domes associated with rock salt similar to
those of the Gulf Coastal Plain of the United States. The rocks that
contain it are chiefly limestones and sandstones of Upper Jurassic
age. In Batavia some oil has been obtained from sandstone of Eocene
age.

14

BULLETIN NUMBER SIXTEEN OF

6 COAL W^OA

/« lojAnati.Mt -Jik"* LA/re
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CAuroRniPi

Fig-. 5 — Map Showing- Producing- Areas and Pipe Lines for Petroleur

in California.

KANSAS CITY TESTING LABORATORY 15

In Alsace some oil has been produced from sandstone of Eocene
and Olig-ocene age but the general structure is not such as would ordi-
narily be considered favorable.

In Italy oil occurs in the Emilia district, on the northeast slope
of the Appenines in disturbed lenticular sandstones of Eocene and
Miocene age. A small output of petroleum has. been obtained in two
other districts in Italy — in the Pescari Valley, central Italy and in the
Liri Valley, midway between Naples and Rome.

Indications of petroleum are found at many places in Europe
other than those described including England. In fact, practically
every country in Europe contains some indications of petroleum. In-
telligent and efficient search is likely to lead to further discoveries
of oil in many areas, including some where the presence of oil is not
now suspected.

Asia — The principal producing oil fields of Asia are in India,
Persia and Japan. Almost the entire output of India is produced in
Burma. The main oil field is in rocks of Miocene age along the Irra-
waddy in Upper Burma about midway between Rangoon and Man-
dalay. In Assam and in Punjab, coal bearing rocks of Eocene age
have yielded oil in small quantities.

The chief oil fields in Japan are on the island of Nippon, about
200 miles northwest of Tokyo but indications of petroleum have been
found and a small output has been obtained at many other places in
Japan as well as in Taiwan (Formosa). Most of the oil is obtained
from loosely cemented sandstones that lie on the flanks of well devel-
oped closely folded anticlines.

In Persia and Mesopotamia, along the northeast side of the Per-
sian Gulf and the Tigris-Euphrates basin, lies what is probably des-
tined to be one of the large oil fields of the world. The indications
of oil extend over an immense area and oil has been produced in
small quantities here for many years. The only notable development
however is in Persia, 150 miles north of the head of the Persian Gulf,
where about 1,000,000 metric tons of crude oil was produced in 1918.

Other promising oil fields lie in the Ural-Caspian and Trans-
Caspian regions of Russia, in Ferghana (eastern Turkestan) in Chinca
and on Sakhalin Island. In the Ferghana basin^ oil occurs in Lower
Tertiary beds in rather closely folded anticlines on the borders of the
mountains around the basin. In China, small quantities of oil have
been obtained for centuries in the Shensi province, from which large
future production may be expected. The oil occurs in Carboniferous
strata and the general geologic conditions are similar to those in the
Appalachian and Mid-Continent fields of the United States. Indi-
cations of oil have been noted in other provinces. In Sakhalin (Sag-
halien) Island the oil is similar to that in Japan in quality and mode
of occurrence. Oil springs and asphalt deposits are scattered through
a belt that extends along the greater part of the eastern coast of
the Russian part of the island. Pronounced indications of oil are also
reported from Palestine and from the vicinity of Lake Baikal in Si-
beria.

Oceanica and the Malay Archipelago — The islands of Borneo,
Sumatra and Java in the Dutch East Indies contain oil fields that may
be of immense value and other neighboring islands show promising
signs of productive fields The oil is found in anticlinal folds that
have sharply dipping flanks. Most of the oil bearing rocks are as-

16

BULLETIN NUMBER SIXTEEN OF

Oil riCLOs i pipc una

or

MtAICO

PiPC una

' lOOO a0L PRODVCTIOfI

yf\

^

' pom Loaostcoftrex cc^

TAf«m<u<i\\ ¥ iiLAnO<JiLi.TRAfiSPOKr COR^

rcpnrr, cnAi. 0ST C9

O

cmconrtPic

Fig. t>— Map Showin-g- Producing Areas and Pipe Lines for Petroleum

in Mexico.

KANSAS CITY TESTING LABORATORY 17

sociated with beds of coal and lignite of Miocene age. In Borneo, oils
of both asphaltic and paraffin base are found at different depths in
the same fields. Sumatra produces some oils that are very rich in
the lighter products and make a much larger output than the other
two islands of the group.

Indications of oil are found at many places in the Philippine
Islands and small quantities have been obtained there for nearly 50
years.

PRODUCTION AND PROSPECTS.

The most notable contributions to the world's supply of petroleum
in the next decade will undoubtedly be made by the South American
countries that border the Caribbean Sea, by Mexico and by Mesopo-
tamia and Persia.

The annual production of petroleum in Mexico increased from
21,000,000 barrels in 1913 to nearly 64,000,000 barrels in 1918 and the
future production in that country will certainly be very great. Ex-
ploratory work done in Venezuela and Colombia shows that both
those countries may become large contributors to the world's supply
of peti'oleum within the next decade. In Trinidad, the production of
petroleum which for several years has exceeded 1,500,000 barrels a
year, has been doubled within the last four years and with the im-
proved facilities for ocean transportation cf oil that are now avail-
able will no doubt be further increased. Argentine and Bolivia give
promise of considerable production. Cuba is not likely to become a
large producer of petroleum and our present knowledge of the pe-
troleum resoui'ces of the Central American countries is not sufficient
to warrant the assertion that oil fields of great output will be devel-
oped in them.

The production of petroleum in the United States has probably
nearly reached its maximum and is likely to decline slowly but rather
steadily, though this country may remain the leading oil producer of
the world for many years.

The oil fields of Persia produced about 7.000,000 barrels of oil
in 1918 and the wells already drilled are reported to be capable of
producing five times that quantity. The capabilities of the field are
practically undetermined. Difficulties of transportation have greatly
retarded development but an enormous increase in production in the
near future is predicted.

The petroleum resources of Russia are believed to be sufficient
to make that country the leading producer of petroleum in the East-
ern Hemisphere for a long time. The oil fields of both Rumania and
Galicia are believed to have passed their maximum yield and val-
uable new fields will probably not be found in those countries.

The next decade will doubtless witness a steady increase in the
production of oil in India and Persia and the development of one or
more highly productive oil fields in Mesopotamia and possibly in
Asia Minor, Ferghana and China. The same period will doubtless wit-
ness a material increase in the production of petroleum in Taiwan
(Formosa) and Sakhalin and in the Dutch East Indies and possibly
also the opening of new fields in Papua (New Guinea). The oil re-
sources of the Philippine Islands are untested. Africa, including
Madagascar, will doubtless receive attention f>"om oil operators dur-
ing the next ten years, but the output there during that period will
probably not be large enough to affect the world's peti'oleum market
seriously.

18 BULLETIN NUMBER SIXTEEN OF

KANSAS CITY TESTING LABORATORY

19

Geologic Occurrence of Petroleum and Natural Gas.

Petroleum and natural gas are formed by the decomposition of
organic matter of any kind under the proper conditions. Usually it
originates from plant and animal remains that have been deposited
with sediment in the sea. They are never found in commercial quan-
tities in igneous rocks, in the metamorphosed rocks or in fresh water
sediments not associated with marine formations. They generally
originate in shales, marls or limestones. Petroleum cannot ordinarily
accumulate in shales in large quantities because of their close tex-
ture. Sands or sandstone are distributed more or less through all
shales and these sands as vvell as porous limestones offer adequate
reservoirs for the accumulation of petroleum and gas. •

Fig. 7 — Diagra-ii Showing- Accumulation of Oil and Gas in Anticlines

The following summarizes the geological conditions under which
petroleum and natural gas occur:

1. They occur in sedimentary rocks of all geologic ages from Si-
lurian upward. The most productive areas are the Paleozoic in North
America and the Miocene in Russia.

2. There is no relation of the occurrence of petroleum to vol-
canic or igneous action. There seems to be some relation particularly
in the Carboniferous and the Mississippian to the deposits of coal.

3. The most productive areas for oil in great quantity are where
the strata are comparatively undisturbed. Oil frequently occurs
where the strata are highly contorted and disturbed but in less abun-
dance and gas is usually absent.

4. In comparatively undisturbed as well as in disturbed areas a
folded or domed structure often favors the accumulation of oil and
gas in the domes or anticlines.

5. Important requisites for a productive oil or gas field are an
impervious cap rock or cover and a porous reservoir.

6. Salt water almost universally accompanies oil and eas in the
same sand.

20

BULLETIN NUMBER SIXTEEN OF

In the United States, oil is found most abundantly in the Ter-
tiary rocks in California and the Gulf Coast, in upper Cretaceous in
Wyoming, in Carboniferous locally known as the Cherokee Shales in
the Mid-Continent field, in the sub-Carboniferous or Mississippian
and the Upper Devonian in the Appalachian field and in Illinois, and
in the Ordovician in Ohio and Indiana. The oils from the Tertiary are
heavy and of low grade, those from the Cretaceous, Carboniferous
and sub-Carboniferous are light, high grade oils. The Mississippian
in the Mid-Continent field is not believed to carry any oil and very
little is known of it or deeper strata in this territory. It is assumed
that the deeper strata have vanished west of the Ozark uplift.

Fig. 8 — Diagram Showing Accumulation of Oil in Synclines.

The accumulation of petroleum occurs in a pervious reservoir
which usually consists of a loose sand though it may be a coarse gravel
or a disrupted shale or limestone. It is merely necessary that the
rock should contain a considerable amount of voids. The ordinary
sand v.ill have from 15 to 35 percent of voids and the amount of
oil contained and the ease with which it is discharged into a well
vary greatly. As a general rule, one gallon of oil may be obtained
from one cubic foot of oil sand. It is probable that never over 75
percent of the oil surrounding a well is discharged into it even with
the lighter oils, and the percent abstracted is much lower with the
heavier and more viscous oils. Porous sand and gravel and heavy
gas pressure are conducive to rapid expulsion of oil. Fine sand and
low pressure give steadily producing wells of great longevity. The
ultimate production of a well would be determined by the depth and
extent of the sand, the physical character of the sand, the physical
character of the oil and the pressure. Water is a very important ele-
ment in the actual production of a well. It frequently causes very
extensive subterranean oil movements destroying one productive
structure and making new productive structures.

KANSAS CITY TESTING LABORATORY

21

In nearly every oil sand there occur together, gas, oil and salt
water. Salt water is believed to be sea water that filled the pores
of the sand when it was deposited in the sea. Water from oil
bearing strata differs from sea water in concentration and composi-
tion but changes might readily have taken place in the original sea
water while stored in the rocks. In rare instances, oil bearing strata
are associated with fresh water and in some cases there is no water
at all. When these three substances are associated, the gas of course
occupies the uppermost portion of the sand, the salt water the bot-
tom, and the oil, the intermediate portion. The sand commonly
lies at the same angle or dip as the stratum in which it is contained.
This fact offers the basis to a great extent, of the engineer's work
in locating the favorable formations. The strata that contain petro-

I'ig-. 9 — Diagram Showing- Accumulation- of Oil in Faults.

leum are folded. In some places, the folding is very slight, in others
the strata are thrown into sharp folds, the beds dipping as much as
30°. In consolidated rocks such as shales, limestones and sandstone
which have besn intensely deformed by faulting and sharp folding,
oil is generally not found in large amounts. In loose or uncom-
pressed rocks such as clays, marls, sands and conglomerates, large
accumulations are known in areas of highly complicated structures.
The tops of the folds or the anticlines offer the cover for the prin-
cipal accumulation of petroleum, particularly when water and gas are
associated. The bottom of the folds or the synclines may carry oil
when water is absent in the porous stratum. Many oil fields are
on monoclines on which are developed secondary folds such as anti-
clines, domes and terraces. In rocks that are highly saturated with
oil and in beds that dip very gently, the oil gathers in domes if these
exist, but accumulation takes place also in gentle folds and in some
structures such as terraces which are not completely closed. Surface
topography as a general rule, bsars no relation to the probable loca-
tion of oil or the strike of the formation beneath the surface.

22

BULLETIN NUMBER SIXTEEN OF

Asphalt exposures or oil springs are not usually good indications
of oil in immediate vicinities. If oil is found in the immediate vi-
cinity, it is likely to be of heavy asphaltic character.

Asphalt exposures, however, are of value in that they indicate
that oil of good quality may be found where this same geologic
structure is capped by an impervious cover. The depth at which oil
is found of course varies greatly. Oil of good quality is usually
found at sufficient depth that the lighter fractions have not evap-
orated, though some good wells are found at depths as shallow as
250 feet. The best wells of the Mid-Continent field vary from 1,000
to 3,500 feet in depth. The deepest well in the United States is the
Lake Well in Harrison County, West Virginia, and is 7,579 feet deep.
Wells at Ranger, Texas, are about 3,400 feet deep. A well in Banner
County, Nebraska, is 5,600 feet deep. Named in order of depth the

SALT DOME

Fig. 10 — Diagram Sliowing- Tlieoretical Salt Domes of Texas Coast
District. (Oil and Gas Journal.)

three deepest wells in the world are the Lake; the Goff, West Virginia,
7,386 feet and a well at Czuchow, Germany, 7,348 feet. In compari-
son with these great depths, other depths reached by wells or mines
sunk in the crust of the earth are rather insignificant. The deepest
mine in the world is Shaft No. 3 of the Tamarack mine in Hough-
ton County, Michigan, which has reached a depth of 5,200 feet.

The temperature at which oil issues from the ground depends
more upon the depth than upon the latitude of the country in which
the well is located. The temperature of the oil issuing from wells
near the Arctic circle is very much the same as that from the Tem-
perate zone. Gradients as to increase of temperature from the sur-
face of the earth inward have very little bearing upon the average
yearly air temperature. As a general rule, the temperature increases
at the rate of about 1° F. for each fifty feet in depth. On this basis,
the temperature of the earth at a depth of ten miles would be 1000° F.
This is a far greater temperature than necessary for the decomposi-
tion of organic matter or heavy petroleums into light hydrocarbons.
The record of a well in West Virginia as to increase in temperature
is as follows: iqo feet 55 6°

1,000 feet 63.5°

2,000 feet 74 9°

3,000 feet 87.6°

5,000 feet 114.2°

6.000 feet 132.1°

7,000 feet 153.2°

7,310 feet 158.3°

KANSAS CITY TESTING LABORATORY

23

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Fig-. 11 — Correlation Chart of Oil Sands of Oklahoma.

24 BULLETIN NUMBER SIXTEEN OF

The rate of temperatuie increase varies continuo.sly from 1° F.
in 97.5 feet at the surface to 1° F. in 46.5 feet over the interval
6,000 to 7,000 feet. In the Texas and Oklahoma fields, temperatures
at a given depth differ widely from those found in Pennsylvania and
West Virginia. The temperature of the oil in two wells near Man-
nington, West Va., is 83.2° F. at a depth of about 2,900 feet. In the
Ranger field, Texas, the temperature of the oil at 3,400 feet is esti-
mated from measurements at higher levels, to be about 135° F. The
average rate of temperature increase at the surface for thirteen wells
in Texas and Oklahoma is about 1° F. in 51 feet as compared with
1° in 91.5 feet for twelve wells in Pennsylvania and West Virginia.
Mexican oil issues at an average temperature of 165° F.

KANSAS CITY TESTING LABORATORY

25

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KANSAS CITY TESTING LABORATORY 27

General Description of Oil Well Drilling.

Ihe usual method of drilling for oil and gas is the cable system
which depends upon the weight of a heavy string of tools hung on a
stretched rope or cable, lijpe is more satisfactory than cable for
shallow depths. Wire cable is satisfactory below 1,00U feet. The
general equipment requued excepting the power plant is shown in
figure 12. a timber or metal derrick 6U to luO feet nigh with a 16
to 20 foot base is mounted on heavy frame. On one side of the der-
rick, the rig is erected. The main drive is transmitted from the en-
gine to a large wooden wheel known as the band wheel which is from
8 to 12 feet in diameter. The shaft of the band wheel at one end is
attached to a crank that transmits through a connecting rod an os-
cillating movement to an overhead beam known as the walking
beam. Holes are bored in the crank enabling the pin to be placed at
varying distances from the center thus allowing an adjustment of the
stroke of the walking beam to suit requirements. From the end of
the walking beam just overlying the mouth of the well is hung a
temper screw and rope clamp to which the cable is attached when
the string of tools is lowered into the well. The string of tools is
suspended from a cable which is coiled on the bull wheel shaft on
the side of the derrick opposite the rig. The bull wheel is driven by
a chain or crossed drive-ropes leading from a tug wheel on the side
of the band wheel to a corresponding bull wheel about 8 feet in di-
ameter on the end of the bull wheel shaft. Immediately behind the
band wheel is the sand reel at the inner side of which is fitted a
small pulley that can be drawn against the face of the revolving
band wheel by levers thus causing its rapid rotation. The sand line
is coiled on the sand reel and carries the bailer. The bailer is al-
lowed to descend by gravity, its speed being regulated by forcing the
lever backwards and bringing the friction pulley in contact with a
stationary wood block brake. Many combinations of the bailer opera-
tion are used to facilitate and speed the operation of drilling.

The calf wheel is used for manipulating the line from the cas-
ing block. It is mounted on a shaft on the rig side of the framing
and is operated by ropes from a groove or sprocket pulley on the
end of the band wheel shaft.

Three pulleys are placed at the summit of the derrick over which
pass respectively, the drilling cable, the sand line and the casing line.
For cable drilling, a reversing engine is necessary, enabling the op-
erator by means of a rope or rod to have full control from the der-
rick.

The string of tools is shown in fig. 14 and is about 40 feet long.
It consists of a bit or drill, auger stem, jars, sinker and rope socket.
When attached to the rope, they are suspended in the dei'rick and
lowered into the well, a band brake on one end of the bull wheel shaft
being used to retard the speed of descent. When the tools are at or
near the bottom of the well, the temper screw is attached to the
cable, the weight then being thrown onto the walking beam and the
bull wheel shaft is released. Some slack cable is uncoiled from the

28

BULLETIN NUMBER SIXTEEN OF

P'iS. 12— Standard Derrick and Equipment for Drilling Deep Oil Well

■■ells.

KANSAS CITY TESTING LABORATORY

29

bull wheel shaft. The engine is started and the speed is adjusted to
correspond with the vibration of the drill rope. The temper screw
is fed out a little at a time, lowering the bit until a blow is delivered
on the bottom of the well. The tools are then fed out with the tem-
per screw so that the bit strikes an effective blow. When the bit
shows signs of not falling freely, the slack rope is taken up and the
temper screw is relieved of weight, the connecting rod or pitman is
disconnected from the crank pin, the beam is allowed to take an in-
clined position and the tools are raised to the surface. The bailer is
now lowered and the well is cleaned out, sufficient water having pre-
viously been run into the well to make a thin mud such as can be
taken up by the bailer.

In starting a well, it is not possible to operate with the cumber-
some stx'ing of tools so that the first 100 to 150 feet are drilled by
the method known as spudding. The method of spudding is shown
in fig. 15. A special spudding shoe is connected by a rope to the
roller, gripping the drilling cable near the bull wheel shaft. The
figure clearly shows how the vertical motion is imparted to the tools.

The proper operation of a drill is a matter of expert manipula-
tion as considerable judgment is needed to secure the full capacity
of a cable drilling outfit. The speed of drilling must be carefully
regulated to accord with the depth of the well, the nature of the
foraiation and the amount of fluid in the well. Ordinarily, it is not
necessary to rotate the rope to get equal distribution of the attrition
of the bit as the changeable strains in the cable and beam take care
of this.

Fig. 13 — Individual Simplex Pumping- Jack for Connection witli Central

Power.s.

30

BULLETIN NUMBER SIXTEEN OF

WflLk^ING 3£.^M-

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Fig-. 14 — Standard String of Cable Drilling Tools.

KANSAS CITY TESTING LABORATORY 31

Rotary or Flush Drilling.

Rotary flush drills are successfully used on a large scale par-
ticularly in Texas and Louisiana. They have the advantage that very
rapid speed may be made, as much as 3,100 feet of hole being drilled
in a month. Rotary drilling is not advisable nor is it used in wild cat
or pi'ospect work when it is necessary to know the character of all
formations that are passed through. It is very easy for a rotary
drill to pass through a rich formation without any evidence of its
presence. This type of drilling then is used where the producing
horizon is very definitely known and the well is drilled to within a
hundred feet or so of this producing horizon and is finished with the
ordinary cable tools.

The main feature of all rotary flush drills is a rotating table
driven by a gear erected on one side of the derrick. The rotary mo-
tion is transferred by means of pipe to a special bit. A typical bit
is a double cone shaped affair with numerous wedge shaped knives
which turn with the bit. The circulating fluid for removing the cut-
tings is set over the bit under a pressure of about 150 to 200 pounds
per square inch by pum.ps with a capacity of about 200 gallons per
minute. For rotary drilling, derricks of 120 feet in height are desir-
able for convenience in withdrawing the drill pipe.

Percussion Drilling.

A system of drilling by percussion is used to a very limited ex-
tent. Very rapid blows at ths rate of 100 to 150 per minute are
struck by using an eccentric instead of a walking beam.

Fishing Operations.

The most difficult features in drilling wells are those occasioned
by the losing of tools, collapsing of casing or locking of tools by
caving. These accidents occasion weeks and even months of delay
and sometimes cause abandonment of the wells. To recover these
tools or to proceed with the drilling it is necessary to clear the hole
by means of special fishing tools. Almost every conceivable type of
tool has been produced for this service.

Under-Reaming.

On the end of the casing is applied a special steel ring known
as the casing shoe to protect the end of the casing from bending or
distortion. The casing shoe is larger than the drill and when it is
necessary to lower the casing, the hole below the casing shoe must
be enlarged. This is done by under-reaming. Under-reamers are in-
struments provided with side cutters which are opened automatically
when the under-reamers are lowered below the casing. Some under-
reamers provide for both drilling and under-reaming at the same time.
Under-reamers are used whenever it is desirable to enlarge the hole
at any point.

Portable Rigs.

When wells of slight depth are to be drilled, light portable rigs
are used to avoid the expense of dismantling and re-erecting a der-
rick and rig at each well site. For depths less than 1,000 feet, port-
able rigs are satisfactory but are not ordinarily used for depths
greater than 1,000 feet.

32

BULLETIN NUMBER SIXTEEN OF

15 — Adaptation of Drilling Rig- for Spudding- In.

Shooting of Wells.

When an oil well is drilled in, in some sections, the formation is
so hard that it is necessary to break it up so that the oil will flow.
In Oklahoma and Kansas, wells are nearly always shot soon after
they are drilled in. The shooting consists in setting off a large
charge of explosive placed in the well at the level of the oil sand. The
explosive used is usually nitro-glycerin. The explosive is set in the
bore of the well corresponding as nearly as possible to the producing
sand. The amount of the charge depends upon the thickness of the
producing sand. A sand 40 feet thick is usually given a charge of
about 150 quarts of nitro-glycerin. The nitro-glycerin is introduced
into the well by means of a shell containing 20 quarts. Whenever it
is thought that the shooting may have a bad effect and cause a well
to be flooded out with salt water or whenever any other damage ma>
possibly result, shooting is eliminated. Hard compact sands are uni-
versally benefited by shooting. Some sands will not produce at all
until they are shot. The action is to form cracks and crevices in the
oil bearing formation for a considerable distance from the hole.

Sand Screens or Strainers.

In pumping the oil from the well, the fine sand cuts away the
valves and plungers so rapidly thai the plungers must be frequently
removed and replaced. The sand also clogs up the well so. that the
flow of oil is considerably diminished. To overcome these difficulties,
sand screens are set in the bottom of the well to keep out the sand.
These screens consist of perforated brass cylinders wound with heavy
copper or brass wire. The screens are commonly used in the Gulf
Coast territory but not in the Mid-Continent field. The screens them-
selves frequently clog up so that the production can often be much
increased by removing them.

KANSAS CITY TESTING LABORATORY

33

Bailers.

Bailers are long cylindrical vessels fitted on the bottom with a
lift valve and of sufficient flexibility that they can be lowered to
the bottom of a well. When the lift valve strikes the bottom of the
well, fluid is admitted until the bailer is full. It is then withdrawn
and emptied at the top of the well. Bailers are used particularly for
cleaning out the well and sometimes for obtaining the actual oil
production.

Swabbing.

The swab consists of a steel bar with an internal ball valve made
to closely fit the casing by means of rubber rings. The swabbing
consists in very rapidly pulling the swab upwards in the casing so
that it suddenly creates diminished pressure with much agitation of
the fluid contents of the well. It momentarily removes the pressure
head due to the height of the fluid in the well as well as producing
a partial vacuum beneath the swab. This causes the oil or gas in
the formation to flow out readily and cleans off the wax, mud or
other adherent matter on the exposed face of the sand. When there
is a high pressure against the oil sand or a tendency for the well
to wax up, swabbing is extensively used for obtaining the actual oil
production of the well.

J'ig. 16 — Effect of Spacing- Oil Wells on Their Ultimate Production.

34

BULLETIN NUMBER SIXTEEN OF

Pumping of Oil.

The production of oil when there is no natural flow or the natural
flow has subsided is obtained by the use of ordinary lifting pumps.
The kind of pumps used are practically the same as those used for
deep pumping of water. Some pumps are double acting in which each
stroke lifts oil and balances against a counter stroke. In this case,
a sucker rod operates on a piston which is inside of a pipe which
operates the other piston. Oil is produced to a limited extent by the
use of compressed air in the same manner that it is used for water.
A very common method of lifting oil is by means of free air. In
this case a double pipe is introduced into the oil in the bottom of
the well, the inner pipe being perforated at the bottom with holes,
the air being introduced in the annular space between the two pipes.
The air in entering the inside pipe greatly diminishes the length of
the column of oil so that it is raised in the well. This causes it to
overflow at the top of the well. This operates on the same principle
as the original gas found in the crude oil which is a frequent cause of
the gushing of the oil.

Pump Equipment,

The pumping equipment above ground on a lease consists of a
power plant which operates a horizontal spindle eccentrically at-
tached to several wheels. On the periphery of each wheel are at-
tached several pins on which are connected the wire jerker lines.
These jerker lines radiate to the various wells where they are at-
tached to the pumping jack which operates the pump.

€ri/?r/ on of f. 'Est >2v ^i^'s 0/l

P/iODUCT/On TO (jLT/fl/ITE

P/soDUcr/ory -7yp/C/^l &iS£S

J. 000 /ox 00 /S.OOO so 000

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C/i. T//^/^T r P/^ ODL CT/Or/ p. -/S IVSL L

Fig. 17— Relation of Fir.st Year's Production of Oil to the Ultimate

Production Per Well.

KANSAS CITY TESTING LABORATORY

35

Casinghead.

When a well is first brought in, the walking beam of the drill-
ing rig is generally used for operating the pump. The casinghead
is attached to the top of the casing and from it are side outlets, one
at the top for conducting the gas and the other at the bottom for
conducting the oil. The gas is usually conducted to the gas engine
for the source of power and the oil is carried in pipes to the flow
tank where the water is separated by a swing pipe on the outside.
Oil flows from the top of the flow tank to another tank in which the
gauging is done when the pipe line takes the oil. The flow of the
oil into the flow tank usually does not correspond exactly with the
stroke of the plunger. It is discharged at times more or less vio-
lently, usually with a slow expulsion of foam followed by rapid ejec-
tion of oil or oil and gas. This lack of uniformity of flow is caused
chiefly by the expansion of the gas that is dissolved in the oil when
the pressure is lowered as the oil reaches the surface.

Well Drilling by Motor.

A test by Empire Gas & Fuel Co. at 2,500 feet in Kansas showed
the following costs:

Boiler and
Engine

Motor

Loss

432.50 *768.03 $335.53

290.
480.

32.50
60.00

Initial cost $1,862.00 $1,625.00

Cost of installation (includ-
ing belts, etc.)

Estimated depreciation per
well

Cost of water

Estimated cost of fuel oil at

$36 per day 2,160

Cost of electric power

Saving'in cost of power

Savingjin installing pumping
motor in same house on
same foundation

Saving in oil production dur-
ing change to pump

00
00

.00

574.93

Total .

Saving
$237.00

257.50
420.00

1,585.07

186.16
1,305.00

$335.00 $3,990.73

Net estimated saving of electric drilling over steam $3,955.20

* The installation charge of the motor drilling equipment was high
due to the fact that the equipment was new and changes had to be made
which involved labor charges that will not be necessary in future outfits.
It also includes the cost of building the motor house.

36 BULLS'. N NUMBER SIXTEEN OF

Table Showing Price Per Foot for Drilling Oil and Gas
Wells in Various Fields.

(Oklahoma Geological Survey)

Feb. 22, 1916 June 23, 1917 July 27, 1917

To shallow sand in Bartles-
ville, Nowata and Tulsa
districts $0.80to$1.00 $1.00to$1.25 $1.25

To Layton sand in Gushing
field $1.35 $1.50- $2.50

To Bartlesville sand in Gush-
ing field, northwest 1 . 50 2 . 00 3 . 50

To Bartlesville sand in Gush-
ing field, southesat 2.00 2.25 $3.50-$4.00

To shallow sand in Newkirk,
Ponca Gity and Garber
fields 1.50 1.50 1.50

To deeper sands in Newkirk
and Ponca City fields (over
2,500 feet) 2.50 3.50 3.50-4.00

Healdton field 1.40-1.50 1.75 1.75

Electra and Burkburnett to

1200 feet depth 2.00 NOTE.— Price for rotary

Electra and Burkburnett to drilling to 2,000 feet

2100 feet depth 8 . 50 is $3.00.

Electra and Burkburnett to

more than 2,500 ft. depth. 5.00

The regular charge for work by the day Feb. 22, 1917, was $50.00 fo r
a double shift. This held good thorughout the above fields. All wild-
cat propositions some distance (50 miles or more) from any of the above
mentioned fields demanded $3.00 per foot. Contracts were let in 1918-
1919, in Pine Island, La., at $11,000 to $15,000 per well.

KANSAS CITY TESTING LABORATORY

37

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38 BULLETIN NUMBER SIXTEEN OF

The Exploitation of Petroleum by Means of Pits and

Galleries.

M. Couran, ex-engineer of the Corps des Mines and a former
member of the French General Committee on Petroleum, calls at-
tention to the exploitation of petroleum by means of pits and gal-
leries in Technique des Petroles, according to L'Echo des Mines et
de la Metsillurgie. "The complete exploitation of a deposit," says
M. Couran, "should logically pass through three distinct phases,
whose abilities of extraction should correspond approximately to the
following proportions of the total volume of oil originally contained
by the sandstone: Drilling, 10% to 20%; drainage by means of
subterranean galleries, 30% to 40%, and mining of the sandstones
and washing with boiling water, 30% to 40 %o."

These figures given by Paul de Chambrier, director general of
the Pechelbronn mines are not absolute and may vary from one de-
posit to another, but at least they give an idea of the order of
magnitude of the phenomena involved. It is certainly true that
the quantity of oil discharged through a boring that taps a
petroleum deposit represents but a small fraction of the crude oil
saturating it.

De Chambrier's method, which is described in a small publica-
tion, offers the following advantages over ordinary well drilling: It
permits the recovery of two or three times as much oil as that
already secured from the same deposit by means of boring; it in-
creases to the above extent the value of a concession by permitting
one to at least estimate with sufficient accuracy, if not to calcu-
late precisely, the oil reserves still held in the ground; from the
economic point of view it offers possibilities in countries where
oil deposits appear to have reached the limits of their yield; from
the scientific standpoint, it is destined to solve a multitude of prob-
lems that have remained obscure heretofore involving the origin
of crude oil, its migration, its concentration in the lower strata,
the behavior of the natural gas associated with the petroleum and
the stratification of the porus rocks.

It is probably that the first mining of petroleum was by means
of pits, even before the drilling of wells.

KANSAS CITY TESTING LABORATORY 39

Oil Gushers.

In many cases wells drilled for oil penetrate porous reservoirs
that yield at the outset large amounts of oil that flows strongly from
the well and is often thrown under high pressure above the derrick
floor. Such wells are termed "gushers" in the United States and
"spouters" or "fountains" in Europe and Asia. This type of flow is
characteristic of oil under high gas pressure. In some cases, the oil
is forced out by hydrostatic pressure in the same manner as the
flow of artesian water. The gas pressure may force the oil out with-
out being itself discharged to any material extent. Usually both oil
and gas come out, the oil being sprayed high into the air with the
escape of the gas. When the formation is loosened, sand, gravel and
mud are frequently thrown out. Some wells in Mexico throw out gravel
particles weighing as much as 3 to 4 pounds. This blowing out of the
sand often causes the well to "drill itself in." This is commonly
attended by increased production in the early stages of the well's
life.

Gushers usually very rapidly diminish in volume due to the de-
crease in gas pressure and to the rapid exhaustion of the sand in
the immediate vicinity of the oil. Some wells that yield only gas
at first, gradually are converted into oil wells. For this reason, the
wasteful practice of allowing the gas to escape in order to get the
oil is still carried out where it has not been made illegal.

The largest oil well in the world is one which came in near Tam-
pico, Mexico, February 10, 1916. It was known as Cerro Azul No.
4 and was drilled by the Pan-American Petroleum and Transport Co.
The first twenty-four hours of oil flow yielded 260,000 barrels. In
two years it is said to have produced approximately 60 million bar-
rels of oil or about one-half of the total production of oil from Mex-
ico. Its initial pressure was 1,035 pounds per square inch and the
gravity of the oil is 21° Baume' and without sediment or water. This
well continued to produce at its usual rate during 1918.

In September, 1910, the Mexican Petroleum Co. brought in a
well in the Juan Casiano field. It showed on a test that it was cap-
able of giving a daily yield of something more than 100,000 barrels
of oil. Pipeline connections were made, however, but not until more
than 1,500,000 barrels of the inflammable product had been burned
in order to prevent it from flowing into Lake Tamaihua, thus endan-
gering boats and other property. • It was throttled down to a flow of
20,000 barrels a day and for more than eight years it has been giv-
ing this yield. It has yielded, up to the present time, more than 65,-
000,000 barrels of crude petroleum. Accompanying this oil is a gas
pressure of 265 pounds per square inch. This natural gas is piped
to the top of a hill a mile and a half distant from the well and is
there burned in twelve great flares day and night, lighting up the
country for a long way around. On account of the lack of trans-
portation facilities, it has not been allowed to flow at its maximum,
being restrained to one million barrels per month at this time.

In June, 1921, the Mexican Petroleum Co. again brought in a
well twenty-five miles south of the celebrated Cerro Azul No. 4 well
above described, which started flowing at the rate of 15,000 barrels

40 BULLETIN NUMBER SIXTEEN OF

per day and quickly increased to 75,000 or 100,000 barrels per day
with a pressure of 500 pounds per square inch.

A number of wells in the Saboontchy-Romany oil fields of Rus-
sia have given daily yields of from 75,000 to 120,000 barrels for
weeks and as much as 7,500,000 barrels in a year.

Another Mexican well at Dos Bocas, south of Tampico, yielded
approximately five million barrels within two months.

A well in the Jennings pool in Louisiana, in 1904, is reputed
to be the largest gusher in the United States and gave 1,275,000
barrels of oil in four months.

Wells in Texas, California and Rumania have yielded 60,000
to 75,000 barrels of oil per day on the initial production.

The largest wells in the Mid-Continent field were in Butler
County, Kansas, where, in the Towanda pool, gushers as large as
25,000 barrels per day, initial production, were struck in 1917.

Wells in the Homer, Louisiana, and El Dorado, Arkansas, dis-
trict started in originally from 10,000 to 30,000 barrels per day
but quickly dropped to 2,000 barrels or less of high grade oil.

KANSAS CITY TESTING LABORATORY 41

PRODUCTION AND DECLINE OF INDIVIDUAL OIL WELLS.

Mid-Continent Field, 1916.

Total number of wells drilled during year 11,240

Total number of dry holes (including gas) 1,970

Total number with gas 475

Total production at end of year 9,270

Average production of this year's producing wells drilled during

the year 26 bbls.

Average production of this year's producing wells, including dry

holes 21.5 bbls.

Per cent producing at end of year 92 . 5%

Total number of wells drilled up to end of this year 81,150

Total number of wells drilled and producing at end of this year 43,420

Per cent of wells drilled now productive 53 .2%

Average production of all producing wells in field per day, in-
cluding this year 8 bbls.

Average production of all producing wells drilled, excluding this

year 3 bbls.

OIL WELLS DRILLED IN UNITED STATES IN 1917-1918.

Completed Dry

DISTRICT 1917 1918 1917 1918

Pennsylvania 5,435 4,400 985 738

Lima-Indiana 800 793 140 140

Central Ohio 582 605 139 159

Kentucky-Tennessee 1,651 2,191 411 360

Illinois 647 396 151 108

Kansas 3,469 4,671 547 925

Oklahoma-Arkansas 6,717 8,381 1,334 2,116

Texas Panhandle 1,020 ,1140 262 625

North Louisiana 472 534 110 105

Gulf Coast 1,562 1,597 639 625

Total 22,355 24,708 4,718 5,901

OIL WELLS IN MEXICO, 1919.

Wells drilled during 1917 producing oil at end of year 70. 11%

Wells drilled durign 1918 producing oil at end of year 76 . 12%

The total number of wells is 1,056, as follows:

Wells located 131

Wells being driven 114

Wells in production 298

Wells not profitable 27

Wells exhausted 64

Wells not producing 422

Total 1,056

42 BULLETIN NUMBER SIXTEEN OF

OIL WELLS IN MEXICO, 1919

The largest number of productive wells belong to the following com-
panies:

Aguila Company (Lord Cowdray) 55

Mexican Petroleum Company of California 33

The Corona Company 10

Union Petroleum Company, Hispano-Americano 17

The Texas Company of Mexico ' 10

Mexican Gulf Oil Company 8

Chicholes Oil Company, Ltd 7

Mexican Combustible Co 9

Penn. Mex. Fuel Oil Co 7

Freeport & Mexican Fuel Oil Co 7

Transcontinental Petroleum Co 12

Oil Fields of Mexico 12

DAILY PRODUCTION OF CRUDE OIL BY POOLS (JAN., 1922).

ARKANSAS— Barrels

El Dorado 38,000

CALIFORNIA 337,101

Coalinga 39,592

Huntington Beach 5,397

Kern River 21,155

Lompoc and Santa Maria 14,663

Los Angeles and Salt Lake ■ 4,065

Lost Hills-Belridge 10,744

McKittrick 6,730

Midway-Sunset 138,773

Summerland, Watsonville. etc 213

Ventura County and Newhall 6,249

Whittier-FuUerton 89 520

COLORADO ' 300

ILLINOIS ; ; ■ 30,000

INDIANA 4,000

KANSAS 109 412

Au&usta 12,968 '

E bing. 9,965

El Dorado 30,592

Covert-Sellers 3 592

Florence 25975

Greenwood County 4*200

Peabody '..".'.'.'.'. 4*680

Southeastern Kansas and Miscellaneous. . . 17*440

KENTUCKY . .. ,

LOUISIANA 21,000

North Louisiana qo onn 1"«''^«"

Caddo, heavy '.'.].[ 4106

Caddo, light 7'5qq

DeSoto and Red River 7*500

HomeT^'"'' • '.■.'.'.■.'.■.■.■.■.■.■.■. 59;700

South LouL'iana.'.' .■.'.■.' ^^'^^^ „ .„„

Edgerly •.;•.■.•.; ,„„ 9'500

Vinton and others o ^nn

Jennings ;; ^'IH

MONTANA

Winnett and Cat Creek! .' •^'^""

NEW YORK

OHIO 2'°""

29,000

. 1

KANSAS CITY TESTING LABORATORY

43

DAILY PRODUCTION OF CRUDE OIL BY POOLS (Concluded)

OKLAHOMA

Washington County

Nowata County,

Osage County

Tulsa County

Bixby, Bird Creek Jenks, Broken Arrow, Flat Rock,

etc.
Okmulgee County

Beggs, Bald Hill, etc.

Okfuskee County

Muskogee and Wagner Counties

Creek County

Gushing, Shamrock, Glenn, Kiefer, Bristcw, etc.
Pawnee County '.

Jennings and Cleveland.
Payne County

Yale, Quay, etc.

Kay County — Blackwell, Ponca

Garfield and Noble Counties

Garber and Billings.
Carter County

Healdton, Hewitt, Fox.
Cotton and Stephens (Duncan)

PENNSYLVANIA

6,620

6,150

54,625

10,274

38,943

11,445

5,825

58,405

10,677

9,800

5,935
10,173

67,004

31,222

327,459

TEXAS

Burkburnett

Iowa Park, Holliday

Electra

Eastland County (Ranger)

Stephens County (Breckenridge)

Commanche, Young, Brcwn, Ccleman, Shackel-
ford :

Total North Texas

East Texas

Corsicana, Mexia, Wortham. .
Total South Texas

Goose Creek

Humble

Hull

Damon Mound

Sour Lake

West Columbia

Orange

Saratoga

Pierce Juncti on

WEST VIRGINIA

Cabin Creek, etc.

WYOMING

Salt Creek

Grass Creek

Elk Basin

Big Muddy

Pilot Butte

Rock River

I>ost Soldier

Mule Creek

Osage

35,000
5,500
11,800
12,500
51,000

15,700

11,000
6.800

14,500
2,600
4,700

42,700

11,700
2,000
8,000

40,000
4,000
3,000
5,600
200
7,000
7,280
3,870
6,550

CANADA

Eastern

Northwest

MEXICO

Panuco ....

Topila

Tamaulipas.
Chihuahua .

22,000
388,800

131,500
165,000

32,300

22,500

77,500

500,000

44

BULLETIN NUMBER SIXTEEN OF

PRICES OF PETROLEUM AND ITS PRODUCTS

June 1, 1921

Crude at Wells

The following prices are those paid by the pipe lines for crude
as delivered from the wells, with a comparison for the corresponding
period of 1920:

PENNSYLVANIA-OHIO-WEST VIRGINIA

Cabell, West Virginia.

Coming, Ohio

Lima

McKinney

Pennsylvania

Waterloo

Wooster, Ohio

Illinois

Indiana

Plymouth, Dl..
Princeton, Ind.

INDIANA-ILLINOIS

Per Barrel

June 1st,

June 1st

1921

1920

$1.81

$3.42

1.90

4.00

2.08

3.73

2.00

3.00

6.10

1.25

2.30

4.05

2.02

3.77

2.13

3.63

1.15

3.63

1.77

3.77

J-50

^so

—

-r-;-

i"-r— »-— -

MANSA5 CJTY TfSTJJVa LABOSAra^r.-.

I90Z "■# , oi, , OS /9/0 , 'is ' 7? 76 ••■'fe " f^e»--^^'2z

03 OS 07 09 /I /3 /S /7 '/9 £/

Kig. IS— Chart Showing Principal Price Changes of Crude Oil in

Twenty Years.

KANSAS CITY TESTING LABORATORY

45

PRICES OF PETROLEUM AND ITS PRODUCTS (Continued)

Crude at Wells.

KENTUCKY-TENNESSEE

Ragland .

Somerset,

light,

38 gravity and above.
32 to 38 gravity

OKLAHOMA-KANSAS

Healdton

Mid-Continent

Wlters and Beaver Creek.

WESTERN KENTUCKY

Wester Kentucky .

LOUISIANA AND ARKANSAS

Bull Bayou, 38 gravity and above
32 to 34.9° gravity...

35 to 37.9°

heavy, below 32

Caddo, 38 gravity and above

35 to 37.9° gravity

32 to 34.9° gravity

heavy

Crichton, light

DeSoto

E) Dorado, 35 gravitv and above .
33 to 34.9° gravity . .
below 33° gravity. . . .

Homer, 36 gravitv and above

35 to 35.9° gravity

32 to 34.9° gravity ,

below 32° gravity

Pine Island

NORTH TEXAS AND NORTH CENTRAL TEXAS

Burkburnett

Corsicana, light

Heavy

Electra

Henrietta

Moran

North Central Texas .

Petrolia

Ranger

Stephens

Strawn

Thrall

GULF COAST

Batson

Dayton

Edgerly

Goose Creek . . . .

Hull

Humble

Jennings

Markham

Saratoga

Somerset

Sour Lake

Spindletop

Vinton

West Columbia .

June 1st,

June 1st,

1921

1920

1.25

1.75

1.80

4.00

1.60

4.00

1.00

2.75

1.50

3.50

1.00

1.28

1.40

3.15

1.25

3.00

1.30

3.05

.25

2.00

1.75

3.50

1.65

3.40

1.60

3.35

1.00

2.50

1.25

3.00

1.65

3.40

0.70

0.60

0.50

1.50

3.25

1.40

3.15

1.35

3.10

1.00

1.75

1.00

2.50

TEXAS

$1.50

$3.50

1.25

3.00

.75

1.75

1.50

3.50

1.50

3.50

1.50

3.50

1.50

3.50

1.50

3.50

1.50

3.50

1.50

3.50

1.50

3.50

1.50

3.50

1.00 @ 1.25

3.00

1.25

3.00

1.00

3.00

1.00® 1.25

3.00

1.00

3.00

1.00 @ 1.25

3.00

1.00

3.00

1.00

3.00

1.00

3.00

1.50

3.00

1.00® 1.25

3.00

1.00® 1.25

3.00

1.00® 1.25

3.00

1.00® 1.25

3.00

46

BULLETIN NUMBER SIXTEEN OF

PRICES OF PETROLEUM AND ITS PRODUCTS (Continued)

Crude at Wells.

WYOMING

Big Muddy

Elk Basin

Grass Creek

Greybull

Lance Creek

Mule Creek

Rock Creek

Salt Creek

Torchlight

ine 1st,

June 1st,

1921

1920

1.00

2.25

1.50

2.60

1.50

2.60

1.50

2.85

1.45

2.25

.80

1.10

1.10

2.50

1.50

2.85

CALIFORNIA

San Joaquin Valley and Whittier-FuUerton Fields —

14° to and including 17° gravity

18° gravity

19° gravitv

20° gravity

21° gravity

22° gravity

23° gravitv

24° gravity

25° gravity

26° gravity

27° to and including 27.9° gravity

28° gravity to and including 28.9° gravity

29° gravity to and including 29.9° gravity

30° gravity to and including 30.9° gravity .

31° to and including 31.9°

32° to and including 32.9°

33° to and including 33.9°

34° to and including 34.9°

35° gravity and above

Prices for each increase in gravity of 1 full degree above 26°
gravity up to and including 34.9° gravity, 10c per barrel additional.

1.35

1.48

1.36

1.49

1.38

1.51

1.41

1.54

1.45

1.58

1.50

1.63

1.56

1.69

1.63

1.76

1.71

1.84

1.80

1.93

1.90

2.03

2.00

2.13

2.10

2.33

2.20

2.33

2.30

2.43

2.40

2.53

2.50

2.63

2.60

2.73

2.70

2.83

Mexican Crude 12-14°

Texas points $0 . 90

CANADA

Oil Springs $2.55

Petrolia 2.48

Add 52J-2C per barrel to each grade to include allowance by
government to producers.

19-21°
$1.50

$2.83
2.58

Road and Paving Materials

ROAD OILS. — Following are prices per gallon in tank cars 8,000
gallons minimum f. o. b. place named:

New York, 45':; asphalt (at terminal) $0.06^

New York, 65'/; asphalt (at terminal) .06

New York, binder (at terminal) 07

New York, flux (at terminal) 0634

New York, liquid asphalt (at terminal) 08

Chicago, 40-50'; asphalt '/' ' 06

Chicago, 60-70' ; asphalt ' ' " ' 0614"

IJallas, 40-50'. ; asphalt ' lo

I )allas, 60-70';; asphalt 13

Dallas, 75-90';; a.sphalt '.'.'.'.'.'.'.'.'.'.'. 13

San Francisco, binder, per ton 15 00

$0.13
.13

.14
.10
.08
.08J^
.07
.08
.10
12.25

KANSAS CITY TESTING LABORATORY

47

ASPHALT. — Price per ton in packages (350-lb. bbls. or 425-lb.
drums) and in bulk, in carload lots:

Package Bulk

New York (Bayonne, N. J.) $28 . 00 $16 . 00

Boston

Chicago 28.50

San Francisco 21 . 50

Dallas 35.00

Seattle 27.50

Denver

Minneapolis

Baltimore 40 . 00

Los Angeles at factory 22 . 15

Montreal 28.00

Atlanta 33.00

Detroit (petroleum asphalt) : 24 . 50

Cincinnati.. 37.50

Maurer, N. J. (asphalt) 27 @ 38

Maurer, N. J. (asphaltic cement) 29 @ 36 25 (t^ 31

21
15

27

00
00
00

50@70
25.93

15
21

00
.00

20
31

.00
00

/?/^ /9/^ /9/S /9/6 /9/T /<9/e /9/9 /9Z0 /93/ /922

i'ig. 19 — Chart Showing Price Changes of Gasoline, Crude Oil and Fuel

Oils.

48

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY

49

PRICES OF PETROLEUM AND ITS PRODUCTS
January 3, 1922

REFINED PRODUCTS.
(Tank Car Quotations at Refineries)

Gasoline and Naplitha

Per
Gal.

Cts.
NORTH TEXAS

56-57, 450 end point \2}4

58-60, 437 end point (new navy) 13 1^

60-61, 400 end point 15

OKLAHOMA

80-86 grav. casinghead 12

66-68 grav. blend 14J^

50-52, 450 end point. 13

56-57, 450 end point 14

60-61, 400 end point 16

62-63, 365 end point 16J^

64-66, 365 end point 17

58-60, 140 I. B. P. @ 428 E. P 15

60-62, blend 435 end point 14 '

58-60, blend 440(5(450 E. P 1314

74-76, absorpt. gasoline, 300 end pt.. 14

PENNSYLVANIA

Painters' Naphtha 18

54 gravity 16

56 gravity 17

58 gravity 173^

60 gravity, S. R 20K

62 gravity, S. R 21

64-66 gravity 21M

68 gravity, S. R 22^

64 gravity, blend, f . o. b. W.Va 18 '

68-70 gravity blend 18

66-68 gravity blend, 450 E. P 20

68-70 gravity blend, 420 E. P 20}^

60-62 gravity blend 17

Burning Oils

OKLAHOMA
42-44 water white kerosene 2

NORTH TEXAS

40-41 prime winter 2

42-44 water white 23^

PENNSYLVANIA

45 prime white S}4

45 water white 6J^

46 water white 7

47 water white 71^

48 water white 8}^

300 mineral seal 71-^

Fuel and Gas Oil

BAYONNE

28-36 degrees 6

24-28 degrees 51^

18-20 degrees 5

14 plus 4

NORTH TEXAS

34-36 gas oil 2

32-34 gas oil 2

30-32 gas oil 2

24-28 fuel, per bbl 80

Fuel and Gas Oil

PENNSYLVANIA

36-40 fuel oil

38-42 gravity

OKLAHOMA
32-36 gas oil, f. o. b. group 3, Okla.

24-26 fuel oil, bbl

35-37 gas oil, straw

Road oil, 50 (a}, 60 asphalt

45-50 asphalt

100 vise,
200 vise.
160 vise.
200 vise.
200 vise.

200 vise.
180 vise.
150 vise.

75 vise.
100 vise,
150 vise.
200 vise.
300 vise.,
500 vise.
750 vise.!

70 vise.,
100 vise.,
150 vise.,
200 vise.,
300 vise.,
500 vise.,
750 vise.,
200 vise.,
300 vise.,
500 vise..

Neutral Oils

OKLAHOMA

No. 2 color

No. 3 color

, No. 4 color . .

No. 4 color

No. 5 color

PENNSYLVANIA

No. 3 color

No . 3 color

No. 3 color

SOUTH TEXAS

No. 2
No. 2

color, unfil. pale .
color, unfil. pale .

No. 23-2 color, unfil. pale .
No. 3 color, unfil. pale. .
No. 3 color, unfil. pale . .
No. 4 color, unfil. pale. .
No. 4 color, unfil. pale . .
No. 1'2 color, filtered pale.
No. 1}2 color, filtered pale.
No. IJ^ color, filtered pale.
No. 2 color, filtered pale.
No. 2 color, filtered pale.
No. 2^2 color, filtered pale.
No. 2(2 color, filtered pale.

No. 5}'2 color, red oil

No. 51^ color, red oil

No. 6 color, red oil

Natural

Per
Gal.
Cts.

5

50
2M
5J^
5

5^
14

103^
12 M
12

18J^
163^
1434

4

5
10
18
19
20
25

12
14
19

WEST VIRGINIA

30 degrees, carloads 24

29 degrees, carloads 25

28 degrees, carloads 26

Cylinder Stocks

PENNSYLVANIA

600 steam refined 10

650 steam refined 15

600 filtered E 15

600 filtered D 18

OKLAHOMA

600 steam refined 4

650 steam refined

Wax

OKLAHOMA
122-124 white cr. sc. N. Y., carloads. 23^

Oxidized Asphalt

Asphalt f. o. b. N. J. refinery $23.00

F. a. s. New Orleans in cont 23.00

50

BULLETIN NUMBER SIXTEEN OF

PRICES OF PETROLEUM AND ITS PRODUCTS
June 1, 1921

Petrolatums
(Prices Per Pound in Barrels, Carloads)

Snow White

Lily Cream

Cream Petrolatvim Jelly.

Amber

Dark Amber

Veterinary

Dark Green

12
9
7
5

3

2H

Heavy White Mineral Medicinal Oil

Gallon

880-885 specific gravity *1 ' i n

865-870 specific gravity • i • ^"

Ex. Russian crude oil, 885-890 sp. gr., m bbls. to arrive 1 .8&

$2.00

GASOLINE AND KEROSENE SERVICE STATION PRICES

Gaso- Kero-

line sene

Augusta, Maine 17c

Bartlesville, Okla 21.4 9.8

Beaumont, Tex 23 13

Buffalo, N.Y 28 15

Butte, Mont 30 15

Calgary, Canada 41.5 26

Montreal, Canada 38 21 . 5

Toronto, Canada 40 23

Winnipeg, Can 42 24

Casper, Wyo 23 14.5

Chicago, 111 22 10.5

Cincinnati, Ohio 25 14

Columbus, Ohio 25% 14

Dallas, Tex 18 8

Denver, Col 24 17

Harrisburg, Pa

Hou.ston, Tex 18 8

Joplin. Mo 18 12.3

Kan.HaH City, Mo 18 9.5

Place

Gaso-
line

Little Rock, Ark 18

Memphis, Tenn 25

Miami, Fla 28

New Orleans, La 23 . 5

New York City 29

Oklahoma City, Okla • 18

Omaha, Neb 22.5

Philadelphia, Pa 27

Pittsburgh, Pa 27

Portland, Ore 28

Portland, Me

Providence, R. I

St. Louis, Mo 20.1

Salt Lake City, Utah 29

Seattle, Wash 28

Topeka, Kan 20.4

Tulsa, Okla 18

Washington, D. C 25

Wichita, Kan 21.5

Kero-
sene

8
14
17
14
14

8
WU.
13
14

17.5
15
15

10.2
16.5
17.5

9.8

8
11
10

PRICE SCHEDULE FOR CALIFORNIA CRUDE OIL 1919

Gravity Price

14 to 17.9 $1.23

18 to 18.9 1 24

19 to 19.9 1 25

20 to 20.9 1 27

21 to 21.9 129

22 to 22.9 1 31

2:j to2:j.9 ;.::: 1:33

24 to 24.9 1 35

25 to 25.9 ■ ■ ■ 1 37

2« to 26.9 1 39

27 to 27.9 1 41

28 to 28.9 1 43

29 to 29.9 ... 145

.10 Uj :I0.9 1 47

31 to 31.9 i4q

•'2to:t2.9 ••::;; i-^i

33to.X'1.9 153

•'■>t"-'<«" ..;; 1.55

Gravity Price

35 to 35.9 $1.57

36 to 36.9 1.59

37 to 37.9 1.62

38 to 38.9 1.65

39 to 39.9 1.68

40 to 40.9 1.71

41 to 41.9 1.75

42 to 42.9 1.77

43 to 43.9 1.80

44 to 44.9 1 83

45 to 45.9 1.86

46 to 46.9 1.89

47 to 47.9 1.92

48 to 48.9 1.95

49 to 49.9 1.98

69 to 50.9 2.01

51 to 51.9 2 04

52 to 52.9 ' 2 07

KANSAS CITY TESTING LABORATORY

51

HIGHEST AND LOWEST PRICES OF CRUDE PETROLEUM OF
PENNSYLVANIA GRADE, 1859-1918, PER BARREL

Year

1859
1860
1861
1862
1863
1864
1865
1866
1867
1868
1869
1870
1871
1872
1873
1874
1875
1876
1877
1878
1879
1880
1881
1882
1883
1884
1885
1886
1887
1888
1889
1890
1891
1892
1893
1894
1895
1896
1897
1898
1899
1900
1901
1902
1903

1904
1905
1906

1907
1908
1909
1910
1911
1912
1913
1914
1915
1916
1917
1918

HIGHEST LOWEST

Month Price Month Price

December $20 . 00

December 2 . 00

December 10

January 10

January 2 . 00

February 3.75

August 4 . 00

December 1.35

June 1 . 50

January 1 . 70

December 4.25

Augxist 2.75

January 3.25

December 2 . 67>^

November S2}4

November .62>g

January 75

January 1.4714

June 1.53%

September 78

June 62 5^8

April 71M

July 72M

July 49^

January 83}^

June 51 J^

January 68

August 59%

July 54

June 71 J^

April 791^

December 60%

August 50

October 50

January 52 Vg

January 78J^

January 95'4

December 90

October 65

January ■. 65

February 1.13

November 1 . 05

May 80

January, February, March 1.15

Jan., Feb., Mar., Apr., May,

June, July 1 . 50

1 . 85 July, December 1 . 50

1.61 May 1.27

1.64 Jan., Feb., Mch., Apr., Aug.,

Sept., Oct, Nov., Dec 1.58

1 . 78 January 1 . 58

1.78 No change 1.78

1.78 December 1.43

1 .43 June to December, incl 1 .30

1 .35 January to December 1 .30

2.00 January 1.35

2.50 January 2.00

2 . 50 September to December, incl. . . 1.45

2.25 Apiil to August, incl 1.35

2.85 January 2.25

3.75 January 2 to 5, incl 2.85

4.00 January 1 to February 8, inch. 3.75

September $20 . 00

January . 20.00

January 1.75

December 2 . 50

December 4 . 00

July 14.00

January 10.00

January 5 . 50

October 4.00

July 5.75

January 7.00

January 4 . 90

June 5.25

October 4.55

January 2.75

February 2.25

February 1 . 82 ^

December 4.23%

January 3 . 69 J g

February 1 .8114

December 1.28%

June 1.24^8

September 1.01»4

November 1.37

June 1.24%

January 1 . 15 5^

October 1.12 5^

January 92%

December 90

March 1.00

November 1.12'^

January 1 . 07 5^

February 81?^

January 64 J^

December 80

December 95%

April 2 . 60

January 1 . 50

March 96

December 1.19

December 1 . 66

January 1 . 68

January, September 1.45

December 1 . 54

December 1.90

January

October

April, May, June, July.

March to December, incl

No change

January, February, March . . .

January

December

December

March to December, incl

January to March, inclusive. .

December

December

August 22, December 30

February 8, December 31, incl

52

BULLETIN NUMBER SIXTEEN OF

MID-CONTINENT CRUDE OIL MARKET

1902

Date Field

Dec. Neodesha

1903
Jan. South Neodesha
Apr. South Neodesha .
May South Neodesha .
July 1 South Neodesha .

North Neodesha .

Bartlesville

Coisicana light. .

Coisicana heavy.
July 23 South Neodesha

North Neodesha.

Bartlesville

Corsicana light .
Sep. 28 South Neodesha.

North Neodesha.

Bartlesville

Corsicana light. .
Sep. 30 South Neodesha.

North Neodesha

Bartlesville

Corsicana light. .
Oct. 8 South Neodesha .

North Neodesha

Bartlesville

Corsicana light .
Oct. 11 South Neodesha

North Neodesha

Kansas Humboldt heavy

Bartlesville

Corsicana light

Oct. 26 South Neodesha

North Neodesha

Bartlesville

Corsicana light
Nov. 20 South Neodesha

North Neodesha

Bartlesville

Corsicana light. .
Dec. 2 South Neodesha

North Neodesha

Bartlesville

Corsicana light
Dec. 9 South Neodesha. .

North Neodesha

Kan.sas Humboldt, heavy

Bartlesville

Corsicana light

Corsicana heavv
Dec. 29 South Neodesha

North Neodesha

Kan.sa.s Humboldt heavy.

Cornirana light. .

t'orsioana Heavy. .

Bartlesville.

1904
Jan. 1 South Neodesha

North Neodesha

Bartlesville

KansiLM heavy

<'or«ifana light

(.'orHirana In ;i . .
Feb. 12 South Neo.i. i .

N"^'" V I. -I,.,

<^orhiiuiiia light
Contirana heav,

Price
SI. 12

1.15
1.16
1.14
1.16

.96

.94
1.10

.60

1,18

98

.96

12

20

00

98

14

22

02

00

16

24

1.04

1.02

1.18

1.26

1.06

.60

.04
.20
.30
.10
.08
1.26
1.35
1.15
1.13
1.29
1.37
1.17
1.15
1.31
1.38
1.18
.60
16
32
60
36
16
.60
1.27
.55
1.14

$1.36

16
1 14

.60
1.27

.55
1.31
1.11
1.15

.55
1.02

.40

Date
Mch. 1

Mch. 4

Mch. 12

Mch. 29

Apr. 8

Apr. 29

June 7

June 17

July 9

July 13

Aug. 12
Sep. 1

Field

Pi ice

1904

South Neodesha 1 .28

North Neodesha 1 .08

Bartlesville 1 . 12

Corsicana light 99

South Neodesha 1.25

North Neodesha 1.05

Bartlesville 1.09

Corsicana light 96

South Neodesha 1 .22

South Neodesha 1 . 02

Bartlesville 1.06

Corsi cana light 93

South Neodesha 1 . 19

North Neodesha 99

Bartlesville 1.03

Corsicana light 90

South Neodesha 1 . 16

North Neodesha 96

Bartlesville 1.00

Corsicana light 87

South Neodesha 1 . 13

North Neodesha 93

Bartlesville 97

Corsicana light 84

South Neodesha 1.08

North Neodesha 88

Bartlesville 92

Corsicana light 81

South Neodesha 1 .03

North Neodesha 83

Bartlesville 87

Corsicana light 78

South Neodesha 95

North Neodesha 75

Bartlesville 95

Kansas heavy 50

Corsicana light , 73

South Neodesha 88

North Neodesha 68

Bartlesville .88

Kansas heavy 47

Corsicana light 70

Corsicana 1 ight '. . .80

Corsicana heavy 45

South Neodesha 90

North Neodesha 70

Bartlesville 90

Kansas heavy 49

Corsicana light 85

Corsicana heavy 50

Oct. 18 South Neodesha 87

North Neodesha 67

Bartlesville 87

Kansas heavy 46

Dec. 16 South Neodesha 82

North Neodesha 67

Bartlesville 82

Kansas heavy 41

Dec. 29 South Neod sha 80

Bartlesville 80

Corsicana light 80

Corsicana heavy 50

1905

Jan. 1 Kansas heavy .41

South Neodesha 80

Bartlesville ^ 80

Corsicana light 80

Corsicana heavy 50

KANSAS CITY TESTING LABORATORY

53

MID-CONTINENT CRUDE OIL MARKET (Continued)

Date Field Pi ice

1905

Jan. 5 Kansas heavy ". 36

South Neodesha 77

Bartlesville 77

Corsicana light 82

Jan. 11 Kansas heavy • .31

South Neodesha 72

Bartlesville 74

Corsicana heavy 45

Jan. 31 Kansas heavy 50

South Neodesha 70

Corsicana heavy 50

Mch. 25 South Neodesha 68

Apr. 12 South Neodesha 66

Apr. 18 South Neodesha 61

Apr. 25 South Neodesha 57

May 27 South Neodesha 53

Corsicana light 81

June 17 South Neodesha 50

Sep. 12 Corsicana light 83

Corsicana heavy 50

Sep. 16 Corsicana light 85

Sep. 19 Corsicana light 87

Sep. 28 Kansas heavy 35

South Neodesha 51

Corsicana light 89

Oct. 20 South Neodesha 52

Corsicana light 91

Nov. 11 Kansas heavy 35

South Neodesha 52

Corsicana light 89

Corsicana heavy 50

1906

Jan. 1 Kansas 52

Corsicana light 89

Corsicana heavy 50

Apr. 25 Kansas fuel 35

Corsicana light 91

Corsicana heavy 52

July 28 Kansas 50

Corsicana light 89

Corsicana heavy 50

Aug. 2 Kansas 48

Corsicana light 87

Corsicana heavy 48

Aug. 9 Kansas fuel 32

Kansas 45

Aug. 15 Kansas fuel 29

Kansas 42

Corsicana light 89

Corsicana heavy 50

Aug. 28 Kansas 39

1907

Jan. 1 Kansas 32° 39

Kansas heavy 26

Corsicana light 1.00

Corsicana heavy 60

Henrietta 60

Feb. 11 Kansas 32° 40

Kansas heavy 27

Corsicana light 1 .02

Feb. 26 Corsicana heavy 65

Mch. 9 Kansas 32° 41

Kansas heavy 28

Mch. 21 Corsicana heavy 70

Dec. 1 Corsicana light 1 . 00

1908

Jan. 1 Kansas 42° 41

Corsicana light 1 . 00

Corsicana heavy 70

Date Field Price

1908

Mch. 30 Henrietta 75

Corsicana light 85

Corsicana heavy 65

Apr. 24 Henrietta 70

Corsicana light 82

Corsicana heavy 60

June 1 Henrietta 65

Corsicana light 75

Corsicana heavy 55

June 10 Henrietta 60

Corsicana light 72

Corsicana heavy 50

1909"

Jan. 1 Kansas 41

Kansas heavy 28

Corsicana light 01

Corsicana heavy 47

Henrietta 89

1909

Mch. 13 Corsicana heavy 50

Henrietta 50

Apr. 27 Coisicana heavy 53

Henrietta 53

July 22 Kansas 35

1910

Jan. 1 Kansas light 35

Kansas heavy 28

Mch. 17 Kansas light 38

Kansas heavy 30

May 23 Corsicana light 60

Sep. 2 Corsicana light 58

Corsicana heavy 53

Caddo light 40

Kansas light .40

Sep. 20 Kansas heavy 40

Nov. 14 Kansas heavy. . . 42

Corsicana light 55

Corsicana heavy 50

1911

Jan. 2 Kansas 44

Caddo light 44

Caddo litavy 44

Corsicana light 55

Corsicana heavy 50

Mch. 14 Caddo 1 ight 50

May 2 Kansas 46

Caddo light 55

Caddo heavy 50

June 14 Kansas 48

Caddo light 60

Aug. 9 Caddo heavy 40

Sep. 15 Kansas 50

Caddo light 62

1912

Jan. 1 Kansas-Oklahoma 53

Caddo light 62

Caddo heavy 40

Corsicana light 55

Corsicana heavy .50

Jan. 15 Kansas -Oklahoma 55

Jan. 18 Caddo light 65

Jan. 18 Caddo light 65

Jan. 26 Kansas-Oklahoma 57

Jan. 27 Caddo light 69

Feb. 1 Corsicana light 60

Electra-Henrietta 60

Feb. 5 Kansas -Oklahoma 60

Feb. 7 Caddo light 72

54

BULLETIN NUMBER SIXTEEN OF

Mch. 20

Apr. 9
Apr. 16

May 7
May 17
May 20

June 17

June 17

Sep. 10
Oct. 25
Nov. 7
Nov. 9

Nov. 14

Nov. 27
Dec. 12

Dec. 14

Dec. 16
Dec. 17

Dec. 24
Dec. 26

Jan. 1

Jan.

7

Jan.

<J

Jan.

29

Feb.

1

Apr. 7
July 7
July 10

July 24

July 21
July 19

MID-CONTINENT CRUDE

Fijld P"'='

Corsicana light «»

Corsicana heavy 55

Kansas-Oklahoma o-i

Kansas -Oklahoma 64

Electra-Henrietta 65

Kansas-Oklahoma 66

Kansas-Oklahoma 68

Caddo light 77

Corsicana light ' JJ

Electra-Henrietta 70

Kansas-Oklahoma 70

Caddo light 80

Electra-Henrietta 70

Kansas-Oklahoma 70

Caddo light 80

Caddo heavy 6o

Corsicana light 75

Electra-Henri etta 75

Corsicana heavy 60

Corsicana heavy 65

Kansas -Oklahoma 73

Caddo light 83

Caddo heavy 68

Corsicana light 80

Electra-Henrietta 80

Kansas-Oklahoma 76

Kansas-Oklahoma 78

Caddo light 88

Corsicana light 85

Corsicana heavy 70

Electra-Henrietta 85

Kansas-Oklahoma 80

Caddo light 91

Caddo heavy 81

Kansas-Oklahoma 83

Corsicana light 88

Electra-Henrietta. 88

1913

Kansas-Oklahoma 83

Caddo 38° up 91

Caddo 35-37.9° 81

Caddo 32-34.9° 76

Caddo heavy 70

Corsicana light 88

('oisicana heavy 70

Electra 88

Henrietta 88

Caddo 38° up 93

Caddo 35-37.9° 83

( ■addo-32-34.9° 78

Corsicana light 90

Electra 90

Henrietta \^q

CoiHicana light !96

Electra '95

Henrietta 1 95

("addo 38 up '98

Caddo 35-37.9° gg

Caddo 33-34.9°...; ',\ [33

('orwioana light 80

KanHa.M -Oklahoma 93

('addu :i«° up 1 05

("addo 35-37.9°... 95

Caddo 32-34.9° 90

Conticana light.., ., . gs

•"il'-'-lr" '. l.QO

Hi-nriftla j 05

KunHUH-Oklahoma 98

KanHan-Oklahoma . l'o3

OIL MARKET (Continued)

Date Field Price

1913

Aug. 21 Caddo 38° up 1.05

Caddo 35-37.9° 95

Caddo 32-34.9° 90

Aug. 25 Corsicana light 1 .05

Electra 1.05

Henrietta 1 . 05

1914

Jan. 1 Kansas-Oklahoma 1 . 03

Caddo 38 1.05

Caddo 35-37.9° 95

Caddo 32-34.9° 95

Caddo heavy 70

Electra heavy 1 .05

Henrietta 1.05

Corsicana light 1 .05

Corsicana heavy 80

Feb. 2 Kansas-Oklahoma 1 . 05

Mch. 2 Corsicana heavy 70

Mch. 26 Healdton 70

Apr. 4 Caddo heavy 60

Apr. 8 Kansas-Oklahoma 1 .00

Corsicana heavy 65

Apr. 10 Kansas-Oklahoma 95

Apr. 13 Kansas-Oklahoma 90

Electra 95

Henrietta 95

Corsicana light 95

Corsicana heavy 60

Healdton 60

Apr. 15 Kansas-Oklahoma 85

Apr. 16 Caddo heavy 60

Apr. 20 Electra 85

Henrietta 85

Corsicana light 85

Corsicana heavy 50

Healdton 50

Apr. 27 Kansas-Oklahoma 80

Apr. 30 Kansas-Oklahoma 75

May 5 Corsicana 75

Electra 75

Henrietta 75

July 9 Caddo 38° 1.00

Caddo 35-37.9° 90

^, , Caddo 32-34.9° 85

July 15 DeSoto 95

Aug- 8 Caddo 38° 95

Caddo 35-37.9° 85

Caddo 32-34.9° 80

Caddo heavy 45

Aug. 12 DeSoto 85

Aug. 13 Caddo 38° 85

Caddo 35-37.9° 75

„ ,„ Caddo 32-34.9° 70

bep. 12 Kansas-Oklahoma 65

Sep. 14 Caddo 38° 80

Caddo 35-37.9° 70

Caddo 32-34.9° 65

DeSoto 80

bep. Zi Kansas-Oklahoma 55

Electra 65

Henrietta 65

,- ^ Corsicana light 65

Oct. 6 Electra 60

Henrietta .'. 60

., Corsicana light 60

Nov. 13 Electra 55

Henrietta 55

Corsicana ; 55

KANSAS CITY TESTING LABORATORY

55

MID-CONTINENT CRUDE OIL MARKET (Continued)

Date Field Price Date

1915
Jan. 1 Kansas-Oklahoma 55 Sep. 15

Caddo 38° up 80

Caddo 34-37.9° 70

Caddo 32-34.9° 65

Caddo heavy 45

DeSoto .80 Sep. 23

Electra 55 ,

Henrietta 55

Corsicana 55

Healdton 50

Feb. 8 Healdton 30 Sep. 28

Feb. 16 Electra 45

Henrietta 45 Oct. 6

Corsicana light 45

Corsicana heavy 40

Feb. 18 Kansas-Oklahoma 40

Caddo 38° up 70

Caddo 34-37.9° 60

Caddo 32-34.9° 55 Oct. 11

DeSoto 70 Oct. 13

Mch. 3 DeSoto 60 Nov. 13

Mch. 24 Caddo 38° up 60 Nov. 15

Caddo 34-37.9° 50

Caddo 34-32.9° 45

Caddo heavy 35

DeSoto 70

Aug. 2 Kansas-Oklahoma 50

Aug. 4 Kansas 55

Electra 55

Henrietta 55 Nov. 18

Corsicana light 55

Aug. 6 Electra 60

Henrietta 60

Corsicana light 60

Corsicana light 60

Thrall 55 Nov. 20

Strawn 55

Aug. 11 Kansas-Oklahoma 60

Aug. 11 Kansas-Oklahoma 60

Aug. 13 Electra 65

Henrietta 65

Corsicana light 65 Dec. 14

Thrall 60

Strawn 60

Aug. 19 Kansas-Oklahoma 65

Aug. 21 Kansas-Oklahoma 75

Electra 70

Henrietta 70

Corsicana light 70

Aug. 26 Electra 75 Dec. 17

Heimetta 75

Corsicana light 75

Thrall 65

Strawn 65

Aug. 27 Caddo 38° up 65

Caddo 34-37.9° 55 Dec. 28

Caddo 34-32.9° 50

Caddo heavy 45

DeSoto 55

Crichton 45

Sep. 11 Kansas-Oklahoma 80

Thrall 70 Jan. 1

Strawn 70

Sep. 15 Caddo 38° up 70

Caddo 34-37.9° 60

Caddo 32-34.9° 55

Caddo heavy 45

DeSoto 60

Electra 80

Field Pi ice

1915

Henrietta 80

Corsicana light 80

Crichton 50

Thrall 75

Strawn 75

Caddo 38° up 75

Caddo 34-37.9° 65

Caddo 32-34.9° 60

Caddo heavy 50

DeSoto 65

Healdton 35

Cri chton .55

Caddo 38° up 80

Caddo 34-37.9° .70

Caddo 32-34.9° .65

Caddo heavy .55

DeSoto .70

Crichton .60

Healdton .40

Kansas-Oklahoma .90

Kansas-Oklahoma 1 . 00

Electra 1.00

Henrietta 1 . 00

Corsicana light 1.00

Corsicana heavy .55

Healdton .55

Thrall .95

Strawn .95

Moran 95

Caddo 38° up -90

Caddo 34-37.9° 80

Caddo 32-34.9° 75

Caddo heavy 65

DeSoto 80

Crichton 70

Caddo 38° up 1.00

Caddo 34-37.9° 90

Caddo 32-34.9° 85

Caddo heavy 75

DeSoto .90

Crichton .80

Kansas-Oklahoma 1 .20

Henrietta 1.20

Corsicana light 1 .20

Corsicana heavy .60

Healdton .60

Thrall 1.05

Strawn 1.05

Moran 1.05

Caddo 38° up 1.10

Caddo 34-37.9° 1.00

Caddo 32-34.9° .95

DeSoto 1.00

Caddo heavy .80

Crichton .85

Caddo 38° up 1.20

Caddo 34-37.9° 1.10

Caddo 32-34.9° 1 .00

Caddo heavy .80

DeSoto 1.10

1916

Kansas and Oklahoma 1 .20

Healdton 60

Corsicana heavy 60

Corsicana light 1.20

Electra 1.20

Henrietta 1.20

Thrall 1.05

Strawn 1.05

56

BULLETIN NUMBER SIXTEEN OF

MID-CONTINENT CRUDE OIL MARKET (Continued)

Date Field

1916
Jan. 1 Moran

Crichton.

DeSoto

Caddo 32-34.9°..
Caddo 34-37.9°..
Caddo 38° up .
Caddo heavy . .
Jan. 7 Healdton

Corsicana heav'v

Jan. 21 Healdton

Corsicana heav^"
Corsicana light.

Electra

Henrietta

Jan. 25 Crichton

DeSoto

Caddo 32-34.9°..
Caddo 35-37.9°.
Caddo 38° up
Caddo heav-j- .
Jan. 26 Kansas-Oklahoma

Jan. 27 Healdton

Corsicana heavy . .
Corsicana light. .

Electra

Henrietta

Thrall

Strawn

Moran

Crichton

Jan. 28 Caddo 32-34.9°. .
Caddo 35-37.9°.
Caddo 38° up.
Caddo heavy .

Feb. 2 Caddo heavy

Mch. 4 Kansas-Oklahoma
Mch. 6 Corsicana light. .

Electra

Henrietta

Thrall

Strawn

Moran

Mch. 11 Kansa.s-Oklahoma
Crichton . . . ■
DeSoto ...
Caddo 32-34.9°
Caddo 34-37.9°

Mch. 13 DeSoto

.Mch. 13 Caddo 32-34.9°
Caddo 34-37.9°

Mch. 27 DeSoto

C:addo 32-34.9°
Caddo 34-37.9°
June 16 fTJchton
Jum- 24 Crichton

<]ad(|() ;i8'' up
< addii heavy
Mrh. l.J Healdton.

Corxirana lji{ht

Electra

Henrietta .
Strawn
Thrall
Moran
Mrh. U KanmiM-Oklahomii
Mch. 15 CofKirana HkHI
Klecl ra
Henrietta .

Price

Date

Field

1.05

.85

1.10

1.05

1.10

1.20

.55

.75

.67

.60

.70

1.25

1.25

1.25

.90

1.15

1.10

1.15

1.25

.80

1.30

.75

.75

1.30

1.30

1.30

1.30

1.40

1.30

.95

1.15

1.20

1.30

.85

.90

.40

,40

1
1
1.40

1.40
1.40
1.40
1.40
1.45
1 00
1 30
1.25
1.30
1.35
1.30
1.35
1.45
1.40
1.45

.90

80

1.40

1.00

.80
1.45
1.45
1.45
1.45
1.45
1.45
1.55
1.50

1916

Price

50
50

Mch. 15 Thrall..

Strawn

Moran

Crichton

July 15 Crichton. .

Caddo 32-34.9°...,

Caddo 35-37.9°....

July|24 Kansas-Oklahoma .

Healdton

Corsicana heavy. .
Corsicana light. .

Electra

Henrietta

Thrall

Strawn . .
Moran .
July 29 Crichton

Kansas-Oklahoma

Caddo 38° up

July 31 Healdton

Corsicana heavy. .
Corsicana light . .

Electra

Henrietta .
Thrall....

Strawn

Moran

Aug. 1 Kansas-Oklahoma
Caddo 32-34.9°...
Caddo 35-37.9°....

Aug. 2 Healdton

Corsicana heavy. . .
Corsicana light. .

Electra

Henrietta

Thrall

Strawn

Moran

DeSoto

Caddo 32-34.9°....
Caddo 35-37.9°... .
Aug. 7 Kansas-Oklahoma
Corsicana light.. . .

Electra . ,

Henrietta

Thrall....
Strawn . . .

Moran

Aug. 8 DeSoto

Caddo 32-34.9°... .

Caddo 35-37.9°

Caddo 38° up

Aug. 12 Kansas-Oklahoma .

Corsicana light

Electra

Henrietta

Thrall

Strawn

Moran

Aug. 12 Healdton

Corsicana heavy. . . .

Corsicana light

Electra

Henri Ata

Thrall

Strawn

Moran

DeSoto

1.50

1.50

1.50

1.05

.70

1.30

1.35

.45

.65

.65

1.40

1.40

1.40

1.40

1.40

1.40

.65

1.35

1.35

.60

.55

1.30

1.30

1.30

1.30

1.30

1.30

1.25

1.20

1.25

.50

.45

1.20

1.20

1.20

1.20

1.20

1.20

1.35

1.10

1.15

1.15

1.10

1. 10

1.10

1.10

1.10

1.10

1.25

1.10

1.05

1.25

1.05

1.00

1.00

1.00

1.00

1.00

1.00

.45

.40

.90

.90

.90

.90

.90

.90

1.15

KANSAS CITY TESTING LABORATORY

57

MID-CONTINENT CRUDE OIL MARKET (Continued)

Date

Field

1916

Price

Aug.

12
15

Caddo 32-34.9°...

90

Caddo 35-37.9°

95

Aug.

Kansas-Oklahoma

85

DeSoto

1.05

Caddo 32-34.9°

. .80

Caddo 35-37.9°

.85

Aug.

16

Corsicana heavy

.30

Corsicana light

80

Electra

80

Henrietta

80

Aug.

16

Thrall

,80

Strawn

.80

Moran

80

Aug.

17

Kansas-Oklahoma .

.75

Corsicana light

75

Electra

75

Henrietta

75

Thrall

75

Strawn ■. . .

,75

Moran

75

DeSoto

95

Caddo 32-34.9°...

70

Caddo 35-37.9°...

75

Caddo heavy

. .65

Aug.

26

Crichton

. .60

DeSoto

90

29

Caddo 32-34.9°

60

Caddo 35-37.9°. .

65

Aug.

Crichton

55

DeSoto

85

Caddo 32-34.9° .

55

Caddo 35-37.9°

60

Dec.

2

Kansas-Oklahoma

. .00

Healdton

45

Corsicana heavy.

.. .45

Corsicana light. .

. . 1.00

Electra

1.00

Henrietta

1 . 00

Thrall

. .. 1.00

Strawn

1 . 00

Moran

1 . 00

Caddo 32-34.9°

.85

Caddo 35-37.9°

90

Caddo 38° up

1 . 00

Caddo heavy

63

Dec.

4

Crichton

90

Dec.

12

Kansas-Oklahoma

1.10

Dec.

13

Healdton

. .50

Corsicana heavy. . .

.50

Corsicana light . .

1.10

Electra

1.10

Henrietta

1 10

Thrall

1 10

Strawn

1 10

Moran

1,10

Crichton. . .

. 1 . 00

DeSoto

. 1.00

Caddo 35-37.9°

1 00

Caddo 38° up .

. 110

Dec.

14

Crichton

. ... 1.10

Caddo .32-34.9°

95

Caddo 35-37.9°

.... 1.10

Caddo 38° up

.... 1.20

Caddo heavy

73

Dec.

18

Kansas-Oklahoma

. 1.20

Dec.

19

Healdton

60

Corsicana heavy

55

Corsicana light

.... 1.20

Electra

. .. . 1.20

Date
Dec. 19

Field Price

1916

Henrietta 1.20

Thrall 1.20

Strawn 1.20

Moran 1 . 20

Crichton 1.20

DeSoto 1.20

Caddo heavy 78

Dec. 23 Kansas-Oklahoma .- . . . 1 .40

Healdton 70

Corsicana heavy 63

Corsicana light 1 .30

Electra 1 . 30

Henrietta

. . . . 1.30

Thrall

. . 1.30

Strawn

.... 1.30

Moran

.... 1.30

Dec

27

Crichton

.... 1.20

Caddo 32-34.9°

. . . 1.15

Caddo 35-37.9°

... 1.20

Caddo 38° up

1.30

Caddo heavy

. . 88

Dec.

28

Kansas-Oklahoma

. . 1.50

Dec.

29

Healdton

75

Corsicana heavy

70

Corsicana light

.. . 1.40

Electra

1.40

Henrietta

. . 1.40

Thrall

... 1.40

Strawn

1.40

Moran

. . 1.40

Crichton

. 1.30

DeSoto

1 . 30

Caddo 32-34.9°

. .. . 1.25

Caddo 35-37.9°

. . .. 1.30

Caddo 38° up

... . 1.40

1917

Jan.

3

Kansas-Oklahoma ...

... 1.60

Corsicana light

. . 1.50

DeSoto

. . . 1.40

Jan.

4

Healdton

80

Jan. 6

Jan. 8

Jan. 12
Jan. 13

Corsicana light 1 .60

Corsicana heavy 75

Electra 1 . 50

Thrall 1.50

Strawn 1.50

Moran 1 . 50

DeSoto .1.50

Caddo 32-34.9° . .1.35

Caddo 35-37.9° 1.40

Caddo 38° up 1 . 50

Caddo heavy 98

Kansas-Oklahoma 1.30

Corsicana light 1.70

Caddo 32-34.9° 1.45

Caddo 35-37.9° 1.50

Caddo 38° up 1.60

Caddo heavy 1 .08

Healdton 85

Corsicana heavy 80

Corsicana light 1.80

Electra 1.50

Henrietta 1.60

Thrall 1.60

Strawn 1.60

Moran 1 . 60

Kansas-Oklahoma 1 .40

Corsicana light 1 .90

Healdton 90

Electra 1.70

58

BULLETIN NUMBER SIXTEEN OF

MID-CONTINENT CRUDE OIL MARKET (Concluded)

Date
Jan. 13

Jan. 23
Mch. 9

Mch. 14
Mch. 17

Field Price
1917

Henrietta I'^O

Thrall 1 70

Strawn I'O

Moran 1-70

Crichton 1 10

DeSoto 1 60

Caddo 32-34.9° 155

Caddo 35-37.9° 160

Caddo 38° up 170

DeSoto 1 75

Caddo 32-34.9° 1.65

Caddo 35-37.9° 170

Caddo 38° up 1.80

Caddo heavy 95

Caddo heavy 1 . 00

Caddo 32-34.9° 1.75

Caddo 35-37.9° 1.80

Caddo 38° up 1.90

DeSoto 1.80

.\ug. 1 Healdton 95

Corsicana heavy 85

Aug. 7 Healdton 1 . 05

Corsicana light 1.95

Aug. 15 Kansas-Oklahoma 1 .60

Aug. 16 Healdton 1.10

Corsicana heavy 90

Electra 1.90

HenrietU 1.90

Thrall 1.90

Strawn 1.90

Moran 1.90

Aug. 20 Kansas-Oklahoma 2.05

Healdton 1.10

Corsicana light 2.05

Electra 2.00

Henrietta 2.00

Thrall 2.00

Strawn 2.00

Moran 2 00

Aug. 22 DeSoto 1 90

Caddo 32-34.9° 1

Caddo 35-37.9° 1

Caddo 38° up 2

Crichton 1

1918

Mch. 16 Healdton 1

Corsicana heavy 1

Mch. 19 Kan.xas-Oklahoma 2

Mch. 20 Corsicana light 2

Electra ] 2

Henrietta 2

DeSoto 2

80

90
00
50

45
40
25
25
25
25
15

Caddo 38° up 2.25

Date Field

1918
Mch. 20 Caddo 35-37.9°

Caddo 32-34.9°

Caddo heavy

Crichton

Aug. 12 DeSoto

Caddo 38° up

Caddo 35-37.9°

Caddo 35-34.9°

Caddo heavy . .
1919
Mch. 21 Healdton

Corsicanan heavy

Caddo below 32°

June Homer

Oct. 4 Burkburnett

Henrietta

Nov. 21 Healdton

Nov. 20 Corsicana light

Kansas-Oklahoma

Electra

Dee. 2 Henrietta

Strawn

Moran

Dec. 19 Healdton

DeSoto

Caddo 38° up

Caddo 35-37.9°

Caddo 32-34.9°

Caddo heavy

Hewitt .

Dec. 22 Healdton

Kansas-Oklahoma all grades

Electra

Henrietta

Moran

Thrall

Brukburnett

Corsicana light

Corsicana heavy

Strawn

Ranger

Desdemona

Caddo 38° up

Caddo 35-37.9°

Caddo 32-34.9°

Caddo heavy

DeSoto

Crichton

Homer

Burkburnett

Ranger

Hewitt

Crichton crude

Prica

2.15
2.10
1.25
1.75
2.25
2.25
2 25
2.25
1 55

1.20
1.05
.75
2.25
2.00
2.25
1.35
2.50
2,50
2.50
2.50
2.50
2.50
1.85
2.40
2.50
2.40
2.25
1.00

75
00
75
75
75
75
2.75
2.75
2.75
1.30
2.75
2.75
2.75
2.75
2.65
2.50
1.25
2.65
2.25
2.50
2.75
2.75
2.75
2.25

KANSAS CITY TESTING LABORATORY 59

PETROLEUM PRODUCTION CONDITIONS IN MEXICO.

(Roy H. Flamm in U. S. Commerce Reports.)

Mexico's Increasing Contribution to World's Oil Supply.

A comparison of the following figures of oil production in
Mexico, in the United States and in the world since 1901 indicates
the phenomenal growth of this industry in Mexico. While in 1913,
Mexico furnished but one-fifteenth of the world's supply of oil, in
1920 it furnished nearly one-fourth. The production in the table
below is given in barrels of 42 gallons each:

Production of Oil Since 1901.

Total World
Years Mexico United States Production

1901 10,345 G9,G20,529 167,434,434

1902 ... 40,200 88,766,916 182,006,076

1903 75,375 100,461,337 194,879,669

1904 125,625 117,080,960 218,204,391

1905 - 251,250 134,717,580 215,292,167

1906 502,500 126,493,936 213,415,360

1907 1,005,000 166,095,335 264,245,419

1908 3,932,900 178,527,355 285,552,746

1909 2,713,500 183,170,874 298,616,405

1910 3,634,080 209,557,248 327,937,629

1911 12,552,798 220,449,391 344,174,355

1912 16,558,215 222,935,044 352,446,598

1913 25,696,291 248,446,230 383,547,399

1914 26,235,403 265,762,535 403,745,342

1915 32,910,508 281,104,104 427,740,129

1916 40,545,712 300,767,158 461,493,226

1917 55,292,770 335,315,601 506,702,902

1918 63,828,326 355,927,716 514,729,354

1919 87,072,955 377,719,000 544,885,000

1920....- 163,540,000 443,402,000 688,474,251

Potential and Actual Production of Oil.

The above statistics show the world's actual production of oil in
1920 to have been approximately 688,000,000 barrels. The potential
production in Mexico during 1920, according to Mexican official fig-
ures, was nearly 800,000,000 barrels. By the term "potential pro-
duction" is meant the amount of oil that would be produced if each
well were permitted to flow without restraint. This estimate of
the Mexican government is undoubtedly too high, as it fails to take
into consideration the failing wells and has been based on the
initial production of large gushers which quickly settle down to a
flow of only one-half or two-thirds of their initial production. Con-
servative estimates as of August 1, 1921, give about 1,500,000 barrels
as the daily potential capacity of existing wells. The actual produc-
tion, based on statistics of the oil movement, amounts to 600,000
barrels daily. The daily potential production of the fields fluctu-
ates greatly, as new wells are being constantly developed and salt
water encroachments show up frequently without warning.

60

BULLETIN NUMBER SIXTEEN OF

The Mexican wells flow continuously under their own Pressure
wells often coming in with an initial flow of more than 100,000
barrels daily, under a water and gas pressure as high as 1,085 pounds
to the square inch, but averaging between 300 and 800 pounds.
Pumps are never required as the wells produce under their own pres-
sure until exhausted. There is no "oil sand" (in our use of the
term) found in the producing fields of Mexico, although recent bor-
ings in the "Tehuantepec-Tabasco" region indicate the presence of
oil-bearing sands. A notable characteristic of Mexican oil is the
great heat of the oil produced, the temperature ranging from
90° to 181°F (32° to 83°C). The average temperature at the Ebano
fields is 105 °F and that of the salt water and oil of the Dos Bocas
is 165°F. The temperature of the oil is of great importance from
an economic viewpoint, in that it decreases the viscosity of the oil
and permits it to flow more freely. Since viscosity retards the move-
ment of oil in the containing formation, the heat is of importance as
a factor in determining the rate of daily production. In most of the
producing fields of Mexico large amounts of gas are present under
considerable pressure, but very little attempt has been made to
divert the gas to economic usefulness.

Mexican oil, because of its low gravity, is of low gasoline con-
tent, averaging from 5% to 16%. American oil, averaging a higher
gravity, produces 20% to 40% gasoline, besides kerosene, lubricating
oils, paraffin, etc. One authority averages Mexican oil as composed
of about 9% naphtha, 10% illuminants, 50% to 75% fuel and the
remainder lubricants, paraffin, asphalt, etc.

An average of 300 wells produced in Mexico during 1920 ap-
proximately 164,000,000 barrels of oil, or an average actual daily
production of 1,800 barrels per well. From January 1 to May 1,
1921, the Mexican Government reports 42 new wells completed with
a daily potential production of 828,728 barrels. During the week
ending September 4, 1921, nine wells were completed in Mexico
with a daily actual production of 140,000 barrels.

Geographical Division and Production of American Wells.

The oil wells of the United States may be geographically divided
into the following fields:

Number of producing wells.

Appalachian 109,000

Lima-Indiana ; 42 000

'''"'^» ;: ; 16,800

Mid-Contment 78 360

'lUlf Coast 1 840

Rocky Mountains • i'n7n

California :::: ::::::;:::::::::::::::::z:::::z;::;:::::;;:;;;::::: lilo

'^"^"^ ^58^560

Wi»h'^bi,."Tir'"'''^'\-''''''^.r°'''''^*''^" P^^ we" averages 4.9 barrels.

i^umno ifr,!^ fh'.'r^''"?u ^^' ^f.l'^ ^" ^^^ United States must be
F»umpp(l from the time they are "brought in."

KANSAS CITY TESTING LABORATORY 61

Oil Producing Areas of Mexico.

The known oil-producing areas of Mexico may be divided into
three main regions, as follows: Panuco River region, Tampico-
Tuxpan or "South Fields" region, and the Tehuantepec-Tabasco region.

In the Panuco River region the Ebano field is situated 40 miles
west of Tampico. The oil from this field has a very high percentage
of asphaltum and averages about 12° Be' (0.986 specific gravity).
The Panuco field, comprising the productive areas between the
Tamesi and Panuco rivers, is 20 to 30 miles southwest of Tampico
and the Topila field is situated a few miles east of the Panuco.
Both the Panuco and Topila production is a heavy viscous oil of from
10° to 15° Be', the deposits being found at approximately 2,200 feet.
These fields have been noted for the relatively few failures in
drilling. From the east end of the Topila field to the west end of
the Panuco field (a distance of 17 miles) is an undrilled gap of
nearly 3 miles, which is being closed by exploitation. From this
Panuco-Topila district there has been produced to date 130,000,000
barrels of oil, or 20 '/r of Mexico's total output and there is a present
daily production of 130,000 barrels. From the Ebano field there has
been produced to date 24,000,000 barrels of oil, or SV27r of Mexico's
total output. Today there is a daily production of 4,000 barrels.
While there is a general salt water table below which no oil will
be found, neither of these fields has been finally delineated by dry
holes and there is good reason to believe that they will be extended.

Developments in the Tampico-Tuxpan or "South Fields" region
have been made upon a long, narrow strip of productive territory
running in a north and south direction from Dos Bocas to Alamo.
This strip has been developed to a length of about 40 miles and to
a width of about 1 mile. Local elevations and variations in struc-
ture make some portions of the strip more productive than others,
but over the entire 40 miles it is remarkably uniform. The oil from
this territory averages from 19° to 21° Be' (0.9395 to 0 9271 specific
gravity). This region has produced 492,446,170 bbls. of oil or 75%
of Mexico's output and is now producing daily at the rate of nearly
400,000 bbls. The various sectors or pools of the "South Fields" re-
gions have been given various names. A short description of each
of the various sectors or pools of this region follows:

Dos Bocas — This is the most northern pool of the area. The first
large well was brought in in 1908 with an initial flow accoi'ding to
its owners of more than 100,000 bbls. daily. After catching fire and
running wild for three months, the well turned to hot salt water and
is not now productive. Many well versed oil men believe Dos Bocas
was a "gasser" as it burned without smoke.

Tepetate-Chinampa — This pool has produced more than 100,000,-
000 bbls. of oil, but production is only obtained from this pool at this
time by stripping. The salt water table started at 2,175 feet and
rapidly rose to 1,800 feet. The average depth of the wells was 2,000
feet.

Casiano Pool — The famous Juan Casiano well No. 7 was com-
pleted in this pool in 1910, flowing continuously for 10 years and pro-
duced 85,000,000 bbls. of oil. Contrary to a popular belief this pool

62

BULLETIN NUMBER SIXTEEN OF

is not a part of the Chinampa pool from which it is separated by
volcanic dikes.

Amatlan-Naranjos-Zacamixtle-This district^has^ ^^^^^^^^

120,000,000 bbls,of oil up to Ju^y i. 1921 f ^^^^t saK water table
l^^^^^'ri^S^feet'at'XTorfher^e'nfand'rose to 1,660 while on the
Shern eYd n Lower'Amatlan the salt water has reached the 1,800
f ; w.l Arnatlan is being intensely developed by a score of op-
frlrs 1th o"d Une'ompTnies and independents and will probably
not have a long life. The average depth of wells m this area is 1,900
feet.

Toteco— This pool was not drilled until early in 1921. The fee
title to the pool is held partly by the Huasteca ^^^^'^l^^T ^\, ^^^
International and Mexican Gulf Companies hold leasehold rights on
the remainder. The average depth of wells is 1,800 feet.

Cerro Azul and Juan Felipe— The most famous well in this area
is the Huasteca Petroleum Co.'s No. 4 brought in in 1916, and which
has produced 60,000,000 bbls. The Juan Felipe area is held by some
authorities to be separate from Cerro Azul, being cut off by a well
defined basalt dike. One well in the Juan Felipe boundaries now
shows the extraordinary pressure of 1,080 pounds, and has not been
exploited due to the more convenient location of the Cerro Azul wells
belonging to the same American company.

Potrero del Llano and Atazan — The Potrero del Llano well was
completed in 1910 and produced 94,000,000 bbls. of oil before it went
to salt water in 1918. By strategic drilling and pinching in oil wells
a considerable production has been developed since 1918 and it is
being maintained. The average depth of wells in this district is
2,000 feet.

Cerro-Viejo — This large property, lying south of Cerro Azul and
adjoining Potrero del Llano, is just beginning to be drilled. It belongs
to the Huasteca Petroleum Co. and the Aguila Co. Indications point
to its overlying a separate pool which, judged by surface indications,
will equal any of the larger pools. It contains a small well at a shal-
low depth which was drilled in 1878. The recent drilling has encoun-
tered oil at the 1,600-foot level.

Tierra Blanca and Chapapote Nuenz — This is a non-competitive
pool controlled by the Huasteca Petroleum Co., the first well having
been completed in May, 1921, with a potential production of 75,000
barrels per day.

Tanhuijo and Tierra Amarilla — Drilling has been deferred in this
district because of the greater production of wells to the west, which
produce lighter oils.

Molino Pool— One well has been drilled in this pool at 2,710 feet,
producing a heavy viscous oil of 11° Be'. While exceptionally heavy,
the oil from this well has been discharged successfully under the well
pressure through a pipe line to a pumping station at a distance of
20 kilometers.

Alamo — This pool is controlled by the Penn.-Mex. Fuel Co. Ap-
proximately 35,000,000 barrels of oil have been produced, consisting

KANSAS CITY TESTING LABORATORY 63

of two distinct grades. Salt water has seriously invaded the pool and
stripping has been resorted to.

Furbrero — This area is located about 40 miles southwest of
Tuxpan. The oil found is of very high grade, being 24° Be', but the
yield has not been large and the district is not now producing.
Between Alamo and Furbrero are some of the best indications of oil
pools in Mexico on lands which are largely taken up by American
companies. South of Furbrero, at Pahuatatempa and Vega, are
extensive seepages, although no development has yet been undertaken
in this region.

In the Tehuantepec-Tabasco region, the Tabasco-Chiapas field is
noted for the quality of its oil, which has a paraffin base, is very
light, and contains a large proportion of illuminating oils. Exploita-
tion of this field promises to become active after having been dor-
mant since 1917. The Isthmus of Tehuantepec field produces an oil
of from 25 to 32° Be' and is characterized by the short productivity
and the shallow depth to oil. Operations in this field have not been
of great importance in the past few years. Oil is found at a depth
of 500 to 600 feet.

The following table shows all of the Mexican oil fields discovered
up to June 1, 1921, with the date of discovery, number of wells drilled
number of productive wells and the production of these wells:

Number and Production of Wells in Mexican Oil Fields.

Production

Year No. of Wells Present

Dis- Produc- Averages

REGION AND FIELDS covered Drilled tive Total Daily
Panuco, Topila, Ebano fields:

Panuco ... 1910 218 112 121,000,000 127,000

Topila. ... 1910 75 18 8,539,000 3,500

Ebano 1910 71 38 22,400,000 4,000

Total 364 168 151,939,000 134,500

South Fields:

Tepetate and Upper Chinampa 1910 28 17 126,874,000 (o)

Lower Chinampa and Amatlan 1913 89 43 141,566,000 240,000

Zacamixtle 1920 10 8 12,039,000 50,000

Toteco 1921 3 3 1,000,000 30,000

Cerro Azul 1916 6 2 59,002,364 60,000

Potrero del Llano & Alazan 1910 21 11 115,650,000 (o)

Tanhuijo & Tierra Amarilla 1919 39 21 500,000 (v)

Alamo 1913 9 6 35,803,806 15,000

Molino 1917 2 1 11,000 500

Total 207 112 492,446,170 395,500

Tehauntepec region 1904 220 54 7,000,000

Miscellaneous 500,000 200

Grand total 791 334 651,885,170 530,200

oSa t water.
vAbandoned.

64 BULLETIN NUMBER SIXTEEN OF

Explanation of Mexican Gushers.

Mr. E. de Golyer, geologist, in a paper read before the Society of

Automotive Engineers is quoted as follows:

"We have been so impressed with the unprecedented size of some
of the Mexican gushers and by their continued production of large
quantities of petroleum over long periods of time without any ap-
preciable decline in the amount of production, that we have perhaps
overestimated the total amount of petroleum to be accrued from any
<!ino-le pool The explanation of the great gushers seems to lie in the
very great porosity of the rock in which the petroleum occurs It col-
lects in a network of caves and channels previously dissolved out of
a bed of thick limestone. This condition allows the petroleum to
move about very freely while still underground. Furthermore, the
petroleum generally lies over water under an artesian head, and as
a consequence the 'field pressure is largely hydrostatic rather than
gas pressure, which, in most fields is the expulsive force causing the
oil to flow. The result of these conditions is deposits of petroleum
which can be exhausted with a single well, whereas a deposit of
the same size under different conditions of occuri-ence would require
hundreds if not thousands of wells to exhaust it."

Salt Water Invasion.

No salt water has yet appeared in the Cerro Azul and Toteco
fields. In all other fields some of the wells have been damaged or
destroyed by the encroachment of salt water. An unwarranted im-
pression as to the significance of the invasion of salt water in the
various Mexican fields has recently been created by articles appear-
ing in the press. The wells now producing oil in Mexico are doing
so under a great hydrostatic pressure, the flow of oil continuing un-
til exhausted, and the salt water then following the oil to the sur-
face. The "salt water menace" so-called, does not usually appear
until after vast quantities of oil have been taken from a pool and
the exhaustion of one pool has no more bearing on an unconnected
virgin pool than does the exhaustion of a sector in the United States
condemn a sector not yet developed.

The other fields of Mexico will continue to give oil for a con-
siderable t'me to come, but such production probably will be in-
creasingly smaller from the peak of 1920-21. Many of the wells now
being developed in the Amatlan pool show tendencies to develop salt
water more rapidly than heretofore. This condition may be ac-
counted for, in a mea;sure, because the producers in competing pools
have been forcing production to the limit in order to get out as
mich oil as possible before a rival concern drains the pool. The
exten.sively developed pools in the South fields region have been
pu led on by every pipe line and storage available in the region in a
wild sr-ramhle to get the oil to the surface and they are now witness-
mg the mevitable result— a rapid exhaustion of the pools and the early
aj)[)earanc-e of salt water. Even after a pool has apparently been
(iraincd substantial amounts of oil may be produced by "pinching in"
ihe wills. I his consists in closing the flow valve, creating a back
pressure and pemiitting the oil to flow through a smaller aperature;
the water, as the heavier material, going to the bottom. This process

KANSAS CITY TESTING LABORATORY 65

is repeated so long as clear oil can be made to flow. Pinching in
or stripping was resorted to after the Chinampa pool was drained
and is now being done to Alamo and Potrero and will be resorted to
in Zacamixtle and Amatlan.

Estimation of Mexican Fields.

The following recent estimate of the Mexican fields has been
made by Messrs. L. G. Huntley and Stirling Huntley, prominent
American geologists:

Estimating the life of Cerro Azul and Tierra Blanca, with an
estimated reserve of 200,000,000 bbls. at 1,000 days (on the assump-
tion that they produce at the combined rate of 200.000 bbls. per day
after the Amatlan pool is drained) at the time of their being finally
flooded, they in their turn should strip 10 000 bbls. or more per day
each from wells on the crests. This reserve will be partly sold to
other companies and therefore will probably be pulled on much faster
than this. While it is impossible to say how long this stripping can
go on, there is good evidence that such wells will be long lived, as
they are probably fed by oil working up the flanks of the structure
over the entire former producing area. Much of this oil must have
been cut off by the sudden flooding of the pools and will now be
largely available to such strategic wells as those mentioned. This
will allow one to est-mate that after all the Southern pools have been
flooded there will still be a production in the Mexican fields of 250,000
bbls. per day at the end of 1.000 days from July 1, 1921 (December
1, 1924) on the assumption that the new drilling in the Panuco River
field increases production.

This alone is sufficient to be a considerable factor in the oil
market, particularly the fuel oil market. Meanwhile it can be as-
sumed that the prospecting will have probably extended the producing
areas in the Panuco River district and those to the south and west
of the Alamo. In the latter region there are good indications that
there will be found pools of relatively light oil in sand and lime-
stone formations above the Tamasopa, as well as in the latter forma-
tion itself. In the case of the probable pools yielding from reser-
voirs above the Tamasopa, these will undoubtedly have smaller wells
producing over a longer period of time in comparison with the large
Tamasopa wells to the north. It is even possible, if later and higher
prices warrant it, that th's region will see pumps installed for the
first time in Mexico.

"The present reserves in producing pools may be shown as fol-
lows: Barrels

Amatlan Zacamixtle 50,000,000

Cerro Azul-Toteco 150,000,000

Tierra Blanca 50,000,000

Total 250,000,000

"In addition to the above reserves are the Panuco River pools
which have not been limited and seem capable of considerable exten-
sion.

"These amounts disregard later recoveries from the same areas
through stripping wells, as the factor used in the calculations was

66 BULLETIN NUMBER SIXTEEN OF

derived from the data in the Tepetate-Chinampa area, which excludes
later recoveries. Early in 1921, before the market decline, the daily

production was. i^cnnn

Panuco River fields 14o,000

Amatlan-Naranjos-Zacamixtle on'nnn

Cerro Azul and Toteco f"-"^"

Alamo - • ^"'"""

Total 585,000

Less Amatlan, in 125 days will lower production to 185,000

"But this disregards oil reserves from various sources, which
may therefore be added and summarized, giving the following esti-
mated possible production by fields after Amatlan goes to sea water:

Barrels

Panuco River fields 145,000

Tepetate-Chinampa (stripping) 10,000

Naranjos-Amatlan-Zacamixtle (stripping) 20,000

Cerro Azul (3 companies) 140,000*

Tierra Amarilla (stripping) 10,000

Potrero Alazon (stripping) 10,000

Alamo (stripping) 7,000

Tierra Blanca (noncompetitive) 60,000**

Total 402,000

^Probably greater on account of the sales to other companies.
**Depending on company's policy.

Operations in Panuco and Topila.

The American consul at Tampico has observed that production
operations in the Panuco and Topila fields are somewhat different in
character than in the Southern fields, in that part of them are con-
ducted by individuals and small companies or aggregations of in-
dividuals; whereas the major part of development work in the South-
ern fields is conducted by large corporations which not only drill the
wells but construct refineries, pipe line, pumping stations, and loading
terminals, and ship the oil by their own tank steamers. Thus they
conduct all the operations of production and marketing and the mat-
ter of cost price or value at the well concerns them but little. Many
of these companies also have valuable properties in the Panuco dis-
trict. Shipments of Panuco oil have been practically confined to
such companies. Lately much activity has been noted among inde-
pendent producers (confined largely to the Panuco field) finding out-
lets for their product through brokers and as a result, something re-
sembling a trading market has been formed and a value for the dif-
ferent oils established.

Formerly the big producing pools of Mexico were controlled in
most cases by a single company and neither fear of having their
property drained by a rival nor competition operated to force pro-
duction by the individual companies. From the standpoint of con-
Beryation of the oil supply, such an arrangement was desirable for a
minimum amount of oil was wasted through over-production and in-

KANSAS CITY TESTING LABORATORY 67

sufficient storage. At the present time, the heavy producing pools,
particularly in the South fields region, are in most instances being
pulled on by competing companies with little regard to conserva-
tion of the supply.

Exploration of New Fields.

George Otis Smith, director of the United States Geological Sur-
vey, puts the proved area of Mexican oil lands at about 10,000
square miles, with resources of 4.500,000,000 bbls. and the potential
output of unproved territory at 1.250,000,000 bbls.; a total estimate
of 5,750,000,000 bbls. or a supply adequate for 45 years at the 1920
rate of exports. A greater part of the unproven territory in the
known oil zones is already in the hands of the large corporations.
The exhaustion of the Amatlan pool will mark the passing of the
independent operator in the South fields region to a considerable
extent. The Panuco River region has always been essentially a small
man's field. The enormous reserves of petroleum lands situated
in the producing regions held by the Mexican Petroleum Co. (Doheny)
and the Aguila Co. (British) allow these companies to regard the in-
trusion of salt water in their present wells with a certain degree of
equanimity. The Royal Dutch Shell interests control nearly 400
square miles of valuable fee-simple and leasehold oil lands. The Mex-
ican Petroleum Co. has obtained a 40 year lease on nearly 800,000
acres in the Tampico district on land which shows extensive oil seep-
ages. This addition increases greatly the life of the extensive prop-
erties already owned by this company. The Marland Oil Co. of Mexico
has extensive holdings of undeveloped lands in Mexico, including 280,-
000 acres in the Tuxpan-Tampico area, 65,000 acres in the Tabasco-
Chiapas region and large concessions in Lower California and Sonora.

Increasing attention is now being given to exploration or "wild-
catting" in various parts of Mexico for the discovery of oil. Geological
conditions indicate that other petroleum fields of great importance
will be discovered in Mexico, and that such discoveries will be of a
petroleum of a much better quality than that now being produced.
A report of the Mexican Petroleum Section of the Department of
Commerce, Industry and Labor, places the zone of possible produc-
tion in the Gulf States at more than 80,000,000 acres and in Lower
California at about 18.000,000 acres. Of this immense area, only
about 10,000,000 acres have been investigated which illustrates the
scope offered for wildcat operations in Mexico. The combined area
of the fields now being exploited in Mexico does not. exceed 1,200
square miles.

Exploitation has now extended into the districts of Tlacalulu and
Cobos. The Tlacalulu district is in an oil bearing formation, situated
in the extreme southeast corner of the State of San Luis Potosi, 50
miles southwest of Tampico. The Cobos district lies directly across
the Gonzales River from Tuxpan and extends southwest for 50 miles.
It is regarded as a determined field and exploitation is going on.
Exploration is particularly active in the Isthmus of Tehuantepec and
in the region south of Vera Cruz. Many seepages occur in this re-
gion. The Tabasco district is the oldest oil field in Mexico, the oil
produced being of 32° Be' but former production was in such small

68

BULLETIN NUMBER SIXTEEN OF

amounts that competition with the richer Panuco and South fields
wSsii possible. Extensive leasing is under way and actual devel-
opment again in progress, principally by the Roya Dutch-Shell in-
herits althorgh the Standard Oil and Mexican Gulf companies are
active/ The Grijalva River is being deepened at Frontera, which city
is to be the port of the Tabasco field.

Possibilities in Scattered Regions.

The discovery of what is believed to be extensive petroleum de-
posits on some islands in the Gulf of California has been announced.
These islands are close to the shore of Sinaloa, due west of Her-
mosillo, and the deposit is thought to extend to the mainland of Lower
California. The proximity of these areas to the producing areas of
the State of California, the probability that portions of Lower Cali-
fornia and Sonora are underlaid by a counterpart of the producing
horizon of the California fields in the United States, the evidence of
petroleum on the surrounding waters and the continued extension of
the California fields southward leads to the belief that these areas
on the west coast will yet produce petroleum in commercial quantities.

Explorations are being carried on in other parts of Mexico as fol-
lows: Durango, in the neighborhood of Mapimi; Oaxaxa, near Puerto
Angel; Colima, in the vicinity of Santa Rosalia and of Manzanillo;
Chihuahua, in the vicinity of Casas Grandes, Guzman, Trinidad, Santa
Maria, and southwest of Ojinaja; Coahuila, at Ubalde, near Piedras
Negras, and Nuevo Laredo; Chiapas, in the Departments of Palenque
and Mezcalapa; San Luis Potosi in the Valles district; Jalisco in the
vicinity of Lake Chapala, and in various parts of Yucatan. On Sep-
tember 1, 1921, there were 240 strings of drilling tools in operation
throughout Mexico as follows:

FIELDS Dig.

Panuco 24

Topila 3

South Fields 64

Wildcat 19

Total 110 42 88 240

While the cost of drilling wells in Mexico is high, there are other
costs which precede drilling and which amounts to a considerable fig-
ure. These include the cost of prospecting by highly-paid geologists,
the expense's of negotiating the purchase and lease of oil territory, the
amount paid for the properties if purchased, or the rentals if leased,
the very substantial recording and stamp fees encountered in Mex-
ico, the expense of perfecting title (which is considerable, due to the
successive divisions of the land) the cost of clearing the land, the con-
struction of roads and water lines, materials for transporting sup-
plies thn.ugh the jungles, and many other items of expense peculiar
to operations in Mexico.

Der.

Loc.

Ttl.

10

11

45

2

5

10

19

48

131

11

24

54

KANSAS CITY TESTING LABORATORY

69

ACTUAL PRODUCTION BY COMPANIES IN MEXICO.

COMPANIES

Cia. Pet. La Victoria

Topila Petroleum Company

Cia. Mex. Pet. del Golfo

National Oil Company

Panuco Petro. Maat. (Royal Dutch)

Cia. Exp. de Pet. La Universal

Hispano Mexicana (Tex. Mex. Fuel) . '

Mexico y Espana

Mexican Oil Company

Cia. Pet. Monterrey

Chijoles Oil Ltd. (R. Dutch)

Oil Fields of Mexico

Vera Cruz Mexico (S. O. N. J.)

La Petrolera Poblana

Cia. Mex. de Combustible (Pierce O 1)

La Corona (Royal Dutch)

Transcontinental de Petroleo (S. O. N. J.)

Panuco Bost. Oil (Atlan. Ref.)

Tampascas Oil Company

Internat. Pet. (J. H. Hamm'd)

Cia. Pet. Tal. Vez. (So. O. & T.)

Tex. Co. of Mex. (Texas Co.)

Cia. Mex. de Petroleo (Mex. Pet. of Calif.)

Cia. Mex. de Pet. La Libertad (Island O. & T.) .

Mex. Gulf Oil (Gulf Oil Co.)

Cortez Oil Corp. (Port Lobos Pet. Corp.)

East Coast Oil (So. Pac. Co.)

Freeport & Mex. F. O. Corp. (Sinclair Gulf)

Penn. Mex. Fuel Co. (South Penn. Oil)

Cia. Mex. de Pet. El Aguila (Mex. Eagle Oil) . . .
Huasteca Pet. Co. (Mex. Pet. of Delaware)

1918
Bbls.

2,748

3,075

4,226

5,459

3,490

25,021

25,266

29,906

51,716

91,311

300,064

337,603

382,029

531,511

578,478

609,733

1,152,063

1,279,746

1,445,976

1,550,869

1,728,190

2,161,775

3,457,235

4,119,654

6,854,080

16,910,646

20,186,459

1917

Bbls.
1,574
2,000
29,993

753,589

873

29,625

288,770

24,958

1,515

34,689

360,258

32,871

60,852

740,576

119,315

828,067

174,924

619,828

989,561

,315,433

,125,702

Totals 63,828,329

1,160,794

3,143,220

4,076,982

4,129,296

16,922,322

17,325,171

55,292,758

PIPE LINES IN MEXICO.

The pipe lines in Mexico on November 30, 1919, with the name of
the owners and the capacity of the pipe lines are as follows:

Total

No.

3

11

1

1

3

1

3

3

7

4

4

6

7

1

2

29

1

5

1

6

1

1

1

1

1

1

2

1

_6

Total. 113

OWNERS
Freeport & Mexican Fuel Oil Corporation.

Cia. Transcontinental de Patroleo

Tampascas Oil Co

National Petroleum Corporation

National Oil Co

Oil Fields of Mexico Co

New England Fuel Oil Co

Standard Oil Co

Cortez Oil Corporation

Cia. de Petrolio La Corona

Mexican Gulf Oil Co

East Coast Oil

Texas Co. of Mexico

Mexican Oil Co

Cia. Mexicana de Combustible

El Aguila S. A

Cia. Mexicana de Petroleo

Huasteca Petroleum Co

Tampico Oil Ltd

Penn. Mex. Fuel Co

Panuco Boston Oil

Cia. Regiones Pet. Mexicanas

Cia. Terminal de Lobos

Pierce Oil Corporation

Cia. Mex. de Oleoductos Imperio

La Atlanti ca Cia

Cia. Terminal Union S. A

Cia. de Fomento del Sureste

Cia. Metrolopitana de Oleoductos

Lengths,

Meters

4,750

20,743

1,470

350

10,985

88,950

2,276

8,953

78,603

68,188

113,276

44,843

49,534

2,707

6,499

421,498

11,260

362,724

8,500

62,367

1,380

1,357

812

2,463

1,213

2,674

875

1,100

40.570

Daily
Capacity,

Cubic
Meters
7,950

40,131
1,590

5,724
2,880
1,590

14,000
6,930

48,472
9,641

11,144

11,888

17,195
1,590
3,338

79,876

138

7,950

318

41,657
1,145
4,190

11,400
1,590
5,540
9,000

10,000
1,000

19,302

1,420,920 377,169

70

BULLETIN NUMBER SIXTEEN OF

The number of storage tanks in Mexico January 1, 1920, with the
name of the owners, the capacity of the tanks, are as follows:

TO

No.

4

20

1

1

1

2

1

1

4

9

4

23

6

37

1

.'. 76

3

4

18

Texas Co. of Mexico 17

Mexican Oil Co 2

Cia. Mex. de Combustible 8

El Aguila S. A '.'.'.'.'..'.. 374

Cia. Mexicana de Pet 16

Huasteca Pet. Co 129

Tampico Oil Ltd 5

Penn. Mex. Fuel Co. . . I7

Eureka Pet. Co. S. A

Panuco Boston Oil Co 3

Cia. Terminalde de Lobos 5

Pierce Oil Corporation , _ , II4

I-a Atlantica Cia

Ferrocarril Interoceanico 1

North American Dredging Co. ...... 1

Cia. de Fomento del Sureste. ... 0

Cia. Metrop. de Oleoductos 4

915

Freeport & Mexican Oil Corp.
Cia. Transcont. de Pet. S. A..

English Oil Co

Tampascas Oil Co

National Petrol. Corp

Interocean Oil Co

Hispana Mex. S. A

Cia. Pet. Tal. Vez

National Oil Co

Oil Fields of Mexico

New England Fuel Oil Co. .

SUndard Oil Co

Cortez Oil Corporation

Cia. de Pet. La Corona

Topila Pet. Co....

Mexican Gulf Oil Co

Chijoles Oil (Ltd.) ,

Producers Terminal Corp

East Coast Oil Co

Felix de Martino Diaz.

TO

DEC. 31, 1919

Capacity,

Cubic

Meters

26,234

153,420

1,590

3,180

8,745

17,488

8,745

3,180

34,980

28,303

35,980

212,800

52,470

345,467

5,962

91,031

3,180

34,976

129,572

8,745

118,400

4,212

41,914

4,501,900

96,089

1,169,951

12,918

148,665

17,806

43,720

111,722

8,745

5,962

17,490

34,980

CONSTRUCTED
DURING 1919

Capacity,

Cubic

Meters

No.
1
2

5,962
17,598

i

'5,961

i

8,744

'4
4

33,980
21,218

5

31,409

1
12

8,745
20,150

2

11,925

3

3,968

3

25,232

5

42,533

4

34,980

7,540,531 48

272.406

KANSAS CITY TESTING LABORATORY

71

OIL TANKERS IN USE JUNE, 1921, HANDLING MEXICAN

PETROLEUM.

Name of Tanker

Barrels
Capacity,

Name of Tanker

HQASTECA PETROLEUM CO.

I-a Habra 68,200

I. C. White 54,000

E. L. Doheny 61,200

C. E. Harwood 30,800

Sunshine 67,100

Solana 63,200

C. Anderson 79,500

San Joaquin 60,600

Tamaha 72,100

G. G. Henry 64,100

Caloric 58,600

Franklin K. Lane 66,900

E. Walker 66,400

Montana 64,300

G. W. Barnes 60,600

C. A. Canfield 61,400

Cerro Ebano 74,000

H. G. Wylie 39,700

Mendocino 54,300

J. Macy 77,400

J. M. Danziger 61,300

Norman Bridge 39,600

Mantilla 53,100

Wm. Green 66,400

Wyneric 38,700

Nora 95,800

Oyleric 53,500

Ario 73,200

MEXICAN GULF OIL CO.

Gulf Oil 50,400

Shenango 25,300

Gulf Trade 65,700

Currier 46,000

Gulfstar 72,900

Gulflight 32,200

Ligonier 30,000

Oural 19,500

Agwisea 78,700

FREEPORT & MEXICAN FUEL OIL
CORP.

Darden 53,200

Farnum 32,100

Tamesi 20,400

Madrone 55,400

•Panuco 25,800

J. M. Cudahy 69,200

E. R. Kemp 44,500

Hardcastle 34,200

Hugenot 61,600

A. E. Watts 64,800

Barrels

Capacity,

MEXICAN EAGLE OIL CO., LTD.

War Shikari 49,000

War Begum 49,100

War Ranee 52,200

San Florentine 67,600

San Leon 50,500

San Dunstano 68,800

Camden 60,900

Anomia 41,400

San Lorenzo 81,800

San Narario 82,500

British Maple 58,600

San Tiburcio 62,000

War Glackwar 49,500

Bloomfield 43,300

El Cano 45,700

San Silvestro 7,500

-San Zotico 49,600

San Ubaldo 46,500

Grenella 46,200

San Teodore 57,4.00

San Fernando 18,300

Kekoskee 47,600

San Geronimo 108,200

San Ricardo 49,100

Borgestad 36,600

San Patricio 107,500

TRANSCONTINENTAL PETROLEUM
CO.

Comet & Brg. S2 47,200

Princeton 19,500

H. H. Rogers 51,600

Caloria 37,200

Gedania 31,900

Corning 20,300

H. M. Flagler 23,300

Glenpool 48,000

Baytown 20,700

C. M. Everest 53,100

Geo. H. Jones 61,000

Baton Rouge 46,500

James McGee 68,400

Sandtows 1-2 38,200

Wm. G. Warden 51,900

F. W. Weller 41,200

W. Jennings 97,800

F. Q. Barstow 103,700

Zoppot 106,000

Bradford 58,200

Chinampa 63,600

Richconcal 62,900

Bostwick 77,300

J. D. Rockefeller 72,500

72

BULLETIN NUMBER SIXTEEN OF

OIL TANKERS IN USE JUNE,
PETROLEUM

Xame of Tanker ^Ban^.ls_

EAST COAST OIL CO.

F Sulphur 6 3^,500

Torres ".000

F-Sulphur 1 21,u00

Gladsbye '*'^-»*'<'

Topila 52,200

PEXX. MEX. FUEL OIL CO.

Mattole 64,500

Standard 119,300

XEW EXGLAXD FUEL OIL CO.

Radian! 24,300

Socony 90 1S.300

Gen. Pettibone 8,300

Socony 85 23,800

Perfection 14,900

M. P. 7 17,700

Chagres 9,800

LA COROXA PETROLEUM CO.

Utaearbon 53,000

Alabama 26,600

William Isom 28,800

Lucellum 42,100

Ar. Von Gwinner 28,800

NATIOXAL OIL CO.

Kathrrlne 17,300

W. A. Ibsen 31,200

V. J. Reilly 27,100

DauBhtTty 26,200

TEXAS COMPANY

Pennsylvania 56,300

Texas 58,800

Ocddr.ntal 58,900

Harvester 60,500

Hucrosa 52,300

Shenandoah 65,500

-Murli opa 35,000

Yurl,a Linda 66,200

K'UV'T 64,000

LouiHiina 25,900

"••''■'dKe 68 300

NATIONAL PETROLEUM CORP.

Newona 22.200

Tani'iirvllle 19 400

"""^"« 34!o00

PIKUCE OIL CORPORATION

Mexicnna 21,400

llumpt'in Rondf .42 100

1921, HANDLING MEXICAN
(Concluded)

Xame of Tanker Barrels

Capacity,

FRVXCE & CANADA OIL TRANS-
PORT CO.

Swiftarrow 43,800

Swiftsuie 41,300

Winapie 18.000

INTEROCEAX OIL CO.

Aztec 51.300

Pinthis 8.600

ISLAXD OIL & TRANSPORT CORP.

Uncas 4-l.-'00

Sabine Sun 70.700

Clement Smith 72.000

Massassoit 45.000

S. B. Hunt 69,000

Xelson 43,800

Crowe 29,500

Hahira 67,700

Muskogee 62.700

Liberty Minguas 48,300

Warden 48,000

Trontolite 61.200

TALVEZ OIL CO.

Sunset Una 14,800

CIA. REFINADORA DEL AGWI

Baldhill 62,100

Remulus 48,300

Agwison 71,800

Hadnot 65,300

Chestnut Hill 43,600

Mevania 66,500

Baldbutte 62.400

Chestersun 75.900

Hoven 66,600

Agwiworld 68.900

Hulaco 67.300

Agwimoon 72.200

CORTEZ OIL CORPORATION

Donnell 105.300

S. L. Fuller 71,700

Japan Arrow 86,000

Halsey 64,200

W. M. Burton 71,900

Devolente 64,900

Tonawanda 28,200

Coalinga 74,900

Montebello 76,000

Laramie 56,500

INTERNATIONAL PETROLEUM CO.

De Soto 55,700

W. C. Teagle 108.500

J. Worthington 79,500

Mottole 64,600

Rapidan 78,300

Chas. Pratt 102,800

KANSAS CITY TESTING LABORATORY

73

RECORD OF ALL MEXICAN OPERATIONS TO DATE— 1919

Prepared by Mexican Petroleum Department, Secretary of Industry.
1 Cubic Meter = 6 29 Barrels.

DRILLED BY

La Universal

Mexico y Espana

La Libertad

Cantabros en Panuco.

La Nacional

Panuco Tamesi

Alamo de Panuco ....

Tux. Ozuluama

Pet. Maritima

Preeport & Mex

Esfuerzo Tampiqueno.

El Caiman

Panuco Valley

Southern Co

Expl. Topila

La Transatlantica . ...

Panuco Mahuaves

Lluvia de Oro

Esfuerzo Nacional

Vado Oil Fields

La Victoria

Transcontinental

R. A. Mestres

English Oil Co

El Espino

Pedro Irisari

Tampascas Oil

National Pet

Gulf Coast Corp

Los Perforadores

Hispana Mexicana . . . .

Tal Vez, S. A

Monterrey, S. A

International Pet

Orbananos et al

Margenes del Pam . . . .

Panuco Topila

El Penix, S. A

Las Dos Estrellas

Productora de Pet

National Oil Co

Mex. National Oil

Zaleta Mar Oil Co

La Herradura

Continental Mex

El Indio

La Oaxaquena

Oil Fields of Mex

New England Fuel . . . .

La Oriental Mex

La Esperanza

Abastecedora

Panuco Excelsior

Adrian Petroleum

Cortez Oil Corp

Inglesa Explot

Tantoyuca y Anexas. . ,

A. p. Wiechers

Mex. Pet. del Golfo . . .

La Corona S. A

Byrd et al

Oro Mexicano

La Bonanza

Am. Fuel Oil

Drilling
Loca- Feb. 28,
tions 1919

Pro-
duc-
ing
1
1
1

1
12

12

4

1
10

Potential Daily

Production Aban-

in Cubic Meters doned

511.00

626.00

8,000.00

5,794.90

66.77
800 . 00
160.00

6.00
15,804.04

' 1,444 ' 66

8.00

713.00

" '22^96
319.00
1,600.00
1,155.00
16.00
6,661.22

80.00

238 . 50
598 . 90

1,500.00

60.37
3,900.02

190.00
5,000.00
804 . 38

95.45
8,095.42

16.00
802.95

1
1
2
1
1
1

"i

23

1
12

Total
No. of
Wells
2
1
1
2
1
1
2
2
1

14
1
1
3
1
1
1
1
1
2
1
1

24
3

10
1
1
7
1
6
2
3
3
1

17
1
1
1
1
1
3
6
3
1
1
2
1
1

37
4
1
1
3
1
4
5
2
2
5
2

26
2
1
1
2

74

BULLETIN NUMBER SIXTEEN OF

RECORD OF ALL MEXICAN OPERATIONS TO DATE— 1919-

Continued.

DRILLED BY

Topila Petroleum

Mexican Gulf

Tampico Panuco

Chijoles Oil

American Inter

Hispano Amer

East Coast Oil

Soria y Socios

Texas Co. of Mex

Mexican Oil Co

Smith's Oil Co

Pan American Oil

Orillas de Panuco

Nuevo Leon

Mex. de Combust

Hispano Cubana

M. C. Anderson

Piedras Devel. Co

Lt Seventeen Co

Punta Arena y Anex

Comercio de Peubla ....

La Argentina

Mexico Fuel Oil

Hidalgo Oil Co

El Nayarit

Financiera de Pet

Mex. Development

El Azadon, S. A

La Concordia

Nueva Bonanza

El Aguila, S. A

Aamiahua Pet

Mex. Pet. Co. Cal

Huasteca Pet. Co

Tuxpam Pet. Co

.Mundacadiz, S. A

Juan (°a.siana Tux

Harry Hummel

!..a Tolteca

Tampico Oil Ltd

Tampico Oil Co

Penn. Mex. Fuel

La Kfjuidad

EHpana, S. A

Pet. de Ti'petate

Cnnsolidala de Pet

Eugfnio K. Jiuiz

Seifuranza, S. A

I<a Ciiralda

1^ .Meridional

Tampiqucna-San Javier

T<x. M.x. Fuel Oil

Narional de Petr

Mexican premier

Eureka \\"

Panuco Tuxpan , .

Sun Oil Co ;

pi-troliTu I'oblana. ....'.

I Ji (omiTrial

I'iiriuro litmlon

It'-Ki"ni'»i I'd Mex.....
I'ui-hla en panuco
Alliwm W. Smith
Kodi.lfci H. Kader
CapurhinuH Oil
Komcnto do ('hapala

Drilling
Loca- Feb. 28,
tions 1919

32
2

21
3

18
1
1

11
1
1

22
1

Pro-
duc-
ing
1
8

' 7
1

17

10
3

1
9
1
2

5

i
i

55

33

4

Potential Daily

Production
in Cubic Meters
63.60
22,370.50

154.33

4.77

4,561.06

17,072.19
639 . 98

' 875.00

is! 90

5,051.62

397 . 00

22.25

6^40

367.13
2,666; 00

20,590.18

2,497.65
48,553.70

47.00
13,969! 35

21,462.86

160.05
494.52

400.00

1,072.00
223 . 00
127.20

2,400.00
5.00

1,113.00

3,465.10

Aban-
doned

8
3

■7

9

2

i

1
1

i

284

4

36

19

4

1

13

Total
No. of

Wells

1

20

8

7

8

1

27

1

17

4

1

3

1

2

16

1

2

1

3

1

1

2

9

1

1

1

1

2

1

1

389

7

91

36

1

1

1

2

1

9

1

26

1

1

9

1

1

3

2

2

1

1

1

1

2

1

2

1

3

2

4

4

1

1

2

1

KANiSA:S CITY T1^:ST1I\U L,AtlUKATUKl

70

RECORD OF ALL MEXICAN OPERATIONS TO DATE— 1919—

DRILLED BY

Mexican Sinclair

Pat. Agric. Mex. San Jose.

Scottish Mex. Oil

Los Brujos

Catopico Oil Co

Dos Banderas Oil

Clipton & Smith

Freggs Oil Co

Hidalgo Petrol. Co

W. H. Miliken

Ohio Mex. Oil

I>roducers Oil Co

Rio Vista

Sims & Bowser

Spanish Mex. Oil

J. W. Sloan

J. R. Sharp

Tampico Banking

Tampico Fuel Oil

Boston Mex. Leasing

H. McKeever

Mex. Tex. Pet

Tamesi Pet. & Asph

Gobiorno de la Fed

Fom. del Sureste

Totals 132

(Cone

Loca-
tions

1
1

luded)

Drilling

Feb. 28,

1919

5

1

"i
i

■ i

' i
1

' i
"i

109

Pre
due
ing

' ']
1

I

2\t

- Potential Daily

Production
' in Cubic Meters
1 2,951.00

A

do

Total

ban- No. of

ned Wells

1 11

2

5 5

2 2

1

1

1

1

1

1 1

1

i

L 3.18
L 795.00
> 1,224.30

1

1

4

1 • 1

L 79.50

1 2
1

1

L 39.75
J 2.24
I 127.20
I 12,720.00

1
2
1
1
1

1 1

2 2

I 3.86

5 9

132

I 253,217.93

J13 1056

LARGE PRODUCERS OF KANSAS— WITH PRODUCTION.

DAILY PRODUCTION IN 1918

NAME

Augusta, El Dorado, Outside,
Barrels Barrels Barrels

Carter Oil Co

Carter & S. W. Oil Co

Magnolia petrol. Co

Mid-Kansas Oil Co ^.

Prairie Oil & Gas Co

Tidal Oil Co

Cosden Oil & Gas Co

Empire Gas & Fuel Co 12,041

Gypsy Oil Co

Monitor Oil & Gas Co

Oklahoma Prod. & Ref. Co. . . '.

Producers Oi 1 Co

C. B. Shaffer

Sinclair Oil & Gas Co

Totals

All other companies .

154

6,799

9,445

3,i26

2,108

747

47

1,073

1,562

12,041

31,376

18,812

1,539

220

31

83

1,502

1,940

21,580

71,025

1,613

14,643

13,000

Total,
Barrels

6,945

9,426

3,108

2,196

773

1,027

1,562

43 419

18,811

1,535

253

80

1,594

1,320

92,607
29,256

23,193 85,668 13,000 121,863

LARGE PRODUCERS IN CALIFORNIA.

Per Cent Proved Land, No.
OPERATOR Total Oil Acres of Wells

Associated Oi Co 9.1 7,347 1,708

Doheny (various companies) 7.3 4,286 348

General petroleum Corporation 4.3 2,584 400

Honolulu Consolidated Oil Co 1.3 2,701 35

A. T. & S. F. Ry. (oil subsidiaries) 4.0 3,097 12

ShellCo. of California 6.8 2,442 236

76 BULLETIN NUMBER SIXTEEN OF

C4SINGHEAD GASOLINE MANUFACTURERS.

Name Address Plant

CALIFORNIA .

American Gas Co 1005 Central Bldg., Los Angeles Santa Mana

^TZToTco"-.:: Sn I W HelWn Bldg F^lmore

Gllm:"e''A"F "ci"' : . 700 VaTfes Bldg.. Los Angeles Z ; : ! ! ! Los Angeles

Huriev Smith Co 339 Consol. Realty Bldg., Lcs Ange es Brea

H^ Pv Sm th Co 339 Consol. Realty Bldg., Lcs Angeles near Sherman Jet.

li Habra GaLohne Co: . . .... 339 Central Realty Bldg.. Lcs Angeles .Brea

h Sab a Crsollne Co. 339 Central Realty Bldg., Los Angeles. .Maricopa

La Habra Ga.soline Co 339 Central Realty Bldg Los Angeles. .Taft

Olie Crude Oil Co 2827 LaSalle Ave., Los Angeles S?."T^ ^

Olinda Gasoline Co Van Nuys Bldg.. Los Angeles . Ohnda, Orange Co.

Pacific Gascline Co 501 I. W. Hellman Bldg., Los Angeles. . . .Brea

Purity Gasoline Co 339 Consol. Realty Bldg., Los Angeles Bicknell

Rancho La Brea Oil Co . 908 Merch. Natl. Bank Bldg., Los Angeles.Los Angeles

Richfield Oil Co 933 Van Nuys Bldg.. Los Angeles Maricopa

Sunset Gasoline Co 932 Van Nuys Bldg.. Los Angeles Taft

Union Oil Co. of California. . .Union Oil Bldg., Los Angeles Avila

Union Oil Co. of California. . Union Oil Bldg., Los Angeles Brea

Union Oil Co. of California Union Oil Bldg., Los Angeles Maltha

Union Oil Co. of California Union Oil Bldg.. Los Angeles Oleum

Union Oil Co. of California. . Union Oil Bldg.. Los Angeles Santa Paula

Union Oil Co. of California. . Union Oil Bldg.. Los Angeles San Pedro

Ventura Refining Co 458 S. Spring St.. Los Angeles Fillmore

Wilshire Oil Co 2455 E. Market St.. Los Angeles Fellows

Honolulu Consol. Oil Co 120 Market St., San Francisco Kern Co.

New Pa. Petroleum Co Santa Maria Santa Maria

COLORADO
Midwest Refining Co First National Bank Bldg., Denver Salt Creek, Wye.

DELAWARE
Leonard Oil Co 901 Market St., Wilmington Cherry Grove, Pa.

ILLINOIS

Vacuum Oil Co West Chestnut St., Bridgeport

Atla.s Oil Co 144 S. Wabash Ave., Chicago Shreveport, La.

Atlas Oil Co 144 S. Wabash Ave., Chiacgo Monroe, La.

Royalties Corporation 140 S. Dearborn St., Chicago Lenapah, Okla.

Central Refining Co Lawrenceville Lawrenceville, 111.

KANSAS

Continental Oil & Ref. Co Independence Independence

I>>June Oil & Gas Co Independence Independence

Roth Gasoline Co p. O. Box 392, Independence Elgin, Kan.

KENTUCKY
Collier Oil & Gas Co West Liberty Cannel City, Ky.

LOUISIANA

Standard Oil Co. of Ixjuisiana Baton Rouge Northern Louisiana

A»«)c. prod. & Ref. Corp Shreveport Commercial Bank Bldg Mansfield. La.

Awtoc. prod. & Ref. Corp Shreveport Commercial Bank Bldg Monroe, La.

( entral Oil & Ga.soline Co Shreveport Vivian, La.

,. ^^ ,. ^, , MASSACHUSETTS

Cabot. Godfrey L Boston West Va. and La.

..„,.„ MISSOURI

aIu V.T r "/• J°^2 Baltimore Ave., Kansas City Delaware, Okla.

AllBM I'., roleum ( o .1012 Baltimore Ave.. Kansas City Jennings, Okla

D..w..y Portland Cement Co.. Mutual Bldg.. Kansas City . Dewey Okla

lulT?, ;"■•"""" ." 1012 Baltimore Ave., Kansas City [ ! Jenks, Okla. '

)^«mo ,.l(,a.ohn.. ( o 1012 Baltimore Ave., Kansas City Nowata, Okla.

u" "'l ,''""""*^ " ='24 Kialto Bldg., Kansas City. .... Bixby Okla

L»k.- ..rk K..|.„,nK Co 324 Rialto Bldg., Kansas City. (2) Sapulpa Okla

i"ll..'si :: "o"!? •:: ^^l commerce Bldg.. Kansas City. . . . . : . Neodesha^ Kas

w»«K" <.K.K.,l,n.- < o 1012 Baltimore Ave.. Kan.sas City Ochelata, Okla.

T.-.I fiiif NEW YORK

rlr ..V ) I " •„ Vr u"\ ^'- ^a^-'^'i} Dewey, Okla.

Polti-r ( L. r . .f,' i^oa'lway. New York City

^"'"^ ''""'" 2' K- "Oth St., New York City Shinglehouse, Pa.

KANSAS CITY TESTING LABORATORY 77

CASINGHEAD GASOLINE MANUFACTURERS— Continued.

Name Address Plant

OHIO

Buckeye State Gas & Fuel Co . Coshocton near Coshocton

Medina Gas & Fuel Co P. O. Box 390, Wooster Mansfield, Ohio

OKLAHOMA

Cull nan Oil Association Ardmore near Ardmore

Dahlgren, Paul F 227 Masonic Temple, Bartlesville Bigheart, Okla.

Dahlgren, Paul F 227 Masonic Temple, Bartlasville Osage Junction

Foster, H. V 202 Masonic Temple, Bartlesville Bigheart

Foster, H. V • 202 Masonic Temple, Bartlesville Osage Junction

Foster & Davis, Inc 227 Masonic Temple, Bartlesville Osage, Okla.

Foster & Norwood Oil Co 227 Masonic Temple, Bartlesville Bigheart

Phillips Petroleum Co Bartlesville Washington and

Osage Co.

Four Gasoline Co Bixby near Bixby

Aureli US-Thomas Gasoline Co. Box 707, Drumright Drumright

Rav Flood Gas Co Drumright Lawton

Champlin Refining Co First National Bank Bldg., Enid. . . near Enid

Peppers Gasoline Co Rm. 9, First Natl. Bank Bldg., Enid near Enid

Lawton Refining Co Lawton Lawton

Barnes Oil & Gas Co 712 Barnes Bldg., Muskogee

Boynton Oil & Gas Co Muskogee

Motor Gasoline Co Muskogee near Muskogee

Seaboard Oil & Gas Co Muskogee Okmulgee Co.

Stoutz Bros Box 1433, Muskogee near Muskogee

Childers Gasoline Co Nowata Nowata

Henderson Gasoline Co Nowata near Delaware

All-American Oil & Gas Co. . . .816 Colcord Bldg., Oklahoma City Healdton field

Triumph Gasoline Co 209 Mercantile Co., Oklahoma City Okmulgee Co.

Kingwood Oil Co 316 Parkinson Bldg., Okmulgee Okmulgee, Okla.

Kingwood Oil Co 316 Parkinson Bldg., Okmulgee Weleetka, Okla.

Okmulgee Prod. & Ref. Co. . . 505 S. Boulder Ave., Okmulgee Bartlett, Okla.

Okmulgee Prod. & Ref. Co . . 505 S. Boulder Ave., Okmulgee Kusa, Okla.

Bluff Gasoline Co Sapulpa Sapulpa

Brighton Gasoline Co Berryhill Bldg., Sapulpa near Sapulpa

Akin Gasoline Co 503 Exchange Natl. Bank Bldg., Tulsa. Bartlesville

Akin Gasoline Co 503 Exchange Natl. Bank Bldg., Tulsa. . Bartlesville

Akin Gasoline Co 503 Exchange Natl. Bank Bldg., Tulsa. . Bixby

Benmo Oil Co 420 S. Cheyenne St., Tulsa Bald Hill

Bixby Gasoline Co Tulsa near Bixby

Boynton Gasoline Co Kennedy Bldg., Tulsa near Tulsa

Chestnut & Smith Corporation 306 Exchange Natl. Bank Bldg., Tulsa. Okla., Kas. & Texas

Cloco Gasoline Co 401-15 Unitv Bldg., Tulsa Shamrock, Okla.

Clover-Dietz Gas Co 409 Unity Bldg., Tulsa Mohawk, Okla.

Consumers Oil & Refining Co. Tulsa Broken Arrow

Cosden & Co Tulsa Stone Bluff

Cosden & Co Tulsa Gushing field

Cosden & Co Tulsa Garber field

Elliott, W. C 420 Palace Bldg., Tulsa Sperry, Okla.

GiUiland Oil Co First National Bank Bldg., Tulsa Gushing

Gilliland Oil Co First National Bank Bldg., Tulsa Shamrock

Gilliland Oil Co First National Bank Bldg., Tulsa Oilton

Gilliland Oil Co First National Bank Bldg., Tulsa Drumright

Gillilnad Oil Co First National Bank Bldg., Tulsa Bigheart

Gilliland Oil Co First National Bank Bldg., Tulsa Burkburnett, Tex.

GiUiland Oil Co First National Bank Bldg., Tulsa Homer, La.

Highway Oil Refining Corp. . . .207-8-9-10-11 Lynch Bldg., Tulsa Red Fork, Okla.

Highway Oil Refining Corp. . . .207-8-9-10-11 Lynch Bldg., Tulsa Jenks

Highway Oil Refining Corp. . . .207-8-9-10-11 Lynch Bldg., Tulsa T>eonard

Highway Oil Refining Corp. . . .207-8-9-10-11 Lynch Bldg., Tulsa Broken Arrow

Highway Oil Refining Corp. . . .207-8-9-10-11 Lynch Bldg., Tulsa Okmulgee (2)

Highway Oil Refining Corp. . . .207-8-9-10-11 Lvnch Bldg., Tulsa Beggs (3)

Highway Oil Refining Corp. . . .207-8-9-10-11 Lynch Bldg., Tulsa Kellyville

Hope Gasoline Co 1005-13 Kennedy Bldg., Tulsa Turkey Mountam

Hygrade Pet. & Gasoline Co. .1005-13 Kennedy Bldg., Tulsa Stone Bluff

Hygrade Pet. & Gasoline Co. 1005-13 Kennedy Bldg., Tulsa (Wagoner Co.)

Hygrade Pet. & Gasoline Co. .1005-13 Kennedy Bldg., Tulsa Bird Creek pool

Hygrade Pet. & Gasoline Co.. .1005-13 Kennedy Bldg., Tulsa Avant (Osage Co.)

Hygrade Pet. & Gasoline Co.. .1005-13 Kennedy Bldg., Tulsa Hogshooter pool

Hygrade Pet. & Gasoline Co. .1005-13 Kennedy Bldg., Tulsa (Bartlesville)

78

BULLETIN NUMBER SIXTEEN OF

CASIXGHEAD GASOLINE MANUFACTURERS (Continued)

Name Address Plant

OKLAHOMA
Hygrade Pet. & Gasoline Co. . 100_^1| Kennedy Bldg Tulsa . . . , . . -^^f^^- K-^^,^

Indian Gasoline Co o38-9 Kennedy mag., i u Gushing field

Jefferson Gasoline Co :}rrt ,' ii j„ -r.-'icci

&S-SS1 o„ CO. : :MrS£dJ&.; Tuu.;.:: : : : :c>.^. »... «,
SiSlS oal cS'c'i""' : . : : p 5>ifo7-'¥,i.: :::::;:::;:;:;;.: Bu,kbu„.t.. Tex.

Midco Gasoline Co Midco B dg., Tuba Uewey

Moon Gasoline Co Tulsa . ■ „,_ . ^ Bixby field

Kowata Oil & Ref Co 206-8 Cheyenne Ave., Tulsa

Oil^t^te Gat.line Co 407 Kennedy Bldg., Tulsa Jenks & Beggs

8^a'pXo?& Gas^'oUn^Co: . :SNational Bank Bldg.. Tulsa..: l ! l ! .Bixby ^J?^VlJl-

Cleveland, Glenn
Pool, Haywood,
Spur, Jenks, Mo-
hawk, Wateva,
Standard Spur,
Stone Bluff.

Okla. Prod. & Ref. Corp O. P. & R. Bldg., Tulsa

Old Dominion Oil Co 810-13 Mayo Bldg., Tulsa Yale, Olda.

Olsan Bros Tulsa .^ - . • . ^ • Broken Arrow

Pleasant Hill Oil Co 318-9 Cent. Natl. Bank Bldg., Tulsa Drumnght

Revere Oil Co., Ltd 2131$ S. Boston St., Tulsa

Samallen Oil Co 502 Exchg. Natl. Bank Bldg., Tulsa Bixby Dewey, Bar-
ties ville

Sapulpa Refining Co Sapulpa Drumnght

Scaw Oil Co Tulsa . . Tulsa field

Sinclair Oil & Gas Co Sinclair Bldg., Tulsa

Stebbins Oil & Gasoline Co. . . Box 1970, Tulsa Inola and Boynton

T. B. Gasoline Co First National Bank Bldg., Tuka Nowata field

Tidal Gasoline Co 602 S. Cheyenne ST., Tulsa Delaware, Nowata

Ochelata, Drum-
right

ToK-m Gasoline Co Tulsa Jenks

Triangle Pet. & Gas. Co Tulsa near Bixby

Tulsa Gasoline Co Bank of Commerce Bldg., Tulsa Glen Pool

Victor Gasoline Co Tulsa Gushing field

Walker, p. G., Jr 307 Cosden Bldg., Tulsa Boynton

Western Oil Corporation 504 Cosden Bldg., Tulsa Burkbumett, Tex.

HarriH, W. A. and J. A Wagoner, Okla Wagoner

PENNSYLVANIA

Bradford Oil & Gasoline Co. . .287 Congress St., Bradford Bell's Camp

fiilmoH' Gajtoline Co Bradford Gilmore, Pa.

Gilmore Ga.soljne Co Bradford Wafferty Hollow

Jellenton Gasoline Co 43 Main St., Bradford Limestone, Ohio

Kane Oa-wline Co 101 Main St., Bradford Kane, Pa.

I'enn«ylvania Gasoline Co 9 Main St., Bradford Bradford, Pa.

penmtylvania Gasoline Co 9 Main St., Bradford Bolivar, B. Y

Sloan & Zook f^o. of Ohio 101 Main St., Bradford Carrollton, Ohio

Stroud, H. B. Co 130 Main St., Bradford Coleville, Pa.

Warren GaHoline Co 101 Min St., Bradford Eldred, Pa.

Vogt, C.J Bruin, Pa Bruin, Pa.

Johnw.n & Ounlap Chicora, Pa Chicora, Pa.

Ililfhland Oil Co Clarion, Pa

Home (Jan Co Clarion, Pa .'..'.'.'..

Jane ( )j| ( V) Emlenlon, ¥&.......'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'..'. Emlenton, Pa.

Baru- * Snov, Karns City, Pa Butler Co.Pa.

< rawford Oil & Cas Co Meadville . . . . Friendly, W. Va.

C»»iinifhea'l C.ai, fo Oil City Oil City

7."",' •■ • Finance Bldg., Philadelphia

'•"• ,.ie Oil Co Union Bank Bldg., Pittsburgh Billings, Okla.

KANSAS CITY TESTING LABORATORY 79

CASINGHEAD GASOLINE MANUFACTURERS (Concluded)

Name Address Plant

PENNSYLVANIA

Hope Natural Gas Co 424 Sixth Ave., Pittsburgh West Virginia

Imperial Oil & Gas Prod. Co.. .1106 Union Bank Bldg., Pittsburgh Hannahdale, W.Va.

Laughner, E. E 1107 Standard Life Bldg., Pittsburgh. . . .near Ambridge, Pa.

Manufacturers Light & Heat Co.248 Fourth Ave., Pittsburgh West Virginia

Ohio Fuel Oil Co 2017 Farmers Bank Bldg., Pittsburgh. . . .West Virginia

Penn. Mex. Fuel Co 424 Sixth Ave., Pittsburgh Tuxpan, Mex.

Showalter, J. B Pittsburgh Butler Co., Pa.

Transcontinental Oil Co Benedum-Trees Bldg., Pittsburgh

Wavne Naphtha Co 308 Columbia Bk. Bldg., Pittsburgh near Waynesburg, Pa.

Haskell, H. H Pleasantville Venango and War-
ren County, Pa.

Deerlick Oil Co Russell

Wolcott Gas Co Shinglehouse Shinglehouse, Pa.

Tidioute Refining Co Tidioute Warren Co., Pa.

Warren Oil Co., of Pa Warren, Pa Henrys Mills, Pa.

Henry Farm Oil Co Warren, Pa Warren

Pavania Oil Co Warren, Pa

Sayre, J. J West Sunbury Forest Co., Pa.

TEXAS

DeSoto Gasoline Co P. O. Box 929, Beaumont Goss, La., Musko-
gee and Wann,
Okla.

Higgins Oil & Fuel Co Beaumont Caddo, La.

Lone Star Gas Co Fallas Petrolia, Tex.

Panhandle Refining Co 1412 Royal St., Dallas

Phoenix Oil Co 411 F. & M. Bank Bldg., Ft. Worth Erath Co., Tex.

Higgins Oil & Fuel Co Scanlan Bldg., Houston Daddo Field, La.

Humble Oil & Ref. Co Coggan Bldg., Houston Iowa Park,

Healdton, Okla.

Parties & Jones P. O. Box 84, Ranger Ranger District

Ranger Gulf Corp Ranger Burkburnett, Tex.

Grayburg Oil Co Box 1097, San Antonio Somerset, Tex.

Internat'l Petroleum Co 234 Bedell Bldg., San Antonio White Point, Tex.

UTAH
Utah- Wyoming Consol. Oil Co.McIntyre Bldg., Salt Lake City Byron, Wyo.

WEST VIRGINIA

Transylvania Oil & Gas Corp. Day and Night Bldg., Huntington Lawrence Co.

O'Brien, Wm New Cumberland — same

Petterson Bros. Co Parkersburg Elizabeth, W.Va.

Robert Bros Parkersburg Burning Spring,

W.Va.

McKelvy Oil & Gas Co Sisterville West Virginia

LaSalle Oil & Gas Co 93 11th St., Wheeling Jefferson Co.

Penn.-Ky. Oil & Gas Ref. Corp.City Bank Bldg., Wheeling Hancock Co., W.Va.

WYOMING

Enalpac Oil & Gsa Co Casper Mineral Wells,

Desdemona and
Burkburnett, Tex.

so

BULLETIN NUMBER SIXTEEN OF

STANDARD OIL CO. (N. J) AND SUBSIDIARIES CON-
SOLIDATED GENERAL BALANCE SHEET.

DEC. 31, 1918.

Assets.

Total value of plant stable and floating equipment ^^_^^

(less depreciation) 23 009 449 64

Stock in other companies Zd,uuy.44y,D*

Government bonds and other investment

securities *^ 9^,4t.^,ciby./ j

Inventories of merchandise 160,505,280.15

Accounts receivable 151,320,085.90

r^^}, 13 201,851.66

'"^^" : 418,479,587.48

Total assets $691,316,969.04

Less accounts payable ...- $116,816,714 77

Marine insurance reserves - 11,957,228,46 „

Net value --- $562,543,025.81

Nominal Liabilities.

Capital stock - $ 98,338,300 00

Reserve for annuities 492,315.84

Surplus including reserve for working capital 463,712,409.97

$562,543,025 81

STATEMENT OF EARNINGS AND DIVIDENDS FOR THE YEARS

1912-1918 INCLUSIVE, WITH INCOME AND WAR TAXES

DEDUCTED FROM THE EARNINGS OF THE YEAR

ON WHICH SAME WERE CALCULATED. (S. O. Co.)

Year
1912
I'JIU
1UI4
VJ}h
]'.nr,
l!tl7
lUIK

•Under "Dividunds paid" for the year 1913 there is included the
distribution of $40 per share made from repayments by former sub-
.sidiaries of cash which had previously been advanced by this com-
pany.

11918 taxes subject to adjustments.

Earnings Before

Federal Taxes

Earnings After

Dividends

Deducting

Paid and

Deducting

Paid

Federal Taxts

Accrued

Federal Taxes

.*:i.5,:i<»7,717.:J7

289,830.33

$35,107,887.04

19,667,660

■Ifi, 168,955. 06

7,085.57

45,691,869.49

*59,002,980

31,898,849.62

341,215.45

31,457,634.17

19,667,660

61,396,922 73

619,679.39

60,777,243.34

19,667,660

72,126,692.36

1,634,633.19

70,792,059.17

19,667,660

105, 785,8.58. 91

25,019,916.97

80,765,941.94

19,667,660

101,614,143.84

t44,330,359.15

57,283,784.69

19,667,660

KANSAS CITY TESTING LABORATORY

81

BY-PRODUCT COKE PLANTS IN UNITED STATES
CANADA (BENZOL PRODUCERS).

OWNER OR OPERATOR

LOCATION

Coal
Used

Calhoun Gas Co Battle Creek, Mich 36,000

Ford Motor Co Detroit, Mich 864,000

Semet-Solvay Co Detroit, Mich 1,343,300

Michigan Light Co Flint, Mich 96,400

Michigan Light Co Kalamazoo, Mich 43,800

Michigan Alkali Co Wyandotte, Mich 94,000

Minnesota Steel Co Duluth, Mich 600,000

Zenith Furnace Co Duluth, Minn 200,000

Minnesota By-Products Coke St. Paul, Minn 380,000

Laclede Gas Light Co St. Louis, Mo 320,000

Camden Coke Co Camden, N. J 360,000

Seaboard By- Product Coke Co Jersey City, N. J 340,500

Seaboard By-Product Coke Co Jersey City, N. J 681,000

Semet-Solvay Co Buffalo, N. Y 386,000

Empire Coke Co Geneva, N. Y 146,000

Solvay Process Co Syracuse, N. Y 65,000

Dominion Iron & Steel Co . .Sydney, N. S 720,000

Dominion Iron & Steel Co Sydney, N. S 1,664,000

Nova Scotia Steel & Coal Co Sydney Mines 159,000

Dover By-Products Coke Co Canal Dover, Ohio 120,000

United Furnace Co Canton, Ohio 280,000

Cleveland Furnace Co Cleveland, Ohio 450,000

River Furnace Co Cleveland, Ohio 1,300,000

American Steel & Wire Co Cleveland, Ohio 1,150,000

Hamilton Otto Coke Co Hamilton, Ohio 240,000

Ironton Solvay Coke Co Ironton, Ohio 432,000

National Tube Co Lorain, Ohio 1,320,000

Portsmouth Solvay Coke Co Portsmouth, Ohio 770,000

Toledo Furnace Co Toledo, Ohio 560,000

Brier Hill Steel Co Youngstown, Ohio 520,000

Republic Iron & Steel Co Youngstown, Ohio 1,020,000

Youngstown Sheet & Tube Co Youngstown, Ohio 1,300,000

Youngstown Sheet & Tube Co Youngstown, Ohio.

Steel Co. of Canada Hamilton, Ont

Algoma Steel Co Sault Ste. Marie, Ont .

Algoma Steel Co Sault Ste. Marie, Ont .

Philadelphia Subiu-ban Gas & Electric Co. Chester, Pa

Carnegie Steel Co Clairton, Pa

Carnegie Steel Co Clairton, Pa

Semet-Solvay Co Dunbar, Pa

Carnegie Steel Co Farrell, Pa

Allegheny By-Products Coke Co Glassport, Pa .

650,000
342,000
285,000
681,000
125,000
4,000,000
800,000
280,000
830,000
260,000

Jones & Laughlin Steel Co Hazelwood, Pa 2,000,000

Cambria Steel Co Johnstown, Pa 529,200

Cambria Steel Co Johnstown, Pa 1,529,500

Bethlehem Steel Co Lebanon, Pa .

Bethlehem Steel Co Steelton, Pa

Bethlehem Steel Co Steelton, Pa

Lehigh Coke Co South Bethlehem, Pa .

Providence Gas Co Providence Gas Co . . .

Memphis Gas & Electric Co Memphis, Tenn

Seattle Lighting Co Seattle, Wash

Fairmount By-Products Co Fairmount, W. Va. . . .

LaBelle Iron Works Follansbee, W. Va . . . .

National Tube Co Benwood, W. Va

Northwestern Iron Co Mayville, Wis

Milwaukee Coke & Gas Co Milwaukee, Wis

Northwestern Iron Co Mayville, Wis

Chattanooga Coke & Gas Co Chattanooga, Tenn. . . .

887,000
375,000
516,000
2,400,000
240,000
59,000
48,600

610,606
270,000
320,000
732,000
197,000
173,000

AND

Coke

Made

25,300
622,000

1,009,000

67,500

30,700

65,800

450,000

144,000

273,600

240,000

252,000

255,350

510,700

289,500

102,200

45,000

518,400

1,198,080
110,000
87,600
204,400
337,500
949,000
839,500
168,000
270,000
963,600
559,900
408,800
397,600
744,600
949,000
474,500
260,400
217,000
510,700
87,500

2,800,000
560,000
173,600
581,000
195,000

1,300,000
338,888

1,223,700
638,000
270,000
371,500

1,920,000

172,800

41,300

29,200

445,366
189,000
230,400
549,000
147,000
124,000

82

BULLETIN NUMBER SIXTEEN OF

PETROLEUM PRODUCING COMPANIES OF TEXAS FOR 1921.

The following producing companies, partnerships and individ-
uals operating in the state of Texas, by their sworn statements have
reported to the Oil & Gas Department of the Railroad Commission,
their gross oil production and value of same for the months of Jan-
uary, February and March, 1921.

Total production was 22,693,414.47 bbls. and the sales value of
same, $48,032,959.11.

Number of companies, partnerships and individuals that have
reported to date 680 as against 709 for the last quarter of 1920.

The Humble Oil & Refining Co. of Houston for the first quar-
ter of 1921 was first in production, 3,766,622 bbls., value $6,943,956.
The Texas Co. was second in value, $5,404,692 and third in produc-
tion, 2,608,512 bbls. The Gulf Production Co. third in value, $5,026,-
030 and second in production, 2,783,376 bbls.

For the last quarter 1920, the Texas Co. was first in produc-
tion 4 072,104 bbls, value $12,805,648. Gulf Production Co. was sec-
ond 2,742,108 bbls., value $8,661,216. Humble Oil & Refining Co.
was third with 2,954,747 bbls., value $8,213,768.

Total production in the last quarter of 1920 was 23,689,504 bbls.
valued at $76,168,108.

Company Location

Afom Oil Co Beaumont

American Texas Oii Co Somerset

ApDle. C. B Wichita Falls

Apple, S. A., E. Dunlap & Sykes

Ardmore, Okla.

Apple, Uunlap & Claude Bell. Ardmore, Okla.

Arcade Oil Co Beaumont

Arkajisas-Texas Co Little Rock, Ark.

Ameriran tU-fining Co Wichita Falls

Andorer Texas Oil & Drilling Co

Wellsvllle, N. T.

.\rmstrunit. Jas. R Wichita Falls, N. T.

Aclanui (111 Co Wlcliita Falls, N. Y.

.Vshley & AHliley McKinney

Atlantic Oil Co Philadelphia, Pa.

Argonaut Oil Co Fort Worth

AMoclatrd Oil Co Wichita Falls

.\malKamat«d Oil Co Houston

A No. 1 OII Co Lawlon, Okla.

Ada-nvllo Oil Co Independence, Kas.

Adam*, D. C Aurora, Mo.

Alajc Oil Co Dallas

Ardlzzona-Hraden Oil Co Dallas

Anna Belle oil Co Fort Worth

American f»ll Kngineering Corporation

• ■■ Fort Worth

AllcB Oil Co Tulsa. Okla.

All-Amerlcan Oil & Oas Co

Oklahoma City, Okla.

Amorlcan Ounaolldated Oil Co

Oklahoma City, Okla.

AnUllry, J, n j,„ur L^^g

MiFX r'iiln>li-um Co... New York City, N. Y.

Arkiiiaax .Votural Gai Co PltLsburRh Pa

AlllM Oil Co Wichita Falls

llniu.n. Mm. n,-wie y Houston

Mrrcki-nrldiio Crude Oil Syndicate

Brcckcnrldg*

l.--k Jl Oil Syndicate Bre-kcnrldRe

HrtHlerlck. A.J Now York City N Y

Buhara. M. J Wichita Falli

Company Location

Barkley & Meadows Wichita Falls

Burnett -Van Cleave Oil Co Wichita Falls

Wm. Bartlett Co Electra

Bell Bros. & McDonald Eastland

Birkeland, K. B Humble

Baker Oil Co. of Houston Houston

Burgess, Burgess, Chrestman & Brundldge. .

Dallas

Bradley Co Fort Worth

Burk Venus Oil Co Dallas

Brock Lundy Oil Co Bowie

Buchanan, S. B Batson

Bullington, Orville Wichita Falls

Bell Burke Oil Co Waco

Brooks & strong Breekenridge

Bass Petroleum Co Houston

Birkeland, K. B Minneapolis, Minn.

Buffalo-Texas Oil Co Buffalo, N. Y.

Burk Noel Oil Co Wichita Falls

Bell Burke Oil Co Waco

Big Four Oil Co Wichita Falls

Belen Oil Co Belen, N. M.

Burkbumett Oil Co Custer City, Okla.

Geo. Beggs Oil Co Fort Worth

Bowers & Witherspoon Palestine

Beverly Oil Co Wichita Falls

Bryan Oil Corporation Wichita Falls

Big Pool Oil Co Wichita Falls

Bailey-Winkler Oil & Gas Co. . .Breekenridge

Burk- Mack Oil Co Sheridan, Ind.

Breekenridge Production Co Breekenridge

Blue Bonnet Petroleum Co San Antonio

Brinkley Petroleum & Refining Co

Wichita Falls

Biggs Oil & Gas Co McKinney

Ba.ss & Dillard Wichita Falls

Bexata Oil Co San Antonio

Bowen Olympic Oil Co.. New York City, N. T.

B. B. Oil Co Electra

Bessley, Lincoln & McDonald Electra

Brooks Producing Co. No. 1 Wichita Falls

KANSAS CITY TESTING LABORATORY

83

PETROLEUM PRODUCING COMPANIES OF TEXAS FOR 1921.

(Continued)

Company Location
Brown & Co., Inc Dalla3

B. O. 0. G. Oil Co Iowa Park

Barkley, T. G Sour Laiie

Bankers & Merchants Petroleum Co

Fort Wortli

Belle City Oil Co Wichita Falls

Big i Consolidated Oil Co El Paso

Big John Oil Co Beaumont

Bower & Pillard Wichita Falls

Brown, Geo. I San Antonio

Buckeye Development Co Columbus, Ohio

Burney, I. H San Antonio

Castles Oil Co Corsicana

Chapman, O. H Waxahatchie

Calilwell Oil Co Oklahoma City. Okla

Commercial Petroleum Co San Antonio

Castell Oil Co Houston

Cooper. Henderson & JIartin. . . .Breckenridge
Continental Oil & Refining Co.. Tulsa. Okla.

Cactus Oil Co Fort Worth

Crown Oil & Refining Co Houston

Corsicana Oil & Refining Co Corsicana

Clara Oil Co Wichita Falls

Cornucopia Oil Co Fort Worth

Centerfield OU Co Wichita Falls

C. A. L. Oil Co Eastland

Connell. W. E. Fort Worth

Cohen & Lebow Wichita Falls

Christian, W. G Houston

Crescent Oil Co Wichita Falls

Cezreaux & Martin Humble

Craven Oil & Refining Co Jakeliamon

Clint Woods Oil Cori)oration. . .Wichita Falls

Consolidated Oil Co Cisco

Crosbie, T. S San Antonio

Crystal Oil Corporation Denver, Colo.

Crosbie. J. E Tulsa, Okla.

Comanche Northern Oil Co Fort Worth

Chappell Oil Co Denver, Colo.

Champliu & Winkler (T. & P. Co.) . .Thurber

Cheley. W. .T Denver, Colo.

Continental Petroleum Co Dallas

Considine-Martin Oil Co. San Francisco, Calif.
Central Texas Oil & Gas Association

De Leon

Crowell, L. R Dallas

Carteret Oil Co Fort Worth

Caroline Oil Co Nacogdoches

Central Oil Development Co Cisco

Chapman, P. A., .Tr Eastland

Consolidated Producing Co Fort Worth

C. H. B. C. Oil Co Breckenridge

Cooper-Henderson Oil Co Breckenridge

Cline Oil Co Wichita Falls

Camp Oil & Gas Co Fort Worth

Chenault, N. B Wichita Falls

Crosbie, J. E Tulsa. Okla.

Cabiness. C. C Wichita Falls

Canadian Park Oil Co Canadian

C. Y. T. Oil Co Beaumont

Cedar Creek Oil Co Houston

Clem Oil Co., Inc Houston

Colorado Oil & Gas Co Denver, Colo.

Comanche Duke Oil Co Fort Worth

W. F. Corts Drilling Co. .. .Columbus. Ohio

Cosden Oil & Gas Co Tulsa, Okla.

Cosa. Aubrey N Corsicana

Dale-Knotts Oil Co Wichita Falls

Duggan Oil Co Dallas

Duke of Dublin Oil Co Fort Worth

Daniel, W Wichita Falls

Developers Oil & Gas Co Wichita Falls

Davis. L. R Tulsa, Okla.

Company Location

Deibel Oil Co Thrall

Dale. E. A. (Perkins lease) Electia

Dominion Oil Co Wichita Falls

Danciger. M. O Wichita Falls

Double Standard Oil Co Wichita Falls

Dayton Oil Co Dayton, Ohio

Dennie Roberts Oil Co Wichita Falls

Dugueane Oil Co Eastland

Deep Sand Oil & Gas Co Corsicana

Deshler Oil & Refining Co Breckenridge

Denver Petroleum Co Denver, Colo.

Dalso Oil Co Mineral Wells

Doodlebug Oil Co Sour Lake

Elm Hill Oil Co Corsicana

Ellis & Anderson San Antonio

Ennis Oil & Development Co Ennia

Kconomy Oil Co Fort Worth

Erie Gas & Oil Co Huntington. Ind.

Eddy Oil Co Guffey

Eagle Petroleum Co Houston

Eaton, B. E Electra

Emerick Oil Co Wichita Falls

Empire Texas Oil Co Brocton, N. Y.

Ellis, Thos S San Antonio

East Batson Oil Co Batson

Eldorado Oil & Gas Co Ranger

Empire Gas & Fuel Co Bartlesville, Okla.

Evangeline Oil Co Brockton, N. Y.

Elliott, Jones & Co., Inc San Antonio

Foster. H. V., et al Bartlesville

Fensland Oil Co Fort Worth

Ferris-Seay Co Wichita Falls

Fisher & Gilliland Wichita Falls

Flynn-TutUe .Oil Co Electra

Fern Glen Oil Co St. Louis, Mo.

Frontit r Oil Co San Antonio

Fisher-Parker Oil Co Wichita Falls

Four &■ Four Oil Co Dallas

Franklin. J. M., et al Wichita Falls

Fox & Lamb Drilling Co Brownwood

Fidelity Oil Corporation Louisville, Ky.

Freedman, Alex Corsicana

Fowler. M Wichita Falls

Ferguson Wells No. 1 and No. 2

Wichita Falls

Forest Oil Co Wichita Falls

Fisher, Gates & Co Wichita Falls

Fiver Rivers Oil & Gas Co Wichita Falls

Franklin. Wirt Ardmore, Okla.

Parish & Ireland lease Houston

Farmer, Robt Wichita Falls

Ferguson, C. J Wichita Falls

Foster & Allen lease Wichita Falls

Foster & Watson Wichita Falls

Federal Oil Co Cleveland, Ohio

Freene Oil Co Wichita Falls

Farquherson Oil Co Wichita Falls

Findley-Minnick Oil & Gas Co. .. .Benjamin

Forty-One Oil Co Wichita Falls

Fletcher Oil Co Wichita Falls

Gulf Production Co Houston

Gabler & Brannon Eastland

Gladstone Oil & Refining Co Fort Worth

Galvez Oil Corporation New York City

Galloway Consolidated Oil Co Fort Worth

Gwynn. O. F. (trustee) Iowa Park

Gilliert Co Beaumont

Golconda Oil Co.. No. 2 Wichita Falls

Gonzales Creek Oil Co Houston

Goose Creek Oil Corporation Houston

Gotham Oil Association Fort Worth

Gatewfmd Oil Co Ennis

Glenridge Oil Corporation St, Xx)uis. Mo.

84

BULLETIN NUMBER SIXTEEN OF

PETROLEUM PRODUCING COMPANIES OF TEXAS FOR 1921.

(Continued)

Location Company ,^^fTu<

Jones, Thos. H ClevelanJ, Ohio

Japhet & Suthcrlaiul ■ • Houston

Company

Grisdale. J. A McInt>Te, Iowa

Glasscoik Leasing Syndicate. .. .San Antonio

GriswoM Oil Co Wichita Falls

Golden Cycle Oil Co Dalhart

Gatewood Oil Co Knnis

Galve/.-Burk Petroleum Co Galveston

Gulf Coast Oil Corporation Houston

Gates Oil Co Ardmore, Okla.

Gohlke & Gerard Wichita Falls

Great States Petrol. Co. of Texas Dallas

Gf tzicr, W. F Burkbumett

Gladiolus Oil Co Wichita FaUs

Gooih & Davis Tract No. 1 Lawton, Okla.

Goo<h & Davis Tract No. 2 Lawton, Okla.

Guffey-Gillespie Oil Co Pittsburgh, Pa.

Golciiiida Oil Co. No. 1 Wichita Falls

GiMilaiul Oil Co Tulsa. Okla.

Godfrey. F. L Enid, Okla.

Glenridge Oil Corporation S:. Louis. Mo.

Gallasher & Lawson Desdemona

Gladys IM'.e Oil Co Tulsa, Okla.

Grayburs Oil Co San Antonio

Grand Duke Oil Co Fort Worth

Greater Breckenridge Oil Co Breckenridge

(ialena Signal Oil Co. of Houston. .. .Houston

<;ul/liT A: Cottingham Bluffton. Ind.

Gat«, T. M Wichita Falls

Guaranty Oil & Gas Co Breckenridge

Granite Oil Co E'.ectra

Houston & Wel'h Abilene

lliio lliio Oil Co Burkbumett

lli-rri-n. II. H Breckenridge

llunilile Oil & Refining Co Hotiston

Kaninn, Jake L Ardmore. Okla.

Ilaney. U. O Wichita Falls

llar\cy Oil Co Wichita Falls

Hawkins. W. L Wichita Falls

Ibifim-lr & Deegans Dallas

Hum, J. C Wichita Falls

llalinack Oil Co Dallas

Houseman, H. D. Co Dallas

lll,-k-iiis on & Fuel Co Houston

1 1 V' I.'. Geo Houston

Mill k Jones Burkbumett

llil.y & Vrooman Electra

ll.ii i.lriy & Cttffell Beaumont

llluh-Lind Oil & Gas Co Electra

lI'MiKloii OH Co. of Texas Houston

Hilwila Copper Oil Co San Antonio

Hub Oil Co Dallas

11. .11-1. .n Production Co Houston

11 IM1I..I1 Krupp New York City

H.irr.ii, Ja*. G. (attorney) Brwkenridge

ll..tru..ri & Dale Wichita Falls

"•""■ Mwrs Trust Wichita Falls

ll.iii.itiin Oil tc Gas Co Marlow

M.-iMl,.r..,n, K. G ...Nowata

"»" '•'■'■• Brownwood

II. r.f.ird (III Co Electra

llm liiH ri'Hiiiirkp Constr. Co Dallas

"'"""" * WpHilielnier Ardmore, Okla.

"•>'""" Krupp New York Cily

I'''" <"l ••<• Fort Worth

I .< I I'nrk Proiluclng «'o i,nvu park

!''"'"' ."" •'" Wichita Falls

IrimUnil on Ic Gas Development Co

„■•■;•;•• Ouluth, Mli'in.

]'•' '" •;"••■ Wichita Falls

'"'■'"' ''••"•"'••um Co Plalnvlew

'•""', ..-^ ." Fort Worth

'"•."" '" New York City

lii»»d..r (Ml ft HcflnlnK Co. Munkogee Okla
Jai.rlirn on Co lulaa, okla!

.Tones Light Petroleum Co Pilot Point

John & ,Teff Oil Co Wichita Falls

Julia Oil Co Sour Lake

Jackson, J. S. (trustee) Sour Lake

Jackson Co San Antonio

Jeffers, S. L San Antonio

.Jefferson Oil Co Dallas

Kernp-Munger-Allen Oil Co Wichita FaHs

Kein, Frank D Wichita Falls

Kerr, T. P Corsicana

Koons DeU Tulsa. Okla.

King Petroleum Co Wichita Falls

Keoury Mike Waco

Knotts, F. F Wichita Falls

Keen & Woolf Co Shreveport, La.

Kirl-y, Harder R Austin

Kansas City Petroleum Co Wichita Falls

Kepley & Bright Wichita Falls

Kavanaugh Petroleum Co Houston

Kemp, G. G Vernon

Kentucky River Oil Co Fort W'orth

Keystone Drilling Co De Leon

Kauth Oil Co Wichita Falls

King Petroleum Co Milwood, West Va.

Keever & Gordon Oil Co Sour Lake

Kansas Gulf Co Chicago, III.

Kurz Oil Co Somerset

Lincoln Oil Co Electra

Levely-JIaxwell Oil Co Wichita Falls

Lesh Bros. Oil Co Wichita Falls

LaRue Oil Association Electra

Long, Taylor & Thomas Houston

Lou Ellen Oil Co Denison

Lone Star Gas Co Dallas

Low e Oil Co De Leon

Little Wonder Oil Co. .. .Bowling Green, Ky.

P. J. Lee & Co Wichita Falls

Le Sil Oil Corporation Wichita Falls

Lucky Seven Oil Co Wichita Falls

Lockhart, Parker & Glasscock Ranger

Landreth, E. A. Co Breckenridge

Lawton Oil Co Lawton. Okla.

Lowry Oil Corporation Muskogee, Okla.

Liberty Petroleum Co Wichita Fal's

Lone Star Oil Co Burkbumett

Lake Oil Co Beaumont

Louisiana- Stephens Oil Corporation

, .Fort Worth

Lake View Oil Co Sour Lake

Lincoln McDonald Oil Co Electra

Mahon, P. J. (receiver) Beauniont

Manhattan Oil & Refining Co.. Wichita Falls

Marathon Oil Co San Antonio

Martin Oil Co Beaumont

Mary D. Oil Co Sherman

.Mennis, G. W' Wichita Falls

Minor Oil Co Beaumont

Montour Oil Co Pittsburgh. Pa.

Mooney. L. E. (trustee) Wichita Falls

McDonald Oil & Gas Co. New Middleton, Ohio

McDowell, H. B El Paso

Mid-Kansas Oil & Gas Co Findlay, Ohio

Moore & McKinney Houston.

.Mulual Oil Co LaPorte

Miller. Herbert G Eastland

Medina Oil & Gas Co San Antonio

MiH)k Texas Co Fort Worth

Macr & Shappell Wichita Falls

McDorman. C. R Ardmore, Okla.

Montrose Oil Ref. Co Fort Worth

.Montrose Oil Ref. Co Fort Worth

KANSAS CITY TESTING LABORATORY

85

PETROLEUM PRODUCING COMPANIES OF TEXAS FOR 1921.

(Continued)

('umpaiiy Location

MrAIan Oil & Gas Co Tulsa, Okla.

Maigay Oil Corporation Tulsa. Okla.

Mi-15an Oil Co Wichita Falls

M'Allister & Brown Wichita Falls

5[cKen7.ie Oil Co Wichita Falls

Monarch Oil & Refining Co Houston

Metroiiolitan Oil Co Houston

Maxon Oil Co Wichita Falls

Mary Elizabeth Oil Co Dallas

Moiris & White Carbon

Matador Oil & Gas Co Quannah

Murphy Oil Co. of Pa Thrall

Mi-SQuite Oil Co Fort Worth

Meyers, Green, Wilson & Brannon

Wichita Falls

Mitchani & Morrison Fort Worth

Majestic Oil & Hefining Co Wichita Falls

McLain Oil & Coal Co Columbus, Ohio

McCamey, Geo. B Cross Plains

Mildren Oil Co Le.vington, Ky.

Mimet Oil & Gas Co Pittsburgh, Pa.

Moore, Edward T Dallas

Martin, G. A Humble

Mann & Ilseng (W. L. Mann) . .Wichita Falls

Mana-M-Pahil Oil Co Wichita Falls

Mann-Power Oil Co Wichita Falls

Mann Oil Co Wichita Falls

M. & P. Burke Extension Oil Co

Lawrence, Kansas

iloore. N. A Eastland

Moore, F. L Tulsa, Okla.

Madden & Madden Rising .Star

Mahlstedt-Mook Oil Co Fort Worth

McXamara Oil Co Beaumont

Minntex Oil Co Wichita Falls

Mitchell Producing Co Fort Worth

Mackenzie f )il Co Fort Worth

M & V Tank Co Wichita Falls

Mc:Goldriek, E. W Batson

Morrissey. Thos. & Heydrick, L. A.... Dallas

Monarch Petroleum Co Dallas

Mayfield. .Jos. L. Oil Co Wichita Falls

McQuaid, M. W Fort Worth

Magnolia Petroleum Co Dallas

Mack. Theodore Fort Worth

Markham. John H., Jr. & Tidal Oil Co.

(T & P) Tliurber

N'utt. Horace Austin

Xew Domain Oil & Gas Co Dallas

Northwest Oil & Gas Co Wichita Falls

Nineteen Oil Co Beaumont

Nortex Drilling & Development Co

St. Louis, Mo.

Necona Burk Oil Co Burkburnett

North American Oil & Ref. Corjioration . . .

Oklahoma City, Okla.

Nutt. Horace Austin

North Texas Oil Co Vernon

Norton & Cline Wichita Falls

Numljcr 77 Oil Co Wichita Falls

Northwest Burk Oil & Gas Co..Lawton, Okla.

Noble, Chas. F Wichita Falls

Natural Oil Co Wichita Falls

Nineteen Oil & Gas Co Wichita Falls

Nortex Drilling Co St. Louis, Mo.

Oil Dominion Oil Co Houston

Oriental f)il Co Dallas

O'Neill, H. A Wichita Falls

Odell Oil Co Wichita Falls

Oil Development Co St. Louis. Mo.

Oktaha Co Tulsa, Ok.

Old Colony Oil Co Dayton

Owon, Burkett & Wheeler Mineral Wells

Comjiany Location

Oil Development Co St. Louis, Mo.

Olil Colony i;nited Oil Co Wichita Falls

Osage Production Co Wichita Falls

Otex Oil Co Columbus, Ohio

Okla. Prod. & Ref, Corp. of America

Tulsa, Okla.

Okla. Petroleum & Gas Co. of Texas

Tulsa, Okla.

Old Dominion Oil Co Wichita Falls

Ohio Fuel Oil Co Pittsburgh, Pa.

Plateau Oil Co Fort Worth

Planet Petroleum Co Fort Worth

Pennok Oil Co Tulsa. Okla.

Petroleum Development Co Wichita Falls

Primrose Oil Co Houston

Placid Petroleum Co Wichita Falls

Powell, ,L h Wichita Falls

Perkins. J. J Wichita Falls

Pace, Geo. L Dallas

Palmer Oil Co Henrietta

Chas. Paggi & Co Saratoga

Portland-Texas Oil Co Wichita Falls

Paraffine Oil Co Beaumont

Pure Oil Co Columhus, Ohio

Phillips Bros Beaumont

Priddy, W. M Wichita Falls

Patton, H. H Fort Worth

Pierce Oil Corporation New York City

Paradox Oil Co Wichita Falls

Paine Oil & Refining Co Houston

Pioneer Oil Corporation Wichita Falls

Prairie Oil & Gas Co. .Independence, Kansas

Patton, H. H Fort Wortli

Panhandle Refining Co Dallas

Paris-Wichita Oil Co Paris

Pivoto, M. E Sour Lake

Pinto Oil Co Mineral Wells

Parker, Arthur G Eastland

Pipiiin Oil Co Brownvvood

P & M Oil Co Houston

Pilot Point Oil & Gas Co Pilot Point

Pioneer Producing Co Wichita Falls

Porter, Works & Hicks Wichita Falls

Southside Oil Co Wichita Falls

Staley, M. L Wichita Falls

Shackelford, F. L Wichita Falls

Sfrawii Petroleum Co Denver, Colo.

Silb-Erman Oil Co Wichita Falls

Schlicher Oil Co Sour Lake

Stephens Oil Co Sour Lake

San Diego Oil & Gas Co Alice

Sankey, John S Fort Worth

Speed, C. D Corsicana

Seibel Oil Co Wichita Falls

Seaystone Oil Co Wichita Falls

Sinims. E. F. & Co Houston

Sink. Jeel Corsicana

Southern Pelroleiun & Refining Co... Houston
Standard Oil Land & Leasing Co.. Beaumont

Sure Pop Oil Co Dallas

Sterling Oil Co Titusville

States Oil Corporation Eastland

Swensondale Oil Co Fort Worth

Shawmut Petroleum Corp., Inc.. Fort W<irth

Shappell. T. O Wichita Falls

Stump Oil & Refining Co Burkburnett

Saxon Oil Co Sour Lake

Slaughter & Hutchinson Bowie

Smoot, Geo. A Wichita Falls

Stull, R. O Wichita Falls

Shaffer-Mankin Dallas

Stella Oil Co Beaumont

Spencer Petroleum Co Cisco

86

BULLETIN NUMBER SIXTEEN OF

PETROLEUM PRODUCING COMPANIES OF TEXAS FOR 1921.

(Continued)

Cumiiany Location

Texas Amalgamated Oil Co Fort Worth

Tliomas. Leon Wichita Falls

T. Y. Oil Co Sour Lake

Texas Operating Syndicate Wichita Falls

Company Location

Snowden. Geo. il Wichita Falls

Su,, Qo Beaumont

Striblmg.' ' J. C. Houston

Star-Tex Petroleiun Co WichiU FaUs

Sipe-Tex Oil Co Moody

Seturity Oil Co Breckenridge

S<-hutt, R. K Wirhita FaUs

Silirian Oil Co St. Louis, Mo.

Schram. J. F Brenham

Simms Oil Co Dallas

Somerset Oil Co San Antonio

Sinclair Oil Co Houston

Sextettt Oil Co Lawton. Okla.

Sixty-Six Oil Co Wichita Falls

Seventy-Two Oil Co Wichita Falls

Superior Oil Co Superior, Wise.

Scanlon & McCourtie Dallas

Sioux Oil & Refining Co Wichita Falls

San Bernard Oil Co Beaumont

Southwestern Oil Development Co.. Eastland

Swastika Oil Co Beaumont

Smith-Hess Oil Co .' CisfO

Snowden & MrSweeney Co New York City

Seaboard Oil & Gas Co Muskogee, Okla.

Silk. W. W Wichita Falls

Street«r-Electra Oil Co Streeter, N. Dak.

Snider, C. W Wichita Falls

Standiford Bros Iowa Park

Sutherland, W. C. & Cox, C. B.Wichita Falls

Sun Co. (North Te.vas Division) Dallas

Skelly Oil Co Tulsa. Okla.

Southwestern Petroleum Co Tulsa, Okla.

Stevenson Lease (A. J. Powell) Waco

Shamrock Oil Co Wichita Falls

Sutherland Oil Co Houston

Skinner. E. W. OU Co Saratoga

Silver Lake Co Abilene

Suley. J. A Wicliita Falls

Texas Southern Oil Co San Antonio

Texola Petroleum Co Electra

Tarvcr Oil Co Dallas

Tidtwrt. .lohn Oil Co Midlothian

Texts-Virginia Oil Co Paris

Texas Oil Corporation Dallas

T.-vao Wcinder Pools Wichita Falls

T.-\m.x Oil Co Fort Worth

Th.imas. Mack Wichita Falls

Texa- Standard Oil Co Houston

Tr1;.'l.i-h. Ikanlfl Wichita Falls

T.xii., riii,.f Oil & Gas Co Wicliita Falls

Trl.iik-lc on Co Wichita Falls

T.-va.. Blue Bonnet Oil Asso Wichita Falls

P'"'""- W. H Austin

Tmm oh a Drilling Co Houston

Tidal Wi-Hti-m Oil Corp Tulsa, Okla.

1"" ['" Houston

Tpi« Pacific Coal & Oil Co Thurber

l^ '"• V" '" &<""• Lake

TMa» on Proiluelng Co Dallas

2:'"" ""/'" Sour Lake

Tr.i,«-oMtlnenul Oil Co PItlslnirgh, P.-i

l""'"" "" '■" Wichita Falls

T.-.lM.i>,a on St ReflnInK Co. .. .Wichita Falls
£'"■'"'*'" * M.KInnl.H Ranger

T ■."' ',;f:'", '"! •'" «"" Antonio

r..>»» oil A Land InveMmcnt Co.. Fort Worth

Tpx« p.. in,, c,,,! 4 on Co ThurUei

J ' '•, ," •• Fort Worth

7' l'dn|«l on Co nanas

'' ' ■ ''i <o Columbus, Ohio

T.fr.iii on Co P,"'.°

Tun.l«,w OU CoriKiratlon '.'.'.'.' Houston

Trxa, Kr.ler.1 Oil Co ! ! FJ^tra

Taylor, T. J & Sibley, S. W Wichita FaUs

Texana Production Co Fort Worth

Tri-Mutual Oil Development Co

Rapid City, S. Dak.

Texas Southern Oil & Devel. Co. San Antonio
United Drilling & Develop. Co.. Wichita FaUs

Unity Oil Co Beaumont

United Petroleum Co Chicago, 111.

United OU & Fuel Co Philadelphia, Fa.

Union .National Oil Co Houston

Lnderwriters Prod. & Ref. Co

Oklahoma City, Okla.

Underwood Drilling Co Wichita Falls

Universal Drilling & Develop. Co

\\'ichita Falls

Universal Texas Oil & Gas Co DaUaB

U n ited Oil Co Shreveport, La.

Victory Oil Producing Co.. Little Rock, Ark.

Vulcan Oil Co Tiffin

Van Cleave Oil Trust Wichita Falls

Volcanic Producing Co Brenham

Val Verde Oil Co Del Bio

Valley Oil Co Petrolia

Vat fJil & Gas Co Byers

Volunteer Oil Co Nashville, Teun.

A'enus Oil Co Denison

Virginia Oil Co Fort Worth

Vulcan Oil Co (T & P) Thurber

Williams, J. L Brownwood

Western Prod. & Drilling Co Wichita Falls

Wagonner, B. M Wichita Falls

Wood. Cranfield Wichita Falls

Western-Keoughhan-Hurst Syndicate

StravTO

Worth Oil Co Tulsa. Okla.

Wonder Oil Co Houston

Woods Oil Co Beaumont

Wood, C. C Wichita Falls

Wichita Clay OU Co Wichita FaUs

Wichita Petroleum Co Wichita Falls

Walker Consolidated Co Dallas

Wilson Breach Co Beaumont

Walker, B. S Breckenridge

Watkins Pool Oil Co Dallas

Waseco Oil Co Fort Worth

Waggoner, Abe W. (trustee 3) Houston

Waggoner. Abe W. (trustee 4) Hoiiston

Weber, Mark U Casper, Wyo.

Webb, W. G Albany

WichUa Burk Oil Co Wichita Falls

Winner Oil & Gas Co Wisner, Nebr.

Woodbum OU Corporation. .Philadelphia, Pa.

Witherspoon Oil Co San Antonio

Wilkoff, B. A. Syndicate Pittsburgh, Pa.

White, S. V Wichita Falls

Walker. P. G., Jr Tulsa. Okla.

Webb OU Co Humble

White & Scarbrough Burkbumett

Woodrow-Lee Trust Wichita FaUs

Wills & Garity Corsicana

Weona OU Co Burkburnett

Weitern Petroleum Co Vemon

Wyatt Oil Co Sour Lake

Webb, W. G Albany

U est Tennessee Lease Wichita Falls

West Virgmia Ranger OU Co

Charleston, West Vt.

Webb, J. R Corsicana

Wichita Southern Oil Prod. Co Houston

KANSAS CITY TESTING LABORATORY

87

PETROLEUM PRODUCING COMPANIES OF TEXAS FOR 1921.

(Concluded)

Company Location

Witr-her, W. C Wichita Falls

Westlieimer & Daube Ardmore. Okla.

Welden Oil Co Houston

Walker Caldwell Producing Co Dallas

Weber, Howard Bartlesville. Okla.

Company Location

Young. Simmons Drilling Co. .. .Wichita Falls

York Production Co Wichita Falls

Yount-Lee Oil Co Sour Lake

Young Bros. & Kennedy Wichita Falls

Y. M. C. A. Block Breckenridge

PETROLEUM PRODUCING COMPANIES OF OKLAHOMA

FOR 1P21.

Company Location

Aaronson, L. E. Z Tulsa

Abraham, Joe Bristow

Acme Oil Co Tulsa

Ackerman, F. T Tulsa

Advance Oil Co Fort Worth, Texas

Adams, E. H. , et al Okmulgee

Adams Oil & Gas Co Washington. D. C.

Aetna Petroleiun Co Pittsburgh, Pa.

Aiken Oil Co Xowata

Akin Oil Co Tulsa

Aladdin Oil Co Tulsa

Albion Oil Co Tulsa

Alexander-Shakely Petroleum Co Tulsa

Alluwe Oil Co Nowata

Almeda Oil Co Bartlesville

Almy, C. C Okmulgee

All- American Oil & Gas Co.. Oklahoma City

American Gas & Carbon Co Tulsa

American Oil Co Oklahoma City

Amerada Petroleum Co Tulsa

American Oil & Gas Co

Anderson & Simpson Ardmore

Anglo-Texas OU Co Okmulgee

Apex Oil & Gas Co Tulsa

Arthur Oil Co Sisterville, W. Va.

Arm Oil Co Walters

Argue & Compton Tulsa

Ashland Oil Co New York City

Atlas Petroleum Co Kansas City. Mo.

Ajlantic Petroleum Co Tulsa

Atlantic Petroleum Co Boston. Mass.

Atlantic Oil Prod. Co Philadelphia, Pa.

Aubyme Oil & Gas Co Garber

Ault & Boss Vinita

Avery, C. S Tulsa

Acme Oil Corp Tulsa

Avery Oil & Gas Co Tulsa

Avon Oil Co Tulsa

Aztec Oil Co Houston. Texas

B. Jack Oil Co Sapulpa

Bagley Oil & Gas Co Auburn, Xebr. ^

Banford Oil Co Tulsa*

Banowetz. M. 0 Coffeyville. Kas.

Baker Oil & Gas Co Independence, Kas.

Bass. C. W Tulsa

Bassett, W. O Okmulgee

Barber Oil Co Tulsa

Bartlesville Oil & Gas Co Bartlesville

Bartles-Johnson OU Co Bartlesville

Barbara Oil Co Okmulgee

Barnsdall Oil Co Bartlesville

Baughman, R. P Ponca City

Bay State Oil & Gas Co Kansas City. Mo.

Baxter, L. W Tu!sa

Beacon Oil Co., et al Bartlesville

Beatty, E. F Oil City. Pa.

Bell Oil & Gas Co Tulsa

Bell Oil & Gas Co Warren, Pa.

Belvy Oil Co St. Louis. Mo.

Benmo Oil Co Tuka

Company Location

Berger Oil & Gas Co Tulsa

Berry, B. H Tulsa

Best Prod. Co Okmulgee

Betty, G. Petroleiun Co Cement

Betty Ruth Oil Co Broken Arrow

Benedum Trees Oil Co Pittsburgh, Pa.

Big Sioux Oil & Gas Co Okmulgee

Big Fifty Oil Co Tulsa

Bigheart Producing & Ref. Co Tulsa

Biddle Oil Co Tulsa

Bird Creek Oil & Gas Co Tulsa

Bird Creek Oil Co Tulsa

Bird, Gaffney & Simons Bradford, Pa.

Billy Oil Co Chelsea

Black, E. L Henryetta

Black, Geo. E Pasadena. Calif.

Blackwell Oil & Gas Co Blackwell, Kas.

Bloch Oil Co Tulsa

Blue Ridge Oil & Gas Co Oklahoma City

Boesche. F. E. C Coffeyville. Kas.

Bolivar Run OU Co Tulsa

Bole. Geo Tulsa

Bokma Oil Co Chicago. 111.

Bradstreet, J. G. & Co Tulsa

Bradley OU Co Tulsa

Braik OU & Gas Co Henryetta

Braley, C. A Kansas City. Mo.

Brann, Jas. (receiver) Bartlesville

Brandes Oil Co Nowata

Breene. Frank M Tulsa

Breener Oil Co Pawhuska

Breene, Mabel V Tulsa

Bright. Samuel Okmulgee

Brilling, Geo. Co Tulsa

Bridgman Oil Co Xowata

Bridgman, Welsh & Haner Muskogee

Briggs, R Tulsa

Brown, F. B. & W. H Bartlesville

Brown Oil & Gas Co Tulsa

Brundred Oil Corp. of OU City, Pa.

Bruner Oil Co Independence. Kan.

Bucher Petroleum Co Bartlesville

Biu-ket, J. G Mineral Wells, Tex.

Burke Hoffeld OU Co Tulsa

Bull-Head Oil Co Ardmore

Bull Dog OU Co Tulsa

Bunvell, H. B Broken Arrow

Burton. N. S Ardmore

Bums. Robt Tulsa

Burt W. & Lyon M. J Joplin, Mo.

Butler & Lafferty Muskogee

Cabin Valley Mining Co ; Chelsea

Cala-Belle Oil Co Cement

Cameron. Mrs. Lillian Tulsa

Campbell. H. C Nowata

Campbell, A. P Wichita. Kan.

Campbell. H. B Welch

Canada Oil Co Nowata

Canary & Sinclair Denver, Colo.

Canary & Canary Denver, Colo.

88

BULLETIN NUMBER SIXTEEN OF

PETROLEUM PRODUCING COMPANIES OF OKLAHOMA
FOR 1921 (Continued)

Company Location

Canary-. J. D °'"'''' T^ua

Canary, S. C Tuls*

Cantield, W. E. & G. W -^ale

Cappeau. J. P XV V

Carr. J. M Okmu gee

Carr. M. L Okmulgee

Carlork & Pexter Ardmore

Carey Oil & Gas Co Wellsville. Ky.

Canit-'iter, I. 0 Mor"S

Carter Bros Tulsa

Carter Oil Co T" sa

Cassidy. Alice M Guthne

Cash Oil & Gas Co Nowata

Caswell. Clias. H

Catlett-Davis Oil Corp Tulsa

Celestine Oil Co Tulsa

Central Union Oil Co .Tulsa

Central Refining Co Tulsa

Central National Oil Co Okmulgee

Chamlierlain. H. G Marietta. Ohio

Chapman. 0. H Waxaliachie. Tex.

ChaJKller. T. A Viuita

Chapman. Fretl A Ardmore

Chicago Oil Co Chicago. HI.

Chief Bighcart Oil & Gas Co

Childers Gasoline Co

Nowata and Wichita. Kan.

rhinango Oil & Gas Co New York City

Choctaw Oil Co Tulsa

Cimarron River Oil & Gas Co. Oklahoma City

Clark. L. P Indejjendence. Kan.

Cleve Oil & Gas Co Bartlesville

('line Oil Co Wichita Falls. Tex.

Clover Oil Co Tulsa

Clover. Marvin K Tulsa

Coo. R. W Ardmore

Collhis Oil Co Vinita

Ciiliiie Oil Co Ardmore

Columhla Petroleum Co Oklahoma City

CommoMHialth Oil Co Warren, Pa.

Commercial Refining Co Wichita, Kan.

Ciimolop Oil Co Tulsa

Compton, ct al Independence. Kan.

Concord Oil Co Oklahoma City

Congri-ss f»ll Co Kansas City. Mo.

Cimsumcrs (111 Co., ct al Okmulgee

Ciiinlnemal Oil Co Independence, Kan.

Ccinliiicntal Oil Co Okmulgee

Corner, Akin & Argue Bartlesville

Corlnc Oil & Oa» Co Guthrie

• •iTnriBdii Oil tc (Jas Co Cleveland

(••■rhlri Oil & Gas Co Tulsa

Comlcn & Co Tulsa

foiMlcn on tc Oag Co Tulsa

Conmo* (III Co Okmulgee

(•••lion Farm Oil Co Independence, Kan.

C'liiioii Belt Petroleum Co Ardmore

'■ " "" Co Garher

«..«|.., ic l,»wlon Nowata

""■' •»" Co Tulsa

" '"■ *• W- » Ardmore

< ' III.' tc IiavlH Ttilsa

' "■ • "'"''s. ct al !.".'! !!!TuIsa

' ' " '■ * '*"""'■ Ardmore

' ' '*'"*"> * Cruco Ardmore

' ■" '•" Co Itochestcr, N. Y

C.PIUI on Cm Okmulgee

"" '" Inilopeiiilenco, Kan.

' "~ '/ ,"". •■" Okmulgee

' '""' * ■^'"" Tulsa

Company Location

Cushing Gasoline Co Tulsa

Cudahy Oil Co Cleveland, O

D. & S. Oil & Gas Co Tulsa

Dallas Osage Co Tulsa

Danciger Oil & Refining Co Tulsa

Dana Oil Co Bartlesville

Davis. R. I) Cleveland

Davis. L. B Tulsa

Davis & Younger Oklahoma City

Daisy Belle Petroleum Co \rdmore

Dover Oil Co Bart'esville

Daw Bell Oil Co Oklahoma City

Day, B. L Oklahoma, City

Deep Fork Oil Co Marietta, O.

Delokee Gas & Oil Co Bartlesville

Devonian Oil Co Tulsa

Dekoma Development Co Tulsa

Deaver, J. J ' Okmulgee

Delmar Oil Co Bartlesville

DeSoto Gasoline Co Beaumont. Tex.

Dempsey. J. J Oklahoma City

Doneghy Lease Tulsa

Delco Oil & Gas Co Tulsa

Dierk Fred H Kansas City. Mo.

Dominion Oil Co Muskogee

Dock Oil & Gas Co Bartlesville

Done Oil & Gas Co Tulsa

Douglass Harvey, Atty Chelsea

Dresser Oil Co Tulsa

Duffield, L. C. & Co Caney, Kan.

Duffey. J. B. et al Tulsa

Dundee Petroleum Co Tulsa

Dunn Oil Co Tulsa

Duffield & Howard Tulsa

Dubbs, E. E Indiana Harbor. Ind.

Dubeth & Okla. Oil Co Dilworth

Eachob. Trumbo & McKay Muskogee

Eag'e Oil & Gas Co Lyons. Kan.

Easteni Oil Co Buffalo. X. Y.

Ebling. L. P. & Co Bartlesville

Echo Oil Co Tulsa

Edgar Oil Co BartlesviUe

Eddystone Oil Co Tulsa

Ellis. M Tulsa

Elliott & Vensel Tulsa

Elin Oil Co Tulsa

Elliott. W. C Tulsa

Elmer Oil Co Elmira. N. Y.

Empire Gas & Fuel Co Bartlesville

Enid 80 Oil & Gas Co Enid

Eafisco Oil & Gas Co Tulsa

English. W. H Ponca City

Enterprise Transit Co

Evidence Oil Co Caney. Kan.

Exchange Oil & Gas Co Tulsa

Exchange Oil Co Tulsa

Eysenbach, O. K., et al Tulsa

Fagundus Oil Co Chelsea

Farmer. A. L. & A. E Tulsa

Fay Drilling Co Tulsa

Fee Oil Co Muskogee

Fever, M. M Marietta, O.

Fcwel, Green A Muskogee

59 Osage Oil Co Bartlesville

Fitzgerald. J. W Bartlesville

Fitzgerald. D. C Ardmore

Finance Oil Co., et al Pawhuska

Flat Rock Oil Co Tulsa

Flesher Petroleum Co., et al. .Lexington. Ky.
Fort Ring Oil & Gas Co... Fort Worth. Tex.
Foster. 11. V Tulsa

KANSAS CITY TESTING LABORATORY

89

PETROLEUM PRODUCING COMPANIES OF OKLAHOMA

FOR 1921 (Continued)

Coniiiany

Location

Coni;>any

Location

Fortuiia Oil Co Dallas, Tex.

FDSter Oil ("o Tulsa

Fox Petroleum Co Ardmore

Fox. \V. T Sapuliia

Franrhot, D. W. & Co ;.. Tulsa

Foster & Davis. Inc I?artlesville

Freese Oil & Gas Co Okmulgee

Freehold Oil & (ias Co Pittsburgh. Pa.

Friedman. Louis Muncie, Ind.

French, M. C Okmulgee

Fierce, C. A Bartlesville

Force Oil Co Tulsa

Francoma Oil Co Ponca City

Franklin, Wirt Ardmore

Fredora Oil & Gas Co Okmulgee

Funk. A. L Tulsa

Gadf uy, F. J Olmiulgee

Gardner Oil Co Tulsa

Gardner & Avery Tulsa

Galbraith, H. H., et al. .Independence, Kan.

Gates Oil Co Ardmore

Gaffney, H. B Bradford. Pa.

Gardner Petroleum Co Tulsa

Garco Oil Co Enid

Gardner, J. L Okmulgee

Gamo Oil Co Claremore

Georgia Petroleum Co Okmulgee

Getty Oil Co Los Angeles, Cal.

Getty, Geo. F Los Angeles, Cal.

Gilmond Oil Corp Pawhuska

Giddings, F. C, et al Tulsa

Gilliland Oil Co Tulsa

Gillespie. F. A Tulsa

Gillespie. Joe Coffeyville, Kan.

Gilmer Oil Co Lamine. Mo.

Gilbert, X. T Tulsa

Gladstone Oil & Refining Co

Fort Wortli, Tex.

Gorton Trust Cement

Greenwalt, H. L Okmulgee

Guardian Oil Co Tulsa

Gypsy Oil Co., J. J. McGraw, et al

Bartlesville

Gypsy Oil Co Tulsa

Geneva Pearl Oil Co Ardmore

Gibney, H. J Bartlesville

Guillot & Hall Ardmore

Goldie Oil & Gas Co Kansas City. Mo.

Grimes, Elliott, et al Tulsa

Guffey-GUlespie Oil Co Pittsburgh, Pa.

Grimes, Blair, et al Tulsa

Griffen Refining Co Tulsa

Gillespie, F. A., et al Tulsa

Gore, Harry Tulsa

Gray. \V. B '. Tulsa

Gnome Oil Corp Chicago, 111.

Great .Southwestern Petroleum Co

Oklahoma City

Grimes, et al Tulsa

Halfmoon Oil Co Dewey

Hillside Oil Co Muskogee

Heenan, .T. A Ardmore

Harris, T. D Okmulgee

Hartley & Suggs Oldahoma City

Heggem & Davis Tulsa

Hulings. M. C Tidsa

Hulings, F. W. Tr Okmulgee

Hull, J. A Tulsa

Hennessey, .T. E Okmulgee

Hoge, .1. B Nowata

Hastings, W. T Marietta, O

Harrington. Wm Marietta. O

Hamilton & Jack Dewey

Hamilton \V. R Dewey

Hutchinson. E. A Muskogee

Hill Oil & Gas Co Muskogee

Hazel Oil Co Inde;)endence, Kan.

Home Gas Co Cushing

Howard Duf field & Berlin Tulsa

Harhn, E. C Wel.h

Hummel. C. S Chelsea

Hazlett. Bradford, et al

Haley Oil & Gas Co Tulsa

Hollis, Elsie Los Angeles. Cal.

Hmnphreys. E. P Okmulgee

Harrington. L. F Tulsa

Houston. H M Bixby

Harvey Crude Oil Co Tulsa

Humphreys Petroleum Co.. et al Tulsa

Hummel. Sadie L Chelsea

Hayner Petroleum Co Tulsa

Haney. Pliil P Coffeyville. Kan.

Hamill, A. W Tulsa

Hivick, L. C Ardmore

Hivlck & Slack Ardmore

Harris, T. D Okmulgee

Healdton Oil & Gas Co Marlow

Huckleberry, J. H Kansas City. Mo.

Haskogee Oil & Gas Co Haskell

Himible Oil & Gas Co Houston. Tex.

Hill Oil & Gas Co Tulsa

HaiTington. W. J Coffeyville. Kan.

Houbert. H. J Tulsa

Haler. W. T Oklahoma City

Hughes, B. H Tidsa

Hane. C. E., Agt Tulsa

Harris-Strawn Oil Co Ardmore

Hamon. J. L Ardmore

Henton, E. L., et al Chelsea

Henderson Co Nowata

HaverhiU Petroleum Co Tulsa

Hamon & Walls Ardmore

Howard. O. R Tulsa

H. C. W. Oil Co Chelsea

H. M. Petroleum Co Tulsa

Halco Oil Co Tulsa

Harris Oil & Gas Co. . .Independence. Kan.

HaiTis, L. C Rising Sun, I?ul.

Harter Drilling Co Tulsa

Heni-y Oil Co Chicago, 111.

Henson Prod. Co Tulsa

Hojoco Oil Co Tulsa

Holbeck Oil Co Artlmore

Huntly Oil Corp Pittsburgh, Pa.

Hull & Bradstreet Tulsa

Hutchinson, E. A Muskogee

Hyman. T. J Chicago. 111.

Ideal Oil Co Ardmore

Imperial Osage Develop. Co Bartlesville

Interstate Oil & Gas Co Bartlesville

Indiana Oil & Gas Co ;... Tulsa

Invincible Oil Co Fort Worth. Tex.

Iiidiahuma Refining Co St. Louis. Mo.

Invader Oil & Refining Co Muskogee

Independence Oil Co Independence. Kan.

Inilian Territory Illuminating Co

Indian Petrolemn Co Okmulgee

lokla Oil & Gas Co Healdtcm

Illinois-Kansas Oil & Gas Co. . .Chicago, 111.

Illinois Oil Co Chicago, 111.

Ideal Royalty Co Tulsa

Irwin & Miller Bartlesville

90

BULLETIN NUMBER SIXTEEN OF

PETROLEUM PRODUCING COMPANIES OF OKLAHOMA
FOR 1921 (Continued)

Company Location

Irwin, John S Bartlesrtlle

Iron Mountain Oil Co Tulsa

Jitney Oil Co UV^l? ,

Jenson, H. A Bed Fork

Jolly. M. V Tulsa

Jane Gwinn Oil Co Tulsa

Jennings. E. H. Bros. Co Pittsburgh, Pa.

Jay Bee Oil Co Bartlesville

Johnson Farm Oil Co Warren, Pa.

Jameson, J. B Concord, N. H.

Jomack Oil Co Bristow

JeweU Oil & Gas Co Lawton

Johnson, Ike Bartlesville

Josey Oil Co Oklahoma City

Jennie Oil Co Chelsea

.Johnson Oil Befining Co Chicago, 111.

Jennings, B. G. & Lawrence Gas Co

New York City

Jackson, Wise & American Pet. Co...Sapulpa

Jackson, Wise & Bovaird Sapulpa

Jackson. WTse & JIarkham Sapulpa

Johnson. W. J Pittsburgh, Pa.

Kansas & Gulf Co Chicago. 111.

Katheryne Oil Co Tulsa

Kent Oil Co DUworth

Ke>stone Oil & Gas Co. .Independence. Kan.

Kingwood Oil Co Okmulgee

Knupp. W. J., et al Warren. Pa.

Keeche Oil & Gas Co Oklahoma City

Klnkaicl. W. B Delmare

King Carlie Oil & Gas Co

Klstler, K. P Tulsa

Kraeer. 0. A., & Co Bartlesville

K ames, H. E Independence, Kan.

Kay tc Kiowa Oil Co Tulsa

Kames. H. E Independence, Kan.

King, Newbert, Shufflin, et al Nowata

Kay-Wagoner Oil & Gas Co. . .Oklahoma City

Kawfield Oil Co Tulsa

Kama, Jxl Coffeyville, Kan.

King. Frank

Kl.«tler. el al Okmulgee

Kaiiola Oil & Refining Co Tulsa

Klefer. B. L

Kirk. H. C Wooven, O.

Klncstnlth Refining To Tulsa

Kmanee Oil tc Gas Co Titusville. Pa.

Kuiikel. W. A Bluffton, Ind.

Kemp. B. R Tulsa

Kn«pi«iberger. D. L Sapulpa

K.-nill Oil Co Tuisa

KatiHw-Ogtge Petroleum Co Bartlesville

'ii itn. A. M Independence, Kan.

l.i'-l (Ml & G«» Co Tulsa

I ■ oil & (iui Co Bartlesville

i . I.<.af (III ft (j„ Co BlackwcU

I . ^.Mer. ei al Tulsa

i^'"'"- <'• '' Bartlesville

LotHI, I)oi. L Gdn Marietta, O.

,■'■"• •>■ A Marietta. O.

■ '■"" ..Marietta. O.

,,';""■""* ""' C" Sapulpa

l.i«liiiilnK Croek Oil & Gas Co.Wellsville Ky

I-.i.r Oil Co Tu,^^

I--r,H.r., Oil Co ■.'.Ardmore

nm' ^" Kl\ Bartlesville

lll'l^ Kay (Nl Co Tulsa

l.in-t.t.m (III Coni Tulsa

l,«i„l«.ri (III A Oi« Co ""Tulsa

l,rmon (;. .v,.,iy c„ Tulsa

Uk' Maramrc Oil ft Om Co .M^mec

Company Location

Lane E Nowata

Locol Oil Co Warren, Pa.

Lucky Tiger Oil Co Oklahoma City

Lowry Oil Corp Muskogee

Layton Oil Co Tulsa

Lucado OU & Gas Co Coffeyville, Kan.

Leopold & Brett Muskogee

Lawrence Gas Co New York City

Larkin & Reynolds Bartlesville

Lawton, E. B Nowata

Lawton, et al Nowata

Leahy Oil Co Pawhuska

Link Oil Co Tulsa

Longfellow, J. M Bristow

Lasoya Oil Co Otuwa. Pa.

Lewis OU Co PitUburgh. Pa.

Loett Oil Co Tulsa

Long Green Oil & Gas Co.. Kansas City. Mo.

Lone Star Gas Co Dallas, Tex.

Lorber, C. C Cleveland

Lebow, Max Tulsa

Lahoma Oil & Gas Co Oklahoma City

Leonard, J. M Joplin, Mo.

Ltacohi Oil & Gas Co Tulsa

Louvain OU Co Bartlesville

Ludlow, Leo TtUsa

MacMuUen, G. W. Co Tulsa

Magnolia OU & Befining Co Tulsa

Mallory, J. F. , et al Tulsa

Marland Refining Co Ponca City

Mason, D. B Tulsa

McLaughlin & Co Tulsa

Melba Oil Co Tulsa

Minnehoma Oil Co Los Angeles, Cal.

ilid-Co. Petroleum Co Tulsa

MlUiken, J. F. et al Tulsa

Mitchell & Marrow Independence, Kan.

Mitchell, Mark D. & Co .. Independence, Kan.

Moran, M Tulsa

Montrose OU & Kef. Co... Fort Worth, Tex.

Mountain State Oil Co BartlesviUe

Mourlson & Jackson Sapulpa

Mudge Oil Co Pittsburgh, Pa.

Magnolia Petroleum Co Dallas

Midland Sec. Co Tulsa

McClintock B. Otis TtUsa

Murray, Jas. M Cleveland

Moore Petroleum Co Tulsa

Merrick F. W' Ardmore

iUd-Southwestem OU Co Cement

Midgert Oil & Gas Co

Monarch Oil & GasoUne Co Tulsa

McKeys Oil & Gas Co Ardmore

McBamme, L. W Gary, Ind.

Markham, John H. Jr. . et al Tulsa

McGraw, Henry Tulsa

McKinney, J. E Tulsa

Minshall. E. R Tulsa

Minsball OU & Gas Co Tulsa

Modern OU Co WeUsville, N. Y.

Marshall Oil Co Nowata

McCaskey, J. G. & Wentz. Louis

Ponca City

Moore. Clint Tulsa

Malou OU Co Pittsburgh. Pa.

Midwest & Gulf OU Corp Tulsa

McGraw, J. J Ponca City

McClelland Bros Okmulgee

Mcl>imnell, J. V Tulsa

McCann, Wni. L Oklahoma City

Martin, B. C

KANSAS CITY TESTING LABORATORY

91

PETROLEUM PRODUCING COMPANIES OF OKLAHOMA

FOR 1921 (Continued)

Comi)any Location

McCoy, S Okmulgee

McDougal. D. A Sapulpa

McLaiiie Farm Oil Co TiJsa

McCurmick, Matt Nowata

Mooney, D. B Ponca City

McCray, W. S Tulsa

Miller, G. L Ponca City

Mead, C. J Kansas City, Mo.

Majestic Oil & Gas Co DeQuein, 111.

Manhattan Oil Co Tulsa

Marshall Oil Co Tulsa

Martin Mamie Lease Nowata

McGraw, T. F Newkirk

Mid-Kansas Oil & Gas Co Flndlay, Ohio

Mallory et al Tulsa

Milroy Petroleum Co Duncan

M. O. Oil Co St. Louis, Mo.

Marietta Oil Co Marietta, Ohio

Maple Leaf Oil Corporation Bartlesville

Mooney, L. E Chelsea

Misener, F. D.. et al Tulsa

Mooney & Holtxendorff Claremore

M. T. C. Oil & Gas Co Wagoner

McMan Oil & Gas Co Tulsa

McFarlin & Chapman Tulsa

Mutual Oil & Gas Co Tulsa

Miehihoma Oil & Gas Co Muskogee

Midland Oil Co Bartlesville

Morton Petroleum Co Bartlesville

Mustul Oil Co Tulsa

Mohawk Petroleum Co Tulsa

Minnehoha Oil Co Newasha, Wis.

Mercer Oil Co Oklahoma City

Metropolitan Petroleum Co Tulsa

Margay Oil Corporation Tulsa

McKay, M. C, Gdn Sapulpa

Mack Oil & Gas Co Bartlesville

Myers & Twichel Okmulgee

Nile Oil Co Tulsa

Newblock Oil & Gas Co Tulsa

Nancy Oil Co Sapulpa

Neal, D. F., & Co Cleveland

National Explor. Co Tulsa

Noco Prod. Co Tulsa

Northrop, C Ponca City

New England Oil Co Boston, Mass.

North American Oil & Gas Co

Oklahoma City

National Oil & Development Co. . .Okmulgee

Nuco Oil Co Indianapolis, Ind.

N. Y. Oil Co Tulsa

Nyanza Refining Co Ardmore

National Union Oil & Gas Co Blackwell

Newman. Wm. C Okmulgee

Nolan Lease Sapulpa

Nowata Oil & Refining Co Tulsa

Noble, Chas. F Tulsa

Neutadt. Walter Ardmore

New Haven Oil Co Bartlesville

Oregon Oil Co Tulsa

Offenbacher Petroleum Co Tulsa

Osage Develop. Co Bartlesville

Oklahoma Syndicate, Ltd Tulsa

Oliphant Petroleum Co Pawhuska

Osage Foraker Oil Co Tulsa

Oil Issues Co Tulsa

Ohio Fuel Oil Co Pittsburgh. Pa.

Okla. Penn Oil Co Tulsa

Oil State Petroleum Co Enid

Okeh Oil & Refining Co Okmulgee

Okla. Prod. & Bef. Co Tulsa

Company

Location

O'Conner, Martin Portville, N. Y.

Oklahoma Central Oil Co Tulsa

Okliana Oil Co Tulsa

Okla. Petroleum & Gasoline Co Tulsa

Oklalioma Natural Gas Co Tulsa

Oklarado Oil Co Okmulgee

Osage Arrow Oil Co Ponca City

Osage Nat'l Oil Syndicate

New York City, N. Y.

Osage Indian Oil Co

Overton, C. H Tulsa

Old Colony Petroleum Co Oklahoma City

Osage Prod. & Ref. Co Bartlesville

Old Dominion Oil & Gas Co Tulsa

Oglesby. Robt Tulsa

Oklavania Oil Co Tulsa

Owsley, D. L Tulsa

Owens, B., Est Buffalo, N. Y.

Obins & Weber Bartlesville

Okla. Natural Gas Co Sapulpa

Parmenter, L. C Muskogee

Paragon Oil Co Tulsa

Panhandle Refining Co Dallas, Tex.

Panama Oil Co Holdenville

Parks Oil Co Chelsea

Patterson, M. P

Pauline Oil & Gas Co Duncan

Pennhoma Oil Co Pittsburgh, Pa.

Paraffine Oil Co ! Beaumont, Tex.

Papoose Oil Co Tulsa

Page Chas, Tr Sand Springs

Paw Paw Oil Co Baltimore, Md.

Painter & Stager et al Nowata

Page. W. B Tulsa

Petroleum Corp. of America Okmulgee

Penn Osage Oil Co Bartlesville

Periscope Oil Co Tulsa

Pensy Oil & Gas Co Tulsa

Petroleum Co Tulsa

Pennok Oil Co Tulsa

Pet. Lock Oil Co

Peters-Leahy Oil Co Pawhuska

Pennsylvania Oil Co Warren, Pa.

Peters, Chas. B Pawhuska

Phillips Petroleum Co Bartlesville

Phillips Pet Co. & Skelly Oil Co. Bartlesville
Phillips Pet. Co. & Gypsy Oil Co. Bartlesville
Phillips Pet. Co. & Beard Bros. . .Bartlesville
Phillips Pet. Co. & A. D. Morton . Bartlesville
Phillips Pet. Co. & Standish Oil Co

Bartlesville

Phillips, W. G., et al Chelsea

Phillips Oil Co Chelsea

Phillips & Milam Chelsea

Phillips, Waite Tulsa

Phillips, J Sapulpa

Phyems, Scott Chelsea

Phillip King Oil Co New Bedford, Mass.

Pieri'e Oil Cori> New York City

Pioneer Oil Co Tulsa

Pilgrim Petroleum Co Tulsa

Pioneer Petroleum Co Tulsa

Pine, W. B Okmulgee

Planet Petroleum Co Fort Worth. Tex.

Plover Drilling Co Bartlesville

Plymouth Petroleum Co Tulsa

Plew, W. L Gary

Planters Oil Co Nowata

Polecat Oil Co Tulsa

Potomac Oil Co Tulsa

Powell & Wasson Muskogee

92

BULLETIN NUMBER SIXTEEN OF

PETROLEUM PRODUCING COMPANIES OF OKLAHOMA
FOR 1921 (Continued)

Cum; any LocatU.ii

roiur Oil Co New York City

I'ollyanna Oil & Gas Co

Poiica OU Co Ponca City

Producers & Kefiuers Corp Tulsa

Preston & Straijlit Bartlesville

Prolwt, Geo. C.. et al Tulsa

Prairie Oil & Gas Co Independence, Kas.

Pulaski Oil Co Tulsa

Pure Oil Co Columbus, Ohio

Quadrangle Oil Co Wichita. Kas.

Quaker Oil Co Coffey ville, Kas.

Quiidin, G. P ....Tulsa

Quaker Oil & Gas Co Tulsa

Ka.vcdiue Oil & Gas Co Orrick, Mo.

Kabliit Foot Oil Co

Kamsey Oil Co Caney. Kas.

Hanger Oil Con) Tulsa

Keliance Oil Co

Keynulds, W. G

Reliance Oil Co Beaumont, Tex.

Reno Oil Co Sisterville, \V. Va.

Iteimblir Oil & Pipe Line Co

Regal Oil Co Pittsburgh, Pa.

Relx)lil, .1. H Okmulgee

Helxdd. .1. H., et al Okmulgee

Red Bank Oil Co Denver, Colo.

Reliu Oil Co Tulsa

Reynolds Oil & Gas Co. . .Independence, Kas.

He.d. II. W Nowata

Kflxdil Drill Co Okmulgee

Rhode Island Oil Co Independence, Kas.

Hhc..le.< (HI Corp Tulsa

Rlner. .1. .1 Nowata

Rliiille, T. L.. Kst Marietta. Ohij

R'riiarils, A. A Tulsa

Rli-e ("reck Prod. Co Tulsa

Riverland Co Tulsa

RiiKcpf, A. H Car.hage. Mo.

Rimil. Foster, Meloy .Bartlesville

Riiblnwn, E. L Tulsa

RolxTU, C. M Okmulgee

Riivana Petroleum Co St. Louis, Mo.

R"ViT. K. 11 Ardmore

II.-.- City (III & Gas Co Kansas

Id" kland (III Co Ardmore

RiH'kwell Petroleum Corp Tulsa

Rime I'elroleum Corp Okmulgee

R. * M. Oil Co Hominy

RoHtdnid Oil Co Muskogee

Riixidlne Petroleum Co Oklahoma City

Rom. C. O Ci>ffeyville, Kas.

lUith Kniii Independenie. Kas.

Roth tc Hhaffcr Independence, Kas.

">■••'• •' » Tulsa

Ryan Conwdlilated Pet. Co Bartlesville

Kwmnore Oil tc Cu.h Co Tulsa

Harniillen Oil Co Marietta, Ohio

Ktvoy (Ml Co Tulsa

H«iif..rd Oil Co ...Bartlesville

Htmuel.. .M X,.„, Y„rk ,.j,j.

H.iitiina oil Co Oklahoma City

K»lilii.. (Ill tc MarketlnK Co Tulsa

"»•""• '■'■ » Ardmore

Hind Hprliiifn Home el al Sand Springs

Maiiter. Thomaa Okmulgee

H..I.I.. '•■ H^....... Okmulgee

Mnpiilp. lurinlnii (■; , Sapulpa

;;"""•" •;" *•• Tuisa

•^7' *,'"•" ; TuLsa

Hi'lioeniiolil. choji

*^""» • ••• '■ Uit Aii'geie^,' '(''I'liir.

Company Location

Security Oil Co Denver, Colo.

Seamans Oil Co Oklahoma City

Sellas, Geo Chicago. 111.

Shipley, J. M Nowata

Shaffer. Danner & Lawrence Gas Co

Shertzer Bros Dewey

Shear, M Bradford, Pa.

Shear & Marcus Oil Co Bradford, Pa.

Shertzer, C. W Dewey

Shulthis, A. \V Independence, Kas.

Showalter & Cutr'hell . . Sapulpa

Shuler, I Tulsa

Shamiock Oil Co Tulsa

Sheeders Oil & Gas Co Pawhuska

Shaffer Oil & Refining Co Chicago. 111.

Sheridan Oil Co Tulsa

Shufnin, M. B Coffeyville. Kas.

Shaffer-Markin Oil Co Dallas, Tex.

Smiplex Oil Co Okmulgee

Silurian Oil Co St. Louis, Mo.

Sitrin, Sam Tulsa

SUers. Marshall & Co Skiat/)ok

Simpson, B. A Ardmore

Siaco Oil Co New York City

Sinclair Oil & Gas Co Tulsa

Skelly, W. G Tulsa

Skelly Oil Co Tulsa

Skelly Oil Co. et al Tulsa

Skelly Oil Co. & Gyp.sy Oil Co. et al

Bartlesville

Skelton-Moore Oil Co Bartlesville

Skiatook Oil & Gas Co Copan

Shrk, T. B Clarion. Pa.

Smith, W. T Okmulgee

Smith, W. S., Special Tulsa

Smith & Cleage Tulsa

Smith & Weathers Okmulgee

Smltli, H. E Marietta, Ohio-Vinita

Smitli Oil Syndicate Tulsa

Smith & Daugherty Nowata

South Dakota Oil & Gas Co

Southwestern OD Fields Co Bartlesville

Southwestern Oil & Gas Co

Independence. Kas.

Southwestern Petroleum Co Tulsa

Southern Oil & Gas Co Coffey Vile, Kas.

Spring Oil Co Independence, Kas.

Spangler, C. W., et al Tulsa

Sperata Oil Co BartlesvUe

Spurgin, J. G BLxby

Stinson & Matthews Tulsa

Studebaker, E. H South Bend. Ind.

Stephens, C. S Coffeyville. Kas.

Stralem, C. I New York City

Steyner Oil Co Bartlesville

Stut. J. A .TiJsa

Standish Oil Co Bartlesville

Stanford, .1. W Nowata

States Petroleum Co Tulsa

Stebbins Oil & Gas Co Tulsa

Stake Oil Co Independence, Kas.

Stevens Oil & Gas Co Pittsburgh, Pa.

Sterling Oil & Gas Co

Stahl, E. S ...Ardmore

Steiidjerger, C. B Tulsa

Sun Ga.soline Co Tulsa

Sunlieam Petroleum Co Tulsa

Surpass Petroleum Co Pittsburgh, Pa.

Summit Oil Co Bartlesville

Sunuiiers. Jack Haskell

Sweeney, J. F. & Co Tulsa

KANSAS CITY TESTING LABORATORY

93

PETROLEUM PRODUCING COMPANIES OF OKLAHOMA

FOR 1921 (Concluded)

Company

Location

Company

Location

Swaiison et al Tulsa

Sykes, C. E Animore

Symsor. A. .1 Bartlesville

System Oil Co Tulsa

Taft Oil Co Independence, Kas.

T. B. Gasoline Co Tulsa

Terrell Co Terrell, Tex.

Texas Co Tulsa

Terriokla Oil & Gas Co Muskogee

Texas-Oklahoma Invest. Co

Independence, Kas.

Testlog Oil Co Tulsa

Texas Prod; Co Independence. Kas.

Test Oil Co Bartlesville

Thefts. John C Buffalo, X. Y.

Tliompson, K. B. & \V. M Tulsa

Thompson. J. N Tulsa

Tulman Oil Co Tulsa

Thompson, Roy B.. et al Tulsa

Thompson, J. L Gas City, Ind.

Thompson, \Vm. O Gas City, Ind.

Thompson, Welder & Neal Cleveland

The Hefner Co Ardmore

Thurvan Oil Co Bartlesville

Thompson Oil & Gas Co Tulsa

The Keno Oil Co Tulsa

Tim Eliza Oil Co Sapulpa

Tidal Oil Co Tulsa

Titus, C. W Tulsa

Tibbens, 0. G Tulsa

Tittle, Mrs. Bertha Gary, Ind.

Togo Oil Co Tulsa

Tom Games Oil Co Ponca City

Traders Oil Corporation Claremore

Trumbo, A. C Muskogee

Travis, L. R Tulsa

Travis, D. R Tulsa

Transcontinental Oil Co Pittsburgh, Pa.

Troy Oil & Gas Co Sapulpa

202 Oil Co Bartlesville

Tuxedo Oil Co Tulsa

31 Oil Co Lawton

32 Oil & Gas Co Ardmore

25 OU Co Tulsa

Tiunnan Oil Co Okmulgee

Twin States Oil Co Tulsa

Tyrell. H. C Tulsa

Twin Hills OU & Gas Co Tulsa

Two Rivers Oil & Gas Co Bartlesville

Twlchel, J. A Okmulgee

Tulsa Interstate Petroleum Co Tulsa

Union Oil & Gas Co Tulsa

Upland Oil Co Tulsa

U. S. Oil & Gas Co Tulsa

Union Oil Co Tulsa

Urbana Oil Co Lawton

Vance, S. B Tulsa

Victoria Oil Co Tulsa

Viwell Lease Sapulpa

Victor Oil Co Tulsa

Verland Oil & Gas Co Tulsa

Van Hay Oil Co Tulsa

Vesta Oil & Gas Co Kansas City, Mo.

Vensel, F. E Tulsa

Van Nostrand, H. I., Tr Claremore

Van Dall Bros Bartlesville

Van Moss Oil Co Bartlesville

Van Horn. R. V Clifton Forge, Va.

Valos. T. K Chicago, 111.

Victor Oil Co Pavilion, N. Y.

Victor Oil Co Tulsa

Walker, J. W Mounds

Watklns, F. B Waurika

Wigwam Oil Co Tulsa

Wrightsman, C. J Tulsa

Wrightsman Oil Co Tulsa

Wrightsman, Eklna Tulsa

Western American Oil Co Bartlesville

Wilcox, Oswalt & Wilcox. .Indianapolis, Ind.

Wilcox, H. E Inilianapolis, Ind.

Whittier, M. H Tulsa

Wesely, C.' T Ochelata

Wolverine Oil Co Tulsa

Weber, Howard Bartlesville

Warren Oil Co St. Louis, Mo.

Welsh, M. P., et al Nowata

Wilkinson, Eugene Miami

White Rose Oil & Gas Co Oklahoma City

Ward Oil & Gas Co Nowata

Wright, J. H Sapulpa

Walsh Oil Co Tulsa

Wilcox, H. F. Tulsa

Wilcox Oil Co Tulsa

Warner-Caldwell Oil Co Titusville, Pa.

Wagoner Oil & Gas Co Wagoner

Washington, J. E Tulsa

Walker, Wm. H Tulsa

Warren Co Bartlesville

Woodward et al Tulsa

Woodward & Reed Tulsa

Woodward, Geo. E Tulsa

Woodward & Robertsop Nowata

Woodward & Crenshaw McMjrris. .. .Nowata

\Miitehall, Donovan, et al

Wliltehall, B. F Wilkinsburg, Pa.

West Hazlett Oil & Gas Co

Inde.sendence, Kas.

Walter Oil Co Pawhuska

Wah-Shah-She Oil Co BartlesvUle

Winona Oil Co Tulsa

Wolf, F Tulsa

Walker, P. M Tulsa

Walker, P. G Tulsa

Wall Oil Co Tulsa

Warren Petroleum Co Warren, Pa.

Wettack, Maude T Nowata

Welsh, J. D Kansas City, Mo.

Welsh Oil & Gas Co Stillwater

Wells, N. D Tulsa

Wertzenberger, D. D Tulsa

SVestheimer & Daube Ardmore

Whitehall Petroleum Co Tulsa

Wiser Oil Co Bartlesville

Wise & Jackson Sapulpa

Winters Oil Co Bradford, Pa.

Wilcox, M. A Dewey

Wooster Oil Co Okmulgee

Workman Oil & Gas Co Oklahoma City

Xetloc Oil Co Denver, Colo.

Y'orkhoraa Oil Co Bartlesville

Zaline Oil Co Muskogee

Zahn, S. A Tulsa

Zola Oil Co Tulsa

94 EJITXETU^NUMBER^SIXTEEN OF

PETROLEUM REFINERIES IN THE UNITED STATES.

BuMding Completed Daily Capacity

Year j^^g

1914 .... 267 1,186,155 Bbls.

1918 ■ \\ 2*9 1,295,115 Bbls.

1919 99 373 1,530,565 Bbis

1920 ^^ 415 1,888.800 Bbls.

1921

In the following table, the refining plants are divided into eleven
classes for the convenience of those desiring to know the products
that are generally manufactured by each refinery:

rnmnlPte Plant (Comp.)— Gasoline, kerosene, gas and fuel oils, lubricating oils,
piraffin wax petroleum coke or asphalt, or both coke and asphalt.

Skimming Plant (Skim.)— Gasoline, kerosene, gas and fuel oils.

Skimming and Lube (S. & L.)— Gasoline, kerosene, gas and fuel oils, lubricating
oils.

Skimming and Asphalt (S. & A.)— Gasoline, kerosene, gas and fuel oils, asphalt.

.Skimming and Coke (S. & C.)— Gasoline, kerosene, gas and fuel oils, coke.

Skimming, Lube and Asphalt (S.-L. & A.)— Gasoline, kerosene, gas and fuel oils,
lubricating oils, asphalt.

Skimming, Lube and Coke (S.-L. & C.)— Gasoline, kerosene, gas and fuel oils,
lubricating oils, coke.

Wax Plant (Wax)— Gasoline, kerosene, gas and fuel oils, lubricating oils, paraffin
wax.

Lube Plant (Lube) — Gas and fuel oil-s, lubricating oils.

Asphalt Plant (Asphalt) — Distillates, gas and fuel oils, asphalt.

Topping I'huil (Top) — Tops, distillates, gas and fuel oils.

KANSAS CITY TESTING LABORATORY

95

PETROLEUM REFINERIES IN THE UNITED STATES.

(Continued)

COMPANY

LOCATION
ARKANSAS

Daily
Capacity

Arkansas Prod. & Refining Co EI Dorado . 1

Dav,s, Abner. ^ ■ e1 Dorado. . ! ! ! ! ! ! ! ! '

Shipper s Petroleum Co El Dorado

Union Oil & Pipe Line Co .El Dorado

Arkansas Oil Refining Co Port Smith . i!:: I" '

Lion Oi & Refining Co El Dorado. .

New Arkansas Petroleum Co EI Dorado

Petroleum Products Co . (Root Refineries) . . El Dorado

Jones Bros. & Tatum El Dorado

Red River Oil & Refining Co El Dorado'. '.

Gnson Refining Co EI Dorado .■.■.■;" 4 000

National Petroleum Products Co El Dorado. . 1 000

000
250
2,000
3,000
500
4,000
2,000
2,000
1,000
2,000

Crude Oil Marketing Co '.■..■'.■ . .' .' .' .' .El Dorado.'

CALIFORNIA
Union Oil Co. of California Avila

Rf^^fi^M OM^^^" ■ -Avon (San Francisco) .'

Richfield Oi Co. . Bakersfleld. .........

Standard Oil Co. (California) Bakersfleld .

Union Oil Co. of California Brea

Puente Oil Co Chino! .■.'.'.".■

Am?-ican Petroleum Co Coalinga

Col:i^^atal Patroleam Rj5iin? Cd. . . " Coalinga

Shsll Cx of California Coalinga

Standard Oil Co. (Cilifo-nia) ' EI S-gjndo

A nvicai Oilfields Co F>]lows

Wilshire Oil Co., Inc ' " ' Fellows

Ventura Refining Co ' ' Fillmore

California-Fresno Oil Co Fresno

St. Helens Petroleum Co .'.'.■.'.'." .Fallerton Field

Associated Oil Co Gaviota (Santo Barbra)

King Refining Co. . Kern River ...

Producers Refining Co Kern River

Amalgamated Oil Co Los Angeles

Asphaltum & Oil Refining Co Los Angeles

c'^fi°7i ^■■,^^^° Los Angeles .'.■.'.■.' .' .' .' .' .'

Richfield Oil Co Los Angeles

T"^ner Oil Co. ^ Los Angeles

Union Oil Co. of California Maltha

Tr),fnn*^n-l°r '^^H^?-'"'^-f • ' ■• Martinez (San Franc.)

Union Oil Co. of California Oleum

fl^t^^nfA^ ^°; i'^?.yf°'"?'^) • ■ Richmond (San Fran.)

Union Oil Co. of California San Pedro (L. A.) .

Capitol Crude Oil Co Santa Paula

Union Oil Co. of California Santa Paula

f?^?f^' P- L. . _^ Tulare

California Oil & Asphalt Co Vernon

General Petroleum Corporation Vernon

Gilmore Petroleum Co Vernon^ ! '.'..'.

Jordon Oil Co Vernon

Pacific American Petroleum Co ... . Vernon

Petroleum Lubricants Co ... . ' Vernon

Pioneer Paper Co .' . ; ; .' Vernon. .'.'. '. '. ' .' .' .' .'.■'■

Union bales Corporation Vernon

Vernon Oil Refining Co ; ; .Vernon! ! ;:::::;:::::

Wilshire Oil Co., Inc Vernon

COLORADO

United Oil Co Florence

Apex Refining Co Loomis

Raven Oil & Refining Co Rangeley

GEORGIA
Atlantic Refining Co Brunswick

3,000

17,000

22,000

3,500

20,000

10,000

1,300

3,600

2,500

2,000

35,500

10,000

5,000

4,200

500

200

10,000

450

150

3,500

600

260

900

1,000

3,000

30,000

22,000

60,000

12,000

40

800

150

.500

20,000

700

600

300

200

400

4.000

1,500

3,000

1,500

200

50

4,000

Type of
Plant

S
S

s
s

S. & L.

s
s
s
s
s
s
s
s

Top

S. & L.

Skim.

S. & A.

Skim.

Skim.

Top.

Skim.

Skim.

Comp.

Top.

Top.

Wax

Skim.

Top.

Skim.

Asphalt

S. L. &

Top.

S. & A.

Skim.

Skim.

S. L. &

Skim.

S. &L.

S. L. &

Comp.

Skim.

Skim.

Skim.

Skim.-^

Skim.

Top.

Skim.

S. & L.

Skim.

Asphalt
Skim.
Skim.
Skim.

Comp.
S. & L.
Skim.

S. & L.

96

BULLETIN NUMBER SIXTEEN OF

PETROLEUM

COMPANY

REFINERIES IN THE
(Continued)

LOCATION

UNITED STATES.

Daily
Capacity

300
3,500
1,000
1,000
4,000

ILLINOIS

Leader Oil Co S^®^' ' t ' ^

Indiahoma Refining Co East St. Louis

Lubfite Refining Co East St. Louis

Warren Oil Co. of Pennsylvania Joilet

Central Refining Co. (Indian) Lawrenceville ,o =nn

Indian Refining Co Lawrenceville ^?'?"a

The Texas Co Lockport 4,500

Interocean Refining Co McCook 1,000

Wabash Refining Co Robinson 1,000

Roxana Petroleum Corporation Wood River 15,000

Standard Oil Co. (Indiana) Wood River 12,000

White Star Refining Co Wood River 1,000

INDLANA

Indiana Oil Refining Co Columbus 700

Consjlidated Oil Refining Co East Chicago 2,000

Sinclair Refining Co East Chicago 10,000

Service Oil Refining Co Fairmount 1,200

Po.-tland Oil & Refining Co Portland 500

Standard Oil Co. (Indiana) Whiting 40,000

KANSAS

The Kanotex Refining Co Arkansas City 3,000

Ti.e Lesh Refiaing Corporation .Arkansas City 2,500

Midco Petroleum Co Arkansas City 4,500

Augusta Oil Refining Co Augusta 1,000

Harvey Crude Oil Co Augusta 2,000

White Eagle Oil & Refining Co Augusta 5,000

General American Oil Co Baxter Springs 1,000

McWhorter-Chanute Refining Co Chanute 200

Mutual Oil Co Chanute 1,000

Sinclair Refining Co Chanute 2,000

The Uncle Sam Oil Co Cherryvale 2,400

Kansas Oil Refining Co Coffeyville 2,000

National Refining Co Coffeyville 4,000

Sinclair Refining Co Coffeyville 3,500

Atlas Refining Corporation El Dorado 1,000

El Dorado Refining Co El Dorado 3,000

Fide ity Refining Co El Dorado 2,500

Midland Refining Co El Dorado 4,000

St. Louis Oil & Refining Co El Dorado 1,500

Tfi-State Oil & Refining Corporation El Dorado 1,200

(.reat Western Oil Refining Co Erie ' 1 500

Miller Petroleum Co Humboldt .'.".■ 2,000

Hutchinson Petroleum Co Hutchinson . 1,000

fcmpire Refineries, Inc Independence 500

Kan.sas City R.-fining Co Kansas City 2,500

Wi f"i^fi "'"^^^ Kansas City 1,000

Sinclair Ht'fin'ng Co Kansas City 5 000

C jmmonweallh O.I & Refining Co Moran .... 800

rhem,V»l '• ^*°r ' '^?"'^^ Neodesha 12,000

VirkTml V 1* ^^-^^ Osawatomie 2 000

Virker.H T'etroleum ( o Potwin 2 000

North American Refining Co. (PuritanRefinery)Rosedaie; '.■.■.■.;■.■. V ' '. LOOO

Su.rl,ng<.il&K..,iningCo 1 ! i i i : ;wS: ;■.■. l •. l ■.; •.•.•. ! 4,000

KENTUCKY

.'ixieueiiRe^i„,cr::::::::::::;:::;::teS:::::::::

1,000
800
1,800
1,500
3,000
1,500

Type of
Plant

S. & L.

Skim.

Lube

Lubr

S. &L.

Comp.

Skim.

Lube

Comp.

Skim.

Comp.

Skim.

Skim.

Comp.

Skim.

Comp.

Skim.

Skim.

Wax

Skim.

Skim.

Skim.

Skim.

Skim.

Skim.

Skim.

S. &L,

Comp.

Wax

Skim.

Skim.

Skim.

Skim.

Skim.

Skim.

Wax

Skim.

Skim.

Skim.

Skim.

Skim.

Skim.

Skim.

S. L.

Skim.

Skim.

S.

Skim.

Skim.

Skim.

& C.

Skim.
Skim.
Skim.
Skim.

KANSAS CITY TESTING LABORATORY

97

PETROLEUM REFINERIES IN THE UNITED STATES.

(Continued)

COMPANY

LOCATION
KENTUCKY

Stoll Oil Refining Co Louisville

Oleum Refining Co Pryse

Standard Oil Co. (Kentucky) Riverside (Louisville)

Massey Refining Co Scottsville

Mutual Oil & Refining Co Winchester

LOUISIANA

Delart Refining Co Anse La Butte.

Great Southern Prod. & Refining Co Ardia

Standard Oil Co. of Louisiana Baton Rouge. .

Louisiana Petroleum Products Co Bossier City . . .

Caddo Central Oil & Refining Co Cedar Grove. . .

Caddo Central Oil & Refining Co Cedar Grove. . .

Crescent Oil & Refining Co Cedar Grove. . .

International Oil & Gas Corporation Cedar Grove. . .

Red River Refining Co Crichton

Mexican Petroleum Corporation of Louisiana . Destrehan

Loaisiana Oil Refining Corporation Gas Center. . . .

New Orleans Refining Co Good Hope . . . .

General Oil & Refining Co Homer

Homer Refining Co Homer

Shreveport Prod. & Refining Co Jewella

Sinclair Refining Co. of Louisiana Meraux

Liberty Oil Co., Ltd New Orleans. . .

General Oil & Refining Co Oil City

Island Refining Corporation Sarpy

Paramount Petroleum Corporation Sheehan

Louisiana Oil Refining Corporation Shreveport. . . .

The Texas Co Shreveport . . . .

U. S. Producers Refining Co Shreveport . . . .

Paramount Petroleum Co Superior

Calcausieu Oil Refining Co Westlake

MARYLAND

Interocean Oil Co Baltimore .

Standard Oil Co. (N. J.) Baltimore .

United States Asphalt Refining Co Baltimore .

Prudential Oil Corporation Fairfield. .

MASSACHUSETTS

Massachusetts Oil Refining Co East Braintree .

Beacon Oil Co Everett

New England Oil Refining Co Fall River

Daily
Capacity

2,000

1,100

5,000

500

Type of
Plant

S. & L.
Skim.
S. &C.

500

100
2,000

Skim.

40,000
3,000

Comp.

3,000
3,600
6,000
1,000
2,000
20,000
5.000
7,000

Skim.
Skim.
Skim.
Lube
Skim.
S. & A.
Skim.
S. & A.

250

3,000

10,000

1,000

2,000

10,000

Skim.
S. & A.
Skim.
S. &L.
Skim.

1,800
3,000

Skim.
Top.

650

1,000

32,000

3,000

6,000

5,000
10,000
20,000

Skim.

S. & L.
Comp.
Asphalt
Comp.

S. & A.
Skim.
S. & A.

Pure Oil Co .

MINNESOTA
Minneapolis.

MISSOURI

Wilhoit Refining Co Joplin

North American Oil & Refining Corporation . . Kansas City .

Ranger Refining & Pipe Line Co Kansas City.

St. Joseph Viscosity Oil Co St. Joseph . . .

Standard Oil Co Sugar Creek .

Montana Refining Co.

MONTANA
Billings.

NEBRASKA

Nicholas, L. V., Oil Co. (White Eagle) Omaha.

Omaha Refining Co Omaha.

1,000

S. & L.

1,000

Skim.

1,500

Skim.

2,000

Skim.

500

Skim.

2,000

Comp.

1,000 Skim.

500
1,000

Skim.

98

BULLETIN NUMBER SIXTEEN OF

PETROLEUM REFINERIES IN THE UNITED STATES.

(Continued)

COMPANY

LOCATION

Daily
Capacity

NEW JERSEY

SUndardOi!Co.(N.J.) Bayonne 20.000

V^^^Z^h^'^'oi^e. Yo..: ; :::::::::: |=e hoou: ; ; : : : 1.000

Standard Oil Co. (N. J.) Jersey City 180.000

ISriS'-M/. 1:.:: :::::::,: : m'S' ;, : :;:.::;::: |.»s

Warner-Quinlan Co Warner -2,500

NEW MEXICO
Tucumcari .

2.000

Pecos Prod. & Refining Co.

NEW YORK

Standard Oil Co. of N. Y BrookI>Ti

Standard Oil Co. of N. Y Brooklyn. ._

Standard Oil Co. of N. Y Long Island City 23,000

Standard Oil Co. of N. Y Long Island City

Standard Oil Co. of N. Y Buffalo

Vacuum Oil Co Olean.

Welbv-ille Refining Co . Wellsville

OHIO

Ohio Refining Co Cincinnati

The Canfield Oil Co Cleveland

Standard Oil Co. (Ohio) Cleveland

Anderson & Gustafson. Inc Columbus

National Refining Co Findlay

The Pure Oil Co Heath

The Craig Oil Co Ironville

Solar Refining Co Lima

National Refining Co Marietta

Paragon Refining Co Toledo

Standard Oil Co. (Ohio) Toledo

Sun Co Toledo.

Rajah Oil & Refining Co. .

. Youngstown .

OKLAHOMA

Big Diamond Oil & Refining Co Addington.

Harvey Crude Oil Co Allen

Arbuckle Refining Co Ardmore . .

CamfTon Refining Co. . Ardmore. .

Chickasaw R<-fining Co Ardmore. .

Imp«-ial Refining Co Ardmore. .

The Pure Oil Co Ardmore . .

Bigh« art Prod. & Refining Co Bigheart .

r. U. & W. Oil & Gas Co .■ Blackwell

Glo»H> Oil & Refining Co Blackwell.

Modern Kefining Co Bladkwell .

ProduriTH & Refiners C;orporation Blackwell. .

TranHcontinental Oil Co Boynton

lUim in liefining Co Bristow

CarU-r Oil Co Cartoco

American Oil & Tank Line Co. Cleveland

Marland lU-fining Co Covington.

AndcrHon & (iustafson, Inc. Cushing

Bi.-ry OilCo... . . . ! Xushing! . !

Kmpire Ri-tinerieH, Inc. . Cushing

IlllnoiHOilCo _ ..Cushing..

Inland Ki-tining (o Cushing

Marigold Oil & ll»-fining Co. . Cushine

Occident Oil & Refining Co. . Cush-ne '

Iw V"!;'; I 'i' ['.". . ;; Cushing ;: :

ShafT.-r ( )i 1 & R.-fining Co . Cushin|

Type of
Plant

Comp.

Comp.

S. &L.

Comp.
S. & A.

4.000

Comp.

7.000

Comp.

1.000

Wax

1,200

Skim.

1,000

Wax

8.400

Comp.

400

Skim.

1.000

Comp.

3,000

Skim.

1,500

Wax

6,500

Caomp.

400

Wax

8,000

Comp.

3,000

Comp.

100

S. & L.

1,500

Skim.

1,000

Skim.

3,000

Skim.

7,500

Skim.

4,000

Skim.

7.000

Skim.

2,500

S. &L.

1,800

S. &L.

1,000

Skim.

2,000

Skim.

3,000

S. &L.

2.500

Skim.

15.000

Skim.

1,250

Skm.

1.000

Skim.

1,500

Skim.

1,800

Skim.

4,000

Skim.

2,500

Skim.

2,500

Skim.

2,0o0

Skim.

1,200

Skim.

6,500

Skim.

6,000

Wax

KANSAS CITY TESTING LABORATORY

99

PETROLEUM

COMPANY

REFINERIES IN THE
(Continued)

LOCATION
OKLAHOMA

UNITED STATES.

Daily
Capacity

Type of
plant

Sinclair Refining Co Cushing 6,500 Skim.

Cyril Refining Co Cyril 600 Skim.

Constantin Refining Co Devol 8,000 Skim.

Beaver Petroleum Refining Co Dilworth Skim.

Tidal Gasoline Co Drumright

Duncan Refining Co Duncan

Bolene Refining Co Enid

Champlin Refining Co Enid

Oil State Refining Co Enid

Francis Oil & Refining Co Francis

Frederick Oil & Refining Co Frederick

Garber Refinery, Inc Garber

Grandfield Oil & Refining Co Grandfield

Oklahoma-Texas Refining Co Grandfield

Union Oil & Refining Co Grandfield

Rock Island Petroleum Co Guthrie

Bay State Refining Co Heal dton

Cogswell Refining Co Henryetta ■ . . . .

Southern Refining Co Haskell

Meridian Petroleum Corporation Hominy

Great American Refining Co Jennings

Republic Refining Co Jennings

Damascus Refining & Manufacturing Co Lawton

Lawton Refining Co Lawton

Oklahoma Prod. & Refining Corp. of A Muskogee

Sinclair Refining Co Muskogee

Nyanza Refining Co New Wilson

Choctaw Oil & Refining Co Oil City

Cherokee Refining Co Oilton

Cushing Petroleum Corporation Oilton

Pirtle-Pitman Oil Co Oilkirk

Atwood Refining Co Oklahoma City

Choate Oil Corporation Oklahoma City

Empire Refineries, Inc Oklahoma City

Home Petroleum Co Oklahoma City

Allied Refining Co Okmulgee

Empire Refineries, Inc Okmulgee

Indiahoma Refining Co Okmulgee

Meridian Petroleum Co Okmulgee

Phillips Higgrade Refining Co Okmulgee

Oneta Refining Co Oneta

Empire Refineries, Inc Ponca City

Marland Refining Co Ponca City

Meridian Petroleum Co Ponca City

Osage Mutual Oil & Refining Co Pawhuska

North American Oil & Refining Co Pemeta

Bison Refinery Co Quay

Mid-Continent Refining Co Ringling

Chestnut & Smith Corporation Sand Springs

Pierce Oil Corporation Sand Springs

Big Six Prod. & Refining Co Sapulpa

Pol ar Prod. & Gasoline Co Sapulpa

Sapulpa Refining Co Sapulpa

Constantin Refining Co Tulsa

Consumers Oil & Refining Co Tulsa

Cosden & Co Tulsa 25,000

Mid-Co Gasoline Tulsa

Pan American Refining Co Tulsa

The Texas Co Tulsa

Tidal Gasoline Co Tulsa

Sin-lair Refining Co Vinita 10,000

Blue Ribbon Oil & Refining Co Walters

Li vingston Refiners Corporation Walters 3,000 Skim.

Southern Oi 1 Corporation Walters 1,500

Canfield Refining Co Yale 500 Skim.

Home Oil Refining Co. of Texas Yale 2,000 Skim.

2,500

Skim.

1,000

2,000

Skim.

8,000

Skim.

1,800

Skim.

1,000

600

Skim.

800

Skim.

2,000

Skim.

1,200

Skim.

2,000

1,500

Skim.

1,000

Lube.

2.000

1,000

Skim.

800

Skim.

4,000

Skim.

1,000

Skim.

1,000

Skim.

1,000

Skim.

2,000

Wax

600

S. & L.

3,500

Skim.

50

Skim.

1,000

Skim.

2,000

Skim.

1,000

S. & L.

2,000

S. & L.

2,000

Skim.

2,500

Skim.

1,000

S. & L.

2,500

Wax

10,000

Skim.

3,000

Skim.

2,000

Skim.

1,500

S. &L.

2,500

Wax

5,000

Wax

2,000

S. & L.

1,000

Skim.

1,500

Skim.

1,000

Skim.

1,000

Skim.

5,000

Skim.

9,000

Wax

800

Skim.

1,500

Skim.

7,500

S. & L.

4,000

Skim.

2,000

Skim.

25,000

Wax

4,000

S. & L.

5,000

Skim.

8,000

S. & L.

1,200

Skim.

10,000

S. & L.

100

BULLETIN NUMBER SIXTEEN OF

PETROLEUM REFINERIES IN THE UNITED STATES.

(Continued)

COMPANY

LOCATION

OKLAHOMA

„ o . ^ Yalp 2,000

Ok-In Prod. & Refining Co i.a e

Pawnee Bill Oil & Refining Co ^a'e

Southern Oil Corporation ^ale

The Sun Oil Co.

Yale

Victor Refining Co Yale

Worth Oil & Refining Co ^a e

Yale Oil Corporation ''ale

PENNSYLVANIA

Emery Manufacturing Co 5''^ j^°''4

Kendall Refining Co Bradford^

Chippewa Oil Co Bndgewater

Butler County Oil Refining Co 5''")"

Valvoline Oil Works, Ltd Mj* "" J

Interior Oil & Gas Corporation Clarendon

Levi Smith Refining Co Clarendon

Tiona Refining Co Clarendon

White Oil Corporation Clarendon

The Canfield Oil Co Coraopolis

Glenshaw Development Co Coraopolis

Pittsburgh Oil Refining Corporation Coraopolis

Vulcan Oil Refining Co Coraopolis

Pennsylvania Oil Products Refining Co Eldred

Emlenton Refining Co Emlenton

Atlantic Refining Co Franklin

Foco Oil Co Franklin

Franklin Quality Refining Co Franklin

Freedom Oi 1 Works Co Freedom

Pann. Refining Co ... Karns City

SUrlight Refining Co Karns City

Conewango Refining Co Langdale and Warren.

Pure Oil Co Marcus Hook

Sun Company Marcus Hook

The Texas Co Marcus Hook

Island Petroleum Co Neville Island

Atlantic Refining Co Oak Grove

Continental Refining Co Oil City

Independent Refining Co Oil City

Penn-American Refining Co Oil City

W. H. Daugherty & Son Refining Co Petrolia

Petrolia Refining Co Petrolia

Atlantic Refining Co Philadelphia

Atlantic Refining Co Pittsburgh

A. I). Miller Sons Co Pittsburgh

Waverly Oil Works Co Pittsburgh

Empire Oil Works Reno... .

CryHUl Oil Works Rouseville

Penn. American Refining Co. . '. Rouseville

Ea«U-rn Oil Refining Co Russell. .

AmiMT Oil & Realty Co Stoneham

Tidiouli' Refining f'o Tidioute.

American Oil Works
Oi'W lycvick fo .
Oil CrM-k Refining Co
TItUHvilleOil Works
Crew U-vick Co. . .
Mutual Refining Co
Svni-ca Oil Works
Pure Oil Co
SutMTior Oil Works.
United Refining Co.
Warren Refining Co
Warr-I'enn Refining Co

Titusville..
Titus vi lie..
Titusville..
Tutusville .
Warren . . .
Warren . . .
Warren. . .
Warren. . .
Warren . . .
Warren . . .
Warren . . .
Warren. . .

WllbUrine Oil Works, Ltd [ \ \ ■.Warren

Daily

Type of

Capacity

Plant

2,000
1,000

Skim.

6,000

Skim.

5,000

Skim.

1,000

Skim.

100

Lube

1,200

Skim.

1,200

Wax

650

Wax

200

S. &L.

1,000

Wax

1,000

Wax

300

S. &L.

1,050

S. &L.

1,000

Wax

1,000

S. &L.

400

S. &L.

600

Skim.

1,000

Wax

850

Wax

1,000

Wax

600

Wax

6,500

Comp.

600

S. &L.

700

S. &L.

1,500

Wax

100

Skim.

100

Skim.

1,400

S. &L.

3,000

Comp.

10,000

S. L. & A

5,000

Asphalt

1,000

Was

200

Skim.

750

Wax

1,000

Wax

3,000

Wax

200

Skim.

30

Skim.

50,000

Domp.

4,000

Wax

1,000

S. &L.

800

Lube.

600

Wax

1,000

W^ax

3,000

Wax

400

S. &L.

75

Skim.

600

S. &L.

800

S. &L.

2,000

Wax

1,000

S. &L.

1,000

S. &L.

935

Wax

500

S. &L.

560

Wax

1,500

Wax

400

Wax

800

Wax

1,700

Wax

400

S. & L.

600

Wax

KANSAS CITY TESTING LABORATORY

101

PETROLEUM REFINERIES IN THE UNITED STATES.

COMPANY

(Continued)

LOCATION

RHODE ISLAND

Standard Oil Co. of N. Y East Providence.

The Texas Co Providence

SOUTH CAROLINA
Standard Oil Co. (N. J.) Charleston. .

TENNESSEE
Victor Refining & Distributing Co Nashville

TEXAS

General Oil & Refining Co Abilene

Allen Reese S. Refining Co Amarillo

Humble Oil & Refining Co Baytown

Magnolia Petroleum Co Beaumont. . . .

World Refining Co Bridgeport. . . .

Baney Refining Corporation Brownwood. . .

Brownwood Refining Co Brownwood. . .

Carson Refining Co Brownwood. . .

Freeport Gas Co Bryanmound . .

Bear Refining Co Burkburnett . .

Burk-Tex. Refining & Pipe Lin Co Burkburnett. .

Crystal Petroleum & Refining Co Burkburnett. .

Invader Oil & Refining Co. of Texas Burkburnett. .

Manhattan Oil Refining Co Burkburnett. .

Chas. F. Noble Oil & Gas Co Burkburnett.

Nortex Refining Co Burkburnett . .

Taxoil Refining Co Burkburnett . .

Tidal- Western Oil Corporation Burkburnett. .

Uniform Gasoline & Petroleum Co Burkburnett. .

Victor Refining Co Burkburnett . .

Liberty Refining Co Cisco

Keen & Woolf Oil Co Clinton

Magnolia Petroleum Co Corsicana ....

Aetna Petroleum Corporation Dallas

Hercules Petroleum Co Dallas

Sun Rise Refining Co DeLeon

Dublin Oil & Refining Co Dublin

Keystone Refining Co Dublin

Keystone Refining Co Dublin

Rex Refining Co DeLeon

General Oil & Refining Co Eastland

Beavers-Electra Refining Co Electra

Waggoner Refining Co Electra

Rio Grande Oil Co El Paso

Gulf Refining Co Fort Worth. . .

Home Oil Refining Co. of Texas Fort Worth. . .

Magnolia Petroleum Co Fort Worth. . .

Montrose Oil Refining Co., Inc Fort Worth. . .

Ok-In Prod. & Refining Co Fort Worth. . .

Pierce Oil Corporation Fort Worth. . .

Souther Oil & Refining Co Fort Worth. . .

Star Refining & Prod. Co Fort Worth . . .

Texas-Arizona Petroleum Co Fort Worth. . .

Texas Eagle Oil & Ref. Co., Inc Fort Worth . . .

Transcontinental Oil Co Fort Worth. . .

White Eagle Oil & Refining Co Fort Worth. . .

Empires Refineries, Inc Gainesville . . .

The Texas Co Gater

Gorman Home Refinery Gorman

State Refining Association Grand Prairie.

North Texas Oil & Refining Co Greenville . . . .

Beacon Refining Co Henrietta

Galena Signal Oil Co. of Texas Houston

Transatlantic Petroleum Co Houston

Deepwater Oil Refineries Houston

Burk Pipe Line & Refining Co Iowa Park. . . .

Daily
Capacity

10,000
5,000

500

Type of
Plant

Skim.
Asphalt

10,000 Skim

Skim.

3,000

Skim.

2,000

Skim.

10,000

S. & L.

25,000

Comp.

500

500

Skim.

200

Skim.

400

Skim.

5,000

Skim.

1,000

Skim.

4,000

600

Skim.

1,500

Skim.

3,500

Skim.

5,000

Skim.

1,200

Skim.

300

Skim.

1,500

Skim.

4,000

Top.

1,500

Skim.

4,000

Skim.

750

Top.

2,000

Skim.

2,500

Skim.

3,500

S. ;L.

700

2,500

Skim.

1,000

Skim.

5,000

1,500

2,000

Skim.

2,000

Skim.

1,500

Skim.

2,000

Skim.

5,000

Skim.

5,000

Skim.

10,000

Skim.

4,000

Skim.

5,000

8,000

S. &L.

1,000

1,000

Skim.

4,000

5,000

5,000

S. &L.

5,000

S. & L.

10,000

Skim.

15,000

Skim.

2,000

Skim.

1,200

Skim.

2,500

Skim.

3,000

S. &L.

1,000

Jube.

1,000

Lube.

2,500

Skim.

102

BULLETIN NUMBER SIXTEEN OF

PETROLEUM REFINERIES IN THE UNITED STATES.

(Continued)

COMPANY

LOCATION

Daily
Capacity

Type of
Plant

TEXAS

Walker consolidated Petroleum Co Iowa Pfrk.

K. M. A. Refining Co KM A. Held. .

Golden Star Refining Co Mex a

Texas-Mexia Refining Co VJ V ■^:,:„t '

L Porte Oil Refining Co Morgan s Po nt ,

•^ (^o Morgan s Point.

Pa-Tex Petroleum Co '<i ^ AZ^X^li

Carolina Oil Co Nacogodoches

Mogul Prod. & Refining Co 9'^^^^^ \

Orienul Oil Co ^ °"?u^'

Panther City Oil & Refining Co Panther

Port Houston Oil & Refining Co Pasadena

White Oil Corporation E^^? * "I

Gulf Refining Co Port Arthur

The Texas Co Port Arthur . . .

Turnbow Oil Corporation Port Houston . .

The Texas Co Port Neches

Consolidated Prod. & Refining Co Ranger

Ranger Refining & Pipe Line Co Ranger

Great Eastern Oil & Refining Co Riverside

Great Texas Oil & Refining Co Saginaw

Southern Refining Co San Antonio ....

Gravburg Oil Co San Antonio

Humble Oil & Refining Co San Antonio .

Elliott Jones & Co., Inc San Antonio.

Mogul Prod. & Refining Co San Jacinto

Buffalo Oil & Refining Co Sherman

Rex Oil & Refining Co Sweetwater

Sinclair Refining Co Sinco (Houston).

Farmers Oil & Refining Co Texarkana

Four States Refining Co Texarkana

Pierce Oil Corporation Texas City

Thrall Oil Refining Co Thrall

Ranger Refining & Pipe Line Co Tiffin

Toyah Oil & Refinery Co Toyah

Waco Refining Co Waco

Ti-xa.s f)il Products Co W^axahachie . . . .

W<'alhi-rford Refining Co Weatherford . .

American Refining Co Wichita Falls . . .

Bankers Petroleum & Refining Co Wichita Falls .

Mears Gasoline Co Wichita Falls. . .

Ix)ne Star Refining Co Wichita Falls. . .

Miller Petroleum Co Wichita Falls. . .

New Tex Refining Co Wichita Falls. . .

I'anhandle Refining Co Wichita Falls . . .

powf-r Oil Refining Co Wichita Falls. .

KangiT-Wirhita Oil & Refining Co Wichita Falls.

SduthwesU-rn prod. & Refining Co Wichita Falls. . .

Sunxhine Slate Oil & Refining Co Wichita Falls.

Texhoma Oil & Refining Co Wichita Falls .

t'lah Oil Refining Co.
Dixie Oil Co

UTAH

. . North Salt Lake.
. . .Virgin

3,000

1,250

1,000

1,000

1,000

350

400

3,000

2,400

2,000

200

3,000

65,00

40,000

'15,666

3,000
2,000
2,000
3,000

500
1,800
2,000
4,000

600

500
1,000
5,000
2,000

400
3,000

300

1,500

50

2,500

500
5,000
1,000
2,000
3,500
2,500
1,500
5,500
1,500
3,000
1,000
2,500
2,500

4,000
50

The Texan f'o

Th.- pur., on
U art,, r i^iilnlan Co
I.Ik Itiliiung Co ,
Sluiidurd Oil (U,. (N. J.i
Ohio Valley iteflning Co

VIRGINIA
Norfolk.

WEST VIRGINIA

Cabin Creek Junction.

Cairo

Falling Rock
Parkersburg
St. Mary's

Skim.
Skim.
Skim.
Skim.
Lube.

Skim.

Wax

Lube.

Comp.

Comp.

Asphalt

Skim.

Skim! . .' '.
Skim.
Skim.
Skim.

Skim.
Skim.
S. & L.

Skim.
Wax
Skim.
Skim.

Skim.

Skim.
Skim.
Skim.
Skim.
Skim.
Skim.

Skim.
Skim.
Skim.
Skim.
Skim.
Skim.

Wax

5,000 Asphalt

3,000

Wax

500

Skim.

1,000

S. &L.

2,200

Wax

1,000

Wax

KANSAS CITY TESTING LABORATORY

103

PETROLEUM

COMPANY

REFINERIES IN THE

(Concluded)

LOCATION
WYOMING

UNITED STATES.

Daily
Capacity

Midwest Refining Co Casper ^^-^^^

Standard Oil Co. (Ind.) Casper

Northwestern Oil Refining Co Cowley

Wyatt Oil & Refining Co Fetterman

Mutual Refining & Prod. Co Glenrock

Midwest Refining Co Greybull

■Wind River Refining Co Lander

Standard Oil Co. (Ind.) Laramie ,

Midwest Refining Co Laramie

Lovell Refinery Lovell

McWhorter Oil & Refining Co Lusk

McWhorter Oil & Refining Co Osage

Alliance Oil & Refining Co Thermopolis

8,100

1,000

500

2,500

10,000

900

1,700

5,000

500

250

250

1,000

Type of
Plant

Wax

S. & C.

Skim.

Skim.

Skim.

Slim.

Skim-

S. & ^■

Skim.

Skim.

Skim.

Skim.

Top.

PETROLEUM REFINERIES IN CANADA.

COMPANY

LOCATION

Imperial Oil Co. (L) Dartsmouth, N.

Imperial Oil Co. (L) loco, B. C

Imperial Oil Co. (L) Montreal , Que .

Calgary Petroleum Products, Ltd Okotoks, Alt. . .

Canada Southern Oil & Refining Co Okotoks, Alt. . .

Southern Alberta Ref ., Ltd Okotoks, Alt

Canadian Oil Companies, Ltd. (L) Petrolia, Ont. . .

Canadian Oil Prod. & Ref. Co. (L) Petrolia, Ont. . .

British Columbia Refining Co Moody, B.C..

Continental Oil Co Regina, Sask. . .

Imperial Oil Co. (L) Regina, Sask . . .

Imperial Oil Co. (L) Sarnia, Ontario.

British-American Oil Co. (L) Toronto

Great Lakes Oil & Ref. Co Wallaceburg . . .

North Star Oil & Ref. Co Winnipeg

Daily
Capacity

3,000

3,500

2,500

30

25

30

800

150

500

2,500

20,000

800

250

1000

PETROLEUM REFINERIES IN MEXICO.

COMPANY

LOCATION

Atlantic Refining Co Port Lobos

(Cia. Refinadores y Productori de Petroleo La Atlantica).

Texas Company Port Lobos

Mexican Eagle Co., Ltd Puerto Minatitlan

(Isthmus of Tehaun tepee.)

La Corona Petroleum Co Tampico

Mexican Eagle Oil Co., Ltd Tampico

Pierce Oil Corporation Tampico

Huasteca Petroleum Co Tampico

Standard Oil Co. (N. J.) Tampico

Texas Company Tampico

Mexican Eagle Oil Co., Ltd Tuxpan

Pierce Oil Corporation. . . . Vera Cruz

Daily
Capacity

10,000

15,000

6,000

■12,.500

10,000

60,000

6,000

6,000

5,000

2,500

104 BULLETIN NUMBER SIXTEEN OF

The producing, distributing and marketing organizations owned
and controlled by the Royal Dutch-Shell oil combine: (Oil, Paint, Drug
Reporter)

1. Acetylene Gas and Benzine Maat.

2 Alliance Co. (Mexico).

Operates 16,000 acres held in dispute by Mexican Eagle and Mexican Petro-
leum (Doheny) companies.

3 Anglo-Mexican Petroleum Co., Ltd. (London).

Marketers for Mexican Eagle and Eagle Transport Co.; hence now closely
related to Shell-Dutch. Markets in Central and South American and British
Isles.

4. Anglo-Egj'ptian Oilfields, Ltd. (Egypt).

July 6, 1911. $6,561,000. Managed by Anglo-Saxon.

5. Anglo-Persian Oil Co. (Persia).

Marketing agreement until 1922 with Dutch-Shell.

6. Anglo-Saxon Petroleum Co., Ltd. (London).
June 29, 1907. $38,880,000.

7. Asiatic Petroleum Co., Ltd. (Ceylon).

Refiners, distributors, June 29, 1903. $9,720,000.

8. Asiatic Petroleum Co., Ltd. (Ceylon).

Refiners, distributors, carriers. Nov. 13, 1917. $972,000.

9. Asiatic Petroleum Co., Ltd. (Egypt).

Property acquired from Anglo-Saxon. March 25, 1911. $972,000.

10. Asiatic Petroleum Co., Ltd. (Federated Malay States).

Feb. 29, 1911. $243,000. Property acquired from Anglo-Saxon.

11. Asiatic Petroleum Co., Ltd. (North China).
Aug. 11, 1913. From Anglo-Saxon. $2,430,000.

12. Asiatic Petroleum Co., Ltd. (India).

Property acquired from Anglo-Saxon. $2,673,000.

13. Asiatic Petroleum Co., Ltd. (Philippine Islands).
Registered Jan. 30, 1914. $72,900.

14. Asiatic Petroleum Co., Ltd. (Siam).

Aug. 11, 1913. From Anglo-Saxon. $364,500.

15. Asiatic Petroleum Co (South China).

Property acquired from Anglo-Saxon. Aug. 11, 1913. $1,701,000.

16. Asiatic Petroleum Co., Ltd. (Straits Settlements).
Feb. 28, 1911. From Anglo-Saxon. $1,215,000.

17. Astra Romana Societe Anonyme (Rumania).

Geconsolidceerde HoUandsche Maat. is heavily interested. $13,027,500.

18. Astra Refining Co. (Rumania)). $960,000.

19. Atjan Mining Co. (Sumatra).

20. ISataafche Petroleum Maatschappij (Holland).
Jan. 1, 1907. Anglo-Saxon, managers. $56,000,000.

21. Belgian Benzine Co. $100,000.

22. Benzine Lagerungs Geselschaft (Blexien). $121,500.

23. Benzine Lagerungs Geselschaft (Breslau). $12,150.

24. B.-nzine Lagerungs Geselschaft (Hamburg). $7,000.
26. B.-nzlne Lagerungs Geselschaft (Madgeburg). $85,050.

26. Hi-nzlnwerke Regensburg Geselschaft. $170,000.

27. Btnzlnwerke Rhenania (Dusseldorf). $204 120

-*■ .!;''T,'""'^!? ^'°' V**^- (Venezuela). Sub. of General Asphalt Co.
•Bolivar (.oncesalons (1917), Ltd. (Venezuela)

not"rpa't o" rheTu'tch%°hi,r|?Srp"°"^' '^*^- °"'^- ^ ^""^^'^ °^ ''''""' "'''
Jirltlah-Amerlcan Oil Co. (Toronto).

29

30
31
32

11 l/".'.*^"^'-', "'^^",""-" Tom Angio-.Saxon, Aug. 7, 1912. $97 200

''• AUK 1" TsT'" ^n'"°-.^'^- 4^°"'^ ^f'-*<=a
u ifi K i.r . ^""^ Anglo-Saxon, $4S,600,

3&.
36.
37.

v!il'A """"•"'• ^'^- <I^'^"idated). (Shell Company of California.)
Caribbean Potroloum Syndicate, Ltd. (Venezuela^
Own.-,l Jointly by General Asphalt and Dutch^Shel

-SheU.

KANSAS CITY TESTING LABORATORY 105

38. Ceram Oil Syndicate, Ltd. (Island of Cerani). (Dutch-Shell.) $972,000.

39. Ceram Petroleum Co. (Dutch East Indies). (Dutch-Shell.)

40. Chijoles Oil, Ltd. (Mexico). (See Tampico Panuco Oilfiilds, Ltd.)
$972,000. Tampico Panuco Petroleum Maat.

41. Cleophane Oil & Gas Company (Oklahoma). (Liquidated.)

42. *Colon Development Co., Ltd. (Venezuela).

Friendly to, but probably not as yet a part of the group. $486,000.

43. Commercial & Mining Company (London). $48,600.

44. Curacoa Petroleum Co. $1,600,000.

45. Curacoasche Scheepvaart Maatschappij (Island of Curacoa).
Sept., 1916. Subsidiary of Bat. Peet. Maat. $800,000.

46. Danske Engelske Benzin Petroleum Akt. (Denmark). $135,000.

47. Danske Tyske Petroleum Company, Ltd. (Denmark). $240,000.

48. Dordlsche Petroleum Maatschappij.

Dutch-Shell selling and refining agency in Dutch East Indies. $12,000,000.
49.- Eagle Oil Transport Company. Ltd. (Tank steamers for Mexican crude and
fuel. Now related to Dutch-Shell through Mexican-Eagle purchase.)

50. East Borneo Maat. (Borneo). $883,600.

51. Ernste Bayerische Petroleum Geselschaft. $346,500.

52. Finnische Petroleum Import, Geselschaft (Finland).

53. Geconsolidceerde Hollandsche Petroleum Co. (Holland).

Interested in .\stra Romana, and Dutch-Shell companies are largely inter-
ested in it. Jan., 1907. $9,600,000.

54. General Asphalt Company, U. S. A. (Trinidad and Venezuela).
$31,000,000. (The Dutch-Shell controls the petroleum production of all of
this company's Trinidad and Venezuela holdings, but is apparently not inter-
ested in its asphalt business).

55. Gravenhag Association ^London). (Liquidated.)

56. Grozny-Sundja Oil Fields, Ltd. (Russia).

Managed by Anglo-Saxon. SI, 438, 000. March 31, 1913.

57. Helouan Petroleum Co. (Liquidted.) $243,000.

58. Java Petroleum Co. (Liquidated.) $280,000.

59. Kasbee Syndicate, Ltd. (Russia). $6,240,000.

60. Koetei Exploratie Maat. $520,000.

61. Koninkliijke Nederlandsche ilaatschappij tot Exploitatie van Petroleum in
Nederlandsche Indie.

Incorporated. Holland, June 16, 1890, and amalgamated with Shell Transport
& Trading Co., Ltd., as from Jan. 1, 1907. $60,700,000. (Royal Dutch.)

62. King Oil Company (Oklahoma). (Liquidated.)

63. La Corona Petroleum Maatschappiji (Holland).

- To consolidate Dutch-Shell interests in Mexico. $10,000,000. Steamships.

64. La Corona Petroleum Company (Mexico).

65. Lubricating & Fuel Oils, Ltd. (London). $486,000.

66. Mexican Eagle Oil Co., Ltd. (Mexico). $30,000,000.

67. Mineralol & Benzine Werke (Rhenia). $240,000.

68. Mineralolwerke (Rhena nia).

69. Moeara Enim (Sumatra). $4,000,000.

70. Moesillir (Sumatra). $3,840,000.

71. Nederlandsche-Indische Eploration Syndicate.

72. Nederland-Indische Industrie and Handel. Maat.
Anglo-Saxon, manager. $8,000,000. Blaik Papes, Koete.

73. Nederlandsche-Indische Petroleum Maat. $144,000.

74. Nederlandsche-Indische Tank Stoom-boot Company.
Anglo-Saxon and B. P. M., managers. $1,200,000.

75. New Orleans Refining Co., Roxana Petroleum Corporation. $40n,000.

76. New Schibaieff Petroleum Co., Ltd. (South Russia).
$5,637,000. Anglo-Saxon is manager.

77. Norske Engelske Mineral Oil Akt. (Norway). $147,420.

78. North Caucasian Oil Fields, Ltd. (Grosny, South Russia).
Jan. 29, 1901. Anglo-Saxon, manager. $3,645,000.

79. Nouvelie Societe du Standard Russe de Grosny. (Dutch-Shell.) $6,240,000

80. Oilfields of Mexico Company.

Marketing and shipping obligations with Mexican Eagle. $8,500,000.

81. Panama Canal Storage Company.

106 BULLETIN NUMBER SIXTEEN OF

82. Petroleum Development Co., Ltd. (Trinidad).

Subsidiary of General Asphalt Co.
S3. Puova Oil Company (Oklahoma). (Roxana Corporation.)

84. Periak Petroleum Maatschappij (North Sumatra). Dutch-Shell. 4,000,000.

85. Quintuple Oil Company (Oklahoma). Roxana Corporation. (Liquidated.)

86. Regatul-Roman. $4,632,000.

87. Rising Sun Petroleum Company (Japan). $2,000,000.

88. Red Sea Oilfields, Ltd. (Liquidated.) $2,187,000.

89 Roxana Petroleum Corporation (New Jersey).

Holding company for Mid-Continent and Wyoming propertie.s. $60,000,000.
Mar. S. 1917.

90 Roxana Petroleum Company of Oklahoma. Roxana Petroleum Corporation.
$8,000,000. 1914.

91. Sarawak Brunei (Borneo).

92. Sebatik Petroleum Maat. $800,000.

93. Shanghai Langkat Maat. (Sumatra). $1,095,000.

94. Shell Company of Canada. $243,000.

95. Shell Company of California.

To consolidate Dutch-Shell interests in California. $45,000,000. July, 1915.

96. •'.Shell" Marketing Company, Ltd. (London).
Marketing in United Kingdom. $7,290,000.

97. Shell Transport & Trading Company, Ltd. (London).

Registered Oct. 18, 1887, as a transporter and marketer of oil. Amalgamated
with the Royal Dutch as from Jan. 1, 1907. $111,880,000.

98. Signal Oil Company (Oklahoma). (Roxana Corporation.) (Liquidated.)

99. Simplex Refining Company (California).

100. Soclete Commerciale et Industrielle de Eaphte Caspienne et de la Mer Noire
(Russia). (Rothschilds.) Feb., 1912. $5,200,000. Dutch-Shell.

101. Societa Anonima Italiana. $291,000.
101-a. Societa Nafta (Genoa).

102. Societe de Mazout (Russia). Dutch-Shell, (Rothschilds.)
Feb., 1912. $12,000,000.

103. Sumatra Palembang (Sumatra). $2,800,000.

104. Sumatra Petroleum Company. (Liquidated.) $1,458,000.

105. Svensk Engelske Mineral Oil Akt. (Sweden). $540,000.

106. Tampico-Panuco Oil Fields, Ltd. (Mexico). Held by the Tampico-Panuco
Petroleum Maat., which in turn is held the Bat. Pet. Maat. $1,550,000. Dec,
1916.

107. Tampico-Panuco Petroleum Maatschappij (Holland). Holds the Tampico-
Panuco Oilfield!?, Ltd., the Chijol Oil, Ltd., and the Tampico-Panuco Valley

Railway Co. $2,880,000.
lOS. Tampico-Panuco Valley Railway Company (Mexico). (See above.)

109. Tatakan Petroleum Companj- (?). $1,560,000.

110. Trinidad Lake Petroleum Company, Ltd, .A. subsidiary of the General Asphalt
Company. All oil production controlled bv Dutch-Shell.

111. Trinidad Oilfields, Ltd. Assets taken over by United Britain Oilfields of

Irinidad, Ltd. Aug., 1913. $1,940,000.

"'• T-",'"P^'L'-"' t^onipany (California). Bought out by Shell of California.
$:>00,000.

113. United British Oilfields of Trinidad, Ltd. Managed by the United British
West Indies Petroleum Syndicate, Ltd. $3,152,000. July 1 1913

114. l^nit.-d British Producing Company, Ltd. (Trinidad). Managed by the United
Hrlti.-ih West Inilies Petroleum Syndicate, Ltd. $1,458 000

11;,. United Briti-sh Refineries, Ltd. (Trinidad). Managed by United British West

Indies Petroleum Syndicate, Ltd. $486,000
116. l.-nlled British \yest Indies Petroleum Syndicate, Ltd. (West Indies British
.ulana or .Isewhere) Anglo-Saxon Company heavily interested along with
11- !"','*"''mah and Anglo-Persian crowd. July 18, 1912. $972,000.

.;''.''!.;'?''/.*"„?" Corporation Ltd. 10,000 square miles on northeastern sea-
ii« vi 1 V. i.it. n'^'*'?> ^^''^ April 15, 1910. $4,860,000. Looks like Dutch-Shell,
$10,000,000 Company (California). (Dutch-Shell of California.)

*'"■ h'.'tr,h!^'er«°i'„r^^rT?l°'^V^*'^- Dutch-Shell financially interested, and to
i-jn {;••"''""»'''''•« for at least 15 years from 1915. $2,430,000.
120, Ver.-lgntf Henzlnfabriken Ces, $21 870

'"'■ f^mU "t'so^'ooo"""'' '^^"f""""'*)- Liquidated and owned by Shell of Cali-

1": zS[.?'^trM"a;t^°('?uTa^ra)^.^T60roo^^'^ Corporation.) $10,000,000.

•Not a part of the combine— associated by marketing or other agreements.

KANSAS CITY TESTING LABORATORY 107

STANDARD OIL GROUP.
Refiners and Marketers.

Company Capitalization Market Price Market Value

Anglo-American $15,000,000 25 $ 75,000,000

Atlantic Refining 5,000,000 1350 67,000,000

Borne-Scrymser 200,000 500 1,000,000

Chesebrough Mfg ; 1,500,000 310 4,650,000

Continental Can 3.000,000 655 19,650,000

Galena Signal, 2d pfd 6,000,000 107 6,420,000

Galena Signal Oil, 1st pfd 2,000,000 125 2.500,000

'alena Signal, common 16,000,000 13S 22,080,000

nternational Pet 6,265,000 31 38,844,000

Solar Refining 2,000,000 370 7,400,000

S. O. of California 99,373,310 2S2 280,282,706

S. O. of Indiana 30,000,000 800 240,000,000

'S. O. of Kansas 2,000,000 600 12,000,000

S. O. of Kentucky . 6.000,000 400 24,000,000

S. O. of Nebraska 1,000,000 550 5,500,000

S. O. of New Jersey 98,338.300 710 698,201,930

S. O. of New York 75,000.000 382 286,500,000

S. O. of Ohio 7.000,000 525 36,750,000

Swan & Finch 1,450,000 100 1,450,000

Vacuum Oil 15,000,000 440 66,000,000

Midwest Refining Co. (Wyoming) ...

Producing Companies.

Ohio Oil Company $15,000,000

Prairie Oil & Gas Company 18,000,000

South West Penn 20,000,000

Washington Oil 100,000

Carter Oil Co 25,000,000

Pipe Lines and Carriers.

Buckeye Pipe Line $10,000,000 100 $ 20.000,000

Crescent Pipe Line 3,000,000 36 2,160,000

Cumberland Pipe Line 1,488,851 200 2,977,6(J0

Eureka Pipe Line 5,000,000 167 8,320,000

Illinois Pipe Line 20,000,000 184 36,800,000

Indiana Pipe Line 5,000,000 105 10,500,000

National Transit 6,362,500 22 11,198,000

New York Transit Company 5.000,000 185 9,250,000

Northern Pipe Line 4,000,000 112 4,480,000

Prairie Pipe Line 27,000,000 300 81,000,000

Southern Pipe Line 10,000,000 165 16,500,000

South West Penn 3,500,000 100 3.500,000

Union Tank Line 12,000,000 130 15,600,000

Total market values all companies $2,486,214,236

Market value refining and marketing companies 1,834,928,630

Market value producing companies 429,000,000

Market value pipe line and carrying companies 222,282,600

386

$231,000,000

750

135,000,000

313

62,600,000

40

400,000

108 BULLETIN NUMBER SIXTEEN OF

DIRECTORY OF OIL ASSOCIATIONS.

■n- =,»rn PPtroleum Refiners' Association— President, W. D. Richardson Meridian
Petroreum Co^p. 324 Rialto Bldg.. Kansas City, Mo.; Secretary. H. O. James,
800 Republic Bldg., Kansas City, Mo.

Kansas Oil Mens Association— Presidtnt, John .S Longshore care Sunllower Oil &

lupply Co!, Topeka, Kas. ; Secretary, H. F. Bagby. Wichita. Has.
American Independent Petroleum Association— President, L. V. Nicholas. Nicholas

Bldg, Omaha; Nebr.; Secretary, H. F. Reynolds, 14 East Jackson Blvd.,

Chicago, 111. , „ ^ t,.

Oklahoma Oil Jobbers' Association— President, D. L. Gilland, 118 \V est 6th bt.,
Oklahoma ^^\^;'."gppretary, John E. Hutchens. Box 811, Enid. Okla.
Independent Oil Men's Association— President, T. J. Gay, Gay Oil Co Little Rock,

Ark° Secretary, E. E. Grant, 110 South Dearborn St., Chicago. 111.
Texas Oil Jobbers' Association— President, D. E. Little, Fort Worth, Tex.; Secre-
tary, Albert W. Wolters, Taylor, Texas.
Minnesota Petroleum Club— Secretary, W. B. Cline, care Manhattan Oil Products

Co.. St. Paul. Minn.
Nebraska Independent Oil Mens Association— President, T. Wilbur Thornhill,

Charleston Oil Co., Charleston, S. C.
Southern Petroleum Dealers' Association — President, L. V. Nicholas, Howard and

17th St., Omaha, Nebr.; Secretary, D. C. Patterson. Camden, S. C.
South Dakota Oil Jobbers' Association — President, H. L. Freeman. Lake Park

Corp.. Sioux Falls. S. D
New Mexico Petroleum Association — Address, Allison Bldg.. Roswell, N. M.
Independent Oil Marketers' Association — President. W. L. Moore, Dixie Oil &

Grease Co., Atlanta, Ga.
Louisiana Petroleum Refiners' Association — President, I. G. Abney. Louisana Oil

Refining Corporation, Shieveport, La.; Secretary, E. F. Buchanan, Crichton

Refining Co., Crichton, La.
Wisconsin Independent Oil Men's Association — President, S. G. Hastings, Jr., Bark-

housen Oil Co., Green Bay, Wis.
Indiana Oil Jobbers' Association — President, Paul Moorehead, Moorehead Oil Co..

Hammond. Ind. ; Vice-President, F. C. Enz, Evansville; Secretary, Russell

Galloway, Hammond.

Arkansas-Tennessee OH Jobbers' Association — -President, T. G. Gay, Gay Oil Co.,
Little Rock, Ark.

Central West Oil Men's Association — Bowling Green, Ky. — President, Edward R.
List; Secretary, F. L. Reeves.

Kentucky Oil Men's Association — Lexington, Ky. — President, Albert R. Marshall;
Secretary, E. E. Loomis.

Central New York Oil Jobbers' Association — Syracuse, X. Y. — President, Alfred M.
Cady, Syracu.se. N. Y. ; Secretary, W. D. Metzger, Syracuse, N. Y.

MI<l-Contlnent Oil & Gas Association — 213-14 Kennedy Bldg., Tulsa, Okla. — Presi-
dent. W. N. Davis; Secretary-Counsel. Harry H. Smith.

''""r-^-'^"*'''' ""'^ Louisiana Oil & Gas Association — 14 Rossonian Bldg.. Houston,
Texas — President, W. S. Parish; Vice-President, I. R. Bordages; Secretary,
NIelH Esperson.

Mill-Continent OH & Gas Association — Texas-Louisiana Division, Apartment 14,
UosBonian Bldg.. Houston. Texas — President. W. D. CUne; Secretary, Howard
Hennette.

Gulf Coast OH Producers' Association — Beaumont, Texas— President, J. C. Wilson;
.Secretary-Treasurer, R, J. Braud.

National OH Exchange— Harri.s Trust Bldg., Chicago, III.— President W. D. Sim-
mon«. Viscosity OH Co., Chicago; Secretary, T. J. Gay, Gay Oil Co., Little
i{o( k. Ark.

Ind-pendent Oil and Gas Producers' Association of Louisiana— Shreveport, La.—

I r.Hldent, ( . I). Keen; Secretary, Thos. O. Harris.
New York State OH Producers' Association— Bolivar, N. Y.— President. John P.

ii.-rrKK. (il.-an, N. \.: Secretary-Treasurer. W. Frank Richart, Wellsville, N. Y.

'"'''■-?«n.'^'T' n"o.^''';!;''i'"''^' Agency- Union OH Bldg., Los Angeles, Calif —Presi-
dent, I,. P. Hi. flair; Seen lary-Treasurer, W. B. Robb.

^'"Vcr^^^"v''Ti"„„^V■"''' x-^,*""'",'?"^?— ^'°'"'"^"«' Ohio-Presidem, F. O. Levering-
wccrctary-TruaBur.T, Wm, H, Thompson.

KANSAS CITY TESTING LABORATORY 109

DIRECTORY OF OIL ASSOCIATIONS— Continued.

InUepemlent Petroleum Marketers' Assutiation — y:{0-ol Marsh-Strong Bldg., L,os
Angeles, Calit. — I'resiiUnt, H. tj. Botsford; Secretary-Manager, H. H. Maxson.

Northwestern Oil I'ruilucers' Association — Bradford, Pa. — President, F. D. Wood;
Secetary-Treasurer, Earl Weher.

Oil and Gas Producers' Association — Okmulgee, Okla. — President, John R. Rebold;
Secrttary, W. R. Alexander.

Oil Producers' Association — 60.S Main St., Bradlord, Pa. — President, Wm. J.

Healey ; Secretary, Earl S. Weber.
O.l Traders Association of New York — .'!.5 South William St., New York — President,

P. J. Snyder; Secretary, Jos. C. Smith.
Oil Trade Association of Philadelphia, Inc. — Philadelphia, Pa. — President, T. G.

Cooper, T. G. Cooper .t Co. ; Secretary, James Stevenson, Stevenson Bros. & Co.
West Texas Oil Men's Association — .Mineral Wells, Texas — President, J. Edgar

Pew; Secretary, W. E. O'Neal.

no BULLETIN NUMBER SIXTEEN OF

AMERICAN GAS SYNDICATES.

CALIFORNIA
Southern California Gas Co Sf/^^l^'i^ St LCs Inlelel

W% Boardman Co 718 Mission St San Francisco

Coast Counties Gas & Electric Co 454 California St San Francisco

Northern California Power Co 995 Market St San Francisco

Pacific Gas & Electric Co 445 Sutter St Stan Francisco

COLORADO
Western Light & Power Co Boulder

FLORIDA
Southern Utilities Co Palatka

ILLINOIS

Copley Gas & Electric Syndicate Aurora

Illinois Traction System Champaign

American Coke & Chemical Co 208 S. LaSalle St Chicago

H. M. Bylksby & Co Cont. & Coml. Natl. Bank Chicago

Gas & Electric Improvement Co 33 S. LaSalle St Chicago

Metropolitan Gas & Electric Co Harris Trust Bldg Chicago

L. E. Myers Co Monadnock Block Chicago

Peoples Gas Co 108 S. LaSalle St Chicago

Middle West Utilities Co 72 W. Adams St Chicago

North American Light & Power Co 2013 Peoples Gas Bldg Chicago

Public Service Co. of Northern Illinois 72 W. Adams St Chicago

Union Utilities Co 39 S. LaSalle St Chicago

Wisconsin Power, Light & Heat Co 72 W. Adams St Chicago

United Light & Railways Co 836 Edison Bldg Chicago

E. A. Potter Rector Bldg Chicago

Southern Illinois Light & Power Co Hillsboro

INDIANA

Northern Indiana Gas & Electric Co Hammond

Interstate Public Service Co 510 Board of Trade Bldg Indianapolis

W. A. Martin Gas Syndicate LaPorte

Consolidated Gas & Oil Co Ridgeville

IOWA

Iowa Railway & Light Co. . Cedar Rapids

Runner Gas Co ... Charles City

American Gas Construction Co Newton

Iowa Gas & Electric Co '.'.'.'..'.'.'.'.'.'.'.'.'.'. ! Washington

LOUISIANA
American Cities Co . . 201 Barone St New Or eans

MARYLAND

General Utilities & Operating Co Munsey Bldg . . Baltimore

Southern Gas & Electric Corporation 213 Courtland St. . . ; ; .Baltimore

MASSACHUSETTS

Commonwealth Gas & Electric Co 78 Devonshire St. Boston

MBHHarhuwtt^ Ga.s ( o. Ill Devonshire St. . . Boston

MaMHarhuH.- Ls L.^htrng Co 77 Franklin St Boston

M""'; *u ':^''"^"' v.. • • • 1'" Milk St Boston

T^"''':r, ' ■ T'*"7 t^l- ■ -^ • • ■ • 201 Devonshire St. . . . B^stoS

Tw n StaU- dan & Electric Co r>obion

MICHIGAN

AppU-by & Wagner , ,

W. K. MoHH & Co 7in TT«i„r, T \ ou Alma

Am.T|.-an I'ubli.- Uiiliiies Co ™ ^"•''" ^'"^^ ^^'^« Detroit

llnlli-d I.JKhl & Railways Co Grand Rapids

Mirhiitan LJKht Co Grand Rapida

utiiiu™ o,..rating Co 31Q peck Bldg :;;::::::;:::;:; ;SSLoo

KANSAS CITY TESTING LABORATORY 111

AMERICAN GAS SYNDICATES (Continued)

MINNESOTA
Public Improvement Co 348 Security Bldg Minneapolis

MISSOURI

Union Public Service Co 1116 Commerce Bldg Kansas City

Central Power & Light Co 1420 Chemical Bldg St. Louis

Southern Illinois Light & Power Co St. Louis

Light & Development Co. of St. Louis 750 Railway Exchange Bldg St. Louis

NEBRASKA

Gas Construction Co 48th and Leavenworth Sts Omaha

Union Power & Light Co 424 First Natl. Bank Bldg Omaha

NEVADA
Sierra-Pacific Electric Co Reno

NEW JERSEY

Cumberland County Gas Co Millville

Public Service Gas Co 80 Park Place Newark

Florida Utilities Co 715 Broad St Trenton

NEW YORK

Brooklyn Union Gas Co 176 Remsen St BrookljTi

Eastern Oil Co Buffalo

South Shore National Gas & Fuel Co Marine Trust Co. Bldg Buflalo

Republic Light, Heat & Power Co Marine Trust Co. Bldg Buffalo

Empire Coke Co 103 Castle St Geneva

New York State Gas & Electric Co Ithaca

Associated Gas & Electric Co 43 Exchange Place New York City

American Light & Traction Co 120 Broadway New York City

American Power & Light Co 71 Broadway New York City

Consolidated Gas Co 124-130 E. 15th St New York City

Henrv L. Doherty & Co 60 Wall St New York City

Electric Bond & Share Co 71 Broadway New York City

Federal Light & Traction Co 60 Broadway New York City

General Gas & Electric Co 50 Pine St New York City

Commonweal th Power, Railway & Light Co . 14 Wal 1 St New York City

General Engr. & Management Corporation. 141 Broadway New York City

General Engr. & Management Corporation. 141 Broadway New York City

Lehigh Power Securities Corporation 71 Broadway New York City

Nassau & Suffolk Light Co 149 Broadway New York City

National Fuel Gas Co 26 Broadway New York City

National Utilities Co 61 Broadway New York City

North American Co 30 Broad St New York City

Pearson Engineering Corporation 115 Broadway New York City

United Gas & Electric Engineering Corp ... 61 Broadway New York City

H. D. Wallbridge & Co 14 Wall St New York City

J. G. White Management Corporation 43 Exchange Place New York City

Peck-Shannahan-Cherry, Inc Savings Bank Bldg Syracuse

Utica Gas & Electric Co Utica

NORTH CAROLINA

North Carolina Public Service Co Greensboro

Carolina Power & Light Co Raleigh

OHIO

Consolidated Gas, Electric & Water Co 1123 Ilium Bldg Cleveland

Continental Gas & Electric Corporation Cuyahoga Bldg Cleveland

Ohio Cities Gas Co Columbus

Ohio Fuel Supply Co Columbus

Ohio Gas Light & Coke Co Napoleon

OKLAHOMA
Empire Gas & Fuel Co Bartlesvlle

OREGON
Pacific Power & Light Co Gasco Bldg Portland

112 BULLETIN NUMBER SIXTEEN OF

AMERICAN GAS SYNDICATES (Concluded)

PENNSYLVANIA

American Gas Co West Washington Square Philadelphia

Eastern Light & Fuel Co Real Estate Trust Bldg Philadelphia

Day & Zimmermann .... Philadelphia

C. H. Geist Co Land Trust Bldg Philadelphia

Girardville Gas Co 4014 Chestnut St Philadelphia

Gribbel Sj-ndicate Co 1513 Race St Philadelphia

United Chemical & Industrial Co Widener Bldg Philadelphia

National Gas, Elec. St. & Power Co Witherspoon Bldg Philadelphia

Public Service Co 1142 Real Estate Trust Bldg Philadelphia

Philadelphia Suburban Gas & Elec. Co. . . S. W. Cor. 7th and Locust Philadelphia

J. C. Reed & Co Finance Bldg Philadelphia

Union Railway Supply Co Real Estate Trust Bldg Philadelphia

United Gas Improvement Co Broad and Arch Sts Philadelphia

Arkansas Natural Gas Co 223 Fourth Ave Pittsburgh

Manufacturers Light & Heat Co 248 Fourth Ave Pittsburgh

Ohio Fuel Supply Co Pittsburgh

Philadelphia Co 435 Sixth Ave Pittsburgh

Union Natural Gas Corporation Union Bank Bldg Pittsburgh

Wabash GasCo Benedum-Trees Bldg Pittsburgh

United Service Co 700 Scranton Life Bldg Scranton

RHODE ISLAND
Blackstone Valley Gas & Electric Co Pawtucket

TEXAS

North Texas Gas Co .• Dallas

Texas Power & Light Co Interurban Bldg Dallas

VIRGINIA

Southern Gas & Electric Corporation. Richmond

Virginia Railway & Power Co Richmond

WASHINGTON
North J>acific Public Service Co Tacoma Bldg Tacoma

WEST VIRGINIA

Boyd E. Horner Syndicate Clarksburg

Columbia Gas & Electric Co '.'..'.'.'.'.'.'.['.'.. Huntington

WISCONSIN

Wisconsin Power, Light & Heat Co 900 Gay Bldg Madison

Wisconsin Securities Co 1408 First Natl. Bank Bldg". '.'.'.'.. Milwaukee

CANADA

Dominion Gas Co tto,«;h^«^ r,^<-

Quebec Railway, Light. Heat & Power Co! .' . .' .• .' ; qSc

KANSAS CITY TESTING LABORATORY 113

PRINCIPAL PIPELINES.

Capacity,

ripeline Mileage Barrels

Alluwe Pipeline Co. (Kas. Oil Ref. Co.), Alluwe Dist., Ckli., to

Col'feyville, Kas 40 2.500

Amalgamated Petroleum Co., Salt, Lake Di^t., Cal., to Los Angeles,

Cal. . 70 9,000

American Petroleum Co., Humble to E. Houston, Tex 20 ....

Associated Oil Co., Coalinga Dist., Cal., to Monterey, Cal 105 15,000

Associated Oil Co., Santa Barbara Co., Cal., to Gaviota, Cal 60 23,000

Arkansas City Pipeline Co., Blackwell to Arkansas City, Kas ....

Associated Pipeline Co., Kern River Dist., Cal., to Port Costa, Cal. 2S1 13,000

Associated Pipeline Co., Kern. River Dist., Cal., to Port Costa, Cal. 27S 26,000

Bessemer Pipeline, Tltusville, Pa., to W. Pa ....

Buckeye Pipeline Co., Lima Division, Ohio-Ind. state boundary to

Ohio-Penn. state boundary TOO 75,000

Buckeye Pipeline Co., Macksburg Divi.sinn, Eastern Ohio to Ohio-
Penn. and Ohio-W. Va. bound.ary 330 10,000

Colive Oil Co., Healdton to Ardmore ....

Cosden & Co., adjacent wells to Bigheart, Okia 500

Cosden Pipeline Co., various Okla. oil Dist. to West Tulsa, Okla. . . 30,000

Crescent Pipeline Co., Greggs, Pa., to Marcus Hook, Pa 315 5,600

Crown Pipeline Co., Okmulgee, Okla., to Muskogee, Okla 58 ....

Cumberland Pipeline Co., Southeastern Kentucky to Kentucky-W.

Va. boundary 475 10,000

Emery Pipeline Co., adjacent oil Dist. to Bradford, Pa 4S0 1,000

Empire Pipeline Co., Eldorado and Augusta, Kas., to Ponca City,

Okla S5 ....

Empire Pipeline Co., Ponca City, Okla., to Norfolk, Okla 67 ....

Empire Pipeline Co., northern Oklahoma to Independence, Kas.. 70 ....

Empire Pipeline Co., Healdton, Okla., to Gainesville, Tex. (Total) 55 35,000

Empire Pipeline Co., Gainesville, Tex., to Red River, Tex 17 8 inch

Eureka Pipeline Co., Kentucky-W. Va. boundary and Ohio-W. Va.

boundary to W. Va.-Pa. boundary 4,300 65,000

Franklin Pipe Co., adjacent fields to Franklin, Pa 150

General Pipeline Co., Midway Dist., Cal., to Los Angeles and San

Pedro 156 25,000

General Pipeline Co., Liebere, Cal., to Mojave. Cal 52 5,000

Gulf Pipeline Co., Tex. -Okla. State Line to Port Arthur, Tex 458 28,000

Gulf Pipeline Co., Batson, Tex., to Sour Lake and Houston 76 14,000

Gulf Pipeline Co., La. -Tex. State Line to Lufkin Station, Tex.... 117 9,600

Gulf Pipeline Co., Saltillo Station, Tex., to Fort Worth, Tex 124 7,000

Gulf Pipeline Co. of Okla., Bartlesville, Okla., to Okla. -Tex. bound-
ary 275 25,000

Gulf Refining Co., of La., Mansfield, La., to La. -Tex. boundary.. 21 10,000

Gulf Pipeline Co., Olean, Tex., to Red River, Tex 305 8 inch

Gulf Pipeline Co., Fort Worth, Tex., to Saltillo, Tex 124 6 inch

Gulf Pipeline Co., Caddo, Tex., to Lufkin, Tex 98 6 inch

Gulf Pipeline Co., Ranger, Tex., to Fort Worth, Tex 86 8 inch

Gulf Pipeline Co., Houston to Sour Lake, Tex 63 6 inch

Hale Petroleum Co., Eldorado, Kas., to Wichita, Kas 20 7,500

Illinois Pipeline Co., Alton, 111., to Centerbritlge, Pa 1,300 60,000

Illinois Pipeline Co., Grass Crei k, Wyo., to Chatham, Wyo 25 ....

Illinois Pipeline Co., Elk Basin, Wyo., to Frannie, Wyo 20 ....

Illinois Pipeline Co., Big Muddy, Wyo.. to Casper, Wyo 20 20,000

Imperial Pipeline Co., Ltd.. Sarnia, Ont., to Cygnet, O l.')5 8 inch

Indiana Pipeline Co., Griffith, Ind., to Indiana-Ohio boundary.. 800 110,000

Magnolia Petroleum Co., Electra, Tex., to Sabine, Tex .t69 60.000

Magnolia Petrokum Co., Healdton, Okla.. to Fort Worth, Tex.. 137 60,oo0

Magnolia Petroleum Co., Gushing Dist., Okla., to Addington, Okla. 150 50,000

114 BULLETIN NUMBER SIXTEEN OF

PRINCIPAL PIPELINES— (Continued).

Capacity,

Pipeline Mileage Barrels
Magnolia Petroleum Co. (Double Line) Red River, Tex., to Beau-

mont, Tex ^O" ^ '"•^"

Magnolia Petroleum Co., Electra, Tex., to Bowie, Tex 76 8 inch

Maryland Pipeline Co., Kay County, Okla., to Ponca City, Okla.. ..

Midwest Refining Co., Salt Creek Dist., Wye. to Casper, Wyo 90 13,000

National Pipeline Co., Oil Fields in Wood Co., Ohio, to Findlay, O. 60 1,000
.National Pipeline Co., Oil Fields in Southeastern Ohio to Mari-
etta, Ohio 110 S'"*

National Transit Co., Nedska, Pa., to New York-Pa. boundary.. 205

National Transit Co., Colegrave, Pa., to Milway, Pa ITS

National Transit Co., Milway, Pa., to Fawn Grove, Pa :!r. id, 000

National Transit Co., Milway, Pa., to Point Breeze, P.i 70 ....

National Transit Co., Milway, Pa., to Centerbridge, Pa 70 ....

Natrona Pipeline Co., Salt Creek, Wyo., to Casper, Wyo 90 fi inch

New York Transit Co., Pa.-New York boundary to Buffalo, N. Y. 130 55,000
New York Transit Co., Olean, N. Y., to Bayonne, N. J., and Long

Island. N. Y 1,100

Northern Pipe Co., Pa.-Ohlo boundary to Pa.-N. Y. boundary.... 525 60.000

Oklahoma Pipeline Co., Creek County, Okla., to McCurtain, Okla. 229 35.000

Paragon Refining Co., Sandusky County, Ohio, to Toledo, Ohio.. 237 4,000

Pierce Pipeline Co., Healdton, Okla., to Fort Worth, Tex 135 ....

Prairie Pipeline Co., Drumright, Okla., to Ranger, Tex S inch

Prairie Pipeline Co. (Double Line), Ranger, Tex., to Red River,

Tex 260 S inch

Prairie Pipeline Co., Cushing Dist., Okla., to Humboldt, Kan.... 701 100,000
Prairie Pipeline Co., From Humboldt, Kan., to Sugar Creek, Mo.,

and Wood River, 111 1,820 94,000

Prairie Pipeline Co., McCurtain. Okla., to Ida, La 90 31,000

Prairie Pipeline Co., Eldorado-Augusta, Kan., to Neodesha, Kan. S5 ....

Pierce Pipeline Co., Healdton, Okla., to Fort Worth, Tex 135 ....

villf. Pa 210 9,000

Producers' Transportation Co., Coalinga Dist., Cal., to Junction,

• Cal 41 15,000

Producers" Transportation Co., Sunset Dist., Cal., to Junction, Cal. 50 20,000

Producers' Transportation Co., Kern River Dist., Cal., to McKitt-

rlck, Cal 3<j

Producers' Transportation Co., Lost Hills Dist., Cal., to Trunk

Line, Cal 13

Producers' Transportation Co., Lost Hills Dist., Cal., to Trunk

Line, Cal 3

Producers' Transportation Co., Junction, Cal., to Port San Luis,

Ca' 74 30,000

Pure Oil Pipeline Co., Morgantown, W. Va., to Marcus Hook, Pa. 250 10,000

Hlo Brava Oil Co., Saratoga, Tex., to Sour Lake, Tex 13 1,500

Pierce Pipeline Co., Fort Worth, Tex., to Red River, Tex 76 8 inch

SInclalr-Cudahy Pipeline Co., Cushing Dist., Okla., to Kansas Citv

and Chicago " -jq

.SInclalr-Cudahy Pipeline Co., Cushing Dist, Okla., to CoffevviUe,

'^^" : 70

SInrliilr-Cudnhy Pipeline Co.. branches and lateral in Okla. and

'^""""" 340 50,000

.SInclalr-Cudahy Pipeline Co.. Cushing field, Okla., to Whiting,

^ '"" 8 inch

Rlncliilr-Cudahy Pipeline Co.. Cushing field to Healdton, Okla.. .. 8 inch

Southern Plpellno Co., Pa.-W. Va. boundary to Philadelphia, Pa.. 1,130 51.000

SoulhwcHtcrn Penn. Pipelines, exclusively in southwestern Pa.... 1,650 45,000

atan.Inra Oil Co.. Cal., Kern River Dist, Cal., to Richmond, Cal.. 2S1 65,000

KANSAS CITY TESTING LABORATORY 115

PRINCIPAL PIPELINES (Concluded).

Pipeline Mileage

Standard Oil Co., Cal., Midway Dist., Cal., to Bakersfield, Cal. . 32

Standard Oil Co., Cal., Coalinga Dist., Cal., to Mendota, Cal 29

Standard Oil Co., Cal., Lost Hills Dist., Cal., to Pond, Cal 21

Standard Oil Co., Cal., Xorthan Dist., Ca!., to El Segundo, Cal.. 24

Standard Oil Co., Cal., Newhall Dist., Cal., to Ventura, Cal 45

Standard Oil Co., Cal., Santa .Mina Dist., Cal., to Port Hartford,

Cal 32

Standard Oil Co. of La., Ida, La., to Baton Rouge, La 522

Sun Co., Seneca and Wood Co., O., to Toledo, 0 250

Sun Pipeline Co., Humble. Tex. (also Yale, Okla.) to Sabine Pass,

Tex 100

Sun Pipeline Co., Humble, Tex., to Sour J^ake, Te.x 53

Sun Pipeline Co., Sour Lake, Tex., to Spindle Top. Tex 23

Sun Pipeline Co., Spindle Top, Tex., to Sabine Pass, Tex 25

Sun Pipeline Co., Batson, Tex., to Sour Lake, Tex 16

Sun Pipeline Co., Spindletop, Tex., to Sun Station, Tox 4

Texas Co. (main lines) Bartlesville, Okla., to Port Arthur, Tex. . 742

Texas Co. (main lines) Electra, Tex., to West Dallas, Tex 160

Texas Co. (main lines) Vivian, La., to Port Arthur, Tex 253

Texas Co. (main lines) Evangaline, Tex., to Garrison, Tex 96

Texas Co. (main lines) Healdton, Okla., to Sherman, Tex 60

Texas Co. (laterals) in Oklahoma and Texas 222

Texas Co. Dennison, Tex., to Port Arthur 400

Texas Co., Logansport, Tex., to Port Arthur, Tex 155

Texas Co. Ranger. Tex., to Fort Worth, Tex S5

Texas Co. (two lints) Dallas, Tex., to Fort Worth, Tex 60

Texas Co., Dayton, Tex., to Goose Creek 25

Texas Co., Electia, Tex., to Fort Worth, Tex 130

Texas Co., Humble, Tex., to Houston, Tex 15

Texas Co., Healdton, Okla., to Gates Station, Tex

Tidewater Pipe Co. (main line) Stoy, 111., to Bayonne. N. J S30 11,000

Tidewater Pipe Co. (laterals) in Pennsylvania, N. Y., 111. and

Ind 1,929

Union Oil Co., Orcutt, Cal., to Port San Luis, Cal 65 ....

Union Oil Co., local lines in Ventura County, Cal 43 ....

Union Oil Co.. local lines in Los Angeles, Orange County, Fit Ids,

Cal 51

Valley Pipeline Co., Coalinga Dist., Cal., to San Francisco Bay... 170 25,000

War Pipeline Co., Cushing Field, Okla., to Humboldt, Kan S inch

Wilburine Pipeline Co., Shannopin, Pa., to Warren, Pa 125 5,000

Yarhola Pipeline Co., Healdton, Okla., to Cushing, Okla 135 9,000

Yarhola Pipeline Co., Cushing, Okla., to St. Louis, Mo., and Wood

River, 111 400 36,000

Capacity,
Barrels

65.000

28,000

20,000

27,000

1,400

20,000

35,000

1,000

21,000

6 inch

S inch

S inch

8 inch

6 inch

20,000

17,000

20,000

9,600

12,000

6 inch

8 inch

8 inch

S inch

8 inch

6 inch

6 inch

S inch

116 BULLETIN NUMBER SIXTEEN OF

PIPE LINE TRANSPORTATION.

The oil pipe line was fi^st introduced about 56 years ago and
since that time has so demonstrated its superiority as a means of
carrying- crude oil from the well to the refinery, that this method of
transportation has largely superseded all others This has made pos-
Mble the building of refineries in or near the large consuniing cen-
ters, rather than at the wells, which are usually remote from the
centers of population.

The pipes for conveying the oil are laid on the surface of the
ground or at a depth varying from 18 inches to 3 feet beneath the
surface and the main lines are generally eight inches in diameter.
The oil is forced through the pipes by means of pumps operated either
by steam or by internal combustion engines. The pump stations are
located from IVo to 90 miles apart, varying with the condition of
the country through which the pipe lines extend, and the viscosity of
the oil to be handled.

Some of the large pipe line systems are hundreds of miles in
length. It is estimated by the U. S. Geological Survey that the total
mileage of oil trunk lines in the United States today is approximately
34,000 and that the gathering systems, which are a fundamental part
of the trunk systems, aggregate about 11,500 miles in length, making
a total of 45,500 miles.

At the tim.e most of the lines were constructed, the average cost
per mile based on eight inch pipe was about $6,500. The cost of the
average pump station at that time varied from $130,000 to $250,000.
The fixed investment in pipe lines is estimated to be approximately
$500,000,000.

The difference between the published pipe line tariff rates and
the railroad rates for shipping crude oil have always been so large
that refiners and producers even though they have no pipe line sys-
tems of their own, cannot afford to ship by rail except for compara-
tively short distances. The pipe line rates, although greatly increased
in recent years, are still much lower than those charged by the rail-
roads for tank car shipments.

In the construction of oil trunk lines, a reconnaissance survey
is first made of the route for the line. In making the choice, at-
tention is given to avoiding as much as possible excessively rough
country, swamps, rivers, etc., and selecting a route which will admit
of pumping stations being located near suitable supplies of water.
Where possible, the lines are routed along or near the lines of rail-
roads. In some instances they have been placed in the railroad right
of way, the construction and maintenance of the pipe lines being
greatly facilitated thereby. As soon as the route is definitely de-
cided upon, careful surveys are made and maps prepared showing
the exact locations, grades and contours. Rights of way for one or
more Imes of pipes and for telegraph and telephone lines are pur-
chased outright; in others, they amount to a perpetual easement for
the use of the land upon which the pipe lines and telegraph lines
are constructeo, giving the owners of the lines ingress and egress
to and from the property for the purpose of laying new lines and

KANSAS CITY TESTING LABORATORY 117

operating and maintaining the ones in use. In some states pipe line
companies have been granted powers of acquiring rights of way
by condemnation proceedings.

The specifications for the pipe require that it be of a uniform
quality of steel, that the threads be carefully made so as to make as
perfect a union between the joints as possible, and that it be capable
of safely withstanding an internal pressure of 2,000 pounds per square
inch.

The actual construction work is commenced by the "right-of-way
gang" who prepare the difficult places of the route selected. They
remove the trees where these will interfere with the construction
work, dig ditches and place casings at railroad crossings, build bridges
across rivers and where necessary, build roads to facilitate the haul-
ing and handling of the pipe.

Behind the "right-of-way gang" come the "stringing gang" who
distribute the pipe.

The "stringing gang" is followed by the "pipe-laying gang."
Where the work is done by hand, that is, using ordinary pipe tongs,
this gang consists of about forty men. In its group are stabbers,
tongsmen, rope men, bar men, jack men, etc., each of whom has his
special work to perform in joining one length of pipe to another. In
some instances the pipes have been joined by pipe machine. This is
a more modern method enabling a very much smaller laying gang
to be used and doing much more rapid work. Cases are on record
where one pipe machine operated by a gang of 28 men has laid as
much as 8,700 feet of eight-inch pipe in one day of nine hours, where-
as the usual accomplishment of an ordinary gang of 40 men is from
2,500 to 4,000 feet per day.

Following the pipe gang comes the "ditching gang" whose duty
is to dig the ditch and bury the pipe. Where the route is through
comparatively level country free from rock in place, ditching ma-
chines can be used to good advantage. Where the country is hilly,
plowing the ditch with teams and shoveling the dirt out by hand,
is often advisable, but where rocky country is encountered, it is often
necessary to dig the ditch entirely by hand, blasting much of the
material to be removed. In some instances, the ditch has been dug
first and the pipe joints, resting on skids or sleepers, were screwed
into place over the open ditch. Where rivers or large bodies of water
are to be crossed, it is customaiy to join the pipe on a flat boat or
raft, which is moved along as the w^ork proceeds. In places where
the cost of digging ditches would be excessive, or where the pipe
lines if buried would pass through sti'ongly alkaline soil, it is usual
to paint the pipe with asphalt, then before the asphalt has had op-
portunity to dry, to cover the painted pipe with a good grade of
roofing paper, applying on the outside of the paper a second coat of
asphalt.

The viscosity of the oil to be transported and the topography of
the country through which the pipe lines pass, are the governing
factors determining the distance between pumping stations. The
average distance between pumping stations in the midwestern and

118 BULLETIN NUMBER SIXTEEN OF

<^astern States is about 35 miles, while the average distance between
stations in California, where a relatively thick, viscous oil is han-
dled, is about 12 miles, although stations are sometimes not more
than a mile and a half apart, and in extreme cases are placed as
much as 90 miles apart.

The operating equipment of a pumping station consists of a
pump house, boiler house, tool house, garage or barn, office, prob-
ably two oil tanks, ranging in size from 10,000 to 55,000 barrels ca-
pacity, water tower, fuel oil tanks and feed water tanks.

Equipment is usually provided in excess of ordinary demands
so that there is always in reserve extra pump power to meet un-
usual demands, thereby avoiding shut-downs where repairs are needed
to pumps and boilers. The usual forms of power are steam pumps
and internal combustion engines. The pumps are designed to deliver
through an eight inch pipe line approximately 30,000 barrels of oil
in 24 hours, working under a line pressure of 700 to 900 pounds per
square inch.

Practically all the pipe line companies engaged in the transpoi'ta-
tion of petroleum have, in addition to their trunk lines, extensive
systems of gathering lines. These are provided for the purpose of
collecting the oil from the produceis' tanks and running it to a tank
farm or to some point where it can conveniently enter the main trunk
lines. In some cases, however, these gathering systems are owned
by the producing companies, and not by the same companies that
operate the trunk lines. The pipe used in such systems is usually
smaller than that in the trunk line, most of it being from four to
six inches in diameter.

As in the case of railroad operations, it is necessary to pro-
vide means for instant communication between different parts of a
pipe line system. For this reason it is usual for the pipe line com-
ganies to own and operate their own telegraph and telephone sys-
tems. The telephone lines usually parallel the pipe lines, and are
constructed along the same right of way, so that the line walker who
patrols the pipe lines can also look after the condition of the tele-
phone and telegraph system.

A pipe line system such as described is administered from a gen-
eral office, and from branch offices located at convenient points in
the territory served. The system is divided into divisions, each
division being under the supervision of a superintendent, who looks
after the operations of the line within his territory. The division is
in turn sometimes subdivided into districts, each district being in
charge of a foreman. Foremen report directly to the superintendents
of their districts, and the superintendents to the general manager
who has his office at the headquarters of the company.

The office is divided into several departments, such as an oil
transportation department, an engineering department, a legal de-
partment, a tax department, an accounting department and a treas-
ury deparment. (The above matter v/as furnished by C. P. Bowie in
report of Bureau of Mines No. 2161.)

In general it may be said that the cost of transportation of
petroleum is 4c to 10c per 100 barrels per mile. This widely varies

Without

Typical Oil

Booster

capacity per

Stations

day @ 800 lbs

$6,500

6,000

8,500

18,000

11,000

30,000

18,500

60,000

KANSAS CITY TESTING LABORATORY 119

because of the different ground contours, temperatures and oil vis-
cosities.

Typical costs per mile of pipe line are as follows: (Sulentic
in "Petroleum")

Including
Booster
Stations

4 inch line .....$9,000

6 inch line 12,500

8 inch line 16.000

10 inch line 19,000

In order to make a very crude e.-timats of the cost of transport-
ing oil by pipeline when using equipment of the highest economy,
assume a single line operating under the following conditions at a
load factor of 80 per cent for 300 d.nys per year:

Size of line, 8 inches.

Length of line, 33 miles.

Pressure in line, 700 pounds per sqrare inch.

Rate of discharge, fOO barrels per hour.

At this rate, the discharge would be 21 600 barrels per day or
6.480,000 barrels per year of 300 days. Assuming 6.5 barrels per ton,
the yearly discharge would approx'mate 1,000,000 tons. The work
equivalent of this discharge would be 33,000,000 ton-miles, calling
for the continuous expenditure of 257 hp. Assuming the mechanical
efficiency of the engine to be 75 per cent, the actual horsepower
necessary to install would be 342.

The assumed costs would be as follows:

Line: 33 miles at $165 per foot $287,500

Right of way at $0 25 per rod 2,640

Freight: 79 cars at $250 19,750

Haulage: TOO tons at $14 50 13,050

laying pipe at $0,075 per foot 13,060

Burying pipe at $0.20 per foot 34,850

Engines, pumps, installed accessories 68,500

Pump stations, buildings and foundations 30,000

Tanks-
Two 55,000 barrel at $18,500 each 37,000

Two 500 barrel at $500 each 1,000

Telegraph line: 33 miles at $550 18,150

Superintendence and incidentals 8,500

Total assumed costs $534,000

The operating expense, including fixed charges based on the total
assumed costs would be as follows:

Interest at 6 per cent $32,040

Depreciation at 5 per cent 26,700

Administration 10,000

Attendance at pump stations and lines 11,500

Repairs to equipment, lines, etc 4,000

Fuel for pumping— 3,000 barrels at $2.65 7,950

Total operating expense $92,190

120 BULLETIN NUMBER SIXTEEN OF

From which the cost of operation per ton-mile under the assumed

conditions would be

92,190

= $0.0028

33,000,000

The relation between the cost of pipe line transportation and
rail transportation is in the ratio of 1 to 10.

It should be noted that most of the pipeline costs are fixed and.
are mainly independent of the amount of oil pumped. As a result
the transportation cost per ton-mile will vary almost inversely with
the load factor of the line. If this hypothetical pipe line should be
operated only one-tenth of the time assumed, the unit transportation
cost would equal the rail cost. FurLhermore, these figures are based
on a life of 20 years (5 per cent amortization). A railroad would
probably be used for various classes of freight as long as it existed,
but a pipe line is of service only as long as oil is present for trans-
portation. If the pipe line in question were to become obsolete in 10
years through the exhaustion of the oil fields or other causes, the
ton-mile cost would be greatly increased.

The following examples show the relations existing between pres-
sure, capacity, diameter, length of line and power required.

Disregarding viscosity, the general hydraulic formula for friction
head in a pipe discharging a uniform volume is

v-"L
F = k (1)

2gD

in which

F = friction head in feet of water = lb. per sq. in. -^ 0.433

k = friction coefficient for 38 gravity oil = 0.024

V = velocity of flow, ft. per sec.

g = acceleration of gravity = 32 2 ft. per sec.

L = length of line, ft.

D = diameter of line, ft.

The formula for pressure in the line may be stated as
v=L

P = 0.433 k (2)

2gD
m which P - pressure in line in pounds per sq. in.

The discharge Q of the line, cu. ft. per sec. can be easily de-
rived and stated as ^ j

3.1416 D^r

^ = — r- (^)

i"orn,nr\?/'"'i'',^ directly as v. Since P varies directly as v=^ in
I' varies ifrec'tly ^s'q"'' "^ '' ' '" ^''™"^' ^^^ '' ^""'''' '^^^

KANSAS CITY TESTING LABORATORY 121

The net horsepower required for a pipe line may be most readily
calculated by noting that the pressure per square foot is equal to
the number of foot-pounds required to displace 1 cu. ft. of oil or
144 PQ

Hp. = (4)

550

The following data in regard to the 36-mile, 8-inch Alton pipe
line operating between Carlton and Wood River, is given by S. A.
Sulentic, in "Petroleum." This line, constructed in 1913, has four
stations, in each of which are installed four units each consisting of
a 100 horsepower type of engine direct-connected to a 6 inch by 18
inch herringbone-geared power pump with 8 inch suction and 6 inch
discharge. The performance of one station equipment (three units)
is as follows:

Oil pumped during 10 days, barrels... 140,000

Oil pumped per day, average, barrels 14,000

Pressure maintained in line, pounds per sq. in 700

Brake horsepower, average 196

Pump efficiency, estimated, per cent 85

Fuel consumed by engines during 10 days, barrels.... 65.8

Fuel consumed by engines per day, pounds 2,020

Brake-horsepower-hours per day = 196 X 24 4,704

Fuel consumption per b.hp..-hr. pounds 0.43

Ft.-lb. of work per day developed by the engine

1£6 X 33,000 X 24 X 60 9,320,000,000

Ft.-lb. of work per day in oil pumped = 9,320,000,-

000 X 0.85 (85% efficiency) 7,900,000,000

B.T.U. in fuel consumed per day = 2,000 X 18,000 36 000,000

Ft.-lb. of work per 1,000,000 B.T.U 217,000,000

Daily operating cost:

Fuel oil: 6.58 barrels at $150 9.87

Lubricating oil: 2 gallons at SO. 22 0.44

Cylinder oil: 16 gallons at $0.21 0.34

Attendance: Total salaries of 2 engineers, 2
assistant engineers, 1 chief engineer and 2
telegraph operators 41.50

$52.15

Cost per b.hp.-hr. ($52.15 ^ 4,704) 0.011

Cost per barrel of oil pumped ($52.15 -4- 14 000).... 0.0037

Bbl. of oil pumped per barrel of fuel consumed

(14,000 ^ 6.58) 2,130

122

BULLETIN NUMBER SIXTEEN OF

^6

sso'
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-iMrvTirn»ii-w3

5^ /c? /J so a^ JO js '/o '-ij? so ss ao as
Kir. 20— ViMfOHity and I'hysical Properties of Typical Pipe I^ine Oil.

KANSAS CITY TESTING LABORATORY 123

FRICTION PRESSURE LOSS AND CAPACITY OF OIL PIPE
LINES AS AFFECTED BY VISCOSITY OF THE OIL.

cgq-
P= or

c g

P = friction pressure loss in pounds per square inch per 1000 ft. of pipe.

g = density of the oil at temperature of pumping.

q=gallons of oil per minute.

d= internal diameter of the pipe in inches.

c = coefficient from following table.

s q

M= (from the value found for M look up the value of c in the

d V table below. Use this value in the formulae given above.)

1.8

V=absolute viscosity = g (.00220 S )

S

S = Saybolt viscosity in seconds (for viscosity conversion factors see
section on method of testing for viscosity). (See fig. 21).

M C M C M C

10,000

0.190

750

0.355

85

0.600

9,000

0.195

700

0.360

80

0.550

8,000

0.200

650

0.370

75

0.500

7,000

0.210

600

0.380

70

0.460

6,000

0.220

550

0.390

65

0.425

5,000

0.230

500

0.395

60

0.450

4,000

0.240

450

0.400

55

0.500

3,000

0.250

400

0.415

50

0.550

2,500

0.260

350

0.430

45

0.600

2,000

0.270

300

0.440

40

0.675

1,800

0.285

250

. 0.460

35

0.775

1,600

0.300

200

0.480

30

0.900

1,400

0.310

180

0.500

25

1.100

1,200

0.320

160

0.515

20

1.350

1,000

0.330

140

0.520

18

1.500

950

0.335

120

0.550

16

1.700

900

0.340

100

0.555

14

1.950

850

0.345

95

0.570

12

2.200

800

0.350

90

0.585

, ,

124

BULLETIN NUMBER SIXTEEN OF

DIAMETER FUNCTIONS OF STANDARD IRON AND STEEL

PIPE.

Nominal

Actual

Diameter,

Diameter,

Inches

Inches (d)

d*

d'

.622

.14968

.09310

.824

.46101

.37987

/4

1

1.049

1.2109

1.2702

VA

1.510

6.7190

10.818

2

2.067

18.254

37.731

ly,

2.496

37.161

91.750

3

3.068

88.597

271 . 82

4

4.026

262.72

1057.7

6

6.065

1353.1

8206.4

8

8.071

4243.3

34248.0

8

7.981

4057.2

32381.

10

10.192

10790.

109980.

10

10.136

10555.

106990.

10

10.020

10080.

101000.

12

12.000

20736.

248830.

14

14.250

41234.

587590.

15

15.250

54085.

824800.

PIPE LINE FORMULA.
Compiled by the National Transit Co.

P = Gauge pressure in pounds per square inch.
M = Number of miles.

B = Discharge in barrels (42 gal ) per hour.
C = Constant for pipe sizes.

B

-V

CxP

M

C for 2-inch pipe = 36
C for 3-inch pipe = 289
C for 4-inch pipe = 1225
C for 5-inch pipe = 3600
C for 6-inch pipe = 9025
C for 8-inch pipe = 38416
C for 10-inch pipe = 116964
C for 12-inch pipe = 289444

For every 3 degrees above 35 degrees Be' add 1% to B.

For every 3 degrees below 38 degrees Be' deduct 1% from B.

Net H. P. = BxPx.00041.

KANSAS CITY TESTING LABORATORY

125

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126

BULLETIN NUMBER SIXTEEN OF

Fife' 21.— Relation of Viscosity to Temperature of Typical Crude

Petroleums.

KANSAS CITY TESTING LABORATORY 127

STORAGE OF PETROLEUM.

P'itroleum is usually stored above ground in cylindrical steel or
iron tanks of convenient proportions for requirements. A roof is
provided to prevent admission of rain water and contamination. In
the case of light oils evaporation losses are diminished by the use
of an air tight roof but in the latter case, a special equilibrium valve
is needed to allows the escape of the gas if the pressure exceeds a pre-
determined safe degree and to admit air when oil is abstracted. The
main features characterizing an oil tank are:

1. Large draw-off valve at lowest point to remove water and sedi-
ment.

2. One or two manholes near base for entry.

3. Inlet pipe leading above top of tank and either discharging on
base or flowing into second large pipe that conducts new oil to
the base of tank and prevents undue splashing and consequently
liberation of light products.

4. Garge glass or succession of gauge glasses to read off oil level.

5. Sometimes a float and outside measuring board and indicator to
show level of liquid.

6. Floating or adjustable suction pipe to draw oil from top of
liquid when discharging.

7. Sometimes for light oils in hot climates a water spray for roof
or a dished roof for holding water.

8. The construction of an earthen embankment round the tank en-
closing a space from one and a half to twice the volume of the
tank so that in the event of a fire, the burning oil may be pre-
vented from spreading.

9. All oil tanks should be painted outside: the finishing coat should
be white or nearly so in a hot climate to prevent undue absorp-
tion of heat.

10. Oil tanks, especially when intended for light gravity oil, should
be very closely riveted, and great care should be taken to close
the seams before the rivets are inserted and driven.

11. One or more dipping pipes, sometimes combined with the escape
valves are usually fitted for sampling.

The cost of steel tankage varies with the price of metal and
labor, but for standard sized tanks the price varies from about
$1.00 per barrel of capacity for 1,000 barrel tanks to $0.30 per
barrel for .55,000 barrel tanks (1921).

128 BULLETIN NUMBER SIXTEEN OF

LOSSES IN THEf STORAGE OF CRUDE PETROLEUM.

The principal losses in the storage of crude petroleum are due
to evaporation, to fire and to seepage.

Oils having the greatest loss are the crude oils containing the
most gasoline, since they are the most volatile, most readily form
explosive and inflammable mixtures and due to their low viscosity
most readily flow through walls of loose texture.

The loss from evaporation is greater the larger the amount of
gasoline. The loss also depends upon the temperatures of storage and
upon the amount of surface exposed to atmospheric circulation. If
the tank or container is perfectly tight, then there will be no loss
by evaporation.

There are three general types of storage now in use in the Mid-
Continent fields; — the earthen reservoir, the steel tank with wooden
roof and the steel tank with a steel, gas-tight roof.

The 55,000 and 35,000 barrel steel tanks are the usual sizes. Al-
together there are more than 3500 of these large steel tanks in use
in the Mid-Continent field.

The earthen storage is extremely wasteful from both seepage and
evaporation. Petroleum standing in this type of reservoir has been
known to shrink ^Q';'c in volume in two or three weeks. The shrink-
age in value is of course much greater as the portion lost by evap-
oration is the best of the gasoline.

The following losses by evaporation took place in steel tanks
with no seepage, with wooden roof covered with paper and tarred and
apparently tight. The oil was of 40° Be' gravity and the tanks were
of a diameter of 114% feet.

Capacity Loss in Gauge Actual Loss Period Per Cent Loss
55,000 bbls. 1 ft. 1% in. 2101 bbls. 5 mos. 4.2

55,000 bbls. 1 ft. 2% in. 2235 bbls. 4^/2 mos. 4.6

55,000 bbls. 11 Vs in. 1700 bbls. 31/2 mos. 3.4

55,000 bbls. 1 ft. % in. 1910 bbls. 31/4 mos. 3.8

The above figures indicate that there might be a loss of 1%
per month of storage in wood roof steel tanks and this might amount
to as muc'h as 6,000 barrels per year per tank.

It has been claimed that oil stored in white tanks is subjected to
1 to IVo'-zr less evaporation than in red tanks and 2y2% less evap-
oration than in black tanks.

Various types of insulation have been used with success.
A typical storage temperature for the Mid-Continent field for
oil stored above ground would be 80° F. A typical temperature of the
ground for a submerged tank would be 60° F. which would more
nearly approach the storage temperature of the air for the whole year.
♦ u , 1 u ^''"^l ^^ successfully and cheaply built in the ground,

they would have the advantage of almost perfect insulation from out-

Jf Ljfk •;'" %"'^ "^"u"'"' ^^ '^'^^^^^ ^t practically the temperature
at which It comes from the ground. For this submerged type of tank,

t on ' /; irnM^K""'' ^""^It ^^ ^I'^P'^^' '^ ^^P^ble of perfect construe!
imnnrvio,^« f f mono ith.c, well reinforced and lined with a coatine

impervious to water and gasoline.

KANSAS CITY TESTING LABORATORY 129

APPORTIONMENT OF THE LOSS SUSTAINED BY CRUDE ON
ITS JOURNEY FROM THE WELL TO THE REFINERY.

Per Cent Volume Evaporated.

Autumn

Location of Loss — Summer Spring Winter Ave.

Flow tank 1.2 1.0 0.8 1.0

Filling lease tank 1.2 1.0 0.8 1.0

Lease storage 1.8 1.4 1.2 1.5

Gathering 1.3 0.9 0.8 1.0

Transportation 1.2 0.9 0.8 1.0

Tankfarm 0.9 0.7 0.6 0.7

Total 7.6 5.9 5.0 6.2

Next in quantity after the evaporation losses in the storage of
crude oil is the loss due to fire. Petroleum fires destroyed 12,850,000
barrels of oil in the United States in 1918. From Januarv 1. 1908, to
January 1, 1918, approximately 12,850,000 barrels of oil and 5,024,506,-
000 cubic feet of gas were destroyed by fire in the United States en-
tailing a total estimated property loss of iR25,254.000. During this
period 503 fires were reported. Of these fires 310 were caused by
lightning and 193 by other causes. The losses from the fires caused
by lightning were estimated to be $11,148 000 and from those due
to other causes, $14,106,200. Directly and indirectly the fires resulted
in the deaths of nearly 150 persons and were responsible for almost
as many more being permanently disabled.

Loss from fire in the oil field storage in the year 1916 amounted
to about $4,000,000.

The causes of fires are electrical discharges or open flames in
the presence of an inflammable or explosive mixture of gasoline and
air. The amount of gasoline vapor in air necessary for an explosive
mixture is within the limits of iy2 per cent and 5 per cent by weight.
Less than the lower limit or more than the upper limit will not ignite.
In an open tank if the amount at the surface of the oil exceeds 1%
per cent there is at some point an explosive mixture and an igniting
temperature of 900 degrees F. or over will cause it to take fire.
In a perfectly tight tank with gasoline vapor in excess of the upper
limit for an explosive mixture, there will be no fire unless the roof
of the tank is open at some point.

The ingress of a flame through an opening may be prevented in
the same way that the flame in the Davy miner's lamp is prevented
from passing outward. This operates by having some metal screen
or other material cool the flame and prevent it being propagated into
the tank. This will not prevent ignition from an electrostatic dis-
charge in the vapor space of the tank.

Methods for prevention of fires of oil in storage are as follows:

1. Means of preventing the passage of the spark in a portion of
the unfilled space of the tank.

2. The maintenance of a mixture in the unfilled portion of the
tank which is not an explosive mixture.

130

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY 131

3. A tank so placed and constructed that the cooling effect of
the walls will tend to smother the flames and the ingx'ess of air will
be so arranged that the fire is not readily fed.

4. A means for quickly eradicating the fire after it is ignited.

Several more or less successful methods for extinction of oil
tank fires have been in use. The best involves the use of mixtures of
sodium bicarbonate and sulphuric acid which produce sufficient carbon
dioxide to smother the flame. If some sort of saponifying agent is
used the carbon dioxide will make a froth which will float on the sur-
face of the oil and is very effective in extinguishing the flame.

The application of steam is very effective but in the storage of
a very large amount of oil the steam is not always available when
needed and at the point where needed.

For small oil fires dust or other finely divided mineral matter is
effective in extinguishing the fire.

132 BULLETIN NUMBER SIXTEEN OF

ST\NDARD SPECIFICATIONS FOR BRICK OR TILE
ENCLOSED TANKS.

A concrete foundation must be built around base of tank and upon
this must be built a 12 inch brick or interlocking tile wall leaving
an airspace between wall and tank of not less than 6 inches. At
the ba«e of the air space a concrete gutter must be formed having
a Frade from the quarter points each way to a sewer opening: sewer
to be carried underneath the wall to a running trap just outside and
at least 2 feet underground.

The roof of the structure is to consist of a steel supporting frame
upon which is to be placed successively No. 24 gauge dove-tailed plate
reinforcement, concrete, metallic lath and a finish coat of cement
mortar. The metallic lath to be carried over the cornice and fastened
to the top of the wall and beneath the reinforced concrete ring which
forms the wall plate: by this the whole concrete surface will have a
protection of metallic lath. Walls of structure to be plastered on the
outside with cement mortar.

The structure must have a 24 inch concrete or other incombustible
ventilator resting on a steel ring, lower side of ring to be covered
with No. 4 mesh wire screen: upper side of ring to be sealed with
two flap (butterfly) doors, normally held open by chain with fusible
link which, in case of the presence of heat, will allow the doors to
close and, in case of gas pressure inside of structure, will force the
flap doors open, and when pressure is relieved will allow them to close.

There should be placed about one foot above top of foundation a
cast iron ventilating shutter on the end of a standard 8 inch nipple
pipe, with flap door normally held open by wire rope with two fusible
links, one near top of tank and one near flap door. Flap door to be
provided with brass pin to insure easy operation. The face of the
casting should have such bevel that when the flap door is closed it
will be held closed by gravity. Tanks 20 feet or less in diameter to
be provided with four, over 20 feet and under 50 feet m diameter to
be provided with six, and 50 feet or over in diameter to be provided
with eight such ventilators: to be equally spaced around tank in each
case.

An opening must be left in the roof of the structure to allow of
entrance to the top manhole of the tank, same to be covered with a
door built of tile in steel frame, sealed lightly on asbestos gaskets
and to bo kept closed and locked at all times, except when in use for
repairs.

Opposite the bottom manhole of the tank a door opening must be
left in the wall, same to be covered with a door built of tile in steel
frame, sealed lightly with asbestos gaskets, and to be kept closed and
locked at all times, except when in use for repairs.

At the apex of the tank there must be placed a ring spray capa-
ble of handling all water that may come to it through a 2 inch pipe
under T.*") pounds pressure: pipe to be carried up inside the structure
and to l)c controlled l)y a valve accessibly located at a distance and to
be made automatic by means of a fuse.

All pump connections are to be carried underground into the
nousang.

KANSAS CITY TESTING LABORATORY 133

FUEL OIL STORAGE TANKS KEGULATIONS— DRAFTED BY
FIRE PROTECTION ASSOCIATION.

The Committee on Inflammable Liquids of the National Fire Pro-
tection Association has submitted the following: tentative regulations
covering the construction of concrete tanks for fuel oil storage.

Setting of Tanks. — (a) Tanks, if underground, shall be buried
so that the top of the tank will be not less than three feet below the
level of the surface of the ground and below the level of any piping
to which the tanks may be connected.

(b) Tanks shall be set on a firm foundation.

(c) All tanks shall be provided with a concrete or other non-
bustible roof.

Material and Construction of Tanks. — (a) Reinforcement — Suf-
ficient steel reinforcement shall be used to resist the oil pressure,
and the horizontal and vertical reinforcement shall be proportioned
properly and located to reduce the shrinkage cracks, so that they
will be too minute to permit leakage. The fiber stress in the steel
shall not exceed 10,000 pounds per square inch. (Note. A fiber
stress of 10,000 pounds per sq. in. should prevent shrinkage cracks
although a number of tanks have been designed with a fiber stress of
6,000 to 8,000 pounds.)

(b) Concrete. — The concrete for floor and walls should be at
least 8 inches thick, mixed in the proportion of 1:2:3 or better 1:1% :3
and having the coarse aggregate of clean, dense, crushed rock or
gravel ranging in size from one inch down. The concrete shall be
thoroughly mixed, carefully placed and worked around the reinforce-
ment. The forms should not be held together by wire as is fre-
quently done in building construction because leakage is likely to
take place along the wire. The concrete shall preferably be poured
in a continuous operation so as to foiTn a monolithic construction.
(Note. Where this cannot be done the bottom shall be poured with-
out joints and the walls as a second continuous operation. One
method of making a tight joint between the bottom of the tank and
the walls is by means of a strip of galvanized iron six inches wide
with joints riveted and soldered, so as to form a continuous band.
This strip should be vertically embedded three inches in the floor
slab and on the center line of tVie wall. The floor slab under the
walls should be thoroughly cleaned, and before pouring the walls a
mixture of 1:1 mortar should be placed in the bottom of the forms
and around the galvanized strip to make a tight joint.)

(c) Finish. — As soon as the w&ll and sides have been poured
the floor shall be floated and troweled smooth. The wall forms shall
be removed as soon as the concrete has hardened sufficiently to be
self-sustaining and all projections and irregularities shall be removed
from the surface and all cavities filled with a 1:1 mortar thoroughly
rubbed in and troweled smooth. No plastering shall be applied.

(d) Aging. — The concrete shall be allowed to harden at least
30 days and longer if possible. (Note. To assist in the setting of the
concrete before it beccmes oil soaked it is advantageous to use sev-

134 BULLETIN NUMBER SIXTEEN OF

eral priming coats of a 1:4 solution of 40° Baume' sodium silicate,
followed by a finish coat of a 1:2 solution. This forms a glazed
surface on the concrete, which although it is not permanent, gives the
concrete an opportunity to harden until the protection from the sili-
cate of soda is no longer necessary.)

Location of Pipe Connections. — All pipe connections to the tank
shall be made through the top.

Venting of Tanks. — (a) Tanks shall be provided with a perma-
nently open vent, or with a combined fill and vent fitting so arranged
that the fill pipe cannot be opened without opening the vent pipe.

(b) Vent openings shall be screened with (30x30) brass mesh
or equivalent, and shall provide sufficient area for allowing proper
flow of liquid during the filling operation. Permanently open vent
pipes shall be provided with weather-proof hoods and terminate at a
point at least twelve feet above the top of the fill pipe and never
within less than three feet, measured horizontally and vertically,
from any window or other building opening. Where a battery of
tanks is installed vent pipes may be run into a main header. Individ-
ual vent pipes should, however, be screened between tank and header
and connection to the header should be not less than one foot above
the level of the top of the highest reservoir from which the tanks
may be filled.

(c) Fill pipes shall be screened and when installed in the vi-
cinity of a building, shall not be located within five feet of any door
or other opening and shall terminate in a metal box or casting pro-
vided with means for locking.

KANSAS CITY TESTING LABORATORY

135

PROPERTIES OF STANDARD STEEL ROOF STORAGE TANKS.

Barrels

U.S. Gall

5. Lbs.

Relative

Relative

Relative

Ca-

par

par

per

Weight

Cost

Sailing

Cost per

pacity

Dim

snsions

Inch

1 In.

Bbl.

Pounds

per Bbl.

Price

Pound

55,000

114.

5x30

152.80

6420

7.47

411,000

$0.3673

$20,200

$0.04916

37,500

95

x30

105.20

4420

8.00

300,000

0.4134

15,500

.05168

30,000

85

x30

84.24

3538

7.83

235,000

0.4133

12,400

.05277

25,000

75

x30

65.57

2754

8.08

202,000

0.4340

10,850

.05370

20,000

70

x30

57.12

2399

8.80

176,000

0.4750

9,500

.05398

15,000

60

x30

41.98

1763

8.67

130,000

0.4833

7,250

.05577

10,000

50

x30

29.15

1224

9.67

96,700

0.5400

5,400

.05582

5,000

35

x30

14.28

600

10.46

52,300

0.5800

2,900

.05545

2,000

35

xl2

14.28

600

16.00

32,000

0.9300

1,860

.05810

1.700

35

xlO

14.28

600

17.06

29,000

1.0240

1,740

.06000

3,800

30

x30

10.50

441

11.84

45,000

0.662

2,515

.05590

3,200

30

x25

10.50

441

12.06

38,600

0.688

2,200

.0570

2,500

30

x20

10.50

441

13.60

34,000

0.784

1,960

.0577

1,250

30

xlO

10.50

441

19.20

24,000

1.164

1,455

.0606

1,000

30

X 8

10.50

441

22.00

22,000

1.355

1,355

.0616

2,000

25

x25

7.29

306

15.50

31,000

0.8875

1,775

.0572

1,500

25

xl7'6"

7.29

306

15.80

23,700

0.943

1,415

.059

875

25

XlO

7.29

306

20.23

17,700

1.257

1,100

.0621

1,000

20

x20

4.66

196

20.60

20,600

1.190

1,190

.0578

500

20

XlO

4.66

196

27.60

13,800

1.74

870

.0631

1,000

30

X 8

10.50

441

24.40

24,400

3.10

1,550

Bleacher

760

30

X 6

10.50

441

31.19

23,700

1.89

1,435

Bleacher

Miscellaneous tanks:
U. S. gallons per inch of vertical tank = 0.4897 d'.
Barrels per inch of vertical tank = 0.01166 d".
d — diameter of tank in feet.

136

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY 137

RULES FOR FREIGHT SHU'MENTS OF GASOLINE AND

NAPHTHAS.

(See Pamphlet No. 9 — Bureau of Explosives — 30 Vesey St., New
York)

INFLAMMABLE LIQUIDS— RED LABEL,

1824 (a) All inflammable liquids must be shipped in packages
complying with specifications that apply, as follows:

(b) In tightly closed metal cans of not exceeding ten gallons
capacity, packed in wooden boxes complying with Specification No. 11.

(c) In well-stoppered glass or earthenware vessels of not ex-
ceeding one gallon capacity, cushioned in wooden boxes complying
with Specification No. 2, or cushioned in wooden barrels or kegs com-
plying with Specification No. 11, or in a well-stoppered glass or
earthenware vessel of not exceeding five gallons capacity, well cush-
ioned in a wooden box and not more than one such vessel in the box.
The completed package must comply with swing and drop tests pre-
scribed for boxed carboys by Specification No. 1.

(d) In well-stoppered glass, earthenware, or metal vessels of
not exceeding one pint capacity when flash point is 20 °F or lower
in wooden boxes complying with specification No. 2, or cushioned in
fiber board or corrugated strawboard containers complying with Speci-
fication No. 24.

(e) In wooden kits of not exceeding ten gallons capacity, packed
in wooden boxes complying with Specification No. 2, or cushioned in
wooden barrels or kegs complying with Specification No. 11.

(f) In metal-jacketed cans of not exceeding ten gallons capac-
ity, complying with Specification No. 23.

(g) In well-stoppered carboys of not exceeding thirteen gallons
capacity, cushioned in wooden boxes complying with Specification
No. 1.

(h) In wooden barrels or kegs complying with Specification No.
10 when the flash point of the liquid is not lower than 20°F, or in
wooden barrels or kegs complying with Specification No. 9 when the
flash point is lower than 20 °F unless otherwise provided in the tariffs
under which shipment moves.

(i) In metal barrels or drums complying with Specification
No. 5.

(j) In tank cars complying with Master Car Builders' specifica-
tions provided the vapor tension of the inflammable liquid corre-
sponding to a temperature of 100° F does not exceed ten pounds per
square inch. A tank car must not be used for shipping inflammable
liquids with flash point lower than 20 °F unless it has been tested
with cold water pressure of sixty pounds per square inch and sten-

I

138 BULLETIN NUMBER SIXTEEN OF

ciled as required by Master Car Builders' specifications and is
equipped with safety valves set to operate at 25 pounds per square
inch, and with mechanical arrangement for closing dome cover as
specified in paragraph 1824 (k).

(k) Liquid condensates from natural gas or from casinghead
gas of oil wells, made either by the compression or absorption process, M

alone or blended with other petroleum products, must be described as I

Liquefied Petroleum Gas when the vapor pressure at 100°F (90°F ^

Nov. 1 to Mch. 1 ) exceeds ten pounds per square inch.

When the liquid condensate alone or blended with other petroleum
products has a vapor pressure not exceeding ten pounds per square
inch, it must be described and shipped as Gasoline or Casinghead
Gasoline.

Liquefied petroleum gas of vapor pressure exceeding ten pounds
per square inch and not exceeding 15 pounds per square inch from
April 1 to October 1 and 20 pounds per square inch from October 1
to April 1, must be shipped in metal drums or barrels which com-
ply with Shipping Container Specification No. 5, or in special in-
sulated tank cars approved for this service by the Master Car Build-
ers' Association.

Liquefied petroleum gas of vapor pressure exceeding 15 or 20
pounds per square inch as provided herein, and not exceeding 25
pounds per square inch must be shipped only in metal drums or bar-
rels which comply with Shipping Container Specification No. 5.

Liquefied petroleum gas of vapor pressure exceeding 25 pounds
per square inch m.ust be shipped in cylinders as prescribed for com-
pressed gases.

When the liquid condensate, alone or blended with other petroleum
products has a vapor pressure not exceeding 10 pounds per square
mch, it must be described as Gasoline or Casinghead Gasoline and
must be shipped m metal drums or barrels complying with Specifica-
tion No. 5, or in ordinary tank cars, 60 pounds test class equipped
with mechanical arrangement for closing of dome covers as speci-
fied in Master Car Builders' specifications for tank cars.

Every tank car containing liquid condensates, either blended or
unblended including liquefied petroleum gas, as defined herein must
have safety valves set to operate at 25 pounds per square inch with
a toerance of 3 pounds above or below, and the mechanical arrange-
»H ?r. n!"[ -f "^ ^r" ,f "?^ '"''^^' «^ ^"^h cars must either be such
tho^nu.rtl 'V'^r^^t'^'^lly impossible to remove the dome cover while
wil be onpmJl^nf'''' K 'V^^?^'^ ^^ pressure, or suitable vents that

rhc\Le^:o";i^n?u:rbe^pio'vide'd.^'"'"^ '""^ ^^^^^^^^^ '' ^^^^^^^

KANSAS CITY TESTING LABORATORY 139

The shipper must attach securely and conspicuously to the dome
and dome cover three special white dome placards measuring 4x10
inches, bearing the following wording:

CAUTION

Avoid Accidents

DO NOT REMOVE THIS DOME COVER WHILE GAS
PRESSURE EXISTS IN TANK.

Keep Lighted Lanterns Away.

10 Inches

One placard must be attached to each side of the dome and one
placard be attached to the dome cover. The presence of these spe-
cial dome placards must be noted on the shipping order by the ship-
per and by the carrier on the billing accompanying the car. Pla-
cards must conform to samples furnished by the Chief Inspector of
the Bureau of Explosives.

(1) Carbon bisulphide in interior packages of capacity greater
than one-half gallon must be shipped in metal cans of not less than
28 gauge boxed, complying with Specification No. 2, or in metal bar-
rels or drums complying with Specification No. 5, such barrels or
drums not to exceed 55 gallons capacity. Carbon bisulphide may also
be shipped in tank cars complying with paragraph 1824 (j).

1825. (a) Packages containing inflammable liquids must not
be entirely filled. Sufficient interior space must be left vacant to
prevent leakage or distortion of containers due to increase of tem-
perature during transit. In all such packages this vacant space
must not be less than 2% of the total capacity of the container. In
tank cars the vacant space must not be less than 2'';(- of the total ca-
pacity of the tank, i. e., the shell and dome capacity combined. If
the dome of tank cars does not provide this 2%, sufficient vacant
space must be left in the shell of the tank to make up the differ-
ence.

(b) In packages containing alcohol, cologne spirits, high wines
or other distilled spirits of 150 proof or over, the vacant interior
space or allowance for wantage or ullage must be the maximum per-
mitted by the United States Internal Revenue Regulations.

1826. Interior packages containing one quai't or more of an in-
flammable liquid must be packed with their filling holes up and the
top of the outside package must be plainly marked "THIS SIDE UP."

1827. Wooden-jacketed cans and wooden kits must not be used
for the shipment of inflammable liquids, except as inside container.<5
as provided by Specifications No. 2 or 11.

140 BULLETIN NUMBER SIXTEEN OF

RULES FOR THE SHIPMENT OF PETROLEUM BY EXPRESS.

All shipments of articles subject to these regulations offered
for the transportation by express in interstate commerce must be
properly described by the shipper, and the proper and definite name
of the " dancrerous article must be plainly marked on the outside
of the package, in addition to the labels required herein, (a) Ar-
ticles for which detailed instructions for packing are not given herein
must be securely packed in containers strong enough to stand with-
out rupture or leakage of contents, a drop of four feet to solid brick
or concrete.

(b) Whenever orders are placed in foreign countries for the
importation of dangerous articles to be forwarded from port of entry
by express, the importer must furnish with the order to the for-
eign shipper and also to the forwarding agent at the port of entry,
full and complete information as to the necessary packing, marking
and labeling required by these regulations. The foi^'arding agent
must see that the packages are properly packed, marked and labeled.

35 (d) Interior packages containing 1 pint or more of an in-
flammable or corrosive liquid must be packed with their filling holes
up ard the outside package must be plainly marked "THIS SIDE UP."

Inflammable Liquids — Red Label,

(37) Except as herein prescribed, the maximum quantity of
any inflammable liquid packed in one outside container must not ex-
ceed 1 gallon when the flash point is 20 °F or below and must not ex-
ceed 5 gallons when the flash point is above 20°F and below 80°F.

(38a) Packages containing inflammable I'quids must not be en-
tirely filled. Sufficient interior space must be left vacant to pre-
vent leakage or distortion of containers due to increase of tempera-
ture during transit. In all such packages this vacant space must
not be less than 37r of the capacity of the container.

(39a) All inflammable liquids must be shipped in packages com-
plying with specifications that apply, as follows:

(b) In tightly closed metal cans of not exceeding 5 gallons ca-
pacity packed in wooden boxes complying with Specification No. 2
or cushioned m wooden barrels or kegs complying with Specifica-
tion No. 11. •■'.Of

(c) In well-stoppered glass or earthenware vessels of not ex-
ceeding 1 /luart capacity cushioned in wooden boxes complying with
Specification No. 2 or cushioned in wooden barrels or kegs comply-
ing with Specification No. 11. & i j'

n»» Iv^ ^" well-stoppered glass, earthenware, or metal vessels of

r« 90»v ; 1"^ °"'' F?* ^^^^"^^ ^ P°""^l> capacity when flash point

.JwuJx V'^'^V'^"*' 1 nuart capacity when flash point is above 20°F,

,lvin' within ^"'i"' "m '-o^'ugated strawboard containers com-

'ul ,7 Specification No. 24 and not exceeding 8 quarts in one

i^.J

KANSAS CITY TESTING LABORATORY 141

(e) In metal-jacketed cans of not exceeding 5 gallons capacity,
complying with Specification No. 23.

(f) In metal drums of capacity not exceeding 5 gallons, com-
plying with Specification No. 5.

(h) Liquefied petroleum gas, blended or unblended, when its
vapor tension corresponding to a temperature of 100 °F exceeds 10
pounds per square inch, must not be shipped by express except in
steel containers conforming to paragraphs 57, 58 and 59.

For complete directions see the Bureau of Explosive pamphlet
No. 9, Interstate Commerce Commission Regulations, 30 Vesey St.,
New York City.

142 BULLETIN NUMBER SIXTEEN OF

OWNERSHIP OF TANK CARS.
Tank Cars Owned By Railroads.

Name and Location. Tank Cars

Colorado & Southern 14

Delaware River & Union R. R -ill

Denver & Rio Grande **

East Jersey R. R 120

El Paso & Western »»

Kansas City Southern Ry. Co 19-'*

Los Angeles .t Salt Lake R. R. Co 214

Midland Valley R. R. Co 97

Missouri, Kansas & Texas Ry 6*^'

Moreno: Southern Ry. Co • 2

New Orleans, Texas & Mexico R. R 75

Northern Pacific R. R. Co 34

Oregon-Washington R. R. & Nav. Co 44

Pacific Electric Ry Co 29

Pennsylvania R. R. Co 514

Philadelphia & Reading Ry. Co. 20

St. Louis & San Francisco R. R. Co 629

St. Louis, Brownsville & Mexico Ry 59

St. Louis, Southwestern Ry. Co SI

San Antonio & Arkansas I'ass Ry. Co 81

Santa Fe Ry. Co 3,178

Santa Fe & Arizona Ry 4

Southern Pacific Ry 2.963

Texas & New Orleans R. R. Co 459

Trinity & Brazos Valley R. R. Co 25

9,813

Tank Cars Owned By Oil Industries.

Name and Location. Tank Cars

\imo Petroleum Co., Kansa.s City, Mo 60

.■\"ina Riflnini? Co., I.ouisville, Ky 50

.\.iax Casoline Co., Kansas <?ity, .Mo 3-3

.Akin Oiisoline Co. Tulsa, Okl-i 34

Allied Refining Co., The, Tulsa, Okia 80

American Oil Co., Baltimore, Md 10

.\merican Refining Co., Wichita Falls, Texas 248

.American Oil Works, Ltd., Titusville, Pa 42

Anderson & Gustafson, Chicago, 111 ...!!.......... 105

.\pex Refining & Drilling Co.. Loomis, Col 8

Ardmore Producing & Refining Co., Ardmore, Okla 16

.\rrow Rffiniiig Co., Waco, Texas ..72

Associated Oil Co., Los Angeles, Cal . . ] 31.^

Atlanta Refining & Mfg. Co., Atlanta, Ga 7

Allantle Petroleum Co., The. Tulsa, Okla 25

.Vilas Petroleum Co.. Kansas Citv. Mo 10

Atwon.l Rellning Co., Oklahoma Citv, Okla 39

AureliuB Thoma.s Gasoline Co., Drumright, Okla 15

HarlM r Co., W. H., Minneapolis, Minn... 15

H.-rry'M Son.s Co , J. B., Oil City, Pa. . . . 14S

Hl.-ry Oil Co., Franklin, Pa 95

Hjif Ifeart Petrol, urn Co., Big Heart, Okia .' ] .' .' .' n^

MIlfH Oil * Refining Co., Augusta, Kansas 34

Boynloii Gasoline Co., TuKsa Okla 15

Hoynlon Refining Co., Bovnton. Okla... . 60

Hurkl.urnett Refining Co., Burkburnett, Texas • ' 36

... .W.. ......... . 324

les. Cal 15

,, „,,,.,, - Imore, Okla 50

•inrirM llefinlnc Co., Vale, Okla... . 4"

•iirl.o Oil Co., Guthrie, Okla... ,c

Ciipltol Reflnlnif Co., Buffalo. N. Y 70

arneifle Refining Co., Carneeie, Pa {?

rvn^r". ';;•';,"';•"'" •'■-'•. Chicago. Ill .■.■::;;:.■; 4^

fenlrnl R.flning Co., Lawrenoevllle, HI. . zV^

hamplln Refining Co., H. H., Fnid Okli oa?

;h..N, nul * Smith Corp., Tulsa Okla'. .' ] ] : l^l

hkaHaw U,.flnlng Co., Ardmore, Okla . i%4

< iiiiderH Gnnoiine fo.. N-waia, Okla . .' . ! . .' ! ! .' .' .' ! ; ." .' .' ;:;;:: .' ." ; ; ; ; ; ; ; ; ; ; ; ; 35

Hurkl.urnett Refining Co., Burkburnett Te
IJntler County Oil Refining Cc. Bruin, Pa
fa. do on & Refining Co., Shreveport, La..
Callfo'nln Petroleum Exchange, Los Angele-
."'"'■'■'.'" •<• fining Co., Ardmore. Okla. "

KANSAS CITY TESTING LABORATORY 143

Tank Cars Owned By Oil Industry — Continued.

Name aiid Location. Tank Cars

Choate Oil Corp., Oklahoma City, Okla 184

Clarendon Rcrining Co., Clarendon, Pa 7J!

Cleveland Petroleum Refining Co., Cleveland, Okla 21

Climax Refining Co., Corsicana, Texas 11

Commonwealth Oil & Refining Co., Jloran, Kans 2Z

Conewango Refining Co., Warren, Pa 152

Constantin Refining Co., We.st Tulsa, Okla 1,150

Continental Oil Co., The, Denver. Col 11

Continental Refining Co., Ltd., Oil City, Pa TO

Continental Refining Co., Bristow, Okla 76

Cosden & Co., Tulsa, Okla 2,030

Craig Oil Co., The, Toledo, Ohio 175

Crew Levick Co., Philadelphia, Pa 250

Crystal Oil Works, Oil City, Pa 32

Cushing Refining Co., (Cars operated by Empire Refineries, Inc.) Ponca

City, Okla 150

Daugherty & Son Refining Co., W. H., Petrolia, Pa S

Deepwater Oil Refineries, Houston, Texas 50

De Soto Gasoline Co., Beaumont, Texas S

Diamond Gasoline Co., Kansas City, Mo 40

Doty Oil Co., Oklahoma City, Okla 5

Eagle Gasoline Co., Tulsa, Okla 34

Eagle Refining Co., ^^■ichira Falls, Texas 6u

EI Dorado Refining Co., El Dorado, Kans 186

Elk Refining Co., Charleston, W. Va 72

Emery Mfg. Co., Bradford, Pa 90

Emlenton Refining Co., Emienton, Pa 78

Empire Oil Works, Oil City, Pa 90

Empire Refineries, Inc., Tulsa, Okla 1,860

Ensign Oil Co., of Pa., Pittsburgh, Pa 7

Evans-Thwing Refining Co., Kansas City, Mo 100

Falling Rock Cannel Coal Co., Charleston, W. Va 26

Federal Oil & Refining Co., Cushing, Okla 30

Fidelity Petroleum Co., (Cars operated bv Uncle Sam Oil Co.) TuLsa, Okla.. 75

Foco Oil Co., Franklin, Pa 20

Franchot & Co., D. W., Tulsa, Okla 12

Franklin Qu:illty Refining Co., Franklin, Pa 24

Freedom Oil Works Co., The, Freedom, Pa 195

Preeport & Mexican Fuel Oil Corp., Houston, Texas 348

Galena-Signal Oil Co., of Texas, Houston, Texas SO

Gasoline Corp., New York, N. Y 30

General Petroleum Corporation, Los Angeles, Cal 66

Golden Rule Refining Co., Wichita, Kans 48

Great American Refining Co., Tulsa, Okla 100

Great Western Gil Refining Co., Erie, Kans 100

Gulf Refining Co., Pitt.sburgh, Pa 2,150

Hawkeye Oil Co., Waterloo, la 10

Hercules Petroleum Co., Dallas, Texas 272

Higrade Petroltum & Gasoline Co., Tulsa, Okla 22

High Grade Petroleum Products Co., St. Marys, W. Va 50

Home Oil Refining Co.. of Texas, Ft. Worth, Texas 135

Home Petroleum Co., Oklahoma City, Okla 50

Hope Gasoline Co., Tulsa, Okla 10

Humble Oil & Refining Co., Houston, Texas 188

Illinois Oil Co., of Rock Island, Rock Island, 111 176

Imperial Refining Co., Ardmore. Okla 216

Independent Refining Co., Ltd., ' Oil City, Pa 120

Indiahoma Refining Co., St. I>ouis, Mo 765

Indian Refining Co., Lawrenceville, 111 1,300

Inland Refining Co., Tulsa, Okla 100

Interior Oil & Gas Corp., Clarendon, Pa 10

International-Ardmore Ref. Div., Tulsa, Okla., (The Ohio Cities Gas Co.).. 16

International Oil & Gas Corp., Shreveport, La 20

Interocean Refining Co., Chicago, 111 90

Invader Oil & Refining Co., Muskogee, Okla 25

Invincible Oil Refining Corp., Ft. Worth, Texas 175

Island Refining Co., The Pittsbur.gh, Pa 75

Johnson Oil Refining Co., Chicago Heights, 111 40

Kanotex Refining Co., The, Arkansas (Tity, Kans 220

Kansas City Refining Co., Kansas City, Kans 180

Kansas Oil Refining Co., Coffeyville, Kans 1"0

Kendall Refining Co., Bradford, Pa 50

Lake Park Refining Co., Kansas City, Mo 270

LaPorte Oil & Refining Co., Houston, Texas 10

144 BULLETIN NUMBER SIXTEEN OF

Tank Cars Owned By Oil Industry— Continued.

^ X *■„„ Tank Cars

Name and Location. ^

Leader Oil Co., Casey, 111 ■ ■ Z.

Lesh Refining Co., Arkansas City, Kans ^J

Liberty Oil Co., Ltd., New Orleans, La ■ ; • • • •; °5

Llbertv Pipe Line & Refining Co.. Wichita, Kans 5

Liquefied Petroleum Gas Co., Tulsa, Okla

Lisle Refining Division, Arkansas City Kans ' »

Livingston Refining Corp., Tulsa Okla ' ^"

Lone Star Refining Co., Wichita Falls Texas ,,^0

Louisiana Oil Refining Co., Shreveport La -*"

Lubrite Refining Co., East St. Louis, 111 ....... »^

McCombs Producing & Refining Co., Louisville, Ky ■>»

Magnolia Petroleum Co., Dallas, Texas »""

Marland Refining Co., Ponca City, Okla . . . • . . ■ »"

Mexican Petroleum Corporation, New ^ork, N. Y \(,n

Midco Gasoline Co., Tulsa. Okla ■''J"

Mid Continent Refining Co., Tulsa, Okla ^'a

Midland Refining Co., El Dorado, Kans -»"

Midwest Refining Co., The, Denver, Col ^^

Miller's Oil Refining Works, Allegheny, Pa o"

Miller Petroleum Refining Co., Chanute, Kans »"

Montrose Oil Refining Co., Ft. Worth, Texas 50

Mutual Oil Co., Kansas City, Mo lf»

Mutual Refining & Producing Co., Kansas City, Mo »«

Mutual Refining Co., Warren, Pa ^JJ

Mutual Sales Co., Warren, Pa 1 "

National Refining Co., Cleveland. Ohio 1.0«4

National Oil Co., New York, N. Y fa

Noble Oil * Gas Co., Chas. F., Tulsa, Okla 200

Nortex Refining Co., Burkburnett, Texas 68

Northern American Refining Co.. Oklahoma City, Okla 4(o

Northern Petroleum Co., Pittsburgh, Pa 26

Northern Oil Co., Wilmar, Jlinn 10

Nyanza Refining Co.. New Wilson, Okla 10

Oconee Oil Refining Co., Athens, Ga 10

Ohio Cities Gas Co.. Columbus, Ohio 1,400

Ohio Valley Refining Co., St. Marys, W. Va 75

Oil Products Corp., New York, N, Y 7

Oil State Gasoline Co., Tulsa, Okla 12

Oil State Refining Co., Enid, Okla 50

Oklahoma Natural Gasoline Co., Sapulpa, Okla 5

Oklahoma Petroleum & Gasoline Co., Tulsi, Okla 280

Oklahoma Producing & Refining Corp., Muskogee, Okla 275

Okmulgee Producing & Refining Co., Okmulgee, Okla 115

O. K. Refining Co. (Cars operated by The Home Refining Co. of Texas)

Ft. Worth, Texas 15

Olsan Petroleum Co., Tulsa, Okla 11

Omaha Refining Co., Omaha, Neb 25

Oneta Refining Co., Tulsa, Okla 52

OHage Gasoline Co., Kansas Citv, Mo 25

(Jzark Refining Co., Ft. Smith, Ark 17

Pan-Amirlcan Refining Co., Tulsa, Okla 310

P.Hnhaiidle Refining Co., Wichita Falls, Texas 200

Paragon Refining Co., Toledo, Ohio 600

Pawnee Bill Oil & Refining Co., Yale, Okla 25

l"«ll<-an Oil Refining Co., Inc.. New Orleans, La 19

Pt-nn American Koflning Co., Oil Citv, Pa 250

I'<-nngylvanla & Delaware Oil Co., New York, N. Y 20

I'ennMylvanIa Gasoline Co.. Bradford, Pa 13

P.-nnnylvanla on Products Refining Co., Eldred, Pa 40

I'>-nni4>lvanla Itefining Co., Ltd., The, Karns Citv, Pa 7

P.tt.T.Mon Co.. Geo. C, Chicago, 111 " . 5

ivirolcum Products Co., The, Pittsburgh, Pa 12

Pitroleum Refining Co., Latonia, Ky .47

Phoonlx U.flnlng Co., Tulsa. Okla 180

I'hllllpB Petroleum Co., The, Bartlesvllle, Okla 10

IMirc. on Corp., SI. Loul.s, Mo 1,500

I'lllBburgh Oil Refining Co., Pittsburgh. Pa '....".'. ['.".'.]]]... 85

I'itlHburgh-Texa.s Oil & Gas Co., Muskogee, Okla.. 12

I nlar PrMlu.ing * Gasoline Co., Okmulgee, Okla 10

I rlin.t I'.lrii|r-um Products Co., Chicago 111 92

T.Mlu.i.rH & Hoflnern Corp., Blackwell. Okla.. '. . . . 185

I nid.-ntlal Oil Cdip., Haltimorc. Md . 300

run- Oil c.i., Mlnni-apoliB, Minn 92

Ititndolrih P.ir.il.um Co., Tul.sa, Okla! '.'. 10

KANSAS CITY TESTING LABORATORY 145

Tank Cars Owned By Oil Industry — Concluded

Name and Location. Tank Cars

Ranger Refining Co., Kansas City 80

Record Oil Refining Co., The, New Orleans, La 35

Red C Oil Co., Baltimore, Sid 1.5

Red River Refining Co., Crichton, La 30

Red River Refining Co. of Texas, Wichita Falls, Texas 50

Richfield Oil Co.. Los Angeles, Cal ' 8

Rio Grande Oil Co., EI Paso, Texas 22

Riverside Eastern Oil Co., Pittsburgh, Pa 45

Riverside Western Oil Co.. Tulsa, Okia 100

Robinson Oil Refining Co., Robinson, 111 9

Roth Gasoline Co., Independence, Kans 10

Roxana Petroleum Co., Tulsa, Okla 750

St. Louis Oil & Refining Co., Eldorado, Kans 25

Sapulpa Refining Co., Sapulpa, Okla 445

Seneca Oil Works, Warren. Pa 65

Service Petroleum Co., The, Tulsa, Okla 15

Schaffer Oil & Refining Co., Chicago, 111 450

Shell Co., of California, San Francisco, Cal 100

Simms Oil Co., Houston, Texas 500

Sinclair Refining Co., Chicago, III 3,700

Skagway Gasoline Co., Tulsa, Okla 6

Skelly Oil Co., Tulsa, Okla 12

Sloan & Zook, Bradford, Pa 62

Smiley Petroleum Co., Kansas City, Mo 95

Smith Refining Co., Levi, Clarendon, Pa 20

Southern Oil Corp., Kansas City, Mo 4 60

Southland Gasoline Co., Tulsa, Okla 16

Southwestern Producing & Refining Co.. Wichita Falls, Texas 40

Sterling Oil & Refining Co., Wichita, Kans 175

Sterling Refining Co., Oklahoma City, Okla 20

Stewart Petroleum Co., Tulsa. Okla 20

StoU Oil Co., Inc., Louisville, Kv 35

Stroud Co., B. B Bradford, Pa 25

Sunland Oil Co., Tulsa, Okla 2S

Sunshine State Oil & Refining Co., Wichita Falls, Tex:is 110

Superior Oil Works, Ltd., Warren, Pa 35

Texas Co., The, New York, N. Y 4,100

Texhoma Oil it Refining Co., Wichita Falls, Ttxas SO

Tidal Gasoline Co., Tulsa, Okla 70

Tiona Refining Co., Clarendon, Pa 50

Titusville Oil Works, Titiisvillc, Pa 60

Totem Gasoline Co., Tulsa, Okla 10

Transcontinental Refining Co., Pittsburgh, Pa 815

Travis Oil Co., Tulsa, Okla 50

Tribes Gasoline Co., Tulsa, Okla 15

Turner Oil Co., Los Angeles, Cal 6

Twin Hills Gasoline Co., Okmulgee, Okla 7

Union Oil Co. of California, Los Angeles, Cal 325

Union Petroleum Co.. Philadelphia, Pa 200

United Oil Co., The, Denver, Col 20

United Oil Refining Co., West Lake, La 15

United Refining Co., Warren, Pa 45

Union Tank Line (Standard) 25,000

Valvoline Oil AVorks, Ltd., East Butler, Pa 130

Ventura Refining Co., Los Angeles, Cal 15

Vickers Petroleum Co., Pot win, Kans 25

Vulcan Oil Refining Co., Cleveland, Ohio 48

Wabash Refining Co., Robinson, 111 160

Wadhams Oil Co., Milwaukee, Wis 10

Waggoner Refining Co., Electra, Texas 80

Walker Oil & Refining Co., Houston, Texas 10

Warren Oil Co., Warren, Pa 415

Warren Refining Co., Warren, Pa ' 70

Waverly Oil Works Co., Pittsburgh, Pa 50

Webster Oil & Gasoline Co., Yale, Okla 5

Western Oil Corp., Tulsa, Okla 80

Western Petroleum Co., Chicago, 111 10

White Eagle Petroleum Co., Augusta, Kans 450

White Oil Corp., Houston, Texas 335

Wichita Valley Refining Co., Iowa Park, Texas 125

Wilburne Oil Works, Ltd., Warren, Pa 75

Wilhoit Refining Co., Springfield, Mo 110

Wight Producing & Refining Corp., Tulsa, Okla 11

Tank Car Companies 10,000

146 BULLETIN NUMBER SIXTEEN OF

RULES GOVERNING THE LOCATION OF NEW LOADING RACKS
AND NEW UNLOADING POINTS FOR CASINGHEAD GASO-
LINE, REFINERY GASOLINE, NAPHTHA OR IN-
FLAMMABLE LIQUID WITH FLASH POINT
BELOW 30 °F.

The location of new loading racks and unloading points for
volatile inflammable liquids is considered of great importance, and
there is at present lack of uniformity in the enforcement of proper
safe-guards for the protection of life and property. The following
rules for the location of new installations shall govern all carriers
under Federal control. These rules are not applicable to present
locations.

For the purpose of these rules casinghead gasoline is defined
to be any mixture containing a condensate from casinghead gas or
natural gas obtained by either the compression or the absorption pro-
cess, and having a vapor tension in excess of 8 pounds per square
inch.

Loading.

1. (a) New loading racks for refinery gasoline, naphtha, or
any liquid (other than casinghead gasoline) with flash point below
30 °F. Must not be located nearer than 50 feet to a track over which
passenger trains are moved when physical conditions permit and in
no case less than 25 feet.

(b) New loading racks for casinghead gasoline must be located
not less than 100 feet distant from a track over which passenger
trains are moved when physical conditions permit, and in no case
less than 50 feet. When within 75 feet of such a track a retaining
wall, dike or earthen embankment shall be placed between the in-
stallation and the track, so constructed as effectually to prevent
liquids from flowing on to the track in case of accident.

(c) In loading casinghead gasoline, the tank car and the stor-
age tank shall be so connected as effectually to permit the free flow
of the gasohne vapors from the tank car to the storage tank and to
positively prevent the escape of these vapors to the air, or the vapors
must be carried by a vent line to a point not less than 100 feet dis-
tant from the nearest track over which passenger trains are moved.

Unloading.

t h ^^\ Y^^^ i^^^ unloading points requiring railroad service
Hmn- I ) "Jh ?r^ ""^ ^^"u '^,''' ^^ refinery gasoline, benzine, or any
liquid (other than casinghead gasoline) with flash point below 30 °F

?I^W .n7 ;v, • ^^"^""^T. "'^f " ^^ '"^J^^t to negotiation between the
carrier and the interested oil company.

be nl«cld^,'''^!nf''**'''"'r°5 *^^ ""jo^ding of casinghead gasoline shall
nasscn^^i tr..Tn« """ '^''^^"'u^ ^^ ^° *^^* ^^^"^ ^ ^^^^^ over which
^Jca er di.So ' r'""'' '^•'''''' P^^'^^^' conditions do not permit a
Svrwh.rf nh;J^"V "^?.'^!'"»'" distance of 100 feet shall be re-
tioni Lr^ n n ./ ^ 'vf-' ';?"i''H^"^ P^™it' ^here old or new installa-
tions are placed within 75 feet of a track over which passenger trains

KANSAS CITY TESTING LABORATORY 147

are moved a retaining: wall, dike or earthen embankment shall be
placed between the installation and the track, so constructed as ef-
fectually to prevent liquids from flowing on to the track in case of
accident.

Storage.

3 (a) These regulations apply only to above-ground tanks for
which railroad service is required. Under-ground tanks should be
considered by interested railroads as occasion may arise. All stor-
age tanks will be considered above ground unless they are buried so
that the top of the tank is covered with at least three feet of earth.

(b) All tanks should be set upon a firm foundation and be
electrically grounded.

(c) Each tank over 1,000 gallons in capacity shall have all man-
holes, hand holes, vent openings, and other openings which may con-
tain inflammable vapor, provided with 20x20 mesh brass wire screen
or its equivalent, so attached as to completely cover the openings and
be protected against clogging, these screens may be made removable
but should be kept, normally, firmly attached. Such a tank must also
be properly vented or provided with a suitable safety valve set to
operate at not more than 5 pounds per square inch for both in-
terior pressure and vacuum, manhole covers kept closed by their
weight only will be considered satisfactory.

(d) Tanks used with a pressure discharge system must have a
safety valve set at not more than one-half of the pressure to which
the tank was originallj' tested.

(e) Tanks containing over 500 gallons and not exceeding 18,000
gallons of gasoline, benzine, naphtha, casinghead gasoline, or any
liquid with flash point below SCF, must be located not less than 20
feet from a track over which passenger trains are moved.

(f) For capacities exceeding 18,000 gallons, the following dis-
tances shall govern:

Capacity of tanks Minimum distance from a track over which

(in gallons) passenger trains are moved.

18,001 to 30,000 40 feet

30,001 to 48,000 50 feet

48.001 to 100,000 60 feet

100,001 to 150,000 80 feet

150,001 to 250,000 100 feet

250,001 to 500,000 150 feet

Over 500,000 200 feet

(g) Where practicable, tanks should be located on ground slop-
ing away from railroad property. If this is impracticable, then the
tanks must be surrounded by dikes of earth, or concrete, or other
suitable material, of sufficient capacity to hold all the contents of
the tanks, or of such nature and location that in case of breakage of
the tanks the liquid will be diverted to points such that railroad prop-
ertj'^ and passing trains will not be endangered.

General.

4 (a) In measuring distance from any railroad track the near-
est rail shall be considered as the starting point.

148 BULLETIN NUMBER SIXTEEN OF

(b) During the time that the tank car is connected by loading
or unloading connections, there must be signs placed on track or car
so as to give necessary warning. Such signs must be at least 12x15
inches in size and bear the words "Stop — Tank Car Connected" or
"Stop— Men at Work," the word "Stop" being in letters at least 4
inches high and the other words in letters at least 2 inches high. The
letters must be white on a blue background. The party loading or
unloading the tank car is rsspansible for furnishing, maintaining, and
placing these signs.

(c) In laying pipe lines on railroad p;operty for the loading or
unloading of tank cars, they must be la'd at a depth of at least three
feet, and at points where such pipe lines pass under tracks they must
be laid at least four feet below the bottom of the ties.

(d) All connections between tank cars and pipe lines must be in
good condition and must not permit any leakage. They must be fre-
quently examined and replaced when they have become worn in order
to insure at all times absolutely tight connections. Tank cars must
not be left connected to pipe lines except when loading or unloading
is going on and while a competent man is present and in charge.

(e) The ends of the pipe lines for loading or unloading tank
cars from their bottom opening, when on railroad property should
be placed in shallow pits with brick or concrete walls not closer than
8 feet from center line of track. These pits should be ventilated
and be protected by substantial one-piece covers, level with the sur-
face of the ground, which must be kept locked in place when the pits
are not in use. These pits should not be drained into a sewer or run-
ning stream.

(f ) Except when closed electric lights are available, the loading
or unloadmg of tank cars on railroad property shall not be permitted
except during daylight when artificial light is not required. The
presence of flame lanterns, nearby flame switch lights or other ex-
posed flame lights or fires during the process of loading or unload-
mg IS prohibited.

B. W. DUNN,
Chief Inspector.

i

KANSAS CITY TESTING LABORATORY 149

THE MEASUREMENT AND GAUGING OF PETROLEUM.

The unit of measurement of petroleum in the United States is
the barrel of 42 U. S. gallons. The important units of measurement
with factors for their conversion to one another are given below.
Other units of measurement are to be found on pages 554-5-6. In
measuring petroleum, it is necessary to strap the tanks in which
it is contained and to prepare gauging tables for each tank. The
tanks are usually identified by number. In the case of the vertical
cylindrical tanks it is very simple to prepare gauging tables as the
amount per inch is figured from formulae (1) on pages 135, 151, 182.
Using an adding machine each inch is added and summed until the
height of the tank is reached.

In making gauging tables for horizontal cylindrical tanks formula
(4), page 151, may be used but this is rather tedious. With flat
ends and with diameters up to 10 feet the tables on pages 159 to 173
are useful as it is only necessary to multiply the total capacity
of the tank by the factor given for the depth desired. The result is
in gallons. For horizontal tanks of any size, the tables given on
pages 155-6 are most suitable. It is only necessary to first make
a table showing the per cent of the total diameter represented
by each inch in diameter and to multiply the corresponding per
cent of capacity by the total capacity.

The capacity of tanks with standard bumped ends is derived
from formula (3) on page 151. The contents of tanks with bumped
ends may be found as described on pages 153-4. For irregular
tanks and tanks with coils and pipe, tables are made by measur-
ing out water from the tank. On a lease or at the refinery it is
usual to gauge all tanks every morning. The measurement may be
done with a steel tap plumb bob at the end for the total amount
of fluid and with a "thief" which measures the water in the bot-
tom of the tank. A gauging stick may be used which is chalked with
special chalk or carries a strip of sensitive paper showing the de-
marcation between it and water may be used. A formula for im-
pregnating paper indicator for this purpose is as follows:

Calcium chloride 10 grams

Gum Dextrin 15 grams

Glycerin 5 C. C.

Acetic Acid 99% 3 C. C.

Water 30 C. C.

Umber 10 grams

For the correction of the volume of oil to a temperature of
60 °F use the table on page 152.

150

BULLETIN NUMBER SIXTEEN OF

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tr-

3
o

KANSAS CITY TESTING LABORATORY 151

HORIZONTAL CYLINDRICAL TANKS.

(1) Total capacity of horizontal cylindrical tank in gallons.
C - .0034 d'L

d = diameter in inches. L = length in inches.

c = capacity in U. S. gallons.

(2) Total capacity of horizontal cylindrical tanks in barrels with-
out bumped ends.

O r- 0.14 d-1

d = diameter in feet.

1 = length in feet.

c = capacity in barrels.

(3) Total capacity of horizontal cylindrical tank in barrels with
bumped ends (when radius of bumped end = d ft.)

C = d^' (0.14 1 + .019 d)

Capacity of each bumped end = .019 d' bbls. =: .4024 d^ gallons

(.000233d' if d = inches)

(4) Liquid contents of partially filled tanks.

C — Liquid contents in gallons.

L = Length of tank in inches.

d = Diameter of tank in inches.

X =: Depth of liquid contents in inches.

C .=

(d— 2x d— 2x \ / \

0.004363 d- Cos-^ y x(d— x) 1

231

d— 2x

Cos-' means the value of the angular degrees whose cosine

d

d— 2x

is

The cosine of an angle is the ratio in its right angled triangle, of the
side adjacent the angle to the hypothenuse of the triangle.

When L = 300 inches
d = 100 inches
X = 30 inches
d— 2x

= .4

d
Cos-^ .4 = 66.42" (From Trigonometric tables)

300
C =r

231
300

I 0.004363 (10000) (66 42) — 20 \/ 2100 I

231
= 2617 gallons.

(2897 — 882.)

152

BULLETIN NUMBER SIXTEEN OF

CORRECTIONS OF GAUGED VOLUME OF OIL TO 60° F.

Multiply the volume in the tank or car at the observed tem-
perature by the following factor to get the volume at 60'
F. for each- commodity.

Observed
Temperature

Casinghead
Gasoline

Gasoline and
Naphtha

Kerosene

Gas Oil

Fuel Oil

Asphalt

30
32
34
36
38

1.0240
1.0224
1.0208
1.0193
1.0177

1.0178
1.0166
1.0154
1.0142
1.0130

1.0151
1.0141
1.0131
1.0121
1.0111

1.0135

1.0126
1.0117
1.0108
1.0099

1.0123

1.0115
1.0107
1.0099
1.0091

1.0111
1.0103
1.0095
1.0088
1.0080

40
42
44
46
48

1.0161
1.0145
1 0129
1.0113
1.0098

1.0118
1.0106
1.0095
1.0083
1.0071

1.0101
1.0091
1.0080
1.0070
1.0060

1.0090
1.0081
1.0072
1.0063
1.0054

1 . 0082
1.0074
1.0066
1.0058
1.0050

1.0073
1.0066
1.0059
1.0051
1.0044

50
52

54
56

58

1.0082
1.0065
1 . 0048
1.0032
1.0016

1.0059
1 . 0048
1.0036
1.0024
1.0012

1.0050
1.0040
1.0030
1.0020
1.0010

1.0045
1.0036
1.0027
1.0018
1.0009

1.0041
1.0033
1.0025
1.0017
1.0009

1.0037
1.0029
1.0021
1.0014
1.0007

60
62
64
66
68

1.0000
0.9984
0.9968
0.9952
0.9936

1.0000
0.9988
0.9976
0.9964
0.9952

1.0000
0.9990
0.9980
0.9970
0.9960

1.0000
0.9991
0.9982
0.9973
0.9964

1 . 0000
0.9992
0.9984
0.9976
0.9967

1.0000
0.9992
0.9985
0.9978
0.9971

70

72
74
76
78

0.9919
0.9903
0.9887
0.9871
0.9855

0.9940
0.9928
0.9917
0.9905
0.9893

0 . 9950
0.9940
0.9930
0.9920
0.9909

0.9955
0.9946
0.9937
0.9928
0.9919

0.9959
0.9951
0 . 9943
0.9935
0.9927

0.9963
0.9956
0.9948
0.9941
0.9934

80

82

84
86

88

0.9839
0.9823
0 . 9807
0.9790
0.9774

0.9881
0.9869
0.9857
0.9845
0.9833

0.9899
0.9889
0.9879
0.9868
0.9856

0.9910
0.9901
0.9892
0.9883
0.9875

0.9918
0.9910
0.9902
0.9893
0.9885

0.9927
0.9920
0.9912
0.9905
0.9898

90
92
94
96
98

100
102
104
106

108

110
112
114
116
118

120

0.9758
0.9741
0.9725
0.9708
0 . 9692

0.9676
0.9660
0.9643
0.9626
0.9610

0.9821
0.9809
0.9798
0.9786
0.9774

0.9848
0.9838
0.9828
0.9818
0.9808

0.9865
0.9856
0 . 9847
0.9838
0.9829

0.9877
0.9869
0.9860
0.9852
0 . 9844

0.9891
0.9884
0.9877
0.9870
0.9862

0.9762
0.9750
0.9738
0.9726
0.9714

0.9797
0.9787
0.9777
0.9767
0.9757

0.9820
0.9811
0 . 9802
0.9793
0.9784

0.9836
0.9828
0 . 9820
0.9812
0 . 9804

0.9855
0.9848
0.9841
0.9834
0.9827

0.9594

0 9578
0 9562
0.9545
0.9529

0.9513

0.9702
0 9690
0.9678
0 9666
0.9654
0.9642

0.9747
0.9736
0.9726
0.9716
0.9706

0.9696

0.9776
0.9767
0 9758
0.9749
0 . 9740

0.9796
0.9788
0 . 9880
0.9772
0.9764

0.9819
0.9812
0 . 9805
0.9798
0.9791

0.9731

0.9756

0.9784

KANSAS CITY TESTING LABORATORY

153

METHOD OF GAUGING A HORIZONTAL CYLINDRICAL TANK
WITH BUMPED ENDS (RADIUS OF CURVATURE = d).

- / ~

Fig. 22 — Horizontal Cylindrical Tank Diagram.

d = diameter of tank in inches.

c =: total capacity of cylindrical portion of tank in U. S. gallons.

f = liquid depth of the contents of the tank in inches.

c = 0.0034 d=l

b = 0.0004666 d' = capacity of both bumped ends in U. S. gallons.

lOOf

= % liquid depth of total diameter.

EXAMPLE:

then
and

and

d = 87.0 inches
1 = 378.2 inches
f = 21.1 inches

c = 9733. gallons
b = 307. gallons

10040. gallons = total capacity of tank

lOOf

= 24.25%

From the tables of the following pages 155-158.
24.25% of d = 12.06% of b = 37. gallons
and = 18.78% of c = 1828. gallons

Therefore total contents = 1865. gallons

Take the temperature of the oil with a tank thermometer and in
the preceding table giving the corrections for gauged volume of oil
to 60°F, look up this temperature. Multiply the above calculated
volume by the factor corresponding to this temperature and use the
product as contents of the tank. This gives the volume at 60 °F. In
the case of the above tank containing 1865 gallons of gasoline at a
temperature, for instance of 80 °F the factor used would be 0.9881
and the net contents of the tank at 60 °F would be 1843 gallons.

154

BULLETIN NUMBER SIXTEEN OF

Method of Constructing a Gauging Table for Horizontal Cylindrical
Tank With Standard Bumped Ends, (r = d) for Each .1 Inch.

Assume tank diameter = 87.0 inches,
length = 378.2 inches.

Total capacity of cylindrical portion

bumped ends
total capacity

9,733 gallons.

s = 307 gallons.

10,040 gallons.

To construct this table, a slide rule (Thacher) reading to the
fifth place is very convenient. Set the rule w^ith a divisor of 87.0
and with the one setting of the rule, read off the per cent of diameter
for each 0.1 inch in depth to one-half of the diameter of the tank,
that is 43.5 inches. Now look up in the tables on following pages,
the corresponding values, interpolating if that accuracy is desired,
for the capacity of the cylindrical portion and the bumped end por-
tions of the tank and record these values as shown below. Now set
the slide rule with the total capacity of the cylindrical portion in
gallons as multiplier and read off and record the capacities corre-
sponding to each 0.1 inch of diameter as already set out. Do the same
with the bumped ends. Add the two values and the gauging table is
complete up to half full. Now subtract the preceding value from
each value of total gallons and with the adding machine sum each
value. This completes the table. The following sets forth enough
to illustrate the method:

Depth,

% of Cyl-

%of

Actual Gallons

m

%of

inder

Bumped

Cylinder

Bumped

Inches Diameter

Capacity

Capacity

Part

Part

Total

0.1..

.. 0.12.

... .007.

... 0.00..

.. 0.7. .

... 0.0...

0.7

1.0..

.. 1.15.

... .21 .

... 0.01..

.. 20.4..

... 0.0...

. 20.4

1.1..

.. 1.26..

... .24 .

... 0.01..

.. 23.4..

... 0.0...

. 23.4

2.0. .

.. 2.30..

... .59 .

... 0.03..

.. 57.4..

. .. 0.1.. .

. 57.5

2.1..

.. 2.41..

... .63 .

... 0.04..

.. 61.3..

... 0.1...

. 61.4

3.0..

.. 3.45.

... 1.07 .

... 0.11..

.. 104.1..

... 0.4...

. 104.5

3.1..

.. 3.56.

... 1.12 .

... 0.12..

.. 109.0..

... 0.4...

. 109.4

4.0. .

.. 4.64..

... 1.67 .

... 0.23..

.. 162.5..

... 0.7...

. 163.2

4.1..

.. 4.71..

... 1.71 .

... 0.24..

.. 166.4..

... 0.7...

. 167.1

5.0. .

.. 5.75..

... 2.30 .

... 0.44..

.. 223.8..

... 1.4.. .

. 225.2

6.0. .

.. 6.90..

... 3.01 .

... 0.64..

.. 292.9..

... 2.0...

. 294.9

7.J0. .

.. 8.05..

... 3.78 .

... 0.92..

.. 367.9..

... 2.8...

. 370.7

43 . 0 . .

..49.42..

...49.26 .

...48.96..

..4794.5..

. ..150.3...

.4944.8

43.5. .

. . 50 . 00 . .

...50.00 .

...50.00..

..4866.5..

. ..153.5...

. 5020 . 0

44.0. .

5095 2

«0.0. .

.9669.3

KANSAS CITY TESTING LABORATORY

155

TABLE FOR GAUGING THE CONTENTS AT VARIOUS
DEPTHS OF HORIZONTAL CYLINDRICAL TAN
For Bumped Ends, See Next Table.

% d = percentage of total diameter of tank.
% c = percentage of total capacity of tank.

LIQUID
KS.

%d

%c

%d

%c

%d

C7p

%d

%c

%d

%c

0.1

0.0053

5.1

1 . 9250

10.1

5.2805

15.1

9.497

20.1

14.341

0.2

0.0152

5.2

1.9814

10.2

5.3580

15.2

9.588

20.2

14.444

0.3

0.0279

5.3

2.0383

10.3

5.4350

15.3

9.679

20.3

14.547

0.4

0.0429

5.4

2.0956

10.4

5.5122

15.4

9.771

20.4

14.649

0.5

0.0600

5.5

2.1535

10.5

5 . 5902

15.5

9.863

20.5

14.751

0.6

0.0788

5.6

2.2116

10.6

5.6690

15.6

9.956

20.6

14.854

0.7

0.0992

5.7

2.2705

10.7

5.7472

15.7

10.048

20.7

14.957

0.8

0.1212

5.8

2 . 3297

10.8

5.8258

15.8

10.142

20.8

15.060

0.9

0.1445

5.9

2.3895

10.9

5.9050

15.9

10.234

20.9

15.163

1.0

0.1692

6.0

2.4497

11.0

5.9848
6.0645

16.0

10.327

21.0

15.267

1.1

0.1952

6.1

2.5105

11.1

16.1

10.422

21.1

15.371

1.2

0.2223

6.2

2.5715

11.2

6.1445

16.2

10.515

21.2

15.475

1.3

0.2508

6.3

2.6333

11.3

6.2255

16.3

10.609

21.3

15.579

1.4

0.2800

6.4

2.6952

11.4

6.3060

16.4

10.703

21.4

15.683

1.5

0.3104

6.5

2.7579

11.5

6.3870

16.5

10.797

21.5

15.787

1.6

0.3419

6.6

2.8211

11.6

6.4685

16.6

10.893

21.6

15.892

1.7

0.3744

6.7

2 . 8845

11.7

6.5500

16.7

10.986

21.7

15.998

1.8

0.4077

6.8

2.9483

11.8

6.6320

16.8

11.082

21.8

16.101

1.9

0.4421

6.9

3.0127

11.9

6.7145

16.9

11.178

21.9

16.206

2.0

0.4773

7.0

3.0771

12.0

6.7970

17.0
17.1

11.273
11.369

22.0
22.1

16.312

2.1

0.5134

7.1

3.1426

12.1

6.8795

16.418

2.2

0.5501

7.2

3.2082

12.2

6.9630

17.2

11.465

22.2

16.524

2.3

0.5881

7.3

3.2742

12.3

7 . 0460

17.3

11.561

22.3

16.630

2.4

0.6263

7.4

3.3408

12.4

7.1305

17.4

11.657

22.4

16.737

2.5

0.6660

7.5

3.4075

12.5

7.2145

17.5

11.754

22.5

16.842

2.6

0.7061

7.6

3.4749

12.6

7.2990

17.6

11.851

22.6

16.949

2.7

0.7470

7.7

3 . 5426

12.7

7.3830

17.7

11.949

22.7

17.055

2.8

0.7886

7.8

3.6106

12.8

7.4680

17.8

12.046

22.8

17.161

2.9

0.8310

7.9

3.6790

12.9

7.5540

17.9

12.143

22.9

17.269

3.0

0.8742

8.0

3.7480

13.0

7.6390

7.7245

18.0

12.240

23.0
23.1

17.376

3.1

0.9179

8.1

3.8171

13.1

18.1

12.338

17.483

3.2

0.9625

8.2

3.8869

13.2

7.8110

18.2

12.437

23.2

17.590

3.3

1.0075

8.3

3 . 9570

13.3

7.8970

18.3

12.535

23.3

17.698

3.4

1.0533

8.4

4.0276

13.4

7.9840

18.4

12.633

23.4

17.806

3.5

1.0998

8.5

4 . 0983

13.5

8.0710

18.5

12.732

23.5

17.913

3.6

1 . 1470

8.6

4.1696

13.6

8.1580

18.6

12.831

23.6

18.022

3.7

1.1947

8.7

4.2411

13.7

8.2450

18.7

12.930

23.7

18.130

3.8

1.2432

8.8

4.3131

13.8

8.3330

18.8

13.030

23.8

18.240

3.9

1.2921

8.9

4.3855

13.9

8.4210

18.9

13.130

23.9

18.348

4.0

1.3418

9.0

4.4582

14.0

8.5090
8.5975

19.0

13.229

24.0
24.1

18.457

4.1

1.3920

9.1

4.5312

14.1

19.1

13.329

18.566

4.2

1 .4429

9.2

4.6045

14.2

8.6860

19.2

13.429

24.2

18.675

4.3

1.4941

9.3

4.6782

14.3

8.7755

19.3

13.529

24.3

18.784

4.4

1.5461

9.4

4.7525

14.4

8.8645

19.4

13.630

24.4

18.892

4.5

1 . 5986

9.5

4.8270

14.5

8.9545

19.5

13.731

24.5

19.010

4.6

1.6515

9.6

4.9015

14.6

9.0440

19.6

13.832

24.6

19.110

4.7

1.7052

9.7

4.9769

14.7

9.1345

19.7

13.934

24.7

19.220

4.8

1.7594

9.8

5.0523

14.8

9.2240

19.8

14.035

24.8

19.330

4.9

1.8142

9.9

5.1280

14.9

9.3150

19.9

14.146

24.9

19.440

5.0

1.8693

10.0

5.2040

15.0

9.406

20.0

14.238

25.0

19.551

156

BULLETIN NUMBER SIXTEEN OF

TABLE FOR GAUGING HORIZONTAL CYLINDRICAL TANKS—

Continued.

% d = percentage of total capacity of tank.
% c = percentage of total capacity of tank.

%d

%c

%d

%c

%d

%c

%d

%c

%d
45.1
45.2
45.3
45.4
45.5
45.6
45.7
45.8
45.9
46.0

%c

25.1
25.2
25.3
25.4
25.5
25.6
25.7
25.8
25.9
26.0

19.662
19.773
19.884
19.995
20.106
20.217
20.328
20.439
20.550
20.661

30,1
30.2
30,3
30,4
30,5
30,6
30.7
30.8
30.9
31.0

25.350
25.467
25,584
25,701
25,818
25.935
26,052
26,170
26,288
26,407

26,524
26,642
26,760
26.878
26.996
27.114
27,232
27,351
27.470
27.589
27.708
27.827
27.946
28.C65
28.184
28.302
28.422
28.543
28.660
28.781

35.1
35.2
35.3
35.4
35.5
35.6
35.7
35.8
35.9
36.0

31.314
31.436
31.558
31.680
31.802
31.924
32.046
32.168
32.290
32.412

40.1
40.2
40.3
40.4
40.5
40.6
40.7
40.8
40.9
41.0

37.480
37 . 606
37.731
37.856
37.981
38.106
38.231
38.355
38.479
38 . 604

38.730
38 . 856
38.982
39.108
39.233
39.358
39 , 482
39,608
39,735
39.862

43.775
43.902
44.028
44.155
44.282
44.409
44.538
44.663
44.790
44.918

26.1
26.2
26.3
26.4
26.5
26.6
26.7
26.8
26.9
27.0

20.773
20.886
20.998
21.110
21.222
21.334
21.447
21.560
21.672
21.785

31.1
31.2
31.3
31.4
31.5
31.6
31.7
31.8
31.9
32.0

36 1
36.2
36.3
36.4
36.5
.36.6
36.7
36.8
36.9
37.0

37.1
37.2
37.3
37.4
37.5
37.6
37.7
37.8
37.9
38.0

32 . 534
32.657
32.780
32.902
33.025
33.147
33.269
33.392
33.515
S3. 638
33.762
33 . 885
34.003
34.131
34.254
34.377
34.501
34.625
34.759
34 . 873

34.996
35,119
35.242
35.368
35.491
35.615
35.739
35.865
35.988
36.110

41.1
41.2
41.3
41.4
41.5
41.6
41.7
41.8
41.9
42.0

46.1
46.2
46.3
46.4
46.5
46.6
46.7
46.8
46.9
47.0

45.043
45.171
45.298
45.424
45.550
45.678
45.803
45 . 930
46.058
46.183

27.1
27.2
27.3
27.4
27.5
27.6
27.7
27.8
27.9
28.0

21.898
22.011
22 . 125
22.239
22.353
22.467
22,581
22.695
22.810
22.923

23.038
23 . 152
23.266
23.380
23.494
23.611
23.728
23.842
23.957
24.072
24 . 187
24.302
24.418
24.535
24.651
24.769
24.884
25.000
25,116
25.233

32.1
32.2
32.3
32,4
32.5
32.6
32.7
32.8
32.9
33.0

42.1
42.2
42.3
42.4
42.5
42.6
42.7
42.8
42.9
43.0

43.1
43.2
43.3
43.4
43.5
43.6
43.7
43.8
43.9
44.0

39.988
40.114
40.240
40.365
40.490
40.615
40.741
40.869
40.994
41.120

41.246
41 . 372
41.499
41.628
41.749
41.876
42.002
42 . 129
42.257
42.383

42.510
42.637
42.762
42 . 890
43.018
43.142
43.268
43.397
43.521
43.648

47.1
47.2
47.3
47.4
47.5
47.6
47.7
47.8
47.9
48.0

46.311
46.438
46,565
46.693
46.819
46.947
47 . 074
47.201
47.329
47.457

28.1
28.2
28.3
28.4
28.5
28.6
28.7
28.8
28.9
29.0

33.1
33.2
33.3
33.4
33.5
33.6
33.7
33.8
33.9
34.0
34.1
34,2
34.3
34.4
34.5
34.6
34.7
34.8
34.9
35,0

28.899
29.020
29.140
29,260
29,380
29,500
29.620
29.740
29.860
29.981

30.102
30.223
30.344
30.465
30.587
30.708
30.829
30.950
31.071
31.192

38.1
38.2
38.3
38.4
38.5
38.6
38.7
38.8
38.9
39.0
39.1
39.2
39.3
39.4
39.5
39.6
39.7
39.8
39.9
40.0

48.1
48.2
48.3
48.4
48.5
48.6
48.7
48.8
48.9
49.0

47.583
47.710
47.837
47.965
48.093
48.220
48.348
48.475
48.603
48.729

29.1
29.2
29.3
29.4
29.5
29.6
29.7
29.8
29.9
30.0

36.234
36.359
36.483
36.608
36.732
36.856
36.981
37.106
37.230
37.355

44.1
44.2
44.3
44.4
44.5
44.6
44.7
44.8
44.9
45.0

49.1
49.2
49.3
49.4
49.5
49.6
49.7
49.8
49.9
50.0

48.857
48.983
49.112
49.239
49.366
49.494
49.621
49.748
49.877
50.000

KANSAS CITY TESTING LABORATORY

157

TABLE FOR GAUGING THE CONTENTS AT VARIOUS LIQUID

DEPTHS OF BUMPED ENDS OF HORIZONTAL

CYLINDRICAL TANKS.

% d = percentage of total diameter of tank.

% h = percentage of total contents of both bumped ends.

%d

%b

%d

%b

%d

%b

%d

%b

%d

%b

0.1

0.00

5.1

0.32

10.1

1.62

15.1

4.18

20.1

7.99

0.2

0.00

5.2

0.34

10.2

1.66

15.2

4.24

20.2

8.09

0.3

i).00

5.3

0.36

10.3

1.69

15.3

4.31

20.3

8.19

0.4

0.00

5.4

0.38

10.4

1.73

15.4

4.38

20.4

8.28

0.5

0.01

5 5

0.40

10.5

1.77

15.5

4.44

20.5

8.38

0.6

0.01

5.6

0.41

10.6

1.81

15.6

4.50

20.6

8.46

0.7

0.01

5.7

0.43

10.7

1.85

15.7

4.57

20.7

8.54

0.8

0.01

5.8

0.45

10.8

1.89

15.8

4.63

20.8

8.63

0.9

0.01

5.9

0.47

10.9

1.94

15.9

4.70

20.9

8.72

1.0

0.01

6.0

0.49

11.0

1.98

16.0

4.77

21.0
21.1

8.81

1.1

0.01

6.1

0.50

11.1

2.03

16.1

4.83

8.89

1.2

0.01

6.2

0.52

11.2

2.07

16.2

4.90

21.2

8.97

1.3

0.01

6.3

0.53

11.3

2.11

16.3

4.96

21.3

9.06

1.4

0.02

6.4

0.54

11.4

2.15

16.4

5.03

21.4

9.15

1.5

0.02

6.5

0.56

11.5

2.20

16.5

5.10

21.5

9.24

1.6

0.02

6.6

0.58

11.6

2.24

16.6

5.17

21.6

9.34

1.7

0.02

6.7

0.60

11.7

2.29

16.7

5.25

21.7

9.44

1.8

0.02

6.8

0.62

11.8

2.33

16.8

5.32

21.8

9.54

1.9

0.02

6.9

0.64

11.9

2.38

16.9

5.40

21.9

9.64

2.0

0.02

7.0

0.66

12.0

2.43

17.0

5.48

22.0

9.74

2.1

0.03

7.1

0.68

12.1

2.48

17.1

5.55

22.1

9.84

2.2

0.03

7.2

0.70

12.2

2.54

17.2

5.63

22.2

9.93

2.3

0.04

7.3

0.73

12.3

2.59

17.3

5.71

22.3

10.03

2.4

0.04

7.4

0.75

12.4

2.65

17.4

5.78

22.4

10.12

2.5

0.05

7.5

0.78

12.5

2.70

17.5

5.86

22.5

10.22

2.6

0.05

7.6

0.81

12.6

2.75

17.6

5.94

22.6

10.32

2.7

0.06

7.7

0.84

12.7

2.80

17.7

6.02

22.7

10.42

2.8

0.06

7.8

0.87

12.8

2.85

17.8

6.10

22.8

10.52

2.9

0.07

7.9

0.90

12.9

2.90

17.9

6.17

22.9

10.62

3.0

0.07

8.0

0.92

13.0

2.95

18.0

6.25

23.0

10.72

3.1

0.08

8.1

0.95

13.1

3.01

18.1

6.33

23.1

10.82

3.2

0.08

8.2

0.98

13.2

3.06

18.2

6.41

23.2

10.93

3.3

0.09

8.3

1.01

13.3

3.12

18.3

6.49

23.3

11.04

3.4

0.10

8.4

1.05

13.4

3.17

18.4

6.57

23.4

11.14

3.5

0.11

8.5

1.08

13.5

3.22

18.5

6.64

23.5

11.25

3.6

0.12

8.6

1.11

13.6

3.28

18.6

6.72

23.6

11.36

3.7

0.13

8.7

1.14

13.7

3.33

18.7

6.80

23.7

11.47

3.8

0.14

8.8

1.17

13.8

3.39

18.8

6.88

23.8

11.58

3.9

0.15

8.9

1.20

13.9

3.44

18.9

6.96

23.9

11.69

4.0

0.16

9.0

1.23

14.0

3.50

19.0

7.05

24.0

11.80

4.1

0.17

9.1

1.26

14.1

3.56

19.1

7.13

24.1

11.90

4.2

0.18

9.2

1.30

14.2

3.62

19.2

7.21

24.2

12.01

4.3

0.19

9.3

1.33

14.3

3.68

19.3

7.29

24.3

12.12

4.4

0.20

9.4

1.36

14.4

3.74

19.4

7.37

24.4

12.22

4.5

0.21

9.5

1.40

14.5

3.80

19.5

7.46

24.5

12.32

4.6

0.22

9.6

1.43

14.6

3.87

19.6

7.55

24.6

12.43

4.7

0.24

9.7

1.46

14.7

3.93

19.7

7.63

24.7

12.54

4.8

0.26

9.8

1.50

14.8

4.00

19.8

7.72

24.8

12.66

4.9

0.28

9.9

1.54

14.9

4.06

19.9

7.81

24.9

12.77

5.0

0.30

10.0

1.58

15.0

4.12

20.0

7.90

25.0

12.89

158

BULLETIN NUMBER SIXTEEN OF

T\BLE FOR GAUGING THE CONTENTS AT VARIOUS LIQUID
^ DEPTHS OF BUMPED ENDS OF HORIZONTAL

CYLINDRICAL TANKS (Concluded)

% d = percentage of total diameter of tank.

e^^ ^ — percentage of total contents of both bumped ends.

%d

25.1
25.2
25.3
25.4
25.5
25.6
25.7
25.8
25.9
26.0

26.1
26.2
26.3
26.4
26.5
26.6
26.7
26.8
26.9
27.0

27.1
27.2
27,3
27.4
27.5
27.6
27.7
27.8
27.9
28.0
28.1
28.2
28.3
28.4
28,5
28.6
28.7
28,8
28,9
29,0

29, 1
29,2
29,3
29.4
29,5
29,6
29.7
29.8
29,9
30,0

%b

%d

12.95
13.06
13,17
13,29
13.40
13,51
13.63
13,75
13,87
13,98

14,10
14.22
14,34
14 46
14,58
14,70
14,82
14,94
15,16
15,19

30,1
30,2

15,31
15,43
15,56
15,68
15.80
15.92
16.04
16.16
16,28
16,40

16,53
16,65
16,77
16,90
17,02
17,14
17,27
17.39
17,51
17.63

17.76
17.89
18.02
18.15
18.27
18,40
18,53
18,66
18,80
18,93

30
30
30
30
30
30
30
31

31,1
31.2
31,3

31

31

31

31

31,8

31.9

32.0

32.1
32.2
32.3
32.4
32,5
32,6
32,7
32,8
32,9
33,0

33,1
33,2
33.3
33.4
33.5
33.6
33.7
33,8
33,9
34,0

34.1
34.2
34.3
34.4
34.5
34.6
34.7
34.8
34.9
35.0

19.06
19,19
19,32
19,43
19,55
19.68
19.81
19.94
20.07
20.22

%d I %b

20.37
20.52
20,67

20
20
21
21
21

82
97
11
25
39

21,52
21,65

21.79
21.93
22.07
22.20
22.34
22.47
22.60
22.74
22.87
23.00

23.14
23.28
23.41
23.55

23
23
23
24
24
24

69
84
99
15
31
45

35
35
35
35
35
35
35
35
35
36

36.1
36.2
36.3
36.4
36.5
36.6
36.7
36.8
36.9
37.0

37.1

37.2
37.3
37.4
37.5
37.6
37.7
37.8
37.9
38.0

24.59
24.74
24.89
25.05
25.20
25.36
25.52
25.68
25.84
25.90

38

38

38

38

38

38

38.7

38.8

38.9

39.0

39.1
39.2
39.3
39.4
39.5
39.6
39,7
39.8
39.9
40.0

26.05

26.20
26.35
26.50
26.65
26.80
26.95
27.10
27.25
27,40

27,55

27.70
27.84
27.99
28.13
28.28
28.43
28,59
28.75
28.90

29.05
29.20
29.35
29.50
29.65
29.80
29.95
30.10
30.26
30.42

30.58
30.74
30.91
31.08
31.25
31.40
31.56
31.72
31.87
32.02

32.16
32.31
32.46
32.60
32.75
32.91
33.06
33.32
33,45
33.58

%b
40.1
40.2
40.3
40.4
40.5
40,6
40,7
40,8
40,9
41,0

41,1

41,2

41

41

41

41

41,7

41,8

41,9

42,0

42.1
42.2
42.3
42.4
42.5
42.6
42,7
42,8
42,9
43,0

%b

43

43

43

43

43

43

43

43.8

43.9

44.0

.1
.2
.3
.4
.5
.6
.7

44.1

44.2
44,3
44,4
44,5
44,6
44,7
44:8
44,9
45,0

33,74
33,90
34.05
34.20
34.35
34.50
34.65
34.80
34.95
35.10

35.26
35.42
35.58
35.75
35.92
36.08
36.24
36.39
36.55
36 . 70

%d

36.86
37.02
37.18
37.34
37.50
37.67
37.83
37.99
38.16
38.32

38.49
38.65
38.81
38.97
39.13
39.30
39.46
39.62
39.78
39.95

40.12
40.29
40.46

40
40
40
41
41
41
41

62

,79
95
,11
,27
,44
,60

45.1
45.2
45.3
45.4
45.5
45.6
45.7
45.8
45.9
46.0

46.1
46.2
46.3
46.4
46.5
46.6
46.7
46.8
46.9
47.0

47.1
47.2
47.3
47.4
47.5
47.6
47.7
47.8
47.9
48.0

%b

48.1
48.2
48.3
48.4
48.5
48.6
48.7
48.8
48.9
49.0

49.1
49.2
49.3
49.4
49.5
49.6
49.7
49.8
49.9
50.0

41.77
41.94
42,11
42,28
42,45
42,61
42,77
42,93
43,09
43,25
43.41
43 . 57
43.73
43.89
44.05
44.22
44.38
44.54
44.71
44.88

45.05
45.23
45,31
45,59

45 , 77
45,95

46 , 12
46,29
46,46
46,63

46,80
46,96
47,13
47,30
47,46
47,62
47,77
47,93
48.09
48.25

48
48
48
48
49
49

42
59
76
93
10
28

49.46
49.64
49.82
50.00

KANSAS CITY TESTING LABORATORY

159

CONTENTS OF HORIZONTAL TANKS (GALLONS).

Multiply Capacity in Tables by Length of Tanks in Inches.

36 Inches in

37 Inches in

38 Inches in

Depth

39 Inches in

40 Inches in

41 Inches in

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

20y2
20
193^
19

im

18

2 858

2.720

2 769

2.586
2.501

2.445

2.547

2 951

2.327
2.247

2 203

2.290

2.332

2.374

2.415

2.047

2.087

2.126

17

2 165

2 202

2.239

1 893

1.92S

I 963

16

1.998

2.032

2.065

1.739

1.770

1.801

15

1.832

1 863

1.894

1.585

1.613

1 . 643

14

1.669

1 697

1.724

1.434

1 459

1.484

13

1 509

1 533

1.557

1.286

1 . 308

1 330

12

1 351

1 372

1.393

1.140

1.159

1.179

11

1.198

1.216

1.233

.999

1.015

1.032

10

1.047

1.063

1.079

.861

.875

.889

■ 9

.903

.916

.929

.729

.740

.752

8

.763

.774

.785

.603

.612

.621

7

.631

.639

.648

.483

.490

.497

6

.505

.512

.518

.371

.376

.382

5

.387

.392

.398

.268

.271

.275

4

.280

.283

.287

.175

.178

.180

3

.183

.185

.188

.096

.098

.099

2

.100

.102

.103

.034

.035

.035

1

.036

.036

.037

42 Inches in

43 Inches in

44 Inches in

Depth

45 Inches in

46 Inches in

47 Inches in

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

2VA

23

22^

22

21Ji

21

2.755

3.597

3.653

3.442

3.291

3.344

3.337

3.453

3.143
3.050

2.998

3.100

3 149

3 199

3 218

2.817

2.864

2.908

20

2.955

3.002

3 047

2.633

2.679

2.721

19

2.763

2.805

2.846

2.455

2.495

2.533

18

2 572

2.609

2,647

2.276

2.313

2.347

17

2 381

2.416

2.450

2.098

2.132

2.163

16

2.193

2 225

2 256

1.922

1.952

1.981

15

2.009

2.037

2.064

1.750

1.776

1.802

14

1.827

1 852

1.876

1.580

1 . 603

1.623 •

13

1 648

1.672

1.693

1 414

1 4.34

1 454

12

1,473

1 494

1,513

1.252

1.269

1.287

11

I 304

1.321

1 338

1.094

1.110

1 . 125

10

1 139

1 154

1.168

.942

.955

.968

9

.980

.993

1.005

.797

.807

.817

8

.827

.838

.848

.657

.668

.675

7

.6B2

.691

.699

.526

.532

.540

6

.543

.552

.558

.403

.408

.414

5

.418

.424

.428

.291

.294

.297

4

.301

.3)4

.308

.190

.193

.194

3

.197

.199

.200

.104

.103

.107

2

.108

.110

• 111

037

.038

.038

1

.038

.039

.039

160

BULLETIN NUMBER SIXTEEN OF

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tanks m Inches.

48 Inches in
Diameter

49 Inches in
Diameter

50 Inches in
Diameter

Depth
Inches

51 Inches in
Diameter

52 Inches in
Diameter

53 Inches in
Diameter

2m

26

25y2

25

2iy2

24

4.776

i i99

4.597

4.660

■■■■4!256"

4.309

4.371

4.431

3.m"

3 707

4.082
3 975

"i.m"

4.085

4.146

4 203

3.765

3.817

23

3.865

3.922

3.976

3.498
' 289

3 555

3.602

22

3.647

3.700

3.749

3.345

3.388

21

3.431

3.479

3.523

3 084

3 136

3.175

20

3.216

3.259

3 300

2 881

2.928

2.964

19

3.002

3.044

3.078

■' 679

2 722

2.755

18

2.790

2.825

2.859

2 478

2.517

2.548

17

2.580

2.613

2 644

2 281

2.316

2.344

16

2 374

2.405

2.243

2 087

2.118

1.145

15

2.170

2.199

2.222

1.924

1.948

14

1.971

1.996

2.016

1 716

1.734

1.756

13

1.777

1 797

1.815

1.550

1.509

12

1.585

1 605

1.622

1.353

1.370

1.386

11

1.402

1 417

1.4.33

1 195

1.210

10

1.223

1.235

1.251

1.017

1.027

1.040

9

1.052

1.063

1.077

.866

.878

8

.888

.897

.907

.708

.716

.723

7

.729

.737

.746

.565

.575

.578

6

.583

.587

.595

.432

.440

.442

5

.447

.451

.454

.310

.317

.319

4

.319

.326

.329

.201

.205

.208

3

.211

.214

.214

.133

.114

.114

2

.114

.117

.119

040

.041

.041

1

.041

.041

.042

54 Inches in

55 Inches in

56 Inches in

Depth

57 Inches in

58 Inches in

59 Inches in

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

2m

29

28^

28

27y2

27

5.918

5.719

5.790

5.523

5.331

5.390

5.467

5 535

5.143

4.957

5.023

5.089

5.153

5.217

5.280

4 723

4.785

4.847

23

4.907

4.967

5.026

4.490

4.547

4.605

25

4.662

4.717

4.773

4.258

4.311

4.365

24

4.417

4.469

4.521

4.490

4 547

4.005

25

4.662

4.717

4.773

4 258

4.311

4.365

24

4.417

4.469

4.521

4 026

4.076

4.125

23

4.175

4.223

4.271

3 794

3.842

3.886

22

3.934

3.987

4.023

3.566

3 611

3.651

21

3.694

3.736

3.777

3 340

3.381

3.418

20

3.456

3.495

3.534

3 116

3 152

3.188

19

3 222

3.256

3.293

2.893

2 926

2.950

18

2.992

3.020

3.057

2.674

2.704

2.734

17

2.766

2.788

2.823

2 459

2.486

2.513

16

2 543

2.563

2.594

2 248

2.271

2.296

15

2.321

2 344

2.369

2 04!

2 061

2.084

14

2 104

2.128

2.149

1 838

1,857

1.878

13

1.805

1 916

1.934

1 6-10

1 657

1.675

12

1 692

1 710

1.726

1 449

1 461

1 478

11

1 496

1 509

1..524

1 2tW

1 279

1.290

10

1.304

1 316

1.329

I 086

1 099

1.108

9

1.120

1 . 130

1.141

.915

.926

.936

8

.943

.953

.961

755

.759

.769

7

.776

.784

.791

.tKK!

.607

.614

6

.620

.626

.631

461

.466

.470

5

.473

.479

.483

.331
217

.335

.3.37

4

.340

.344

.347

.210

.220

3

.223

.425

.227

119

.120

.121

2

122

.123

.124

• AH2

.0'»2

.043

1

.043

.044

.044

KANSAS CITY TESTING LABORATORY

161

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tanks in Inches.

60 Inches in

61 Inches in

62 Inches in

Depth

63 Inches in

64 Inches in

65 Inches in

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

323^

7.182

32

3IJ2
31

30}^2
30

6.963

7.039

6.747
6.610

6.535

6.686

6.755

6.326
6.193

6.119

6.267

6.3.37

6.410

6.4/2

5.858

5.929

5.999

29

6.065

6.134

6.193

5.598

5.668

5.732

28

5.794

5.858

5.915

5.339

5.407

5 465

27

5 523

.5.584

5.639

5.082

5 146

5.199

26

5.254

5.310

5.363

4.826

4.885

4.935

25

4.986

5.038

5.089

4.572

4.625

4.672

24

4.722

4.709

4.817

4.318

4.366

4.412

23

4.458

4.503

4.547

4.066

4.111

4.153

22

4 196

4.239

4.281

3.818

3.859

3.898

21

3.937

3.976

4.016

3.572

3.609

3.645

20

3.683

3.718

3.756

3.328

3.363

3.397

19

3.490

3.464

3.496

3.088

3.120

3.151

18

3.181

3.213

3.242

2.582

2.881

2.910

17

2.937

2.964

2.992

2.621

2.646

2.672

16

2.608

2.723

2.748

2.392

2.417

2.440

15

2.463-

2.486

2.508

2.171

2.192

2 213

14

2.232

2.254

2.274

1.954

1.972

1.991

13

2.008

2.027

2.045

1 743

1.759

1 776

12

1.791

1.808

1.823

1.538

1.552

1 567

11

1.581

1.505

1.608

1.341

1.352

1.366

10

1.378

1.390

1.401

1.152

1.161

1 . 173

9

1.183

1.192

1.203

.971

.980

.988

8

.906

1.005

1.013

.799

.806

.812

7

.819

.827

.833

.634

.642

.648

6

.653

.659

.664

.487

.491

.496

5

.500

.504

.506

.349

.354

.357

4

.359

.362

.365

.229

.230

.233

3

.235

.2.38

.238

.125

.126

.128

2

.128

.129

.131

.045

.045

.045

1

.046

.046

.047

162

BULLETIN NUMBER SIXTEEN OF

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

66 Inches in

67 Inches in

68 Inches in

Depth

69 Inches in

70 Inches in

71 Inches in

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

35 Ji
35

34

33^

33

8.570

8.330

8 413

8.094
7.944

7.861

8.026

8.107

7.631
7.485

7.406

7.567

7.640

7.723

7 801

7.120

7.194

7.273

32

7.348

7.421

7.495

6.834

6.904

6.979

31

7.051

7.120

7.190

6.549

6 617

6 687

30

6 755

6.819

6.886

6.264

6.327

6.395

29

6.459

6 519

6.583

5,981

6.041

6.104

28

6 164

6.222

6.283

5.699

5.756

5 814

27

5.870

5 927

5.983

5.419

5.473

5 528

26

5 580

5.6.34

5.686

5.141

5 191

5 244

25

5.292

5 343

5.291

4.865

4 913

4.961

24

5.006

5.052

5.098

4.592

4 637

4.681

23

4.724

4.764

4.809

4.322

4.363

4.403

22

4 444

4 481

4 524

4.054

4.092

4.128

21

4.167

4.204

4 241

3.789

3 824

3.859

20

3.893

3.929

3 962

3.529

3.561

3.593

19

3.625

3.657

3.688

3.273

3.302

3.331

18

3.. 360

3. 388

3.418

3.020

3.046

3.074

17

3.101

3 125

3 152

2.772

2.797

2 821

16

2.846

2.868

2.894

2.530

2.553

2.575

15

2.595

2.617

2.640

2.294

2.314

2 333

14

2.352

2.372

2.391

2.064

2.080

2.099

13

2.116

2 135

2.150

1.839

1 855

1.871

12

1.886

1 901

1.916

1.622

1.635

1.6.50

11

1 . 663

1.674

1.693

1.413

1.426

1 439

10

1.449

1.459

1 476

1.213

1 223

1.235

9

1 242

1.254

1 264

1.022

1.030

1.041

8

1.047

1.060

1 063

.841

.847

.855

1

.859

.871

.874

.670

.675

.680

6

.687

.689

.697

.512

.516

.529

5

.524

.528

.531

.368

.371

.374

4

.377

.378

382

.240
.131
.047

.243

.244

3

.246

.249

250

.132

.133

2

.1.34

.135

136

047

.047

1

.048

.048

.048

KANSAS CITY TESTING LABORATORY

163

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

72 Inches in

73 Inches in

74 Inches in

Depth

75 Inches in

76 Inches in

77 In ,],'.

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

38J^o

10.079

38 '

37
36) i
36

■'"9;819"

9.912

""9.562 "
9.400

"■■9'369 "■

■■■9!489 '"

9^579 '

""oioM "
8.899

s.m"

■'■■8'989"

""9'076"'

"9'i66"'

""9.2A6""

8 500

8-582

8.669

35

8.752

8.832

8.914

8 188

8.267

8.349

34

8.428

8.505

8.583

7.887

7 953

8.030

33

8.104

8,178

8.253

7.887

7 953

8 030

33

8.104

8.178

8.253

7.567

7.639

7 712

32

7.782

7,782

7.924

7.259

7.326

7,395

31

7.461

7.528

7.596

6.952

7.015

7.080

30

7.142

7.205

7,268

6.645

6.706

6.766

29

6.824

6.885

6 944

6 341

6.397

6.454

28

6.509

6 567

6,622

6.038

6.091

6 145

27

6 195

6.250

6,302

5.736

5.786

5 839

26

5.885

5.938

5,988

5 439

5.485

5 535

25

5.578

5,628

5,675

5 144

5-188

5 232

24

5 274

5.320

5,364

4.852

4.892

4 934

23

4.975

5.014

5.056

4 563

4.599

4.639

22

4.677

4.715

4.753

4,278

4 311

4 374

21

4.383

4.418

4.453

3.997

4.025

4.062

20

4.094

4.127

4.161

3.719

3.748

3.781

19

3.809

3.839

3 871

3.446

3.474

3.501

18

3 529

3.556

3.585

3.179

3.204

3.229

17

3.255

3.280

3.305

2.917

2.938

2.962

16

2 985

3.008

3.032

2.658

2.681

2.702

15

2 723

2.744

2.764

2.408

2.429

2.447

14

2 467

2.485

2.503

2.167

1.184

2.200

13

2 216

2.234

2.250

1.932

1.946

1.960

12

1.978

1.990

2.003

1.703

1.716

1.727

11

1.742

1.753

1.767

1.483

1.494

1 505

10

1 515

1.527

1.538

1.272

1.281

1.291

9

1 300

1.309

1.318

1.071

1.079

1.086

8

1 095

1.102

1.110

.880

.887

.893

7

899

.906

.912

.701

.707

.712

6

.717

.722

.727

.536

.540

.544

5

,548

.651

.555

.386

.388

.391

4

.393

.396

.399

.252

.253

.254

3

.256

.259

.260

.138

.138

.139

2

.140

.141

.142

.048

.049

.049

1

.050

.050

.050

164

BULLETIN NUMBER SIXTEEN OF

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tanks in Inches.

78 Inches in

79 Inches in

80 Inches in

Depth

81 Inches in

82 Inches in

83 Inches in

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

41H
41

40

39J4

39

11.711

"■ir.43r"

11.531

"ilJM"
10.978

"io^sso"

■■■li;075'"

" ii!i72 ■"

"io^eio "

10.439

■ "i6'343 "

■"i6;533 "■

'■'i6;627 "

■' l6'726''

"'i0^814 ""

10.000

10.097

10.187

38

10.277

10.365

10.456

9.666

9.756

9.841

37

9.927

10.012

10.098

9.329

9 416

9.496

36

9.578

9.659

9.741

8.994

9.076

9.151

35

9.231

9.307

9.385

8.659

8.737

8.809

34

8.884

8.958

9.032

8.325

8.398

8.468

33

8.538

8.608

8.679

7.992

8.060

8.128

32

8.194

8.260

8.328

7.660

7.724

7.789

31

7.854

7.916

7.980

7.330

7.391

7.454

30

7.514

7.575

7.633

7.001

7.059

7.120

29

7.176

7.234

7.286

6.676

6.7.34

6.788

28

6.842

6.893

6.947

6.354

6.407

6.458

27

6.508

6.557

6.610

6.035

6.085

6.132

26

6.181

6.228

6.274

5.719

5.764

5.809

25

5.583

5.899

5.943

5.406

5.449

5 490

24

5.532

5.574

5.615

5 096

5 138

5.175

23

5.212

5.252

5.291

4 791

4.829

4.864

22

4.900

4.933

4.970

4.487

4.523

4.557

21

4.592

4.624

4.657

4.189

4.224

4.254

20

4.286

4.316

4.436

3.897

3.928

3.956

19

3.987

4.013

4.043

3.610

3.637

3.665

18

3.691

3.717

3.742

3 329

3.355

3.377

17

3.403

3.426

3.450

3.053

3 076

3.098

16

3.120

3.141

3.164

2 784

2.804

2.825

15

2.846

2.863

2.883

2 522

2.540

2.558

14

2.576

2.592

2.612

2 267

2.282

2.299

13

2.315

2.329

2.345

2.019

2.033

2.047

12

2.062

2.074

2.089

1.779

1 791

1.804

11

1.816

1.827

1.840

1.548

1 560

1.570

10

1.582

1.501

1.606

1.328

1 3.36

1 345

9

1.355

1.365

1.372

1.118

1.126

1.132

8

1.141

1.148

1.156

.919

.925

.931

7

.937

.943

.950

.731

.736

.742

6

.746

.752

.757

.559

.563

.565

5

.569

.574

.576

.401

.404

.407

4

.409

.412

.415

.261

.264

.265

3

.267

.269

.269

.143

.143

.145

2

.146

.147

.148

.051

.051

.051

1

.052

.052

.053

KANSAS CITY TESTING LABORATORY

165

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

84 Inches in

85 Inches in

86 Inches in

Depth

87 Inches in

88 Inches in

89 Inches in

Diameter

Diameter

Diameter

Inches

Diameter

Diameter

Diameter

44J^
44
43}^
43

421-2
42

13.466

"n.m"

■■■i2!867"
12.679

"■i2!573"

"'i2:783"'

"V2.8S7

" i2'283"
12 099

""11.995 "

"i2!26r"

■■■i2',303' ■

'"'i2'46i"'

"'i2!56i'""

11.632

11.731

11.829

41

11.927

12 019

12.116

11.269

11 363

11 457

40

11 552

11.6.38

11-734

10.906

10.997

11.086

39

11.177

11 261

11.352

10.544

10 632

10.716

38

10.802

10.884

10.970

10.183

10.267

10.347

37

10.430

10 .508

10.589

9.822

9.903

9 979

36

10 058

10 1.32

10.209

9.462

9.540

9.611

35

9.759

9.759

9.832

9.104

9.177

9 245

34

9.318

9.387

9.458

8.747

8.816

8.883

33

8.951

9.018

9.085

8.392

8.459

8.523

32

8.587

8.651

8 713

8.040

8.105

8 164

31

8.226

8.287

8 .345

7.690

7.751

7.807

30

7.865

7.925

7.978

7.344

7.401

7.454

29

7.509

7.566

7.617

7.000

7.054

7.104

28

7.156

7.210

7.258

6 658

6.710

6.756

27

6.805

6.856

6.901

6.320

6.. 369

6.413

26

6.458

6.504

6.549

5.986

6.030

6.074

25

6.118

6.158

6.201

5.656

5.699

5 7.38

24

5.773

5.816

5.858

5 330

5. 368

5 404

23

5.445

5.482

5.516

5.007

5.043

5.078

22

5.114

5.150

5.182

4.690

4 724

4.756

21

4.790

4.821

4.855

4.378

4.410

4.440

20

4.469

4.499

4.528

4.071

4.098

4.126

19

4 155

4.181

4 211

3.770

3.796

3.821

18

3.847

3.872

3,896

3.475

3.497

3 522

17

3.544

3.576

3 590

3.186

3.206

3,227

16

3.249

3.269

3 291

2.904

2.924

2.941

15

2.961

2 980

2.999

2.629

2.646

2.663

14

2.679

2,699

2.714

2.362

2.378

2.393

13

2.406

2 421

2.4.39

2.104

2.116

2.129

12

2.142

2 154

2.169

1.853

1.865

1.876

11

1.888

1.900

1.200

1.613

1.621

1.633

10

1.641

1.656

1.663

1.383

1.391

1.400

9

1.407

1.416

1.425

1.162

1.169

1.176

8

1 . 185

I 190

1.200

.954

.962

.967

7

.973

.979

.983

.760

.765

.770

6

.776

.778

.784

.580

.585

.587

5

.592

.595

.598

.417

.420

.422

4

.429

.429

.4.30

.272

.274

.275

3

.278

.279

.280

.148

.149

.151

2

.151

.153

.154

.053

053

.053

1

.0.54

.055

.055

166

BULLETIN NUMBER SIXTEEN OF

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tanks in Inches.

90 Inches in
Diameter

91 Inches in
Diameter

92 Inches in
Diameter

Depth
Inches

93 Inches in
Diameter

94 Inches in
Diameter

95 Inches in
Diameter

47}^
47

46H
46
45H
45

15 .342

i i 7n'?

■■'i5:62i' '

15 1.36

"14:388 "
"'i3!988"

14 501

■ 14:6i2"

' 14^726' '

is 770

14.078
13.880

■■■l4'.098' '

■ 14'207"'

" i4!3i6" '

13.378

13.487

13 590

44

13.696

13.802

13.905

12 987

13.094

13 194

43

13.296

13.397

13.495

12.597

12.701

12.798

42

12.896

12.993

13.086

12.209

12.308

12.403

41

12.497

12 590

12 679

11.822

11.915

12.008

40

12.098

12 187

12 273

11.436

11.525

11.613

39

11.699

11.785

11.867

11.051

11.137

11.218

38

11.301

11 384

11 463

10.667

10.750

10.826

37

10.906

10 983

11 061

10.284

10.363

10.438

36

10.513

10 587

10.662

9.903

9.977

10.050

35

10.123

10.193

10.265

9.524

9.596

9.665

34

9.733

9.800

9.870

9.184

9.216

9.281

33

9.344

9.410

9.476

8.837

8.900

32

8.962

9.024

9.084

8.403

8.463

8.523

31

8.580

8.639

8.697

8.093

8.149

30

8 200

8.257

8.313

7 670

7.724

7.777

29

7.827

7.880

7.932

7.358

7.409

28

7.456

7.506

7.553

6 948

6.996

7.046

27

7.089

7.1.38

7.182

6.638

6.687

26

6.727

6.771

6.812

6 242

6.283

6-331

25

6. 367

6.407

6.450

5.934

5 976

24

6.013

6.052

6.090

5 .5.52

5.588

5.626

23

5.662

5.700

5.734

5 215

5 248

5.284

22

5.320

5.352

5.386

4 88.-i

4.916

4.948

21

4.979

5.010

5.042

4 6.56

4.587

4.617

20

4 647

4.673

4.701

4 2:i5

4.264

4.292

19

4.317

4.343

4.368

3 921

3.946

3.972

18

3.996

4.021

4.045

3 611

3.6.35

3.657

17

3.681

3.703

3.727

3 .309

3.331

3.353

16

3.375

3.393

3.414

3 014

3.035

3.056

15

3.073

3.091

3.109

2.729

2.747

2.763

14

2.781

2.796

2.814

2 452

2.468

2.480

13

2.497

2 510

2.524

2 183

2.196

2.210

12

2.222

2.232

2.248

1 'J22

1.934

1.946

11

1 957

1.966

1.981

1 673

1.682

1.696

10

1 703

1.714

1.723

1 433

1.443

1.455

9

1.455

1.469

1.474

1 2()4

1 214

1.216

8

1.226

1.232

1.240

.989

.995

1.000

7

1.007

1.010

1.019

.787

.793

.799

6

.803

.807

.812

.601

.605

.608

5

.613

.616

.618

.4.32

.435

.440

4

.440

.445

.445

281

.284

.290

3

.290

.291

.292

154

155

.156

2

.157

.158

.160

055

055

.056

1

.056

.056

056

KANSAS CITY TESTING LABORATORY

167

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tanks in Inches.

96 Inches in

Depth

97 Inches in

96 Inches in

Depth

97 Inches in

Diameter

Inches

Diameter

Diameter

Inches

Diameter

48H
48

15.995
15 785

6.128
5 770

24
23

6 163

15.668

5.803

15.248

47

15.365

5.416

22

5.450

14.828

46

14 945

5 066

21

5.101

14.410

45

14.525

4.726

20

4.757

13.992

44

14.108

4 394

19

4.421

13.574

43

13.692

4.068

18

4.092

13.158

42

13.276

3 752

17

3.770

12.744

41

12 860

3 444

16

3.455

12.336

40

12 446

3 139

15

3.145

11 930

39

12 033

2.838

14

2.844

11.524

38

11 622

2 546

13

2.554

11.119

37

11.214

2.260

12

2.273

10.716

36

10.807

1.990

11

2.001

10.315

35

10.400

1.728

10

1.742

9.915

34

9.997

1.480

9

1.492

9.518

33

9.599

1.240

8

1 254

9.124

32

9.204

1.016

7

1 032

8.736

31

8.810

.804

6

.821

8 352

30

8.420

.620

5

.625

7.974

29

8.035

.447

4

.448

7.600

28

7 654

.292

3

.293

7.230

27

7.274

.160

2

.160

6.862

26

6.897

.057

1

.057

6.494

25

6.526

98 Inches in

Depth

99 Inch33 in

98 Inches in

Depth

99 Inches in

Diameter

Inches

Diameter

Diameter

Inches

Diameter

49,1 2
49

166.662
16.446

6.569
6.203

25
24

6 607

16.327

6 239

15.898

48

16.016

5 841

23

5.874

15.473

47

15 587

5.484

22

5.514

15 049

46

15.159

5.131

21

5.160

14.626

45

14.732

4.786

20

4.814

14 205

44

14.305

4.449

19

4.472

13 784

43

13.880

4.116

18

4.138

13.363

42

13.458

3.792

17

3.811

12.944

41

13.036

3 472

16

3.941

12.527

40

12.615

3.160

15

3.181

12.111

39

12 197

2 856

14

2.878

11 698

38

11 780

2 565

13

2 583

11 287

37

11 365

2 282

12

2.298

10.877

36

10.952

2.016

11

2.025

10 468

35

10.539

1.754

10

1.759

10.063

34

10.128

1.501

9

1.508

9.661

33

9.723

1.260

8

1.266

9.263

32

9 , 322

1.035

7

1.040

8.867

31

8 921

.823

6

.828

8.473

30

8 526

.628

5

.633

8.085

29

8 136

.453

4

.453

7.700

28

7.747

.295

3

.297

7.318

27

7.362

.162

2

.162

6.940

26

6 982

.058

1

.058

168

BULLETIN NUMBER SIXTEEN OF

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

100 Inches in
Diameter

Depth
Inches

101 Inches in
Diameter

100 Inches in
Diameter

Depth
Inches

101 Inches in
Diameter

503^
50

17.342
17.122

6.647
6.274

25
24

6.685

17 000

6.311

16 565

49

16.683

5.908

23

5.942

16 132

48

16.247

5.546

22

5 579

15 699

47

15.812

5.190

21

5.221

15 267

46

15.377

4.841

20

4.808

14 837

45

14.942

4.498

19

4.523

14.407

44

14.507

4.162

18

4,185

13 987

43

14.073

3.833

17

3.855

13.551

42

13.642

3.511

16

3.531

13.125

41

13.213

3.198

15

3.215

12.700

40

12 784

2.893

14

2.908

12.277

39

12.356

2.597

13

2.612

11.855

38

11.931

2.311

12

2.324

11.436

37

11 508

2.035

11

2.041

11.020

36

11.000

1.769

10

1 779

10.605

35

10.672

1.516

9

1.524

10.194

34

10.257

1.274

8

1.282

33

9.846

1.040

7

1.053

9.379

32

9 437

.833

6

.838

8.977

31

9.032

.636

5

.640

8.578

30

8.630

.456

4

.458

8.184

29

8.233

.297

3

.298

7.793

28

7.840

.162

2

.162

7.407

27

7 450

.058

1

.158

7.024

26

7.065

102 Inches in

Depth

103 Inches in

102 Inches in

Depth

103 Inches in

Diameter

Inchei

Diameter

Diameter

Incties

Diameter

51H
51

18 033

7 108

26

7.148
6.764

17.687

17 811

6.722

25

17 246

50

17.. 364

6 340

24

6.387

16 805

49

16 918

5.972

23

6.010

16 364

48

16.473

5.608

22

5.644

15 924

47

16 030

5 251

21

5 281

15 485

46

15.587

4.895

20

4 924

15 047

45

15.144

4.549

19

4 576

14 6(J9

44

14.701

4.208

18

4.230

14.172

43

14.259

3.877

17

3 896

13 738

42

13.819

3.554

16

3 508

13 .304

41

13.384

3,235

15

3.250

12 871

40

12.950

2.916

14

2 938

12 440

39

12 516

2.622

13

2.639

12 Oil

38

12.083

2.333

12

2.348

11 587

37

11.655

2.056

11

2.069

II l&l

36

11.229

1.787

10

1.798

10 74.)

35

10 805

1.531

9

1.542

10 .(25

34

10.386

2.178

8

1 295

9 911

33

9.968

2.057

7

1.064

9.498
9.087

32
31

9.556
9.147

.854
.642

6
5

.844
.646

30

8 738

.458

4

.462

■

29

8.331

.300

3

.301

7.497

28
27

7.930
7.537

.163
.058

2
1

.164
.059

KANSAS CITY TESTING LABORATORY

169

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

104 Inches in

Depth

105 Inches in

104 Inches in

Depth

105 Inches in

Diameter

Inches

Diameter

Diameter

Inches

Diameter

52' i

18.742

7 190

26

7 229

18.'387

52

18.513

6.804

25

6:841

17.936

51

18.057

6.423

24

6.457

17.485

50

17.603

6.046

23

6.075

17.035

49

17.150

5.671

22

5.704

16.587

48

16.697

5.308

21

5.336

16.140

47

16.245

4.950

20

4.978

15.693

46

15.794

4.599

19

4.626

15.247

45

15.343

4.255

18

4.277

14.802

44

14.893

3.920

17

3.938

14.357

43

14.447

3.588

16

3.608

13.912

42

14.002

3.267

15

3.285

13.470

41

13.558

2.955

14

2.971

13.032

40

13.116

2.653

13

2.667

12.597

39

12.675

2.361

12

2.373

12.164

38

12.237

2.080

11

2.090

11.732

37

11.802

1.809

10

1.814

11.297

36

11.371

1.548

9

1.556

10.872

35

10.940

1.300

8

1..308

10.450

34

10.511

1.068

7

1.074

10.029

33

10.088

.850

6

.853

9.610

32

9.666

.649

5

.652

9.198

31

9.249

.467

4

.469

8.789

30

8.837

.302

3

.304

8.382

29

8.430

.164

2

.165

7.978

28

8.025

.059

1

.059

7.582

27

7.623

t08 Inches in

Depth

107 Inches in

106 Inches in

Depth

107 Inches in

Diameter

Inches

Diameter

Diameter

Inches

Diameter

53J'2

19.463

7.668

'27

7.710

19.101

53

19.230

7.272

26

7.312

18.639

52

18.766

6.877

25

6.919

18.180

51

18.303

6.491

24

6.526

17.723

50

17.841

6.111

23

6.14

17.266

49

17. .381

5.733

22

5.767

16.810

48

16.922

5.366

21

5.395

16.354

47

16.463

5,005

20

5.029

15.898

46

16.004

4.648

19

4.673

15.444

45

15.545

4.300

18

4.323

14.991

44

15.087

3.960

17

3.980

14.539

43

14.629

3.626

16

3.643

14.089

42

14.176

3.302

15

3.. 320

13.642

41

13.724

2.988

14

3.001

13.196

40

13.275

2.680

13

2.696

12.752

39

12.828

2.384

12

2.398

12.310

38

12.384

2.101

11

2.110

11.869

37

11.943

1.824

10

1.8.34

11.434

36

11.503

1.564

9

1.571

11.005

35

11.069

1.314

8

1.320

10.576

34

10.635

1.077

7

1.084

10.150

33

10.205

.858

6

.862

9.725

32

9.779

.655

5

.658

9.303

31

9 354

.470

4

.473

8.888

30

8.937

.306

3

.306

8.474

29

8.523

.166

2

.167

8.069

28

8.116

.059

1

060

170

BULLETIN NUMBER SIXTEEN OF

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

108 Inches in
Diameter

Depth
Inches

109 Inches in
Diameter

108 Inches in
Diameter

Depth
Inches

109 Inc.:es in
Diameter

54H
54

20.198
19.962

7.756
7.352

27
26

7 796
7 391

19 828

19 359

53

19-490

6.953

25

6 993

18 892

52

19 019

6.560

24

6.597

18 426

51

18.548

6.176

23

6.209

17 961

50

18.077

5.797

22

5.827

17 496

49

17.607

5.428

21

5 453

17 031

48

17 137

5.059

20

5 084

16.567

47

16.670

4.696

19

4.720

16 103

46

16.203

4.343

18

4 367

15.639

45

15.737

4.000

17

4.022

15 178

44

15.272

3.661

16

3.682

14 719

43

14 810

3.335

15

3.3.53

14 263

42

14.349

3.020

14

3 032

13 810

41

13.890

2.711

13

2 723

13 359

40

13.435

2.409

12

2.422

12.910

39

12.983

2.121

11

2 131

38

12 531

1.843

10

1 852

12 019

37

12.083

1.575

9

1 586

11 576

36

11.639

1.323

8

1.336

11.135

35

11.197

1.085

7

1.095

10.698

34

10 758

.868

6

.871

10.265

33

10 322

.662

5

.665

9.836

32

9 892

.476

4

.477

9 412

31

9 463

.309

3

.309

9 992

30

9.037

.169

2

.170

8.576

29

8 619

.060

1

.060

8.165

28

8.207

110 Inches in

Depth

111 Inches in

110 Inches in

Depth

111 Inches in

Diameter

Inches

Diameter

Diameter

Inches

Diameter

55>^
55

20 946

8 244

28

8 290

20 570

20.703

7.833

27

7.878

20.093

54

20.219

7.428

26

7.468

19 616

53

19.738

7.026

25

7.063

19.140

52

19.259

6.628

24

6.665

18 664

51

18.781

6.238

23

6.274

18 188

50

18.. 305

5.?56

22

5.888

17 715

49

17.829

5.481

21

5.509

17 214

48

17.353

0.116

20

5.136

Hi 774

47

16.877

4.754

19

4.771

16 .(04

46

16.403

4.396

18

4.413

15 K.'<6

45

15.932

4.046

17

4.059

IS .iliS

44

15.461

3.704

16

3.718

14 !«)5

43

14.992

3.366

15

3.385

14 444

42

14.523

3.036

14

3.062

13 98.3

41

14.064

2.724

13

2.748

13 .524

40

13.589

2.428

12

2.445

13 066

39

13.1.30

2.140

11

1.153

12 (108

38

12.676

1.864

10

1.870

12 1.55

37

12.223

1.599

9

1.600

II 704

36

11.772

1.347

8

1.347

11 2.58

35

11.323

1.102

7

1 106

10 N16

34

10.879

.876

6

880

10 378

33

10.437

.671

5

671

« 944

32

10.002

.479

4

480

9 514

31

9 570

.310

.3

312

« 087
8 664

30
20

9 141
8.714

.170
.060

2

1

.170
.061

KANSAS CITY TESTING LABORATORY

171

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

112 Inches .n

Depth

113 Inches in

112 Inches in

Depth

113 Inche.s in

Diameter

Inches

Diameter

Diameter

Inches

Diameter

56,1 i
56

21.707
21.461

8.338
7.919

28
27

8.383

21^325

7.962

20.837

55

20 971

7 507

26

7.548

20.349

54

20.481

7 101

25

7.139

19.863

53

19 991

6 703

24

6.736

19.379

52

19.504

6 307

23

6.339

18.897

51

19.017

5.916

22

5 948

18.415

50

18.530

5.536

21

5.560

17 936

49

18.044

5 163

20

5.188

17.457

48

17.559

4.795

19

4.817

16 980

47

17.074

4 434

18

4.457

16.503

46

16.590

4.081

17

4.101

16.028

45

16.112

3.738

16

3.755

15.554

44

15.638

3 402

15

3.419

15.080

43

15.165

3.077

14

3.091

14.610

42

14.692

2.764

13

2.772

14.141

41

14.221

2.457

12

2.468

13.672

40

13.751

2.162

11

2.171

13.210

39

13.283

1.881

10

1.887

12 751

38

12.821

1.610

9

1.615

12.292

37

12.361

1.350

8

1.357

11.838

36

11.904

1.111

7

1.113

11.388

35

11.449

.885

6

.886

10.942

34

10.999

.674

5

.675

10.497

33

10.552

.482

4

.486

10.055

32

10 108

.314

3

.317

9 620

31

9.669

.171

2

.171

9.188

30

9 235

.061

1

.062

8 761

29

8 805

114 Inches in

Depth

115 Inches in

114 Inches in

Depth

115 Inches in

Diameter

Inches

Diameter

Diameter

Inches

Diameter

573..
57 "

22.482
22.230

8.856
8.425

29
28

8.898

22 093

8.468

21.599

56

21.733

8.003

27

8.040

21.105

55

21.236

7.583

26

7.622

20.611

54

20.740

7.176

25

7.213

20.117

53

20.244

6.770

24

6 806

19 624

52

19.748

6.369

23

6.401

19.132

51

19 252

5.978

22

6.007

18.643

50

18.756

5 .592

21

5.619

18.155

49

18.262

5 212

20

5.238

17.668

48

17.772

4 841

19

4 865

17.181

47

17.282

4.476

18

4 499

16 695

46

16.795

4 120

17

4 139

16 212

45

16.309

3.771

16

3 786

15.731

44

15.823

3.4.36

15

3 451

15.253

43

15.341

3.109

14

3 121

14.775

42

14.862

2.786

13

2.799

14.299

41

14.383

2.481

12

2.491

13 828

40

13.906

2 183

11

2.192

13 360

39

13 431

1.898

10

1.907

12.893

38

12 964

1 624

9

1 632

12.428

37

12.497

1 365

8

1.371

11.967

36

12.033

1.120

7

1.126

11.511

35

11 572

.890

6

.895

11 057

34

11.116

.681

5

.684

10.609

33

10.664

.488

4

.490

10.165

32

10.217

.317

3

.319

9.722

31

9.771

.172

2

.173

9 288

30

9.331

062

I

.062

172

BULLETIN NUMBER SIXTEEN OF

HORIZONTAL TANKS— (Continued).

Multiply Capacity in Tables by Length of Tank in Inches.

116 Inches in

Depth

117 Inches 'n

116 Inches in

Depth

117 Inches in

Diameter

Inches

Diameter

Diameter

Incics

Diameter

58J/2
58

23.271
23.016

8.944
8.513

29

28

8.988

22.875

8 555

22.371

57

22.506

8.086

27

8 125

21.868

56

21.998

7 663

26

7.701

21. 366

55

21.493

7.247

25

7 282

2;j.865

54

20.989

6.8.38

24

6 870

20 365

53

2 J. 485

6.4.34

23

6 460

19.866

52

19,992

6.036

22

6 065 •

19 .368

51

19.479

5.645

21

5.675

18.870

50

18.977

5.262

20

5 292

18.373

49

18.476

4.888

19

4 913

17.877

48

17.975

4.519

18

4 541

17 .382

47

17.478

4.160

17

4.179

16.888

46

16.984

3.813

16

3 826

16 398

45

16.491

3.468

15

3.483

15 911

44

15.999

3.136

14

3.149

15 427

43

15.510

2.813

13

2 828

14.944

42

15 024

2.502

12

2.516

14.462

41

14.540

2.291

11

2 215

13 981

40

14.056

1.914

10

1.925

13 501

39

13.578

1.639

9

1.645

13 023

38

13.102

1.376

8

1.385

12 549

37

12.632

1.131

7

1.136

12.079

36

12.162

.899

6

.903

11.613

35

11.698

.686

5

.689

11 1.52

34

11. 2.38

.492

4

.496

10 697

33

10 778

.320

3

.321

10 2.50

32

10.323

.175

2

175

9 SIL'
'.1 .■!77

31
30

9.872
9.428

.062

1

.063

118 Inches in
Diameter

Depth
Inches

119 Inches in
Diameter

118 Inches in
Diameter

Depth
Inches

119 Inches in
Diameter

59^2

24.074

9.476

30

23.'67i

23 160

9.524

59

58

23.816
23.301

9.031
8.595

29

28

9' 082
8 643

22 649
22 138

91 ( ' '> 7

57
56
55
54
53
.52
51
50
49
48
47
46
45
44
43
42
41
40
39
38
37
36
35
34
33
32
31

22.787
22.273

8.165
7.739

27
26

8^207
7 779

^1 Uzi

21 117
20 (!0»
20 102
19 .597
19 092
IN .5h7
IN iih:;
17 .5H2
17 0K2
H. .5N1
|i; 0N8
1.5 .595
15 105

11 1120
H 137
13 1151
13 171

12 (198
12 225
II 7.5K
II 29;.'
II) N.'!2
10 377

9 KM

21.760
21.247
20.734
20 221
19 710
19 203
18.697
18 191
. 17.685
17.182
16 081
16 180
15 682
15 188
14.697
14.209
13 725
13 245
12 767
12.291
11 818
II .350
10.888
10.429
0.975

7.319

6 905

6.496

6.094

5.702

5.317

4.937

4 562

4.197

3.845

3.501

3.163

2.841

2.526

2.223

1.932

1.655

1.390

1.141

.909

.694

.497

.322

.175

.063

25

24
23
22
21
23
19
18
17
16
15
14
13
12
11
10

9

8

7

6

S

4

3

2

1

7.357

6.940

6 529

6.127

5 7.30

5 .342

4.959

4.587

4.220

3.867

3.520

3.180

2.853

2.535

2.232

1 . 938

1.659

1.396

1.146

.910

.696

.498

.325

.178

.063

KANSAS CITY TESTING LABORATORY

173

HORIZONTAL TANKS— (Concluded).

Multiply Capacity in Tables by Length of Tank in Inches.

120 Inches in

Depth

121 Inches in

Depth

120 Inches in

Depth

Diameter

Inches

Diameter

Inches

Diameter

Inches

24.479

60

14.287

40

5.363

20

23.954

59

13.797

39

4.981

19

23.434

58

13 314

33

4.608

18

22.914

57

12.833

37

4.240

17

22.395

56

12.354

36

3.882

16

21.877

55

11.881

35

3.538

15

21.359

54

11 411

34

3.198

14

20.842

53

10 944

33

2.866

13

20.328

52

10.483

32

2.537

12

19 815

51

10.024

31

2.239

11

19.305

50

9.567

30

1.949

10

18.795

49

9 124

29

1.668

• 9

18.287

48

8.683

28

1.396

8

17.780

47

8.244

27

1.151

7

17.273

46

7.816

26

.915

6

16.767

45

7.393

25

.699

5

16 265

44

6.976

24

.501

4

15.768

43

6 561

23

.326

3

15.273

42

6.153

22

.178

2

14.779

41

5.751

21

.063

1

174

BULLETIN NUMBER SIXTEEN OF

GAUGING T\BLE FOR EACH ONE-QUARTER INCH IN DEPTH
FOR T\NK AS DETAILED ON PETROLEUM IRON WORKS
COMPANY DRAWING No. 2050-A

8050-Gallon 78-Inch Diameter Tank With Steam Coils for Type

"A" and "A-1" Cars

1

a

o
c

pa

c
o

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a

1

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1

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Gallons

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731
754

2
H

2037
2067

3

3565
3598

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y

5241
5174

5

y

6583
6611

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7695
7713

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80S5

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H
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8088

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5489

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I

DOME 244 gallons = 1L60 gallons to one inch.

Furnished by Pennsylvania Tank Car Company, Sharon, Pa.

KANSAS CITY TESTING LABORATORY

175

Outage Table for Standard 6,000 Gallons Capacity Tank Car.

Table for gauging tanks by the inch. Capacity in U. S. gallons of a
72%" diameter tank. Official dome capacity, including dish in head,
222 gallons. Length of tank, bend line to bend line, 27' 8M".

Inches

1

2

3

4

5

6

7

8

9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25

Gallons

16.62

46.94

85.99

131.84

183.44

240.16

301.30

366.47

435.23

507.47

582 . 80

660.96

741.73

825.15

910.70

998.43

1088.20

1179.82

1273.13

1368.11

1464.53

1562.11

1661.17

1761.46

1862.72

Inches

26

27
28
29
30
31
32
33
34
35
36

37
38
39
40
41
42
43
44
45
46
47
48
49

Gallons

1964.88
2067.94
2171.75
2276.29
2381.39
2487.05
2593.30
2699.71
2806.40
2913.24
3020.24
3047.00
3127.26
3234.18
3340.95
3447.50
3553.82
3659.78
3765.16
3869.98
3974.15
4077.59
4180.20
4281.91
4382.69

Inches
50
51
52
53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
72U

Gallon

4482.36

4580.68

4677.68

4773.38

4868.52

4959.99

5050.69

5139.43

5226.07

5310.56

5392.65

5472 . 12

5548.86

5622 . 65

5693.60

5760.64

5823 . 88

5882 . 82

5937.01

5985.74

6028.37

6063.41

6088.36

6094 . 0 0

Dome capacity is 9.914 gallons per inch.

TANK CAR OUTAGE TABLES

Calculated From 0 25 Inch to 5 Inches Out of Shell, at 60° F.
Capacity of Car in Gallons at 60° F,

4,231

6,000

6,641

7,000

8,087

8,102

8,505

10,000

Inches

Gallons

Gallons

Gallons

Gallons

Gallons

Gallons

Gallons

Gallons

0.25

3

4

4

4

5

5

5

6

0.5

6

8

8

8

10

10

10

12

0.75

9

13

13

13

16

16

17

19

1.

13

18

18

18

23

23

25

26

1.25

18

24

25

25

31

31

33

36

1.5

23

31

33

33

39

39

45

46

1 75

29

38

41

41

48

48

56

58

2.

35

46

49

50

58

58

67

71

2.25

41

54

58

59

69

69

79

84

2.5

48

63

68

69

80

80

92

98

2.75

55

72

78

79

90

91

105

111

3.

63

82

88

90

103

103

119

125

3.25

71

92

99

101

115

115

133

140

3.5

79

103

110

113

128

128

148

156

3.75

87

114

123

125

141

141

163

171

4.

96

125

134

137

154

154

178

186

4 25

105

136

146

150

167

167

194

203

4.5

114

148

159

163

181

181

211

220

4.75

123

160

172

176

195

195

288

237

5.

133

173

186

190

210

210

244

254

176

BULLETIN NUMBER SIXTEEN OF

TANK CAR OUTAGE TABLES (Continued)
Outage Table for Standard 6,648 Gallons Capacity Car Tank.

Table for gauging tanks by the inch. Capacity in U. S. Gallons of a
7414" diameter tank. 29' V2" long. Official dome capacity, including
dish in head, 87.9 gallons.

Inches Gallons Inches Gallons Inches Gallons

1
2
3

4

5

6

7

8

9

10

11

12

13

14

15

16

17

18

19

20

21

22

23

24

25

17.35

47.28

87.99

138.36

195.85

259.34

325.55

394.82

467.81

544.49

623.44

795.18

790.00

877 . 85

967 . 02

1059 . 55

1154.35

1250.30

1348.07

1447.30

1548.89

1651.71

1756.36

1861.57

1968.52

26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50

2076.40
2186.05
2296.28
2407.45
2519.24
2631.44
2744.43
2858.07
2972.14
3087.13
3202 . 94
3319.12
3436.02
3552.30
3668 .07
3782 . 59
3895.89
4008 . 87
4120.85
4232 . 14
4343.13
4453.32
4562.90
4670.73
4777.60

51
52
53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
73

74 M
74

4883 33
4986.74
5089 . 50
5190.91
5290 . 73
5389.40
5485 . 82
5578.96
5670.70
5759.71
5847 . 58
5933.25
6014.58
6091.75
6165.89
6236.98
6306.66
6373.20
6436.49
6494 . 53
6544.95
6587.26
6622.29
6643.02
6647.69

Dome Capacity is 3.06 gallons per inch.

Outage Table for Standard 7,191 Gallons Capacity Car Tank.

Table for gauging tanks by the inch. Capacity in U. S. gallons of an
83" diameter tank. Length of tank 25'.

Inches

Gallons

1

16.50

2

44.86

3

79.72

4

120.47

5

167.45

6

210.30

7

276.14

8

337.48

9

403.44

10

474.27

11

550.22

12

630.21

13

712.19

14

795.58

15

881.37

16

969.07

17

1058.47

18

1149.46

19

1241.56

20

1334.68

21

1428.73

22

1623.83

23

1620.03

21

1717.33

25

1815.68

26

1915 19

27

2015 49

2H

2116 84

Inches

Gallons

29

2219.32

30

2322.74

31

2427.17

32

2532 . 58

33

2638.98

34

2746.36

35

2854.66

36

2963.76

37

3073.76

38

3184.66

39

3296.31

40

3408 . 65

41

3521 . 68

42

3635.18

43

3748.21

44

3860.56

45

3972.23

46

4083.15

47

4193.17

48

4302.29

49

4410.59

50

4517.97

51

4624.37

52

4729.78

53

4834.25

54

4937.71

55

5040.21

56

5141.59

.Dome capacity is 9.914 gallons per inch.

Inches

Gallons

57

5242.01

58

5341.46

59

5439.84

60

5537.19

61

5633.39

62

5728.54

63

5822 . 64

64

5915.82

65

6007.92

66

6098.91

67

6188.90

68

6277.35

69

6364.33

70

6450.11

71

6533.50

72

6615.38

73

6695.37

74

6772.35

75

6843.28

76

6909.26

77

6970.01

78

7025.01

79

7073.85

80

7114.80

81

7145.76

82

7173.96

83

7191.00

KANSAS CITY TESTING LABORATORY

177

TANK CAR OUTAGE TABLES (Continued)
Outage Table for Standard 10,676 Gallons Capacity Car Tank

Table for gauging tanks by the inch. Capacity

i9^^" diameter tai

Inches

Gallons

1

21.32

2

60.13

3

110.07

4

168.83

5

235.30

6

308.16

7

387.04

8

471.14

9

560.20

10

653.72

11

751.57

12

853.15

13

958.45

14

1067.06

15

1178.93

16

1294.34

17

1411.24

18

1531.95

19

1655.37

20

1780.97

21

1907.80

22

2037.89

23

2170.01

24

2302.82

25

2438.48

26

2576.04

27

2714.82

28

2854.15

29

2995.93

30

3137.84

Dome

capacity,

Official dome

Inches
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
56
57
58
59
60

capacity,
Gallons
3282.20
3427.51
3573.91
3720 . 04
3868.20
4017.80
4166.71
4315.69
4466.30
4617.59
4769.17
4920 . 99
5072.96
5223.85
5376.24
5527 . 88
5679.31
5831.21
5982 . 91
6134.34
6285.29
6435.08
6584.34
6733.59
6882.16
7029.31
7175.57
7321.43
7466.26
7609.40

in U. S. gallons of an
ncluding dish in head.

11.532 gallons per inch.

Inches
61
62
63
64
65
66
67
68
69
70
71
72
73
74
75
76
77
78
79
80
81
82
83
84
85
86
87
88
89
89 H

Gallons

7751.24

7891.79

8030 . 85

8169.02

8305.63

8439 . 87

8572.33

8703.44

8831 . 89

8958 . 11

9082 . 62

9204.69

9323.49

9439 . 58

9553 . 62

9663.93

9770.98

9874 . 42

9974.14

10069.89

10161.18

10247 80

10329.37

10405.33

10475.05

10537.75

10592.43

10637.17

10668.70

10676.28

Outage Table for Standard 7,900 Gallons Capacity Tank

Car.

[•able

for

gauging

tanks

by the inch

Capacity in

U. S. gallo

ns of an

:2%"

diameter tank. Official dome

capacity, including dish

in head.

55.6 gall(

3ns. Len

gth of

tank 27' 8'

Inches

Gallons

Inches

Gallons

Inches

Gallons

1

17.91

29

2483.84

56

6718.90

2

50.36

30

2600.79

57

5832.27

3

92.19

31

2718.82

58

5944 . 38

4

141.43

32

2837 . 52

59

6055.17

5

196.90

33

2956.90

60

6164.53

6

257.78

34

3076.85

61

6272.41

7

323.66

35

3197.29

62

6378.66

8

393 . 89

36

3318.29

63

6483.10

9

468.15

37

3439.58

64

6585.79

10

546.16

38

3561.20

65

6686.43

11

627.60

39

3683.09

66

6784.99

12

712.18

40

3805.00

67

6881.33

13

799.82

41

3927.12

68

6975.25

14

890.26

41 A

3950.00

69

7066.62

15

983.16

42

4049.19

70

7155.32

16

1078.63

43

4171.20

71

7241.05

17

1176.38

44

4293.11

72

7323.69

18

1276.30

45

4414.89

73

7403 . 02

19

1378.19

46

4536.28

74

7478.73

20

1481.96

47

4657.37

75

7550.54

21

1587.57

48

4778.04

76

7618.05

22

1694.81

49

4898.23

77

7680.90

23

1803.62

50

5017.81

78

7738.46

24

1913.92

51

5136.76

79

7790.17

25

2025.51

52

5254.99

80

7834 89

26

2138.42

53

5372.40

81

7871.23

27

2252.48

54

5488.83

82

7895.80

28

2367.65

55

5604.40

82^

7900.00

Dome

capacity

is 6.00

gallons per

inch.

178

BULLETIN NUMBER SIXTEEN OF

TANK CAR OUTAGE TABLES (Continued)
Outage Table for Standard 7,920 Gallons Capacity Tank Car.

Table for gauging tanks bv the inch. Capacity in U. S. gallons of an
80" diameter tank. Official dome capacity, including dish in head,
155.6 gallons. Length of tank 28'.

■ CD —

Inches

Gallons

Inches

Gallons

Inches

Gallons

1
2
3
4

18.76

28

2470.39

55

7568.45

52 74

29

2591.10

56

5021.64

96.50

30

2712.71

57

6936 . 50

149 04

31

2835.18

58

0149.84

5

206.12

32

2958.36

59

6261 . 58

6

269 . 85

33

3082.19

60

6371.59

7

338.72

34

3206 . 53

61

6479 . 85

8

412.14

35

3331.42

62

6586.18

9

489 . 83

36

3456.61

63

6690.35

10

571.36

37

3582.21

64

6792 . 40

11

656.43

38

3708.01

65

■ 6892.03

12

744.91

39

3833.96

66

6989.14

13

836.47

40

3960.00

67

7083.53

14

930.86

41

4086.04

68

7175.09

15

1027.97

42

4211.99

69

7263 . 57

16

1127.60

43

4337.79

70

7348 . 64

17

1229.65

44

4463.39

71

7430.17

18

1333 . 82

45

4588.58

72

7507.86

19

1440.15

46

4713.47

73

7581.28

20

1548.41

47

4837 . 81

74

7650.15

21

1658.42

48

4961.64

75

7713.88

22

1770.16

49

5084 . 82

76

7771.96

23

1883.50

50

5208.29

77

7823 . 50

24

1998.36

51

5328.90

78

7867.26

25

2114.53

52

5449.61

79

7901.24

26

2232.01

53

5569.36

80

7920.00

27

2350.64

54

5687.99

Dome capacity 6.00 gallons per inch.

Outage Table for Standard 8,050 Gallons Capacity Car Tank.

Table for gauging tanks by the inch. Capacity in U. S. gallons of a
78" diameter tank. Official dome capacity, including dish in head, 243
gallons. Length of tank, 31' 10 14".

Inches Gallons Inches Gallons Inches Gallons

1

2

3

4

5

6

7

8

9

10

U

12

13

14

15

16

17

18

19

20

21

22

23

24

25

26

Dome

23.18

27

54.59

28

100.65

29

153 87

30

215 71

31

282.54

32

;J55.29

33

431 29

34

511.91

35

596 41

36

681.52

37

775.44

38

870.74

39

968 .59

40

1069.73

41

1172.93

42

1278 57

43

1385 70

44

1497.69

45

1611 06

46

1725.65

47

1841 72

48

1960 51

49

2080 01

50

2201 24

51

2323 93

62

capacity is

11.532

2447.86
2573.08
2699.27
2826 . 66
2954 . 68
3083.27
3212.28
3341.94
3472.16
3603.20
3735.00
3867.38
4000.38
4133.38
4265.76
4397 . 56
4528.60
4658.82
4788.48
4917.49
5046.08
5174.10
5301.49
5427.68
5552.90
5676.83

53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
73
74
75
76
77
78

5799.53
5920 . 70
6040.30
6159.02
6275.09
6389.68
6503.05
6615.04
6722 . 17
6826.81
6929.01
7030.15
7129.00
7223 . 34
7314.39
7402.87
7487.97
7569.50
7646 82
7721.31
7789.58
7854.54
7911.72
7962.83
8000.71
8033 . 10

11.532 gallons per inch.

KANSAS CITY TESTING LABORATORY

179

TANK CAR OUTAGE TABLES (Continued)

Outage Table for Cars Nos. EIRX-3101 to 3150, inclusive, and
3180 to 3i98, inclusive, of Empire Refineries, Inc. Table for gauging
S.OfiO gallons capacity Car Tank by the half inch. Capacity in U. S.
gallons of a 77" diameter tank. Length of tank 31' 8". Official dome
capacity, including dish head, 274 5 gallons.

Inches

Gallon

.>2

8

1

20

H

38

2

57

'A

80

3

104

'A

131

4

159

A

189

5

221

A

255

6

290

A

326

7

364

A

403

8

443

A

484

9

526

A

569

10

614

A

659

11

706

'^

753

1 foot

801

A

849

1

899

A

949

2

1000

A

1052

3

1105

A

1158

4

1212

A

1266

5

1321

A

1376

6

1433

A

1490

7

1547

A

1605

8

1663

A

1721

9

1780

A

1840

10

1900

A

1960

11

2021

A

2082

2 feet

2144

A.

2206

1

2268

A

2330

Inches

Gallons

3-2

2456

3

2520

A.

2584

4

2648

A.

2712

5

2776

Ai

2840

6

2905

A

2970

7

3036

A.

3102

8

3168

Yi

3234

9

3300

A

3366

10

3432

A.

3498

11

3564

A

3630

3 feet

3696

A.

3762

1

3829

A.

3896

2

3963

I.',

4030 (1

3 ■

4097

Yj.

4164

4

4231

A

4298

5

4364

A.

4430

6

4496

Vi

4562

7

4628

A.

4694

8

4760

A.

4826

9

4892

A.

4958

10

5024

Yi

5090

11

5155

H

5220

4 feet

5284

Yi

5476

Yi

5348

1

5412

2

5540

Y%

5604

3

5667

4K

5730

Inches

car)

Gallons

M

5854

5^

5916

Yz

5978

6

6039

Y^

6100

7

6160

Yi

6220

8

6280

I /

72

6339

9

6397

Yi

6455

10

6513

Yi

6570

11

6627

Yi

6684

5 feet

6739

Vi

6794

1

6848

Yi

6902

2

6955

Yi

7008

3

7060

Yi

7111

4

7161

Yi

7211

5

7259

Yi

7307

6

7354

Yi

7401

7

7446

Yi

7491

8

7534

Yi

7576

9

7617

Yi

7657

10

7696

Yi

7734

11

7770

Yi

7805

6 feet

7839

'9

7871

1

7901

Yi

7929

2

7956

Yi

8022

Yi

7980

3

8003

4H

8040

Vi

8052

5

8060

Dome Capacity is 11.5 gallons per inch.

180 BULLETIN NUMBER SIXTEEN OF

TANK CAR OUTAGE TABLES (Continued)

Outage Table for Cars Nos. EIRX-2000 to 2016, inclusive, and
2018 to 2C34, inclusive, of Empire Refineries, Inc. Table for gauging
8090 gallons capacitv car tank by the half inch. Capacity in U. S.
gallons of an 83" diameter tank. Length of tank 28' 2". Official
dome capacity, including dish head, 158 gallons.

Inchts

Gallons

Inches

Gallons

Inches

Gallons

4

2397

8

5809

M

7

V2

2456

A

5866

1

18

5

2516

9

5923

'A

33

A

2576

A

5980

2

51

6

2636

10

6037

H

70

V"

2696

A

6094

3

92

7 '

2756

11

6150

Vt.

117

A

2816

A

6206

4

143

8

2876

Vi

170

A

2936

5 feet

6262

5

198

9

2997

A

6318

H

229

A

3058

1

6374

6

261

10

3119

A

6428

Vi

294

A

3180

2

6482

1

326

11

3241

A

6533

Vi

363

A

3302

3

6588

8

399

A.

6641

'A

435

3 feet

3363

4

6693

9

473

A

3424

A

6745

Vi

513

1

3486

5

6797

10

554

A

3548

Yi

6848

,,^

596

2

3610

6

6898

11

636

A

3672

Yi

6948

'A

678

3

3734

7

6998

1 foot

721

A

3796

Yi

7046

H

765

4

3858

8

7094

1

809

A

3920

Yi

7142

A

854

5

3982

9

7189

2

900

A

4045 {A car)

H

7235

Q*^

947

6

4108

10

7280

3

995

A

4170

Y2

7324

A

104:J

1

4232

11

7368

4

1091
1141

A
8

4294
4356

Yi

7411

5

6^

1191
1241
1292

A
9
A

4418
4480
4542

6 feet

Yi
1

7453
7495
7537

7^

/^

A
9

n^

A

1344
l.'J96
1448
1501
1554
1607
1661
1715
1771
1827
1883

10

11^
A

4 feet

A

1

2^
A

4604
4666
4727
4788

4849
4910
4971
5032
5093
5154

Yi
2

Yi
3

Yi
4

Yi
5

6^^

Yi

7578
7617
7655
7691
7727
7762
7796
7829
7861
7892
7920

3

5214

7

7947

2 feet

A
2

1939
1995
2052
2109
2166

A
4

5

A
6

J^
7

5274
5334
5394
5454
5514

8

9^
Yi

7973
7998
8020
8039
8057

3^

2223
2280

5574
5634
5693

10

Yi
11

8072
8083
8090

Dome Capacity, 6.582 gallons per inch.

KANSAS CITY TESTING LABORATORY

181

TANK CAR OUTAGE TABLES (Concluded).
Outage Table for Standard 10,050 Gallons Capacity Car Tank,

Table for gauging- tanks by tlie inch. Capacity in U. S. gallons of an

i>7%" diameter tank (with Nteain

eluding dish in head, 326 gallons.

Inches
1
2

a

4

5

6

7

8

9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30

Gallons
20.02
55.90

102.61

160.73

225.73

300 . 02

379.20 I

461.47 '

548.31

637 . 56

739.72

826.80

929 21 J
1034.44
1141.50
1252.09
1366.70
1483.62
1602.46
1723.04
1846.79
1973.75 *
2101 74
2230 . 82
2361.19
2492.21
2626.10
2762.09 ^
2898.32
3034.76

Inches
31

I

r _v

32
33
34

35
36
37
38
39
40
41

1 42
43

f 44
45
46
47
48
49
50
51
52
53
54
55
56
57
It 58
59
60

coils). Official dome capacity,
Length of tank 31' 61^".

Gallons

3172.20

3310.90

3449.61

3589.91

3731.11

3873.26

4016.67

4161.06

4305.62

4450.47

4596.08

4741.74

4887.77

5033 . 84

5180.28

2326.35

5471.99

5617.23

5762.39

5906.98
E \ 6050.86

6194.57

6336 . 64
: ^l 6478.51

6619 . 66

6760.43

6900 . 32
I P 7039.31

7175.36

7311.17

Inches

Gallons

61

7445.20

62

7578.94

63

7711.09

64

7841.63

65

7970.41

66

8096 . 54

67

8220 . 57

68

8342.93

69

8462.40

70

8580.25

71

8695.02

72

8806.73

73

8915.39

74

9023.22

75

9125.44

76

9224.51

77

9329.18

78

9412.58

79

9501.30

80

9586.34

81

9664.76

82

9741.15

83

9809.25

84

9871.97

85

9926.75

86

9972.59

87

10006.52

SIH

10019.99

Dome capacity is 11.532 gallons per inch.

Outage

Table for
an 871/2" d
326 gallon

Inches

1

2

3

4

5

6

7

8

9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
Dome

Table for Standard 10

gauging tanks by the
iameter tank. Official d
s. Length of tank, 31'

Gallons Inches

20.02 31

55.90 32

102 . 60 33

160.73 34

225.73 35

300.02 36

379.20 37
461.47 38
548.31 39
637 . 56 40
729.72 41
826 . 80 42

929.21 43
1034.44 44
1141.50 45

1252.09 46
1366.70 47
1483.62 48
1602.46 49
1723.04 50
1846.79 51

1973.75 52
2101.74 53
2230 . 82 54
2361.19 55
2492.21 56

2626 . 10 57
2762.08 58
2898 . 32 59

3035.76 60
capacity is 11.532 gallon

,050 Gallons

inch. Capaci
ome capacity,
61/4".

Gallons

3174.20

3313.20

3453.61

3594.91

3737.11

3880.26

4024 . 67

4170.06

4315.62

4461.47

4608.08

4754.74

4901.77

5048.84

5196.28

5348.35

5489.99

5636,23

5782.39

5927 . 98

6072.86

6217.57

6360 . 64

6503.51

6645.66

6787.43

6928.32

7068.31

7205.36

7342.17
s per inch.

Capacity Car Tank.

ty in U. S. gallons of
including dish in head,

Inches
61
62
63
64
65
66
67
68
69
70
71
72
73
74
75
76
77
78
79
80
81
82
83
84
85
86
87
8TA

Gallons
7477.20
7611.94
7744.09
7874.63
8003.41
8129.54
8253 . 57
8375.93
8495.40
8613.25
8728.02
8839.73
8948.39
9056,22
9158.44
9257,51
9353,18
9445,58
9534,30
9619.34
9697.76
9774,15
9842,25
9904 , 97
9959,75
10005 59
10039,52
10052.99

182

BULLETIN NUMBER SIXTEEN OF

CYLINDRICAL VESSELS, TANKS AND CISTERNS.

Diameter in Ft. and Ins., Area in Sq. Ft. and Capacity in U. S.

Gals, for 1 Ft. in Depth.

(1 gallon=231 cubic inches = 1 cubic foot/7.4805 = 0.13368 cubic foot.)

Diam-

Area,

Gallons,

Diam-

Area,

Gallons,

Diam-

Area,

Gallons,

eter.

Square

1 Foot

eter,

Square

1 Foot

eter,

Square

1 Foot

Ft.

In.

Feet

Depth

Ft.

In.

Feet

Depth

Ft.

In.

Feet

Depth

0

.785

5.87

5

8

25.22

188.66

19

0

283.53

2120.9

1

.922

6.89

5

9

25.97

194.25

19

3

291.04

2177.1

2

1.069

8.00

5

10

26.73

199.92

19

6

298.65

2234.0

3

1.227

9.18

5

11

27.49

205.67

19

9

306.35

2291.7

4

1.396

10.44

6

0

28.27

211.51

20

0

314.16

2350.1

5

1.567

11.79

6

3

30.68

229.50

20

3

.322.06

2409.2

6

1.767

13.22

6

6

33.18

248.23

20

6

330.06

2469.1

7

1.969

14.73

6

9

35.78

267.69

20

9

338.16

2529.6

8

2.182

16.32

7

0

38.48

287.88

21

0

346.36

2591.0

9

2.405

17.99

7

3

41.28

308.81

21

3

354.66

2653.0

10

2.640

19.75

7

6

44.18

330.48

21

6

363.05

2715.8

11

2.885

21.58

7

9

47.17

352.88

21

9

371.54

2779.3

2

0

3.142

23.50

8

0

50.27

376.01

22

0

380.13

2843.6

2

1

3.409

25.50

8

3

53.46

399.88

22

3

388.82

2908.6

2

2

3.687

27.58

8

6

56.75

424.48

22

6

397.61

2974.3

2

3

3.976

29.74

8

9

60.13

449.82

22

9

406.49

3040.8

2

4

4.276

31.99

9

0

63.62

475.89

23

0

415.48

3108.0

2

5

4.587

34.31

9

3

67.20

502.70

23

3

424.56

3175.9

2

6

4.909

36.72

9

6

70.88

530.24

23

6

433.74

3244.6

2

7

5.241

39.21

9

9

74.66

558.51

23

9

443.01

3314.0

2

8

5.585

41.78

10

0

78.54

587.52

24

0

452.39

3384.1

2

9

5.940

44.43

10

3

82.52

617.26

24

3

461.86

3455.0

2

10

6.305

47.16

10

6

86.59

647.74

24

6

471.44

3526.6

2

11

6.681

49.98

10

9

90.76

678.95

24

9

481.11

3598.9

3

0

7.069

52.88

11

0

95.03

710.90

25

0

490.87

3672.0

3

1

7.467

55.86

11

3

99.40

743.58

25

3

500.74

3745.8

3

2

7.876

58.92

11

6

103.87

776.99

25

6

510.71

3820.3

3

3

8.296

62.06

11

9

108.43

811.14

25

9

520.77

3895.6

3

4

8.727

65.28

12

0

113.10

846.03

26

0

530.93

3971.6

3

5

9.168

68.58

12

3

177.86

881.65

26

3

541.19

4048.4

3

6

9.621

71.97

12

6

122.72

918.00

26

6

551.55

4125.9

3

7

10.085

75.44

12

9

127.68

955.09

26

9

562.00

4204.1

3

8

10.559

78.99

13

0

132.73

992.91

27

0

572.56

4283.0

3

9

11.045

82.62

13

3

137.89

1031.5

27

3

583.21

4362.7

3

10

11.541

86.33

13

6

143.14

1070.8

27

6

593.96

4443.1

3

11

12.048

90.13

13

9

148.49

1110.8

27

9

604.81

4524.3

0

12.566

94.00

14

0

153.94

1151.5

28

0

615.75

4606.2

1

13.095

97.96

14

3

159.48

1193.0

28

3

626.80

4688.8

2

13.635

102.00

14

6

165.13

1235.3

28

6

637.94

4772.1

3

14.186

106.12

14

9

170.87

1278.2

28

9

649.18

4856.2

1

5

14.748

110.32

15

0

176.71

1321.9

29

0

660.52

4941.0

15.321

114.61

15

3

182.65

1366.4

29

3

671.96

5026.6

fi

7
H
9
10
11
0
1
2
■3
4
6
6
7

15.90

118.97

15

6

188.69

1411.5

29

6

683.49

5112.9

16.50

123.42

15

9

194.83

1457.4

29

9

695.13

5199.9

17.10

127.95

16

0

201.06

1504.1

30

0

706.86

5287.7

17.72

132.56

16

3

207.39

1551.4

30

3

718.69

5376.2

18.35

137.25

16

6

213.82

1599.5

30

6

730.62

5465.4

5
5
6
6
5
6
6
6

18.99
19.63
20.29
20.97
21.65
22.34
23.04
23.76
24.48

142.02
146.88

16

17

9
0

220.35
226.98

1648.4
1697.9

30
31

9
0

742.64

754.77

5555.4
5646 1

151.82
1.56.83
161.93
167.12
172.38
177.72
183.16

17
17
17
18
18
18
18

3
6
9
0
3
6
9

233.71
240.53
247.45
254.47
261.59
268.80
276.12

1748.2
1799.3
1851.1
1903.6
1956.8
2010.8
2065.5

31
31
31
32
32
32
32

3
6
9
0
3
6
9

766.99
779.31
791.73
804.25
816.86
829.58
842.39

5737.5
5829.7
5922.6
6016.2
6110.6
6205.7
6301.5

KANSAS CITY TESTING LABORATORY 18[

GAUGING TABLE FOR STANDARD 50-GALLON OIL BARREL.

Depth of Fluid, Laying on Side, Standing on End,

Inches Gallons Gallons

1 0.27 1.35

2 1.15 2.74

3 2.64 4.20

4 4 . 50 5 . 72

5 6.63 7.29

6

8.93

8.91

7

11.50

10.59

8

14.16

12.31

9

16.90

14.08

10

19.70

15.90

11

22.56

17.76

12

25.49

19.65

13

28.42

21.58

14

31.28

23.53

15

34.08

25.49

16

36.82

27.45

17

39.48

29.40

18

42.00

31.33

19

44.35

33.22

20

46.48

35.08

21 48.34 36.90

22 49 . 83 38 . 67

23 50 . 71 . • 40.39

24 50.98 42.07

25

43.69

26

45.26

27

46.78

28

48.24

29

49.63

30

50.98

184

BULLETIN NUMBER SIXTEEN OF

CHEMICAL CONSTITUTION OF PETROLEUM.

Petroleum is composed of carbon and hydrogen in chemical com-
bination known as hydrocarbons. In conjunction with the carbon and
hydrogen there frequently is oxygen, nitrogen and sulphur in much
smaller amounts.

In crude oils the amount of carbon varies from 80 to 89%, the
hydrogen from 10 to l^'/c , oxygen from 0 0 to 5.07<^, nitrogen from
0.0 to 1.89'f, and sulphur from .01 to 5.0%.

Typical ultimate analyses of petroleum products are as follows:

Carbon Hydrogen Sulphur Nitrogen Oxygen

Pennsylvania Crude 86.06% 13.88% 0.06% 0.00% 0.00%

TexasCrude 85.05 12.30 1.75 0.70 0.00

California Crude 84.00 12.70 0.75 1.70 1.20

Mexican Crude 83.70 10.20 4,15

Oklahoma Crude 85.70 13.11 0.40 0.30

Kansas Crude (Towanda) 84.15 13.00 1.90 0.45

Kansas Residuum 85.51 11.88 0.71 0.32 0.63

Healdton (Oklahoma) Crude 85.00 12.90 0.76

Kansas Air Blown Residuum 84.37 10.39 0.42 0.21 4.61

Byerlite Pitch 87.61 9.97 0.55 0.29 1.58

Grahamite 87.20 7.50 2.00 0.20

Trinidad Asphalt 82.60 10.50 6.50 0.50

Commercial Gasoline 84.27 15.73 0.00 0 00 0.00

Kerosene 84.74 15.26 0.01 0.00 0.00

Lubricating Oil (Paraffin) 85.13 14.87 0.01

Lubricating Oil (Naphthene) 87 . 49 12.51 0.01

Benzol 92.24 7.76 0 00 0.00 0 00

Paraffin (CnH2n+2) hydrocarbons largely compose the light or
more volatile constituents of all petroleum. They are "sat'jrated"
hydrocarbons and have a very low ratio of specific gravity to distilling
tempei'ature, are not acted upon by concentrated sulphuric acid or by
fuming sulphuric acid (oleum), are not nitrated by nitric acid and are
extremely resistant to all chemical reactions. The chief differences in
petroleum are in the heavy constituents, the heavy hydrocarbons of
th paraffin series being found chiefly in Pennsylvania and some Mid-
Continent oils.

Naphthenes (CnHon), ring or cyclic compounds, are less common
hydrocarbons in lighter portions of petroleum, but are commonly
found as heavy hydrocarbons of petroleum. Thev have a higher ratio
of specific gravity to distilling temperature than the paraffin com-
pounds, are resistant to the action of sulphuric acid and some types
may be distinguished by the "formolit" reaction.* Oils containing
light naphthenes are found in Russia and Louisiana. All heavy oils
contam naphthenes.

*Holde — Examination of Hydrocarbons.

Cnll.n (NAPHTHENES) POLYMETHYLENE SERIES.

Boiling
r. , Formula Temperature

Cyc opropane C, H^ — 35°C =— 31°F

Cyclohutane C4 Hg -M2°C = 54°F

Cyc opentane C5 H,„ 49°C = 120°F

Cycohexane Ce H,, srC = 178°F

M 1 ,T^^",^ • • • ; Cv Hm 117°C = 243°F

Methyl Cyclopentane Or, H,, 72°C = 162°F

mIT^ W-i^^;''uP^"*^"^-- C^Hm 9rC= 136°F

nitl fi Vr^->'"';'''u""^ C; H,., 98°C = 208°F

Tr.^ fK^iW''^''''"*'-- C.H,^ 118°C= 244°F

inmethyl Cyclohexane Ca H.s 198°C = 388°F

Gravity

.709
.769
.799^
.809:

.766:

.778:
.778:

.781 =

.787:

67.5° Be'
52.1° Be'
45.2'
43.1'
52.8'
50.0° Be'
50.0° Be'
49.3'
47.9'

Be'
Be'
Be'

Be'
Be'

KANSAS CITY TESTING LABORATORY 185

Aromatic or Benzene Hydrocarbons (Cn H211-6) exist to some
extent in certain California petroleums and have a very high ratio of
specific gravity to distilling temperature. Gasoline made from the
California petroleum is heavier than light gasoline with the same end
point made from Mid-Continent petroleum. The aromatic compounds
are acted upon by nitric acid forming nitro pi'oducts. They are
formed from paraffin and naphthene hydrocarbons by pyrogenic de-
composition at temperatures above 1000° F. The production of aro-
matic compounds from petroleum has not been commercially satisfac-
tory on account of incomplete conversion and difficulty of freeing
from paraffin hydrocarbons.

Olefines or Ethylenes (CnHon) are "unsaturated" hydrocarbons,
rarely if ever existing naturally in crude oil, but commonly resulting
from its exposure to high temperatures. These compounds contain
less hydrogen and more carbon than paraffin hydrocarbons and are
capable of taking in more hydrogen. They are removed from aromatic
compounds, paraffin compounds and naphthene compounds by the
action of concentrated sulphuric acid in the usual process of refining
gasoline. These hydrocarbons give gasoline, to a large extent, its dis-
agreeable odor before refining. Their combination with sulphur gives
a more intense odor. Each of these groups of hydrocarbons is sup-
posed to exist in a complete series, represented by the general formula
given. The paraffin or methane series of "saturated" hydrocarbons
has been fairly well worked out and is given in the table on page 186.

According to Hofer, the following olefines have been isolated from
"North American" petroleum:

Ethylene Co H4 Heptylene. . . .C7 Hu Dodecylene. . .C12 H24

Propylene C3 He Octylene Cg Hie Decatrilene. . . C13 H26

Butylene C4 Hg Nonylene C9 His Cetene C14 H28

Amylene C5 Hio Decylene Cio H20 Cerotene Cu H30

Hexylene Ce H12 Undecylene. . .Cn H22 Melene Cie H42

If the residue contains much wax, the crude is known as paraffin
base oil, but if naphthenes or similar hydrocarbons predominate, it is
an "asphalt" base oil. Practically the "asphalt" is determined by the
solubility of the solid hydrocarbons in pentane and by the gravity and
physical character of the residue. (See pages 501-2.)

Among the light hydrocarbons of petroleum, either existing nat-
urally or pyrogenically produced, the relation of the specific gravity
to the distilling temperature affords a simple and practical method
of estimating the amount of olefin, paraffin and aromatic compounds.
This relation is set forth in the curves on pages 232 and 2-36.

The value of crude oil is not measured by its ultimate analysis or
by its "base" so much as by the amount of volatile constituents which
it contains. The amount of volatile constituents obtained from various
crude oils is shown on pages 179 to 190.

186

BULLETIN NUMBER SIXTEEN OF

PARAFFIN HYDROCARBONS IN PETROLEUM.

GASEOUS HYDROCARBONS (Natural Gas)

Sp. Gr.
Baume' Liquid Melting

Name Gravity 15.5°C Formula Point

Molec-
Boiling ular
Point Weight

Methane

Ethane 194

Propane 142

Butane 109

0.432
0.525
0.585

C H4

C2 He

C.I Hs
C4 Hiu

— 184.0°C — 165.0°C 16.03
—171.4 — 93.0 30.05
—195.0 — 45.0 44.07
—135.0 + 1.0 58.08

"GASOLINE" HYDROCARBONS

Pentane 92.2

Hexane 78 . 9

Heptane 70.9

Octane 65.0

Nonane 59.2

Decane 56.7

Undecane 54 . 2

0.630
0.670
0.697
718
0.740
0.750
0.760

0

C5H,.:
Cf, Hi4
C? H16
Cg H18

C9 1X20

C11H24

—51.0

— 31.0

— 26.0

HEAVY LIQUID HYDROCARBONS (Kerosene)

Duodecane 51.8 0.770

Tridecane 46.8 0.792

Tetradecane . . . . 45.0 0.800

Pentadecane .... 43 . 5 0 . 807

Hexadecane 41.8 0.815

Heptadecane 40.3 0.822

Octadecane 38.6 0 . 830

C12H26

Cl,3H28
C14H30
C15H32
C K,H34
C17H36

CigHss

+

HEAVY SOLID HYDROCARBONS

Eicosane 37.2

Tricosane 36.5

Tetracosane

Pentacosane

Hexacosane

Mericyl

Octocosane

Nonocosane. . . .

Ceryl

Untriacontane

Duotriacontane

Tetratriacontane ....
Pentatriacontane 35.4

837
841

846

t 20H42
C23H48
C24H50
C20H52
C26H54

C2TH56
C28H58

C29H60
C30H62
C31H64
C32HCC
C34H70
C36H72

12.0
6.0
5.0
10.0
28.0
22.0
28.0

37.0
48.0
51.0
54.0
56.0
59.4
60.0
63.0
65.6
68.0
70.0
72.0
75.0

36.3
69.0
98.4
125.5
150.0
173.0
195.0

214.0
234.0
252.0
270.0
287.0
295.0
317.0

(vacuo)
117.5
138.0
145.5
152.5
160.0
167 0
173.5
179.0
186.0
193.5
201.0
215.0
222.0

72.10
86.12
100 . 13
114.15
128.16
142.18
156.20

170.22
184.24
198.25
212.26
226.27
240.28
254.30

282 . 34
325.38
338.39
352.41
366.43
370.45
384.47
398.48
422.49

436 . 52

450 . 53
478.56
492.58

RpriJnf L 1 "; ""^ petroleum composed exclusivelv of the paraffin
dlsh-ivn^r^^lf '''"';' !r" Pennsylvania and Garber, Oklahoma, crude
Ts m : U .H of n '''ffi^ °u^T '"""^ 'Th^ "^^i" b«dy of the light petroleum
made up o niphtaes ^^^'•^^^''^^^^ -"^ the heavy residues are largely

KANSAS CITY TESTING LABORATORY 187

NATURAL CONTENT OF CRUDE OILS.

(Typical samples, analyses by Kansas City Testing Laboratory^

Specific
Source Gravity

Arkansas — El Dorado 851

California — Heavy 984

Santa Maria 900

Kansas — Moran, Allen Co. . . .871

Neodesha (Wilson Co.) 860

Paola 873

Peabody 860

Sallyards (Butler Co.) 835

Towanda (Butler Co.) 850

Kentucky 876

Wayne Co 835

Louisiana, Homer 832

Pine Island 902

Mexico — Panuco 982

Tuxpan 935

Montana— Winnett 777

Bozeman (Big Horn Co. ) . .942
Oklahoma — Beggs 862

Billings 812

Bixby 845

Cushing 823

Duncan 857

Garber, Garfield Co 780

Healdton 920

Kingwood 829

Newkirk 822

Osage Co 836

Pennsylvania (light) 802

Russia .874

South Dakota— Mule Creek . .863
Texas — Beaumont 912

Breckenridge 811

Burkburnett 824

Mexia 842

Ranger 829

San Antonio . 861

Wortham 800

West Virginia— Cabin Creek . . 788
Wyoming — Big Muddy 860

Elk Basin 805

Ferris Dome 831

Grass Creek 801

Hamilton Dome 891

Lander Co 909

Lance Creek 815

Lost Soldier 865

Maverick Springs 918

Pilot Butte 836

Rock Creek 838

Salt Creek 838

Canada — Fort Norman 833

Baume'

Gravity

34.8°
12.3

Auto-
mobile
Gasoline
% by Vol.

30.0%
0.0

Naphtha

and
Kerosene
7c, by Vol.

20.0%
12.3

Fuel
Oil
Resi-
due

50.0%

82.7

25.7

20.0

20.0

60.0

30.7

15.0

17.5

67.5

33.3

25.0

17.0

58.0

30.6

20.5

19.5

60.0

33.3

20.0

20.0

60.0

38.0

30.0

22,5

47.5

34.7

20.5

27.5

52.0

42.0

40.0

20,0

40.0

37.7

28.0

21,0

51.0

38.6

30.0

25,0

45.0

25.4

0.0

25,0

75.0

12.8

2.0

8,0

90.0

19.8

15.0

15.0

70.0

50.6

55.0

40,0

5.0

18.7

2.5

17.5

80.0

32.7

15,0

21.8

63.2

42.8

40.0

22.5

37.5

36.0

25.0

20,0

55.0

40.1

35.0

15.0

50.0

33.7

20.0

22.5

57.5

49.5

55.0

15.8

29,2

22.1

8.5

17.5

74.0

39.2

30.0

20.0

50.0

40.3

32.5

24,0

43,5

37.7

25.0

20.0

55,0

44.5

37.5

12.7

49.8

30.2

15.0

20.0

65,0

32.5

2.5

27.5

70.0

23.4

4,0

16.0

80.0

42.0

35.0

25.0

40.0

40.1

41.0

20.0

39.0

36.6

5.0

50.0

45.0

39.2

30.0

25.0

45.0

32.8

15.0

21.5

63.5

45.5

37.5

35.0

27.5

48.0

36.0

24.0

40.0

33.0

10,0

25.0

65.0

44.3

45,0

20.0

35.0

38.8

30,0

20.0

50.0

45,1

45.0

20.0

35.0

27.3

17.5

15.0

67.5

24.0

13.0

13.0

74.0

42.1

32.5

27.5

40.0

33.8

0,0

35.0

65,0

22,6

0.0

25 0

75.0

37.7

20,0

35.0

45.0

37.4

30,0

15.0

55.0

37.3

25,0

20.0

55.0

38.0

30.0

32.0

38.0

188 BULLETIN NUMBER SIXTEEN OF

SULPHUR, ASPHALT, CYLINDER STOCK AND GASOLINE IN
IMPORTANT CRUDE PETROLEUMS.

The following tables give an index of the constitution of impor-
tant crude petroleums.

The values are chiefly from the reports of investigations of the
Bureau of Mines. The item marked "carbon residue" refers to the
carbon determined by the Conradson method on the residue from the
distillation. It is an approximate measure of the amount of asphalt in
the oil. Asphalt is a very broad term usually in practical testing com-
prising waxy material. Asphalt with good ductility and cementing
properties is obtainable from the petroleums of high carbon content.
Cylinder stock of good quality is obtainable from the oils of low carbon
and low sulphur content.

Source of Crude Gravity

New York —

Alleghany Co 828 =39.1° Be'

Pennsylvania —

McKean Co 823 =40.1 ° Be'

Venango Co 819 =40.9° Be'

Venango Co 832 =38.3° Be'

Franklin 863 =32.2° Be'

Alleghany and Washing-
ton Counties 800 =45.0° Be'

Green Co 815 =41.8° Be'

Composite 811 =42.6° Be'

West Virginia —

Maryland Pool 805 =43.9° Be'

Eureka Pool 806 =43.7° Be'

Cabin Creek 797 =45.7° Be'

Kelly Creek 799 =45.2° Be'

Ohio (East)—

Washington Co 805 =43.9° Be'

Corning 838 =37.1° Be'

North Lima 835 =37.7° Be'

Oklahoma —

Big Heart 846 =35.5° Be'

Gushing 828 =39.1° Be'

Kentucky —

Ross Creek 838 =37.1° Be'

Cow Creek 866 =31.7° Be'

Big Sinking 844 =35.9° Be'

Compton Pool 842 =36.3° Be'

Wayne Co 869 =31.1° Be'

f^K'and 902 =25.2° Be'

'"'""'■''• 863 =32.2° Be'

Indiana

Lima Pool 846 =35.5° Be'

(Colorado —

Florence 880 =29.1° Be'

Kangely gjg =40.90 gg-

KanHttH —

/^"K""tV .865 =31.9° Be'

SallyardH... .836 =37.8° Be'

f'alifornia

Sunjietlii-Id .878 =29.5° Be'

Moxiro —

''■""''" .982 =12.6° Be'

T^""!""' .935 =19.8° Be'

Gasoline
to 392° F

Carbon
Residue

Sul-
phur

30.07c =57.2° Be'

2.9%

0.109;

32.5

29.6

24.4

9.0

= 59.4° Be'
= 57.7° Be'
= 54.0° Be'
= 39.9° Be'

2.6
2.1
2.0
2.2

0.10
0.10
0.08
0.09

37.8
29.0
33.9

= 61.0° Be'
= 57.9° Be'
= 60.7° Be'

1.6
1.6
3.2

0.08
0.08
0.08

38.3
37.7
40.5
39.6

= 60.7° Be'
= 60.7° Be'
= 61.8° Be'
= 61.5° Be'

2.1

2.4
1.2

0.28
0.24
0.19
0.11

33.5

27.8

= 59.4° Be'
= 59.2° Be'

3.1
7.4

0.05
0.10

31.0

= 56.9° Be'

6.2

0.55

28.0
37.5

= 55.7° Be'
= 58.4° Be'

5.3
6.8

0.19
0.12

35.9
19.7
31.2
30.8
35.9
12.6

= 58.2° Be'
= 51.6° Be'
= 56.4° Be'
= 57.4° Be'
= 56.4° Be'
= 52.5° Be'

8.4
6.5
7.5
5.3
6.4
17.7

0.12
0.13
0.14
0.23
0.49
0.31

20.4

= 52.1° Be'

10.6

0.24

26.0

= 55.9° Be'

6.0

0.48

8.9
34.6

= 54.7° Be'
= 57.2° Be'

6.0
2.6

0.17
0.06

24.2
30.0

= 54.0° Be'
= 61.0° Be'

10.2
6.0

0.41
0.40

21.5

= 47.4° Be'

16.4

0.73

6.0
11.0

= 51.0° Be'
= 60.0° Be'

23.0
19.0

5.34

KANSAS CITY TESTING LABORATORY

189

SULPHUR. ASPHALT, CYLINDER STOCK AND GASOLINE IN
IMPORTANT CRUDE PETROLEUMS— (Continued).

Source of Crude (

Montana — •

Winnett 781 =

Wyoming^

Hamilton Dome 903 =

Shannon 909 =

Newcastle 840 =

Salt Creek 841 =

Rock Creek 843 =

Lost Soldier 875 =

Mule Creek 867 =

Big Muddy 863 =

Ferris 842 =

Warm Spring 987 =

Lander 913 =

Dallas 914 =

Pilot Butte 848 =

Maverick Springs 922 =

Plunkett 846 =

Greybull 803 =

Grass Creek 809 =

Elk Basin 827 =

Osage 837 =

Lance Creek 823 =

Missouri —

Kansas City 874 =

Texas —

Burkburnett 821 =

Ranger 829 =

Mexia 842 =

Wortham (Currie) .800 =

Groesbeck 839 =

Gasoline

Carbon

Sul-

ravity

to 892° F

Residue

Piur

49.3° Be'

63.2

= 57.4° Be'

trace

0.36

25.0° Be'

17.6

= 57.7° Be'

19.0

2.09

24.0° Be'

3.1

= 37.1° Be'

5.1

0.20

36.7° Be'

31.6

= 55.7° Be'

7.5

0.15

36.5° Be'

29.3

= 56.7° Be'

6.1

0.18

36.1° Be'

31.4

= 58.2° Be'

6.8

0.27

30.0° Be'

16.7

= 44.1° Be'

6.5

0.11

31.5° Be'

11.7

= 52.3° Be'

4.8

0.14

32.2° Be'

22.2

= 53.7° Be'

6.0

0.17

36.3° Be'

31.1

= 57.4° Be'

5.5

0.19

11.8° Be'

5.4

=49.9° Be'

21.2

2.61

23.3° Be'

11.0

= 55.4° Be'

15.1

2.62

23.2° Be'

12.8

= 51.3° Be'

18.9

2.42

35.1° Be'

24.0

= 53.0° Be'

5.5

0.22

21.8° Be'

8.6

= 53.0° Be'

17.9

2.46

35.5° Be'

21.0

• =49.7° Be'

2.1

0.55

44.3° Be'

38.6

= 59.7° Be'

2.3

0.08

43.1° Be'

42.6

= 58.9° Be'

4.6

0.14

39.3° Be'

40.5

= 57.2° Be'

5.3

0.14

37.3° Be'

34.8

= 57.7° Be'

5.2

0.29

40.1° Be'

33.5

= 55.7° Be'

2.0

0.18

30.2° Be'

16.0

= 52.0° Be'

4.3

0.45

40.9° Be'

37.5

= 60.5° Be'

6.5

39.2° Be'

30.0

= 57.4° Be'

2.2

o.ib

36.6° Be'

12.0

= 53.2° Be'

2.4

0.23

45.5° Be'

32.0

= 60.8° Be'

1.8

0.08

37.2° Be'

17.5

= 56.6° Be'

3.5

0.30

COLOR OF CRUDE OILS.

Gravity Color

Cabin Creek, W. Va 48.0° Be' 48

Lander, Wyo 43.4° Be' 100

Stevens Co., Tex 42.0° Be' 150

Grass Creek, Wyo 45.1° Be' 570

Elk Basin, Wyo 44.3° Be' 670

Ranger, Tex 39.2° Be' 1,100

Lance Creek, Wyo 42.1° Be' 1,270

Bull Bayou, La 38.0° Be' 1.350

Winnett, Mont 50.6° Be' 1.350

Garber, Okla 49.5° Be' 1.670

Ferris Dome, Wyo 38.8° Be' 2,250

Homer, La 38.6° Be' 3,020

Pilot Butte, Wyo 37.7° Be' 3,200

Caddo, La 3,900

Big Muddy, Wyo 33.0° Be' 4,745

Salt Creek, Wyo

Lost Soldier, Wyo

Healdton, Okla

Rock Creek, Wyo

Edgemont, S. D

Mexia, Tex

Burkburnett, Tex

pine Island, La

Moran, Kas

Maverick Springs, Wyo-
Hamilton Dome, Wyo . .

Tuxpan, Mexico

Panuco, Mexico

Soap Creek, Mont

Gravity

Color

37.3° Be'

5,100

33.8° Be'

5,100

22.1° Be'

5,420

37.4° Be'

6,550

32.5° Be'

6,730

36.6° Be'

7,285

40.1° Be'

9,000

25.4° Be'

10,200

29.7° Be'

13,000

22.6° Be'

39,400

27.3° Be'

47,750

19.8° Be'

68,000

12.8° Be'

156,000

18.2° Be'

51,000

See page 427 for method of determining color.

190

BULLETIN NUMBER SIXTEEN OF

Regional Character of Crude Oils
Fraction Distilling from 250°

New York and Pennsylvania .

West Virginia

Eastern Ohio

Western Ohio

Kentucky

Indiana

Illinois

Kansas

Oklahoma

Wyoming

California

as Shown by the Gravity of the
C.-275° C. (482° F.-527° P.).

Saybolt Viscosity

at 100° F.

Gravity

(Vacuum Distilled

0.813 =42.2° Be'

111

0.809 =43.1° Be'

110

0.813=42.2° Be'

129

0.826 =39.5° Be'

143

0.836 =37.5° Be'

151

0.826 =39.5° Be'

140

0.845=35.7° Be'

148

0.843 =36.1° Be'

153

0.840=36.7° Be'

170

0.836 =37.5° Be'

130

0.878=29.5° Be'

470

PROPERTIES USEFUL IN THE DISTILLATION OF IMPORTANT

CRUDE PETROLEUMS.

SOURCE
OF CRUDE

El Dorado, Arkansas 851

Winnett, Montana 777

Homer, Louisiana 832

Pine Island, Ix)uisiana. . . .902

Sallyards, Kansas 836

Cushing, Oklahoma 824

Moran, Kansas 877

Garber, Oklahoma 780

Kingwood, Oklahoma 829

Billings, Oklahoma 812

Bixby, Oklahoma 845

Bristow, Oklahoma 824

Burkburnett, Texas 821

Ranger. Texas 829

Worlham, Texas 800

Oroesberk, Texas 839

Mexia, Texas 842

Big Muddy, Wyoming. . . .860

Osage, Wyoming 819

I.ana' C;r«'ek, Wyoming 815

Salt Creek, Wyoming 838

Crass Cre<'k, Wyoming 801

Elk Basin, Wyoming 805

KerrJH Dome, Wyoming.. . .831
Ixwt Soldier, Wyoming. . . .864
Rork Cre«'k, Wyoming. . . .838

IjaniU-r, Wyoming 809

Tuxpan, Mexico 934

I'anuco, Mexico , .982

34.
50.
38.
25.
37.
40.
29.
49.
39.
42.
36.
40.
40.
39.
45.
37.
36.
33.
41.
42.
37.
45.
44.
38.
33.
37.
43.
20.
12.

140°
180°

98°
365°

84°
120°
180°
110°
140°
116°
121°
100°
121°
154°
100°
130°
220°
165°
110
170°
119
110°

88

94°
172

96°

95°
135

E

U5

212°

235°

194°

471°

179°

179°

342°

165°

220°

191°

213°

183°

197°

239°

237°

293

314°

210°

186°

216°

218

178

170°

192°

282°

194

187°

184

U5

73.

68.

80.

37.

78.

75.

56.

81.

68.

76.

72.

78.

74.

69,

75.

62.

55

61

75

70

71

74

78

75

53

76

76

67

30.0
65.0
30 °0
2.0
31.3
37.5
13.3
57.5
30.5
42.0
25.1
39.5
40.0

31
37
20
15
20
33
33
27
44
45
28.5
18.7
28.7
37.3
15.0
8.3

06§

Wt1>

5°
8°
2°
0°
8°
9°
5°
4°
1°
7°
6°
3°
5°
0°
4°
9°
,2°
,0°
,2°
.8°
.7°
.1
.1°
.2°
.4
.8°
.5°
.2

S5Q

462 °F
412° F
473° F

14.
33.
33.
26.
47.
48
32,

0
30
38
14

2

■ m

454

437°

300

425

410

450° F

410° F

455

437

385

448

365

350°

410°

410°

392°

454° F

390° F

441°

426° F
420° F
395° F

s°

35.6°

38.5°

41°1.

28.5°

35.8°

37.0°

36.8°

34.0°

38.4°

36.9°

37.3

35.4°

36.7°

37.0°

41.5°

39.0°

39.6

36.0

36.6°

38.6°

37.6

36.2°

36.0°

38.0°

32.4'

37.0°

36.6°

36.0'

^!

50.0
93.9
44.8
25.5
53.0
58.8
36.6
75.0
50.0
62.5
45.0
62.5
62.4
58.0
71.0
54.0
50.0
38.0
55.0
57.5
51.2
65.0
65.0
49.5
40.0
46.0
60.0
32.5

KANSAS CITY TESTING LABORATORY 191

Typical Refinery Practice.

There is much variation in the practice of petroleum distillation
in different refineries. This depends to a large extent upon the
character of the crude oil used, the market to which the refiner sells
^nd the ability of the refiner as to knowledge and equipment.

The following outlines the progressive distillation and treatment
of crude oil in a typical refinery: (See figures 23 and 24).

Crude Benzine (Gasoline and Naphtha) includes all of the light
distillate which vaporizes up to 410° F. In the ordinary Mid-Continent
or Texas petroleum, 420 °F indicates a gravity of the stream of dis-
tillate from the condenser in the receiving house of 46.5° Be' to
47.0° Be'. The gravity of the total distillate at this point varies with
different types of crude. In some crudes this will be as high as 64.0°
gravity, in others as low as 50°. For example, Burkburnett crude
distilled up to 410°F has a gravity of 59.7° Be' of the total benzine
and a stream gravity of 46.5° Be'; Bixby, Okla., crude benzine at
410°F has a gravity of 58 0° Be' and a stream gravity of 46.7° Be';
Cushing, Okla., crude benzine at 410 °F has a gravity of 59.7° and
a stream gravity of 47.0° Be'; Billings, Okla., crude gives a gravity
of 60° Be' at 410°F and a stream gravity of 46.5° Be'; Ranger, Tex.,
crude oil gives a benzine gravity at 410 °F of 56.6° Be' and a stream
gravity of 46.7° Be'. The gravity of crude benzine depends upon the
initial boiling point of the crude, the relative proportion of the dif-
ferent paraffin constituents and the chemical series of hydrocarbons
to which the crude belongs. (See page 236.)

The crude benzine is run off with direct fire under the still, though
after a temperature of 220 °F is reached some open steam may be
put in. The steam decidedly sweetens the product and brings over
the benzine at a lower temperature. In the use of steam, the dis-
tillation must be entirely governed by the gravity of the stream in the
receiving house and not by temperatures. In cases where the crude
is of good quality, it is not necessary to treat the benzine as it may
merely be redistilled with steam coils. In many cases the refiner
puts a good dephlegmator over on his crude still and makes a market-
able gasoline without either treating it with acid or redistilling it with
steam.

When a high sulphur or low grade petroleum is treated, the dis-
tillate is put into an agitator with sulphuric acid, the mixing being
perfected by blowing air through the acid in the bottom of the agi-
tator, thus contacting it with all portions of the benzine. The acid
is drained out and the benzine washed with water. Caustic soda or
"doctor" solution is added to neutralize the acid and the benzine is
thoroughly washed to remove the last traces of caustic or sulfonates.
The benzine is redistilled in a steam still to give a gasoline of 58 to
60 gravity and about 430 end point, this depending largely upon the
perfection of the dephlegmator. The last portion of the distillate is
naphtha if a gasoline of high Baume' is desired. High gravity crudes
are blended with low gravity crudes to eliminate the naphtha fraction.

Kerosene or Water White Distillate comes over just after the
crude benzine, with the gravity of the stream in the receiving house

192

BULLETIN NUMBER SIXTEEN OF

r^oM cfiuc

WAX
DISTILLPlTC

firrRiocf((\7\(iri

PR ESS CO
OlSTlLLf\T£.

OIL

o ntrcRs

Fie- 23— ri(.w Sheet for Complete Petroleum Refinery.

KANSAS CITY TESTING LABORATORY 193

at about 37.0° and a vapor temperature of 572° F. This will give
a kerosene ordinarily of a 41° gravity, but this again varies greatly
with the type of the oil. For example, a certain Wyoming crude
oil under these conditions gives a 31.0° kerosene, whereas Gushing,
Okla. and Bixby, Okla., crude oils give a 41.0° to 42.0° gravity kero-
sene. Pine Island cracked oil gives a 33-34° Be' kerosene and
Wortham, Tex., light crude gives a 46° Be' gravity kerosene. In
distilling kerosene from the crude it is desirable to stop before there
is discoloration from decomposition or cracking. Cracking may be
very largely prevented and kerosene very greatly sweetened by us-
ing open steam throughout the entire distillation. The water white
distillate or first run kerosene is now treated with acid and caustic
in the agitator and exposed to heat, air and light in a shallow tank
or bleacher in which all water is settled out. If the kerosene after
treatment is not water white or has too high an end point, it may be
redistilled with superheated open steam. The residue in the still
may be mixed with the solar oil.

Solar Oil or Distillate Oil is taken out immediately following
the kerosene, being a crude distillate not subjected to refining and
sold for use in explosion engines, as a high grade special fuel oil
or for cracking stock. The making of this product depends upon
the market. It may be about a 36 gravity product or it may be
combined with gas oil or straw oil.

Gas Oil is taken immediately following the distillate oil or kero-
sene and its distillation is continued until the residuum in the still
has a gravity of 23 to 26° Be'. It is distinctly a destructive distilla-
tion and the yield depends largely upon the method and rate of fir-
ing. Gas oil is used in making gas and contains a considerable
amount of olefins and cracked products, and is not refined except for
special purposes. It is also used as cracking stock. By the Burton
process or the Cross process, gas oil commercially yields 60 to 65
per cent of gasoline. If a gas oil fraction low in olefins (straw oil)
is desired, it is necessary to distill using open steam and direct fire.
Straight firing gives a more fluid residue on account of cracking.

Residuum or tar is sold as fuel oil or it may be used to produce
lubricating oil. In the latter case, it may be put into tar or tower
stills and run dftwn to coke (see figure 25). If the crude oil con-
tains no wax, then the lubricants may be made by vacuum, steam
or gas distillation, and the distillate is only filtered through Ful-
ler's earth for use.

Wax distillate is collected following the gas oil and furnishes
the stock from which lubricating oils and wax are made. Wax dis-
tillate usually has a gravity of 30-32° Be', viscosity 50-80 at 100'
F and a cold test of 55-100° F. The amount from different crudes
varies from none up to 35 per cent. About 10 per cent is a usual
amount.

The wax distillate is cooled and the solidified wax pressed out
at a low temperature under a high pressure. The wax-free oil, known
as "pressed distillate" is then reduced in a still to the desired viscos-
ity lubricating stock. When reducing, considerable steam is used
in the distillation in order to prevent the oil from "cracking" or as
stillmen frequently say, from "burning." Heavy benzine, gas oil

194

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY 195

and light lubricating distillate are obtained as overhead products,
the residue being the base for the heavy lubricating oil. The light
lubricating distillate contains volatile products, which must be re-
moved. This is performed by reducing as before with fire and steam
to the viscosity desired.

The reduced lubricating stocks are further refined by treating
and filtering. The oils are agitated, by means of air, with strong sul-
phuric acid in lai-ge agitators. It has been found that better re-
sults are obtained if the acid is added in small portions instead of
adding the acid all at once. A small quantity, known as "water
acid" usually one pound per bai-rel of oil treated, is added and agi-
tated with the oil for a short time. The agitation is then discon-
tinued and the acid sludge is permitted to settle, after which it is
drawn off. Then about four pounds of new acid, known as the "first
body acid" is agitated with the oil. The agitation is again stopped
and the acid sludge drawn off. The larger portion of the acid, "sec-
ond body acid" is then added. This quantity varies with the nature
of the oil treated but is frequently 4 to 10 pounds per barrel of oil.
This is then agitated an hour or more with the oil, after which a
sufficient quantity of water is added to coagulate the asphaltic mate-
rial in the oil. This operation is known as "coking." The acid sludge
is drawn off as quickly as possible and the asphaltic material or
"coke" permitted to settle. If the proper quantity of water is not
added, the asphaltic material becomes finely divided and is difficult
to separate fi'om the oil. The oil which is still acid is pumped into
another agitator where it is neutralized with caustic soda, a 5° Baume'
solution being used. After the acid has been neutralized, the caus-
tic soda is permitted to settle and is drawn off. The oil is then
freed of moisture by heating to about 120 to 140° F and then blow-
ing with air until the oil is bright. During the neutralization, the
oil sometimes becomes emulsified. The emulsion is often broken by
heating or sometimes by heating and agitating with a demulsifying
compound. The oil should be treated in such a manner that a mini-
mum quantity of salts are formed during this process as these cause
the finished oil to have a poor emulsion test. Th acid treatment
the finished oil to have a poor emulsion test. The acid treatment
meet color specifications. The oil is then filtered through Fuller's
earth until the desired color is obtained. The filtering also improves
the emulsion test. After filtering, the oil is ready for the market.

Refiners frequently manufacture two grades -of lubricating oil,
a light and a heavy oil. These oils generally have the following tests:

Light Oil Heavy Oil

Gravity 25 0—32,0° Be' 20.0—27.0° Be'

Hash point 300—400° F 375—425° F

Fire test 400—460° F 460—500° F

Viscosity at 100° F 50—150 200—400

Cold test 10— 30° F 20— 35° F

Color (N. P. A.) 2 3, dark red

196

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY 197

All lubricating oils should have a fair emulsion test arid a low
carbon residue. Many purchasers of lubricating oils demand a light
colored oil, but a good color does not necessarily signify a good lubri-
cant.

Paraffin Wax is also obtained from the wax distillate cut. The
wax distillate is cooled to about 5° F in chillers by means of a cold
brine solution. The solidified mass is granulated and carried for-
ward to the presses by a helicoid conveyor. The wax is then sep-
arated from the oil by forcing the cooled mass of oil and wax through
filter presses under a high pressure, approximately 350 pounds per
square inch. The crude wax remains upon the canvas filter and the
oil drops into the pan below.

The crude wax known as "slack wax" is removed from the press
and conveyed to a tank where it is melted. The slack wax contains
a large percentage of oil, which must be removed. This is done by
a process known as "sweating." The "sweaters" are large shallow
pans which contain wire screens a few inches above the bottom. Suf-
ficient water is placed in the pan to cover the screen. The melted
wax is then pumped on the water and permitted to solidify slowly.
When solid, the water is drawn off at the bottom of the pan, the
cake of wax being supported by the screen. The temperature of the
sweater room is gi'adually increased by means of steam in closed
steam coils.

The oil known as "foots oil" first separates from the wax fol-
lowed by the low melting point or "intermediate wax." The wax
from the sweater is known as "scale wax." The scale wax usually
has a yellow color, which is removed by treating and filtering. The
scale wax is melted and treated with a few pounds of 66° Baume'
sulphuric acid, usually with 1 and 3 pounds in succession. The acid,
is drawn off and the remaining acid in the wax neutralized with 1
to 3° Baume' caustic soda. The alkali is settled from the wax, the
temperature being maintained at about 140° F during the entire pro-
cess. The melted wax is then filtered through Fuller's earth to the
desired color. Wax has a specific gravity of about 0 9, a melting
point of 120 to 140° F and not more than 1 per cent of oil and mois-
ture.

After the wax distillate has been removed from the crude oil,
a fraction containing considerable amorphovs wax, known as "wax
tailings" distills over. The wax tailings are not passed through the
condenser coils, but are permitted to pass directly from the vapor
line to a small tank known as the "wax pot." They are of little
value but may be used for cracking stock.

Crude oil which has a bright green color is distilled with consid-
erable steam in order that a heavy oil may be obtained after the gas
oil and a portion of the wax distillate have been removed. This
product is known as Cylinder Stock. Cylinder stock should have a
high flash and fire test; the color should be green to red, not brown
nor black. If a brighter color is desired, the oil is treated and filtered.

198 BULLETIN NUMBER SIXTEEN OF

Cylinder stock from Mid Continent crude oils usually has the
following tests:

Gravity 19.0—23.0° Be'

Flash point 490—600° F

Fire test 575—700° F

Cold test 40— 70° F

Viscosity at 212° F 130—250

Color brown or green

When asphalt is desired the residue from the gasoline and kero-
sene may be distilled by blowing superheated steam through it until
the desired consistency is reached. Asphalt base oils or cracked
paraffin base oils are necessary to make first class asphalt. An out-
line of the methods used for producing asphalts and road oils is given
on page 367. Frequently, particularly for road oils, the stock remain-
ing after cracking heavy gas oil is run down to a semi-solid or solid
consistency. This gives a specially valuable road oil on account of
its high asphalt content, good hardening or drying properties, low
viscosity and excellent penetration.

For refining by cracking see pages 204 to 242.

For illustration of a refinery operation, see flow sheets on pages
23 and 222.

KANSAS CITY TESTING LABORATORY 199

Color and Odor in Refined Petroleum.

Most distillates from petroleum contain sufficient foreign matter
to give an undesirable odor or a yellowish to red color.

The odor in natural distillates is due ordinarily to sulphur com-
pounds, characteristic of which is hydi'ogen sulphide. Gasoline or
light hydrocarbons produced by cracking have a more or less offensive
odor even though sulphur is not present in appreciable quantity. In
a general way, color is present in proportion as the odor is more dis-
agreeable. The color of petroleum products is thought to be partly
due to nitrogen compounds. Light hydrocarbons produced by crack-
ing have a higher color the larger the amount of nitrogen in the
heavy oils cracked, as' a general rule. Cracked products from paraf-
fin hydrocarbons such as those from Oklahoma give a yellowish color
in the distillate above 300° F though they may be colorless below
300 °F. California and Mexican cracked gasoline gives a red color,
which is not noticeable immediately upon distilling, but becomes more
intense as the gasoline is exposed to the action of the air. This col-
oring matter on standing largely settles out or is oxidised so that the
redistilled gasoline may be free from color.

Kerosene, the first refined product of petroleum marketed on a
large scale, was a yellow or dark red liquid. It was first produced
from coal, and it was found in 1857 that "coal oil" could be deodor-
ized and decolorized by treatment with sulphuric acid and this is the
process that is in general use at the present time. 66° Be' sulphuric
acid is ordinarily used, as it reacts upon the unsaturated compounds,
the sulphur compounds and the nitrogenous compounds in the oil by
forming substances which dissolve largely in the sulphuric acid. The
shrinkage of the oil treated may vary from almost nothing up to
10 per cent, depending upon the character of the oil being refined.
In ordinary natural distillates, one pound of acid per barrel is com-
monly sufficient, but with cracked oil as much as 10 pounds of acid
are often required. Even then the treatment is often not sufficiently
severe and oleum or Nordhausen sulphuric acid, which contains an
excess of sulphur trioxide is necessary. This is the case with Cali-
fornia oil. After treatment with sulphuric acid, thorough washing
and neutralization with caustic soda is always necessary. Other sub-
stances used for neutralizing the acid and acid sulfonates are soda
ash, lime, silicate of soda and sodium plumbite.

Other chemicals may be quite successfully used in removing the
odor of cracked gasoline, among these being sodium plumbite, cop-
per oxide, manganese dioxide, potassium permangate, sodium chro-
mate, aluminum chloride, chlorine and stannic chloride.

Dry hydrochloric acid gas (hydrogen chloride, HCl) and alum-
inum chloride are often highly effective in treating gasoline to re-
move the color.

The "bloom" or fluorescence of mineral oils is supposed to be due
to the presence of asphalt-like or pitchy material in colloidal condi-
tion. This is overcome by the use of mono-nitro-naphthalene
C10H7NO2) in small amounts.

200

BULLETIN NUMBER SIXTEEN OF

The most useful agent in the improvement of the color of refined
petroleum oil is fuller's earth. Chemically, fuller's earth is a hydrous
silicate of alumina, containing small quantities of other substances
such as calcium, magnesia, and iron. Usually it contains about 15
per cent of combined water.

The ability of fuller's earth to remove color from oil is purely
Dhvsical in character. Fuller's earth is not a definite chemical com-
pound and many varieties of fuller's earth will give equally varying
results. A sample of fuller's earth which is perfectly satisfactory
for bleaching vegetable oils may not be satisfactory for the bleaching
of mineral oils. Some fuller's earths have so marked an oxidizing
action on vegetable and animal oils that they cause the oil to catch
fire spontaneously when air is blown through the filter presses to
remove the adhering oil. This type of fuller's earth is of course not
satisfactory for vegetable oils but is quite satisfactory for mineral
oils. This is why the Florida earth is almost exclusively used for
bleaching mineral oils.

Fuller's earth for refining petroleum oil is usually bolted to defi-
nite sized grains and is placed on the market on the basis of 15-30
mesh, 30-60 mesh, 60-80 mesh, etc. The coarser sizes are in greatest
demand for the reason that after treatment of the oils, they are
easier to clarify. The finer sizes are more effective in bleaching
but are more difficult to clarify. The fine material may be used for
the decolorization of gasoline. Fuller's eax'th is ordinarily used but
slightly for decolorizing kerosene, though it is customary to treat
kerosene with a small proportion of fuller's earth to aid in remov-
ing the turbidity.

In its use, fuller's earth of the grade chosen is placed in a tali
cylindrical percolator with closed, rounded ends. Through this col-
umn about 15 feet in height, the oil is forced under sufficient pres-
sure to allow it to run freely from the bottom. The fuller's earth
is classified according to the color which comes through. The per-
colator carries ordinarily fi'om 18 to 25 tons at one time. The de-
coloi'ization capacity of fuller's earth varies from 30 barrels for one
ton of earth down to 7 barrels for one ton of earth on each treatment.
Since fuller's earth may be used satisfactorily from 10 to 16 times,
the amount of fuller's earth consumed varies from one ton of fuller's
earth to 500 barrels of oil down to one ton of fuller's earth for 60
barrels of oil. In each treatment, when the fuller's earth has be-
came useless for decolorizing, the percolator is blown out with air
to remove as much of the oil as is possible and the residue is washed
with naphtha to recover the oil adhering to the particles. The ex-
tractor is then blown out with steam to remove the residual matter.
The naphtha is recovered by distillation and the residual oil is re-
treated in the following batches. The recovered fuller's earth is
conveyed to a rotary kiln similar to those used in burning Portland
cement. The earth is heated at a low red temperature, about 900°F,
to revivify the earth. About 3 per cent of the material is lost in
burning. It is usual to burn the earth before using it for bleach-
ing, thus removing all of the moisture and water of hydration. Great
care must be taken that the temperature of incipient fusion is not
reached.

KANSAS CITY TESTING LABORATORY 201

Fuller's earth is also highly effective in the treatment of off
color naphthas, benzines and gasolines where fairly good results
can often be had by treatment in the same manner as in the case of
illuminating and lubricating oils. The best results can be had by
distilling while agitating with fuller's earth. In this manner, yellow
pressure distillates, such as are obtained in cracking,- can be decol-
orized completely by one distillation if proper towers are used. While
this makes water white gasoline it does not greatly improve the odor
and the usual treatment is necessary for eliminating the odor. On
the other hand, a very light dilute acid treatment may be used for
improving the odor and this may be followed by the distillation with
fuller's earth.

Good results may be had by the use of Bentonite* in the decol-
orization of petroleum. This material is a hydrous silicate of alumina
or zeolite. The material used for examination was greenish white in
its natural state with a greasy consistency and formed a perfect sus-
pension with water. The samples used for test were dried at 300°
F. After drying the material was white. The composition is as
follows.

Natural Dried Ignited

Moisture 35.33% 0.00 0.00

Combined water 4.61 7.13 0.00

Silica _ 38.70 59.85 64.45

Alumina 15.49 23.96 25 80

Iron Oxide _ 2.18 3.38 3.64

Lime 0.83 1.29 1.39

Magnesia ....- 1.81 2.80 3.01

Sulphur 0.71 1.07 1.15

Alkalies 0.34 0.52 0.56

By distilling pressure benzine of very dark color once with this
material of 100 mesh fineness a water white gasoline is obtained.

*See Engineering and Mining Journal, Vol. 112, p. 819, Novem-
ber 19, 1921 and Vol. 112, Page 860, November 26, 1921.

*See A. Seidell J. Am. Chem. Soc, Vol. 40, p. 312, January, 1918.

202 BULLETIN NUMBER SIXTEEN OF

Petroleum Emulsions and Their Dehydration.

Producers of petroleum are usually little concerned with the
refining of petroleum except as they receive a price dependent upon
the refining properties. Often particularly in the case of asphaltic
or heavy waxy crude oils a large amount of water, brine and col-
loidal mineral matter is suspended in the oil. Oil in such condition
may contain as much as 60 to 90 per cent of water. These emul-
sions are variously spoken of as B. S., sediment, roily oil, cut oil
and tank bottoms. Much of this B. S. is often asphaltic and waxy
matter precipitated by the mixing of crudes or the lowering of the
temperature when the oil exudes from the sand due to the release
of pressure. Most crude oil as it comes from the ground carries
some water but anything less than 2 per cent is accepted by the
pipe line companies or the refineries. The actual production of
emulsions probably occurs when the oil and the water mix as they
exude through the fine interstices in the sand.

The main emulsifying agents are probably hydrous silicates of
alumina which though in very small quantities form colloids with
water, asphaltenes or naphthenic acid which form colloidal solu-
tions with the oil and colloidal oxide of iron which separates out
from oil bearing brines. Any finely divided solid may, however,
act as an emulsifying agent. The chief requirement for a stable
emulsion is that the solid substance insoluble in one fluid and in-
soluble or slightly soluble in the other, separate on the surface of
the globule constituting the internal phase. A common condition
is that the liquid in which the emulsifying agent is less soluble con-
stitutes the internal phase. For example, metal soaps such as cal-
cium oleate and copper oleate are more soluble in oil than in water
and the oil is therefore in the external phase. Even in these cases,
however, the emulsion may separate into two layers of emulsion,
in the lower of which, the water is in the external phase and the
upper of which, the water is in the internal phase. If the crude oil
as naturally existing in the oil sand and containing a small amount
of naphthenic acid or similar substance while being forced by pres-
sure through the interstices in the sand is brought into contact
w;ith water containmg calcium bicarbonate, the corresponding cal-
cium soap is precipitated and forms a film on the globules of water,
thus tending to produce a more or less permanent emulsion.

There are two general methods of removing water from oil in
^♦u^ '^^J^ emulsified. One is by vaporization of the water, the
other IS by encouragement of the coalescence of the water globules.
Vaporization IS usually the method employed and merely consists
in heating the oil in pipes to a temperature of approximately 300°
t and (hscharging it into a hot still or vaporizing container. The
water thus goes completely into the vapor phase and condenses in
the coil together with any light oil. This condensate shows no ten-
dency whatever to again emulsify, on account of the absence of
emulsifymg agents and on account of the low viscosity of the oil.

The same effect may be accomplished without coils by heating
the oil to a pressure of about 100 pounds and condensing the vapors

KANSAS CITY TESTING LABORATORY 203

including all of the water vapor at the same pressure. This is the
same method as that for producing synthetic gasoline by pressure dis-
tillation. At the ordinary refinery, the oil is heated to a temperature
not exceeding 212° F and the water separates and is drawn out
through the tar plug. This, however, can only be done in the case
of the lighter crudes.

Various methods are used to induce coalescence of the water
globules. In all of these, the oil is heated. Often by heating alone,
there is sufficient settling out of the water to make the oil accept-
able. A temperature of 160° F is commonly used. As an aid to
this sedimentation, chemicals are frequently successfully employed.
A common formula is the use of a sodium soap containing resin,
wax and sodium silicate in small quantity. Sodium carbonate alone
is occasionally sufficient. The most recent method of coalescing the
water globules is the application of the centrifuge. This is used
in many large producing plants in the Gulf Coast and Mid Continent
region. The Cottrell Electric Precipitation method is claimed to be
quite effective and it is stated that it requires a consumption of
only about 100 watts of electricity per barrel of oil treated.

References on Dehydration of Petroleum.

C. V. Fornes, Petroleum Age, 10, 33, 1921.

E. E. Ayres, Petroleum World, 18, 406, 1921; 18,401.

J. H. Wiggins, National Pet. News, 13, No. 26, 59, 1921.

C. P. Buck, Oil and Gas Journal, 20, 80, 1921.

204 BULLETIN NUMBER SIXTEEN OF

Chemical Nature of Cracking of Oil.

When crude oil is subjected to ordinary distillation by fire the
light products naturally present in the oil are distilled off as such
up to a temperature of about 300° C (572° F) comprising both the
gasoline and the kerosene. Above this temperatui-e, the hydrocarbons
undergo partial decomposition while distilling, with the result that
some light products are produced and distilled along with the heavy
products. Olefins as well as paraffin compounds of lower molecular
weight than the oil being heated are formed. By vigorous firing the
entire oil residue may be distilled, leaving only a variable amount
of residual carbon as' a product of decomposition. The amount of
carbon and gas formed by this pyrogenic decomposition is greater
with the asphaltic or naphthene petroleums than with the paraffin
base petroleums. A typical heavy Mid Continent petroleum gives
4.5 per cent of carbon and 4.0 per cent of gas on distillation to coke
or carbon. With pure paraffin base oils the amounts of carbon and
gas formed are comparatively slight. Mexican oils from Panuco
give 20 per cent of coke.

This property of all heavy petroleums in decomposing into hydro-
carbons of lower molecular weight by heating is generally known as
cracking. The chemical reactions involved in cracking are not def-
inite, it was originally supposed that cracking involved the for-
mation of a large amount of olefins according to the following re-
action: (Redwood)

CnH2n+2 = Cn-mH2'n-ni)4-2 ' -l-CniH2m

a specific illustration of which would be

C|sH32 =C8Hl8 +C7H14

Pentadecane -fHeptylene = Octane

This reaction does not, h-wever, accord -with the facts, since gas
and carbon are always formed in varying amount. A reactian which
corresponds to the yields as experimentally found under certain con-
ditions is the following:

2CnH2n+2 =2 Cn-mH2(n-m)+2 +mCH4+mC

or as a specific illustration

C1.SH32 =CsH„ +7 CH4 +7C

Pentadecane = Octane +Methane -f Carbon

Yet under certain other conditions the amount of gas formed is
very small, indicating that the following reaction was partly car-
ried out.

(jm+s) CnH2n+2 =(2n+2) CmH2n+o +2(n-m) C

or as an illustration

i^''}'^'' =16C8H,8 +7C

Pentadecane = Octane + Carbon.

This last reaction is also indicated by the large yields of gaso-
nne obtamod from some crude oils.

•« ^I"n^^,'^"''^^^'" w^^ of melting point of 130° F and specific grav-
ity ot U.8J2 on repeated cracking confined under pressure up to 57
atmospheres at temperature of 400° C and with a vapor space twice
the volume of the liquid, yielded 32.5 per cent bv volume of gaso-
me of 0 724rrG.3.4 Be' gravity or 29.1 per cent by weight by each
treatment or a total of 94.7 per cent bv weight, or 104 per cent bv

KANSAS CITY TESTING LABORATORY 205

The amount produced on first six treatments was as follows:

First 29.1% by weight of original paraffin

Second 19.9% by weight of original paraffin

Third 14.5% by weight of original paraffin

Fourth 9.9% by weight of original paraffin

Fifth 6.8% by weight of original paraffin

Sixth 4.7% by weight of original paraffin

84.9%

The gasoline produced consisted of paraffin hydrocarbons as
shown in fig. 42.

That the cracking of oil is not simply a decomposition of the
hydrocarbon molecules is shown in fig. 44. These curves show
the relation between the distilling temperature and the specific
gravity of water white Cabin Creek distillate. Before cracking, it
had an end point of about 540° F and its heaviest ends had a spe-
cific gravity of 0.815. After cracking, the end point was above
640° F and the end gravity above 0.900. Both heavier and higher
boiling hydrocarbons as well as lighter and lower boiling hydrocar-
bons were produced simultaneously. There must have been poly-
merization to yield hydrocarbons of both higher boiling point and
higher specific gravity. By continued cracking there may be made
from water white distillate, solid and ductile asphaltic cement of
typical conchoidal fracture.

The gases produced by cracking likewise are not simple split-
off hydrocarbons but vary according to the method of cracking. In
liquid phase cracking, the chief variation is in the olefin and hy-
drogen content. In a general way, there seems to be a tendency
for low percentages of hydrogen to be associated with low per-
centages of olefins. A typical gas made in a Burton still has the
following composition:

Methane and Ethane (CnH2n+.2)=82.0%
Olefins = 8.5%

Hydrogen = 9.5%

One of the problems in cracking is to limit the amount of hydro-
gen. This has been partially done by allowing the hydrogen to re-
main in contact with the cracked distillate under high pressure and
at a temperature somewhat below the ordinary temperature of crack-
ing (see U. S. Patent 1,255,138). (See Figs. 72 and 73.)

Figures 39 and 40 shows some of the relative properties of light
hydi'ocarbons made by various pro:-esses used more or less in a com-
mercial way for the production of gasoline from heavy oil.

206

BULLETIN NUMBER SIXTEEN OF

Classification of Systems of Cracking.

I — Vapor Phase.

A. Atmospheric pressure.

(1) High temperature. Oil gas, Pintscb gas at very high
temperature. Blaugas and liquefiable gas at high tempera-
ture (1200° F). Gasoline substitutes such as Greenstreet
process — cherry red temperature.

(2) Low temperature (700-900° F).

B. Increased Pressure.

(1) High temperatures. Rittman at 950° F and 200-300
pounds. Hall at 1100° F and 75 lbs.

(2) Low temperatures (750-900° F).

II — Liquid Phase.

A. With distillation (distillation necessary).

(1) Atmospheric pressure.

(a) Without chemicals. Atwood (1860) — illuminating
oil practice.

(b) With chemicals. Aluminum chloride and related
chemicals (McAfee, Gray).

(2) Above atmospheric pressure — no differential pressures.
Dewar & Redwood, Dubbs, Burton, Bacon & Clark, E. M.
Clark, Jenkins, Fleming.

(3) Very high pressure — distilling at reduced pressure. Ben-
ton.

B. Without distillation (necessarily high pressure).

(1) Intermittent. Palmer, Snelling, Hubbard.

(2) Continuous.

(a) Identical heating and reaction zones.

(b) Separated heating and reaction zones.

The above outline of the general systems of cracking gasoline
is not based upon any general mechanical arrangement. Most of
the patents relating to the cracking of oil cover mechanical arrange-
ment. Of more than 1,000 patents on this subject, very few of them
are basic.

Those systems that heat the oil vapor at atmospheric pressure
are principally used for making gas. On account of the low spe-
cific heat of the oil vapor the temperatures are very high and are
not subject to exact control. The result is that the product contains
a large percentage of olefins and aromatics and a large proportion
of the heavy oil stock is converted into fixed gas. Possibly the only
chance of making a first class gasoline according to these systems
is to heat the vapor at a temperature of from 700 to 900° F. This
involves a very large apparatus or one in which the oil vapor is put
through at a very high rate of speed. The difficulties in tempera-
ture control are so great that they have not yet been satisfactorily
overcome, althoi-gh some experimental work is being done in the
design of furnaces for holding the vapors at the limited tempera-
ture required.

KANSAS CITY TESTING LABORATORY 207

Much of the pioneering work in the cracking of oil was done
in heating in the vapor phase under increased pressure. These also
have the fault that the temperatures are ordinarily kept too high;
1100° F and a pressure of 75 pounds ai"e typical. Increase of pres-
sure is of interest because of the deceased cost of operation. Like-
wise low temperatures of from 750 to 900° F with vapor phase crack-
ing might prove successful but the question of carbon deposition on
the walls of the tubes present a new difficulty.

The really successful processes that have proved profitable are
those in which the cracking is accomplished by applying the heat
to the liquid phase of the oil. The original work on cracking by
Atwood in 1860 was done at atmospheric pressure and it has been
the practice ever since that time to increase the amount of illum-
inating oil by refluxing while distilling. This method, however, does
not accomplish enough in the production of gasoline unless some
chemical agent is added which causes the reaction of cracking to go
on at a lower temperature. The most common chemical used for
this purpose is technical dry aluminum chloride, the operation of
which is explained more fully further on. By this process, com-
pletely refined gasoline may be made with one operation. Other
chemicals such as tin chloride, ferric chloride, manganic chloride,
zinc chloride and phosphorus pentoxide have the same effect but to
a lesser degree.

The method by which a large proportion of the synthetic gaso-
line is now made is by distillation at pressui'es considerably above
the atmospheric pressure. The reaction and distillation take place
in the same still. An enormous amount of refluxing is necessary and
the gasoline must be removed as fast as it is formed. An enormous
amount of heat is lost by reason of this refluxing and the reaction
is considerably retarded, but nevertheless, the distillation is a neces-
sity as otherwise excessive pressure would develop.

By the use of very high pressure, more reaction can be accom-
plished in a shorter time and methods exist whereby this is done
followed by distillation at a lower pressure.

The most recent development, however, has been the accom-
plishment of the cracking without distillation as a separate and
distinct refinery operation. This is necessarily carried on at a
high pressure and most of these processes provide for intermittent
operation. Intermittent operation is of course not commercial in
handling a cheap material like petroleum as a very long period of
time is necessary for cooling between operations. Continuous sys-
tems have been devised in which the heating zone and the reaction
zone have been one and the same. This brought on difficulties in
continuing the operation for long periods of time without the forma-
tion of an excess of carbon. Possibly one of the most basic patents
has been developed in which the heating zone is separate and dis-
tinct from the reaction zone. This allows an operation to be con-
tinuous for a period of from 3 to 15 days without the necessity of
cleaning carbon as the reaction zone may be changed without in-
terfering with the heating zone.

Electrical processes continue to attract considerable attention
chiefly because of their novel claims rather than because of any

208

BULLETIN NUMBER SIXTEEN OF

"""'''•' G.L.BENTON.

PROCESS OF EEFINING CRUDE PETROLEUM OIL.

No. 342,564. Patented May 25, 1886.

INVENTOR

Fitr. 20 — Ronton Process for Cracking'.

KANSAS CITY TESTING LABORATORY 209

virtues which they possess. Electrical processes have not been dem-
onstrated as having any commercial value though heat from elec-
trical sources is doubtless as effective in cracking as heat from
cheaper sources. No true catalytic processes have been developed
for the cracking of oil. No substance has been found which will
cause the cracking reaction to go on any more rapidly than occurs
in the case of cracking in the liquid phase with high pressure and
without distillation. The highest speed probably attained by the
use of aluminum chloride is 5 per cent conversion per hour whereas
with high pressure and without distillation, conversion can readily
be carried out at the rate of 2 per cent per minute. Many chemical
substances, however, are effective in producing a sweeter and whiter
product.

Advantages of Liquid Phase Cracking.

All processes of making gasoline which have not involved the
treatment of the oil strictly in the liquid phase are said to have
met with only a questionable degree of success.

While the cracking of oil in the vapor phase would be highly
desirable if the product and other conditions were satisfactory, it
has been claimed by many that the advantages of applying the heat
to the liquid phase are as follows:

1. A lower temperature is sufficient to induce cracking.

2. The rate of reaction is greatly increased, being greater the
higher the pressure within certain limits.

3. A product containing smaller amounts of olefins and aromat-
ics is produced.

4. A higher yield of refined gasoline is obtained.

5. There is a better economy of heat.

6. There is a selective action on the oil or heavy portions of
the petroleum by reason of the automatic conversion of the desired
pi'oduct into the vapor phase, thus freeing it from further liability
to decomposition.

7. There is a high oil capacity with small plant dimensions.

8. There is a perfect control of temperatures.

9. There is a rapid and more complete absorption of heat from
the furnace and less tendency to local overheating on account of the
much higher specific heat of oil than of the oil vapor.

10. There is the possibility of operating either by intermittent
charging or by continuous treatment and distillation.

11. The carbon is deposited in a suspended condition in the oil
and not on the retaining walls.

12. There is the possibility of the use of the automatically
developed pressure for mechanical and condensing purposes.

The chief disadvantage in cracking oil in the vapor phase and
under high pressure seems to be the danger attendant upon a pos-
sible failure of steel parts, but this is entirely overcome with proper
design.

210 BULLETIN NUMBER SIXTEEN OF

The following- special physical properties of hydrocarbons enter
into the considerations of liquid phase cracking:

Gasoline Hydrocarbons.

Critical Pressure
Critical Temperature Atmospheres

Pentane 390° F. 24

Hexane 450° F. 22

Heptane 515° F. 20

Octane 565° F. 18

Nonane - 640° F. 16

Decane 680° F. 15

Undecane 720° F. 14

Kerosene Hydrocarbons.

Duodecane 760° F. 13

Tridecane 860° F. 10.5

Tetradecane 900° F. 9

The critical temperatures are somewhat increased by the presence
of the heavier hydrocarbons so that at pressures above about 150 lbs.
per square inch only gasoline and gaseous hydrocarbons would be
removed from the liquid phase. With pressures below this there would
be some difficulty in maintaining the lighter kerosene in the liquid
phase.

References: See Fig. 41 on vapor pressure of gasoline. Denig,
Chem. & Met. Engr., Vol. 25, p. 751; Young, Sci. Proc. Roy. Dub.
Soc, 12, 374.

I

KANSAS CITY TESTING LABORATORY

211

^No Model.')

J. DEWAR & B. REDWOOD.

APPARATUS FOR THE DISTILLATION OP MINERAL OILS AND

LIKE PRODUCTS.

No. 426.173.

^Sffl

Patented Apr. 22. 1890.

cz:^

:««<^V

2Z3^'

l^iS^

Fig-. 27 — Dewar & Redwood Process for Cracking.

212 BULLETIN NUMBER SIXTEEN OF

Development of Commercial Practice in Cracking of Oil.

It has been stated that the commercial cracking of oil was acci-
dentally discovered in the winter of 1861 by a stillman at Newark,
New Jersey. However, this is probably not the case, since a patent
was granted to Luther Atwood, of New York, May 15, 1860, No.
28,246, in the U. S. Patent Office, which provides for the production
of light hydrocarbon illuminating oils from heavy oils, paraffin, etc.
The apparatus provides for the cooling of the heavy oil vapors and
their return to the still for further cracking. This is all carried out
at atmospheric pressure.

The first record of pressure distillation is apparently set forth
by James Young in his patent. No. 3,345 (English) of 1865, in which
a distillation is described as being conducted in a vessel having a
loaded valve or a partially closed stop-cock through which the con-
fined vapors escape under any desired pressure. IJnder these condi-
tions, distillation takes place at higher temperatures than the normal
boiling points of the heavy hydrocarbons and partial cracking results.
The patent was taken out for treatment of shale oil and in practice a
pressure of 20 pounds to the square inch was recommended.

The first extremely high pressure process was that of Benton,
U. S. Patent No. 342,564, May 25. 1886. In this the oil is heated at
a temperature of from 700° to 1,000° F. through a pipe leading to
a low pressure expansion chamber, where it was vaporized, and then
the vapors were condensed. The pressure used was as high as 500
pounds per square inch.

A very important patent in the present development of crackinp-
processes is that issued to Dewar & Redwood, which is partly de'^
scribed as follows:

Specifications and Claims of Dewar and Redwood.

"In distilling mineral oils— such as natural petroleum or similar
ml made from shale, coal or other bituminous substances— in order
to separate the lighter oils, suitable for lamps and other purposes,
trom the heavier oils, there is frequently a very large residue of
neavy oil. Attempts have been made to obtain lighter oils from such
resulues or from heavy natural petroleums by causing the vapor gen-
erated in the stiU-boiler to pass a heavily-loaded valve, so that
ine vaporization takes place under considerable pressure. It has
r^l.1 !" Frr^fu'^ i*"" arrange the still-boiler with its upper part
moio ^r ?p1 ^Y ^'f "^f ^i*'^ P"^t'«" «f the vapor mav become
moch. of on! 'T^^^'l^'- '''"'' ^^" ^^^k ^"t« the hot liquid below, this
n thCls ..?o nf • "*;• '""^'."f commonly termed 'cracking.' Both -these
of the di:^fninr^ '^'^"/i',^' }^^ ^"""^^^ «" «^c«'^'"t of the irregularity
•onluctinJ Si " ^v ^^"^ ^^"^'^ «" ''^"^^"t of the waste of heat in
of th" nsults ""^"^'"^ P'^'^^^^ «"d the slowness and insufficiency

l>v suinhli'^nnnn^of''^^^*^' K"" "'^thod of conducting the distillation

n^guTat vimfrKfn^^ '1 '"' i ^ "'•^"""'' t^^^t we get the benefit of

vc mrvirthos^mrf-"^' conden.sation under high pressure, and that

may at the same time get such advantage as can be obtained from

KANSAS CITY TESTING LABORATORY

213

W. M. BORTON.

MAN0FAC7UEE OF GASOLENE.

AFFUCAIIOR FILED JOIT 3, l»12

1,049,667.

Patented Jan. 7, 1913.

Z^f^jGJ^G^ .

^^0--^^^^

Fig. 28 — Burton Process for Cracking.

214 BULLETIN NUMBER SIXTEEN OF

cracking. For this purpose, we arrange a suitable boiler or retort,
and a condenser in free communication with one another, without
interposing any valve between them; but we provide a regulated out-
let for condensed liquid from the condenser. We charge and keep
charged the space in the boiler or retort and condenser that is not
occupied by liquid with gas under considerable pressure, it may be
with air or it may be with carbonic-acid gas or other gas that cannot
act chemically on" the matter treated. The distillation and condensa-
tion being thus conducted under considerable pressure, which can
be regulated at will, we obtain from the heavy residue a quantity
of more or less light oil suitable for illuminating and other pur-
poses, which cannot be obtained by distillation under atmospheric
pressure. We may also arrange the still-head or upper part of the
boiler or retort so as to operate according to the cracking method
above referred to, the cracking in this case taking place under high
pressure instead of being carried on under atmospheric pressure."

"The apparatus for effecting distillation in the manner described
may be arranged in various ways. The accompanying drawings show
one fcim of apparatus for this purpose.

"By a pipe and cock or a suitably loaded safety-valve D-, gas may
be withdrawn from the space above the liquid in the column D2.

"By regulating the heat and pressure to which the retort is sub-
jected, the character of the distillate may be varied and thus oils
more or less light can be obtained to suit various uses. Also the
proportions of the parts may be varied, and if necessary, means of
cooling may be applied to the still-head C2.

"Having thus described the nature of our invention and the
manner of carrying the same into effect, we claim — the herein-
described method of distilling mineral oils and like products, which
consists in both vaporizing them and condensing the generated vapor
under a regulated pressure of air or gas substantially as specified."

THE BURTON PROCESS.

This is the process by which much of the artificial gasoline now
on the market is made. Dr. Wm Burton states that the total Burton
sti capacity is eight million gallons with an output of two million
gallons of gasoline per day in 1921.

The drawing in the patent is shown in fig. 28.

In the practical operation of this process, a very hot furnace is
required on account of the very great radiation of heat from the
return conduit 7.

Novelty in this process is claimed to lie in the maintenance of
pressure on the condenser, though this is done in the Dewar &
Redwood process with inert gas. The fact is, however, that the
Kurton Process is being successfully operated on a large scale and
presumaby with profit In one of the Burton patents (1,105,961) it is
claimed that 03'^% of the original charge of oil is converted into

KANSAS CITY TESTING LABORATORY

215

The actual operation of the Burton process has been described as
follows:

The stills have a capacity of 200-250 barrels each, and are heavy,
horizontal steel cylinders, with walls one-half inch thick, thoroughly
insulated with asbestos. From the top of the still are long run-backs,
exposed to the air, which return for cracking any undecomposed oil.
The stills, the run-backs and the condenser are all maintained under
a pressure of about eighty-five pounds per square inch, the oil being
heated to a temperature of about 750° F. Each still is charged every
forty-eight hours, the yield being about 50 '^r of 48-52° "pressure
distillate." The carbon tends to be of a granular or mealy nature,
rather than hard and adherent, and is cleaned out after each run.

or fixiiator

To Starnys tatkojtd

tJi£rt ta the fisruft SUtCs

BURTON STILL WfTH VARIOUS MODiriCATIOnS

Fig-. 29 — Modified Burton- Still Practice.

Important modifications of the Burton process are shown in the
Clark patents, 1,119,496, 1,129.034, and 1,132,163; A. S. Hopkins,
1,199,464; R. E. Humphreys, 1,122,002, 1,122,033, and 1,119,700.

One of the Clark modifications allows the application of heat to
tubes and seeks to overcome the danger of heating a large bulk of oil
directly.

The Hopkins patent provides for introducing fresh oil supply into
the run-back 7 with a heat exchanger effect.

One of the Humphreys patents provides for plates in the bottom
of the still to prevent the bad effect of carbon and to give a large
metallic heating area. One provides for starting stills under pressure.

The original Burton claims are as follows (Patent 1,049,667,
filed July 3, 1912):

"1. The method of treating the liquid portions of the paraffin
series of petroleum distillation having a boiling point upward of
500° F. to obtain therefrom low-boiling point products of the same

216

BULLETIN NUMBER SIXTEEN OF

series, which consists in distilling at a temperature of from about
650 to about 850° F. the volatile constituents of said liquid, conduct-
ing off and condensing said constituents and maintaining a pressure
of from about 4 to about 5 atmospheres on said liquid of said vapors
throughout their course to and while undergoing condensation.

3n— Dubbs Process for Cracking.
THE DUBBS PATENT.

t.IicaUon'Vit" P^^^^' ?''*^?.^ ^°- 1'123,502, Patented Jan. 5, 1915. Ap-
plication filed November 20, 1909.

of th!!''n!?vlK''''p^. ""? excerpts from the specifications and the claims
«.f the Dubbs Patent which discloses a method of making gasoline.

KANSAS CITY TESTING LABORATORY 217

This patent is claimed to be a prior invention to that of W. M. Burton:
"This invention relates to improvements in treating oil and refers
more particularly to a process of subjecting the oil to heat and
pressure.

"Among the salient objects of the invention are to provide an
improved method of treating oil v^herein both the vaporization and
condensation take place under the pressure of the generated vapors;
to provide a method which is particularly adapted for the removal
of the finely divided particles of water from emulsified hydrocarbon
oils; to provide a method which will permit of the oil being continu-
ously subjected to the required heat and pressure in both the still
and condenser without the interruption of its flow. . .

"As for example, in oil containing about 28% of water (which
is the case of oil of the Santa Maria field of California), a pressure
of about 25 pounds, and a temperature of 325° F., more or less, has
given very good results, as regard the segregation of the water,
although I have performed my operation under pressure ranging
from three to two hundred and fifty pounds above atmospheric. . .

"Claim 9. The herein described process of treating hydrocarbon
oil which consists in subjecting such oil in a receptacle to a tempera-
ture in excess of 300° F., permitting the volatilized products generated
from the oil under treatment to pass freely to a condenser where
they are condensed, and maintaining substantially the entire pressure
exceeding ten pounds to the square inch in both the receptacle and
condenser during the whole process solely by the vapors generated
from the material under treatment."

ILLUSTRATIVE COMMERCIAL OPERATION OF DUBBS

PROCESS.

(Furnished by Gustav Egloff of Universal Oil Products Co.)

A. . On Fuel Oil. — Two typical runs on fuel oil were a 15.6
Baume Gravity Mexican Fuel resulting from the topping of a southern
field Mexican crude oil and a fuel oil of 25 Baume Gravity from a
mixture of Healdton, Peabody and Gushing crude oil were cracked in
a coil, thirty-six continuous tubes, each twenty feet long 4-in. diam-
eter and heated in a furnace. The liquid from the last tube passes
into one end of a 30-in. expansion chamber, the vapors from which
enter a dephlegmator, where they are partially condensed and the
reflux returned to heating coil. The pressure distillate condensed
passes on to a run-down tank from the receiver. The residuum from
the expansion chamber is continuously drawn off during operation.
The operating pressure of the Mexican Fuel Oil was 110 pounds and
for the Mid-Continent Fuel Oil 135 pounds. It is noteworthy that in
the illustrative runs the carbon produced on the Mid-Continent
Fuel Oil was 2.77 tons while the Mexican Fuel Oil produced 5.86 tons
of carbon, and that these amounts were successfully handled and were
deposited outside of the heating zone where no damage to the ap-
paratus was possible. The detailed data of the two illustrative runs
follows :

218 BULLETIN NUMBER SIXTEEN OF

Mid-Continent
Mexican Fuel Oil Fuel Oil

Hours fire to steam 3 AV2

Hours on stream 13 21

Pressure (pounds) HO 135

Total Charge (gallons) 21,054 30,213

Pressure Distillate 10,834 18,355

Percent Pressure Distillate 51.45 60.75

Residuum 7,906 10,348

Percent Residuum of Charge 37.55 34.25

Percent Gasoline (Navy Spec.) 26.23 26.3

Baume Gravity 58.4 59.6

(Gallons Per Hour)

Raw Oil 1,620 1,439

Pressure Distillate 833 874

Gasoline 425 379

Tons Carbon Produced 5.86 2.77

Percent bv Weight Oil Cracked to Carbon.... 6.69 2.44

Raw Oil, per Day 452 486

Gasoline, per Day 118 128

B. On Gas Oil. — The Gas Oil runs were made in a cracking unit
composed of forty-eight 4-in. diameter tubes 20-ft. lengths in coils of
twelve each connected to a common header. The heated oil passed
into a 16-in. diameter expansion chamber, from which the vapors
traveled to the bottom of a dephlegmator, wherein they are frac-
tionated and the reflux condensate returned to the cracking coils,
while pressure distillate oil is collected in a receiver from which it
passes on to a run-down tank. While pressure distillate oil is being
collected, the residuum from the 16-in. expansion chamber is being
drawTi off and collected in a run-down tank. Four typical runs in the
commercial unit are tabulated as follows:

MID-CONTINENT GAS OIL (35.3 BAUME GRAVITY).

Hours Fire to Stream 9 16 14^/4 13%

Hours on Stream 196y2 336 263% 154^4

Pressure (Pounds) 135 135 135 135

Total Charge (Gallons) 87,031 139,684 123,550 105,352

Pressure Distillate 54,578 86,053 77,485 64,747

Percent Pressure Distillate 62 71 61 61 62 7 61 5

Residuum 30,664 54 566 46,345 42,398

Percent Residuum of

„ Charge 35.23 39.06 37.5 40.2

Percent Gasoline (Navy

„ Spec^) 33.16 26.23 28.9 262

Baume Gravity 58.5 58.3 58 0 58.0

„ ,,., (Gallons Per Hour on Stream)

^^^ ' ^K:-"-.-,;-"-- 443 416 469 683

Pressure Distillate 278 256 294 420

(.a.soline^ . 147 ^^g ^gg ^^9

1 ons Carbon Produced 10 0 5 11 1

Percent by Weight Oil

Cracked (to Carbon).... 0.4 0.16 0.3 0.21

Raw Oil, per Day 240 228 252 5 334

tiasoline, Bbls. per Day.... 79.4 58 8 73 87

KANSAS CITY TESTING LABORATORY 219

THE CROSS PROCESS.

This process is a system of producing a synthetic crude oil. The
patents thoroughly cover that type of process in which there is no
material distillation and in which the reaction zone and the heating
zone are separate and distinct. Distillation is avoided to prevent
retardation of the cracking. The heating zone is free from carbon
as the oil is discharged into the reaction zone before carbon can sep-
arate out.

A test run on 10,000 bbls. of 33° Be' gas oil was as follows:

Gas oil used 10,475 bbls. = 100.00%

Gasoline 6,789 bbls. = 64.8 %

Fuel oil residue 2,600 bbls. = 24 8 %

Loss — gas and carbon 1,086 bbls. = 10 4 %

Some important facts about the operation of the Cross process
are as follows:

1. Heat is applied to the oil in tubes arranged in series. The
tubes are placed horizontally in a heavily constructed, well insulated
furnace in such manner that should a tube fail, the only damage is
from loss of the tube as the small amount of oil discharged is burned
and mostly goes up the chimney or is discharged into a tank.

2. The oil is pumped through the tubes in one direction only
and no oil that has undergone reaction with the separation of carbon
vs returned to the tubes.

3. Decomposition does not take place in the tubes sufficiently to
deposit an excessive amount of carbon.

4. The heated oil is passed from the tubes to a reaction cham-
ber where conversion of the heavy oil into gasoline takes place and
where the carbon is deposited.

5. No heat is applied to the reaction chamber but this chamber
fes well as all pai'ts of the plant are heavily insulated against losses
ftt' heat to the atmosphere.

6. No distillation takes place from the reaction chamber or
from any portion of the system as this would retard the conversion
by reason of its cooling effect.

7. A small amount of oil is in the apparatus at one time.

8. About one-half barrel of oil is pumped through per minute.
About 15 minutes is required for the reaction. Seven hundred bar-
rels of oil are treated per day in one unit of the process.

9. The treated oil and the gas produced come out together, any
gasoline in the vapor phase being absorbed back into the oil when
cooled together, or distillation of the hot oil is carried out in the
ordinary tower still without cooling and with very little additional
firing.

10. Plant operation is very simple, requiring careful observa-
tion but little manipulation by the attendants.

11. No oil level devices are required. Pressure relief valves
regulate the oil level at the point of discharge.

12. The treated oil or synthetic crude requires no more treat-
ment than the pressure distillate and bottoms as made in the pres-
sure distillate system of cracking.

220

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY 221

13. The factors of safety on the steel stresses in the different
parts of the plant are approximately 5:1.

14. The fittings on the end of the tubes are outside of the
furnace and the openings of these tubes are quickly closed and opened
without loss of time.

15. In the normal operation, the plant is kept on stream for
6 days and is cleaned on the 7th day. The complete cycle is 1 week
with the treatment of about 4,500 barrels of oil.

16. One or more units of the Cross process may be added to
any refinery merely as an adjunct without any change in ordinary
refinery operation. With this process added, a greater still capacity
is necessary for a given amount of crude oil or greater yields may be
obtained with the same still capacity and with a smaller amount of
crude oil available.

The scheme of operation is shown by the diagram in figure 32.

The steam pump (1) forces the charging stock against the pres-
sure in the apparatus through line (2) passing it from above dawn-
ward through the preheating tubes (3) in the upper part of the
furnace. No decomposition or cracking takes place in these upper
tubes since they merely serve as fuel economizers while the pressure
in the apparatus is sufficient to maintain the oil in the liquid condi-
tion. The oil passes from these preheater tubes into the lower fur-
nace tubes (4) starting in at the bottom. In this furnace, the main
absorption of heat takes place. The oil temperature is registered as
it issues from the heating tubes at the point (13). The temperature
of the oil and the character of the oil under treatment govern the
rate of pumping At the point (13) all of the heat has been applied
10 the tubes but the oil has not yet been converted as the time ele-
ment is lacking It is therefore discharged into the reaction chamber
(7) where it is held a sufficient length of time for an equilibrium to
be reached between the vapor phase and the liquid phase. Ordi-
narily, this requires less than 15 minutes. The discharge line through
the valve (8) is set at the liquid level and perfectly controls this
level without any other automatic device than an ordinary relief
valve. The oil is then discharged oat through the cooling coil (9)
line under a pressure of approximately 40 pounds and into the gas
separator (10) from which the gas goes out through the line (11)
and the oil is discharged through the line (12) to storage. This
synthetic crude is run in the ordinary skimming plant in the usual
manner.

A flow sheet for a complete gasoline plant in which all of the
crude is made into gasoline and fuel oil is shown in figure 33. It
is of course not advisable to run all of the residue into gasoline as a
point is eventually reached at which the fuel oil becomes so heavy
that the gasoline yields are relatively poor. The yields that can be
obtained from various crudes may be calculated from the formulae
on page 242.

222

BULLETIN NUMBER SIXTEEN OF

KANSAS CITY TESTING LABORATORY 223

CROSS PROCESS PLANT No. 1 (Small Reaction Chamber).
Run No. 44, Jan. 21, 22, 23, 24, 25, 1922.

3,030 bbls. oil used.
2,909 bbls. cracked oil delivered.
727 bbls. gasoline produced.
91 bbls. fuel used.

Vs bbl. fuel used per bbl. of gasoline produced.
96 hours on stream.
98 hours on fire.
31.5 bbls. cracked per hour.
.95 bbl. fuel per hour
915 °F maximum oil temperature.
900° F average oil temperature.
1,375 °F maximum furnace temperature.
765° F maximum stack temperature.
700 °F average stack temperature.
RESULTS OF ONE UNIT CROSS PROCESS PLANT No 1
(Small Reaction Chamber) For Month of January, 1922.
CHARGES:

15,427 bbls. gas oil used @ $1.575 $24 297.53

420 bbls. fuel used @ $1.575 661.50

Total payroll charge for month 1,363.79

Storeroom charges for month 55.78

Fixed charge, 31 davs @ $32 00 992 00

Steam, air, etc, 31 days @ $20 CO 620.00

Distilling and treating 14,852 bbls. @ $0.35 5,201.70

Total charge $33,192.30

CREDITS:

4,186 bbls. gasoline @ $6.09 $25,492.74

10,622 bbls. oil returned @ $1 47 15,614.34

Total credits $41,108.08

Less charges 33,192.30

Estimated profit for month $ 7,914.78

COMPARATIVE COSTS OF MAKING GASOLINE.

While there is much variation in the absolute cost of making
gasoline by any process, the following outlines comparative costs of
operation of one unit of three principal systems: No satisfactory
information is available for vapor phase processe^.

Synthetic
crude
system

Labor "$0 30

Materials 0.16

Fuel oil at $1.00 per bbl 0.10

Overhead 0 20

Fixed charges 0 25

Re-running 1.20

Gas oil equivalent to converted gasoline.. 1.25

Refining los» 0 20

Degrading of gas oil 0.06

License charges 0.20

Pressure

Alummum

istillate

chloride

system

system

$0.90

$0 90

0.20

2.60

0 40

0.40

0.20

0.20

0.75

0 60

1.20

000

1.25

1.25

0.20

0.20

0.06

0.60

0.20

0.20

Cost per bbl $3.92 $5 36 $6.95

224

BULLETIN NUMBER SIXTEEN OF

3ecTiof*^L PLJ^f t/i£tv Of r<jmni^ce /^Boi^e Pvchc^tihq Tubcs

=O.OjO<K);
ObO<»C

1^1 "-wvy-

u^:^-^ I — .... ^-1--"

:^.fc^-

•5/oc Etcu^TioN or futerf^c£

Fig:. 34— Double Unit Cross Process Plant.

KANSAS CITY TESTING LABORATORY

225

'/•Mf* Ar-jj**^ SfSftm Cto^'f t'a-

Coi^reoL Moi/sr

r

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^tS

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Ceosj Pi?oc£S5 0/fJoi/n£ Pimr

0*1'*'' O' C-Jf* ScfLT •/'*■ ■ I O'

Fig. 34 — Double Unit Cross Process Plant (continued).

226 BULLETIN NUMBER SIXTEEN OF

Refinery Engineering Data on Distilling and Cracking

of Petroleum.

The total capacity of a horizontal still is approximately 0.14 d1,
d being the diameter and 1 the length of the still in feet.

The heating area of a horizontal still is 1,0472 d 1 on the as-
sumption that one-third of the shell is fired. In continuous stills a
larger area may be fired on account of a higher minimum oil level.

Continuous stills give a greater crude oil capacity than batch
stills on account of the time required for charging and discharging
batch stills. The amount of benzine or crude gasoline distilled is
1.5 d 1 barrel per day with continuous operation and with no other
products distilled.

The approximate amount of gasoline from crude oil stills per day
per square foot of still bottom area not including charging time or
time for bringing to distillation temperature is 1.0 barrel. This may
vary according to the intensity of firing and the character of the
crude.

The approximate total fuel consumption in producing one gallon
of 58° Be' gasoline in a still by cracking at 85 pounds pressure is
50,000 B.T.U. or 0.4 gallon of fuel oil.

The total fuel consum^ption by cracking in tubes at 600 pounds
pressure in producing one gallon of 58° Be' gasoline is 26,000 B.T.U.
or 0.20 gallon of fuel oil.

The report of the Western Petroleum Refiners' Association of
September, 1919, on a pressure distillation process operating at 135
pounds per square inch pressure may be analyzed as follows:

0.164 gallons of 58° Be' gasoline was produced per square foot
of heating area per hour after the oil was brought to the cracking
temperature.

0.8 gallon of fuel oil equivalent to 112,000 B.T.U. was required
to produce 1 gallon of 58° Be' gasoline.

200 cubic feet of gas was produced for each barrel of 58° Be'
gasoline.

7.0 pounds of still carbon was produced per barrel of 58° Be'
gasoline.

A typical composition of the so-called carbon deposited in crack-
ing stills is as follows. This sample was extracted with 70° Be'
petroleum naphtha before testing:

Moisture (volatile at 105°C) . 0 00%

Volatile (500°C) ZZZIZZZl!! islos

Fixed carbon 80^42

Ash H;!I"!;i;!H';! 6!50

„ , , 100.00%

Sulpfiur T Ig3%

1^0" 2.76%

KANSAS CITY TESTING LABORATORY

227

X

O

§

^- "^ ^^ ^ -^ ^ g\ N Cti vfl <:b

^ ^^^^^^g^^zis^i^^sg

Fie. 35 — Volume of Oil Vapors at Different Temperatures.

228 BULLETIN NUMBER SIXTEEN OF

The following data represents the operation covering a long
period of time of a very extensively used process for cracking oil,
based on one still.

Gallons of oil charged 8,000

Gallons of oil run in.. 1,800

Gallons of oil treated 9,800

Average time feeding in oil 15 hours

Total hours distilled 37 hours

Pounds coal used to distill 11,000 lbs. per run

Total distillate produced 5,295 gallons

Total 58.5° gasoline produced 3,018 gallons

% distillate •- 54 04%

% 58.5° Be' gasoline in distillate 57.0 %

%. 58.5° Be' gasoline of oil treated 30.8 %

Amount of distillate per hour of distilling 143.1 gallons

% distillate of total charge per hour of distillation 1.469'c

Amount of 58.5° Be' gasoline per hour of distilling 81 6 gallons

% of 58.5° Be' gasoline per hour of distilling 0.83%

Area of still bottom 270 sq. ft.

Gallons of 58.5° Be' gasoline per hour per sq. ft. of heat-
ing area 0 302

Pounds of coal per gallon of gasoline (58.5° Be') 3.625 lbs.

Equivalent gallons of fuel oil per gallon of 58.5° Be'

gasoline 0.25

CALCULATION OF HEAT EXCHANGES IN REFINERY

CONDENSERS.

In calculating amount of water required for condenser, use the
following formula: 2OO g

w =

t^-ti

w = gallons of water required per hour.

ti = incoming temperature of condensed water.

t; = outgoing temperature of condenser water.

g = gallons of gasoline to be condensed per hour.

Heat absorbed in condensing 1 gallon of gasoline to 60°F = 1,550
B.T.U.

Heat absorbed in condensing 1 gallon of kerosene to 60°F = 2,400
B.T.U.

Heat absorbed by oil in distilling off 50% from it as gasoline
and kerosene is 2,100 B.T.U. per gallon of crude oil.

Heat absorbed by oil in distilling to coke is approximately 3,000
B.T.U. per gallon.

Amount of condenser surface required to propei'ly condense one
gallon of gasoline per hour = 2 sq. ft; 1 gallon of kerosene per
hour = 1 sq. ft. This is lessened with cold water and with larger
quantities of water and varies with the length and cross section of
the condenser tubes.

'The cross section of the vapor line should be .05 sq. in. per gal-
lon of gasoline per hour. The cross section of the condenser tubes
may be reduced Vz after first % of length and 14 more after second
Va of length.

'The same water used for condensing the benzine or gasoline frac-
tion in crude distillation may be used to condense the kerosene frac-
tion.

KANSAS CITY TESTING LABORATORY

229

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Fie. 30 — Volunif of Oil Vapors and Steam at Different Temperatures

230

BULLETIN NUMBER SIXTEEN OF

Aluminum Chloride in the Production of Gasoline.

When the heavy fractions of petroleum distillates such as kero-
sene, gas oil, lubricating oils or paraffins are slowly heated with a
small quantity of perfectly dry aluminum chloride, the salt dissolves,
imparting a dark color to the solution. If this dark liquor is then
submitted to slow fractional distillation at a temperature below that
at which aluminum chloride volatilizes, a sweet water white, light
distillate is obtained having all of the properties of high grade light
gasoline that has been subjected to complete refining with sulphuric
acid.

The first use of aluminum chloride for its "catalytic" action in
hastening the synthesis or decomposition of hydrocarbons is set forth
in the well known Friedel & Crafts reaction in a British patent of
1877. Aluminum chloride has long been known to have special action
on various types of hydrocarbons in forming complex compounds of

the hydrocarbons with the
aluminum chloride. The
heating of aluminum
y/^\avff4i chloride with unsaturated
hydrocarbons or olefins
such as amylene leads to
the formation of saturated
hydrocarbons or paraffins
of the series CnH2n+2.
This series of hydrocar-
bons is the one which pre-
dominates in refined gaso-
line made from paraffin
base petroleum. This is
set forth in a paper by
Engler & Routala in 1909
in which amylene gives
yields of pentane, hexane,
heptane, octane and de-
, . , , . , cane by the action of

aluminum chloride. These are the usual paraffin hydrocarbons in
gasoline. The nature of artificial gasoline obtained by the use of
aluminum chloride varies with the nature and origin of the petroleum
products treated.

According to Pictet, kerosene oil of Galicia furnishes 50% and
Kussian oil, 40% of its weight in the form of light gasoline. The
practical use of aluminum chloride as a means of refining petro-
leum and producing gasoline has been set forth bv A. M. McAfee
\l <j, aF^^^'^'I No. 1,127,465 of February 9, 1915. The character of
the McAfee patent is set forth by the following claim:

r.»,«^^i!l^^'U ^?' "^" the treating of petroleum oil, the process which
comprises heating such oil with aluminum chloride for 36 to 48 hours

nil fn^""!""'"^ "'"'^u? ?t secondary gasoline, cooling and separating
oil and aluminum chloride." ' & i' &

«o seo tM

KiK. 37— Yields on Distillation of Heavy
Oils in the Presence of Aluminum
< nlorirle.

KANSAS CITY TESTING LABORATORY

231

It has been the experience of the writer that the action of alumi-
num chloride at high pressures is not effective in producing gasoline
at any faster rate or with any greater facility than with the use of
high temperature and pressure alone. However, when the light gaso-
line is removed as rapidly as it is formed by distillation at atmos-
pheric pressure or slightly above, the rate of formation of gasoline
is infinitely increased over that obtainable in exactly the same con-
dition without the use of aluminum chloride.

At very high pressures, heavy hydrocai'bons may be converted
into gasoline at a rate of I'/f per minute or a 30% conversion in
one-half hour.

In the experiments set
forth herewith, it was
assumed that 3.3% of
gasoline produced per
hour would be a prac-
tical rate for a large
still. The amount of
aluminum chloride con-
sidered necessary for at-
taining this rate is from
5% to 10% and in these
tests 8% or 24 pounds
per barrel of freshly pre-
pared anhydrous alumi-
num chloride were used.
The stock used for the
test was the same as
that used in charging the
Burton pressure stills,
being a mixed gas oil
containing about 15%
of olefins.

The following table shows the normal distillation of this gas oil
without aluminum chloride and at the rate of 3.37c per hour.

Distillation of Burton Still charging stock at rate of 3.3% per
hour without the use of aluminum chloride. Gravity of original
charge = .864 = 32.3° Be',

M

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AXO

Fig. 38 — Comparison of Distillation Curves
of Aluminum Chloride Gasoline with
Natural Gasoline.

Gravity of

Gra\'ity of

%

Time

Temp. ° F.

Fraction

Total Over

Oil Temp., ° F

0

11:06
12:30

262
300

52.7° Be'

410

5

52.7°

Be'

480

10

1:00

370

41.1

46.7

530

15

1:30

490

39.0

44.1

540

20

3:00

499

37.8

42.6

550

25

4:00 P.M.

508

36.2

41.3

560

30

9:07 A.M.

518

35.2

40.2

570

35

9:21

530

33.8

39.2

580

40

9:27

542

33.4

38.6

585

45

9:35

550

32.8

38.0

595

50

9:47

558

32.5

37.4

610

55

10:00

570

31.9

36.8

625

60

10:06

582

31.1

36.4

640

65

10:13

598

30.4

36.0

655

70

10:15

612

29.8

35.4

670

75

10:21

628

29.3

35.0

680

80

10:34

636

28.2

34.6

690

232

BULLETIN NUMBER SIXTEEN OF

The next table shows the distilla-
tion of the same oil with the 8%
of aluminum chloride. In the dis-
tillation with aluminum chloride,
the rate of 3.3% per hour was
fairly closely adhered to until such
a temperature was obtained in the
oil at which the aluminum chloride
began to volatilize. To prevent
this, a temperature was maintained
from this point on, such that the
aluminum chloride would not vola-
tilize. At approximately 60%, it
was not possible to get further
gasoline distillate without carry-
ing over tarry matter or aluminum
chloride compounds. 30% of 58.2°
Be' gasoline, water white and free
from olefins was obtained and 60%
of 55° Be' water white naphtha was
obtained.

TEMPTTBO zoo 280 360 AiO 520 600

FiK. 3y — Comparison of Gravity
of Fractions of Aluminum
Chloride Gasoline and Gasoline
from Other Sources.

%

0
5
10
15
20
25
30
35
40
45
50
55
60

Temp. °F.
70
220
250
274
300
320
330
335
340
345
350
360
366
380

Gravity of
Fraction
Start

Initial B.P.
69.1° Be'
62.0
57.9
54.7
54.5
52.3
52.5
52.0
50.9
52.1
53.5
50.0

Distillation of Burton Still
Charging Stock at rate of 3.3%
per hour with the use of 8% of
aluminum chloride. Gravity of
original charge = .864 = 32.3° Be'.

Gravity of
Total Over

69.1° Be'

65.4

62.9

60.9

59.5

58.2

57.4

56.9

56.2

55.2

55.1

55.0

Color
Water
White
White
White
White
White
White
White
White
White
White
White
White
White

Total Time
0
15'

105'

200'

290'

375'

455'

540'

680'

800'

920'
1105'
1410'
1795'

Interval

15'

90'

95'

90'

85'

80'

85'

140'

120'

120'

185'

305'

385'

DossibL nlSfll K "^^"1«" at rate of 3.3% per hour as long as
that wonUl ^fl^ °"0^^' ^^-l^ continued at the fastest possible rate
that uould allow cracking without volatilizing the aluminum chloride,
flifferpnf .V.li ^^^^Ph showing the vapor and oil temperature at
aiunJn'uni thfoHde'.' ''' distillation with and without t'he use of

alumSm^chJo^r n^^ '^"^i^^^ -^l ^^ ^^'«""^ "^^^e by the use of
tieTrend point ^^'''^ ''''^ '^' ^"^"^^ «* "«™^1 ^^^^^^"^ «f
« i^l^' ^^ ^^^'""P ^^^ relation of the specific eravitv of various
wif'^hruse-o^'ir ''"P"l^' "i^^ ^he naphtha or^'asofineprodS
That the lowov ■.ni^-""'" chlor.de. It is to be noted in these curves
much the samo nfti^ ' ^'^^'^^ ,^"^ '^^^^ '^«'li"g Poi"t fractions are
"mrcos but Th .r.,f ^"'[^^^pondrng paraffin hydrocarbons from other

of aluminum rhol^-'"^" ^'""^''^^ «* ^^^^^ 800 the product by use
ol alummum chloiide is more strictly of a paraffin nature.

KANSAS CITY TESTING LABORATORY

233

660 700 740 7^

F.g. 40 — Olefins

n Aluminum
Chloride Gasoline.

Fig. 40 sets forth the olefin
content of gasoline made by dif-
ferent processes for treating
heavier petroleum hydrocarbons.

Curve No. 1 is that using
aluminum chloride which is es-
sentially free from olefins.

Curve No. 2 shov^^s the olefin
content of Burkburnett crude oil.

Curve No. 3 shows the olefin
content of gasoline produced by
very high pressure cracking.

Curves No. 4 and No. 5 shows
the olefin content of gasoline made
by cracking at 80 to 100 pounds.

Curves No. 6 and No. 7
show the olefin content of gaso-
line produced by cracking at
high temperature, such as vapor
phase processes.

Important Literature on the Subject.

Friedel & Crafts — Aluminum chloride for chemical reactions. Brit-
ish Patent No. 4,769—1877.

C. Engler & 0. Routala — The action of aluminum chloride on amy-
lene. Ber. 42— pages 4,613-20—1909.

Wm. Steinkopf & Michael Freund — The formation of naphthenes
and paraffins from olefins by synthesis of the latter with aluminum
chloride— Ber. 47— pages 411-20—1914.

A. M. McAfee — Aluminum Chloride in the production of gasoline
and its recovery. U. S. Patents Nos. 1,099,096, 1914; 1,127,465, 1915;
1,144,304, 1915; 1,202,081, 1916; 1,277,092, 1918; 1, 277, 328-9, 1918.

Pictet & Lerczynska — The action of aluminum chloride on petro-
leum. Bull. Soc. Chim. No. 19, pages 326-34—1914.

A. M. McAfee — Improvements of high boiling petroleum oil and
manufacturing of gasoline by the action of aluminum chloride. Jour-
nal of Industrial & Engineering Chemistry, Sept., 1915.

W. E. Henderson & W. C. Gangloff — Action of anhydrous alumi-
num chloride upon unsaturated compounds. Journal of American
Chemical Society No. 38, pages 1,382-4—1916. Journal of. Am. Chem.
Soc. No. 39, pages 1,420-7—1917.

A. M. McAfee — Manufacture of gasoline. Metallurgical & Chem-
ical Engineering No. 13, pages 592-7 — 1915.

G. W. Gray— Manufacture of gasoline bv the use of aluminum
chloride. U. S. Patents No. 1,193,540-1—1916.

Alexander and Taber— Producing low boiling hydrocarbons by
heating vapors with Al CU, Fe Cb, or Zn Cb— U. S. Patent, 1,381,098—
June 14, 1921.

Danckwardt— Pat. No. 1,373,653— Apr. 5, 1921.

234

BULLETIN NUMBER SIXTEEN OF

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re- of Heavy Oils and Gasoline Under Cracking
Temperatures.

KANSAS CITY TESTING LABORATORY

235

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KIg. 41;— IToperties of Various Types of Synthetic Gasoline.

KANSAS CITY TESTING LABORATORY

237

Effect of Varying Pressure on the Products of Cracking.

KEROSENE.

Using kerosene of specific gravity 0 8155 in vessel with relation
of vapor space to oil of 2 to 1.

Pressure, atmospheres 30 40 55 75 90

% distillate to 410°F 28.0 32.5 38 0 43.7 45 9

Shrinkage, volume 7r 0.0 0,4 2.4 5.0 7.0

Specific gravity of cracked oil.. .810 .808 .807 .806 .805

Specific gravity of residue 828 .833 .845 .871 .888

Cold pressure, atmospheres 2.5 4.0 6 5 10.0 11,8

\ FUEL OIL.

Fuel oil with specific gravity of 0.908 in vessel with relation of
vapor space to oil of 2 to 1.

Pressure, atmospheres 30 40 55 75 90

% distillate to 410°F 14.3 22.3 25.4 32 5 38.7

Shrinkage, volume % 3 0 3.3 9.0 12.0 14.0

Specific gravity of cracked oil .879 .869 .862 .837 .818

Specific gravity of residue 914 .918 .926 .930 .932

Cold pressure, atmospheres 5 6 10 13 15.5

IOC

BEFORE 1 ^,y^

so

/ yAFTEa

as

80
7S

WATER WHTTE DISTILLATE / /
^°Be— BEFORE CRACHIne \ 1
A»D53°Be -AFTEO CRACKING \ 1

TTl

PEflCENT DISTILLED— \ /

65

60
55
X

GRAVITY CUR^/ES \ /

3 /
^ 1/

45

\

40
35

^ A

ZS

\ /

20

y^ [before

y^FTER ^RACKING

10

yORACHING 1

5

0

DEGREES - ' BA UME GRAVITY

>5 90 6680 75 7065605550454035

30 25 20

Fig. 43 — Relation of Gravity
to Percent Distilled of Water
White Distillate Before unJ
After Cracking.

238

BULLETIN NUMBER SIXTEEN OF

Properties of Water White Kerosene Distillate Before

and After Cracking.

%

Distilling Temperature
Before After

Cracking Cracking

Gravity of Stream

Before
Cracking

After
Cracking

0

2.5
5 0

294° F.

355

363

Room
Room
80' F.

.766=53.2° Be'

.614=98.9° Be'

7 5

366

105

.767 = 52.9° Be'

.634 = 91.7° Be'

10.0

367

130

.768=52.7° Be'

.654 = 84.8° Be'

12 5

370

158

769 = 52.5° Be'

.6 7 = 80.6° Be'

15 0

379

188

.770 = 52.2° Be'

.680 = 76.6° Be'

17 5

381

218

.771 = 52.0° Be'

.695 = 72.1° Be'

20.0

382

237

.772 = 51.8° Be'

.710 = 67.8° Be'

22.5

384

256

.773 = 51.5° Be'

.720 = 65.0° Be'

25.0

391

269

.774 = 51 3° Be'

.730 = 63.3° Be'

27.5

395

282

.774 = 51.3° Be'

.739 = 59.9° Be'

30.0

399

296

.775=51.0° Be'

.749 = 57.4° Be'

32.5

402

310

.776 = 50.8° Be'

.756 = 55.6° Be'

35.0

406

319

.777 = 50.6° Be'

.764 = 53.7° Be'

37.5

408

328

.777 = 50.6° Be'

.769 = 52 5° Be'

40.0

410

340

.778=50.3° Be'

.775=51 0°Be'

42.5

414

352

.779=50.1° Be'

.777 = 50.6° Be'

45.0

417

359

.780 = 49.9° Be'

.780 = 49.9° Be'

47.5

420

366

.780=49.9° Be'

.782 = 49.4° Be'

50.0

423

371

.781 = 49.6° Be'

.785 = 48.7° Be'

52.5

425

376

.782 = 49.4° Be'

.787 = 48.3° Be'

55.0

431

386

.783 = 49.2° Be'

.790 = 47.6° Be'

57 . 5

433

396

.784 = 48.9° Be'

.792 = 47.1° Be'

60.0

437

405

.785=48.7° Be'

.793 = 46.9° Be'

62.5

440

414

.786 = 48.5° Be'

.795=46.4° Be'

65.0

444

418

.787 = 48.3° Be'

.798=45.8 Be'

67.5

448

422

.788 = 48.0° Be'

.798 = 45.8° Be'

70.0

453

429

.789 = 47.8° Be'

.800=45.4° Be'

72.5

457

436

.790 = 47.6° Be'

.802 = 44.9° Be'

75 0

462

443

.792 = 47.1° Be'

.805=44.2° Be'

77 5

468

450

.793=46.9° Be'

.808 = 43.6° Be'

80.0

473

459

.794=46.7° Be'

.812 = 42.7° Be'

82.5

479

468

.795 = 46.4° Be'

.817 = 41.7° Be'

85 0

485

484

.797 = 46.0° Be'

.823 = 40.4° Be'

87.5

493

500

.800 = 45.3° Be'

.830 = 38.9° Be'

90.0

506

523

.803 = 44.7° Be'

.837 = 37.5° Be'

92 5

516

547

.807=43.8° Be'

.851 = 34.7° Be'

95 0

533

600

.812=42.7° Be'

.866=31.9° Be'

97 5

560
608

648
700

936-19.6° Be'

100 0

Gravity of sample

.7845=48.9° Be'

.766=53.2° Be'

KANSAS CITY TESTING LABORATORY

239

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Fig-. 44-

3 S s § § .§ ^

-Relation Between Gravity and Distilling Temperature of
Paraffin Base Oils Before and After Cracking.

240

BULLETIN NUMBER SIXTEEN OF

FRACTIONAL GRAVITY DISTILLATION ANALYSIS OF COAL

TAR BENZOL.

Laboratory Number, 44118; Specific Gravity, 0.880; °Be' U. S.,
29.0°; Cold Test, 40°G.

Temp.

Gravity of

Gravity of

Gravity of

%

Time

°F.

Fraction

Total Over

Stream

3:25

0

3:31

173
178

5

3:37

179
180

0.882=28.9° Be'

0.882=28.9° Be'

0.881 = 29.1° Be'

10

3:42

180
180

0.881 =29. l°_Be'

0.881=29.1° Be'

0.882=28.9° Be'

15

3:47

180
180

0.883=28.7° Be'

0.882=28.9° Be'

0.882=28.9° Be'

20

3:51

180
180

0.882=28.9°^Be'

0.882=28.9° Be'

0.882=28.9° Be'

25

3:56

180
180

0.882=28.9° Be'

0.882=28.9° Be'

0.882=28.9° Be'

30

4:00

181
181

0. 882=28. 9°^Be'

0.882=28.9° Be'

0.882=28.9° Be'

35

4:05

182
182

0.882=28.9° Be'

0.882=28.9° Be'

0.881=29.1° Be'

40

4:10

182
182

0.881=29.1° Be'

0.881 = 29.1° Be'

0.881=29.1° Be'

45

4:15

182
182

0.881=29.1° Be'

0.881=29.1° Be'

0.881=29.1° Be'

50

4:19

182
183

0.881=29.1° Be'

0.881=29.1° Be'

0.880=29.3° Be'

55

4:23

183
183

0.880=29.3° Be'

0.881=29.1° Be'

0.880=29.3° Be'

60

4:28

184
184

0.880=29.3° Be'

0.881=29.1° Be'

0.880=29.3° Be'

65

4:33

184
185

0.880=29.3° Be'

0.881=29.1° Be'

0.880=29.3° Be'

70

4:38

186
186

0.880=29.3° Be'

0.881 = 29.1° Be'

0.880=29.3° Be'

75

4:43

187
188

0.880=29.3° Be'

0.881 = 29.1° Be'

0.880=29.3° Be'

80

4:48

189
190

0.880=29.3° Be'

0.881=29.1° Be'

0.879=29.4° Be'

85

4:53

192
196

0.879 = 29.4° Be'

0.880=29.3° Be'

0.879=29.4° Be'

90

4:57

199
205

0.879=29.4° Be'

0.880=29.3° Be'

0.877=29.8° Be'

95

5:01

216

0,876=30.0° Be'

0.888=29.3° Be'

0.876=30.0° Be'

100

5:10

225

0.876=30.0° Be'

0.880=29.3° Be'

0.876=30.0° Be'

KANSAS CITY TESTING LABORATORY

241

FRACTIONAL GRAVITY DISTILLATION ANALYSIS

of Benton Process Gasoline; Specific Gravity, 0.758; °Be' U. S., 54.7
°Be' Tag, 55.1°; Olefins, 16.0%.

Temp.

Gravity of

Gravity of

Gravity of

%

Time

°F.

Fraction

Total Over

Stream

10:09

0

10:14

85
155

5

10:22

164
171

0.694 = 72.4° Be'

0.694=72.4° Be'

0.694=72.4° Be'

10

10:28

176

184

0.695 = 72.1° Be'

0.694 = 72.4° Be'

0.689 = 71.2° Be'

15

10:35

188
193

0.701 = 70.3° Be'

0.696 = 71.8° Be'

0.705 = 69.2° Be'

,20

10:42

199
206

0.710 = 67.8° Be'

0.700 = 70.6° Be'

0.714 = 66.6° Be'

25

10:48

211
216

0.718=65.5° Be'

0.704 = 69.5° Be'

0.722 = 64.4° Be'

30

10:54

222
228

0.727 = 63.1° Be'

0.707 = 68.6° Be'

0.731 = 62.0° Be'

35

10:58

234
238

0.735 = 61.0° Be'

0.711 = 67.5° Be'

0.738 = 60.2° Be'

40

11:03

244

248

0.742 = 59.2° Be'

0.715 = 66.4° Be'

0.745 = 58.4° Be'"

45

11:09

254

258

0.748 = 57.6° Be'

0.719=65.3° Be'

0.751 = 56.9° Be'

50

11:14

264
270

278

0.755 = 55.9° Be'

0.722 = 64.4° Be'

0.758 = 55.1° Be'

55

11:19

0.761=54.4° Be'

0.729 = 62.6° Be'

0.770 = 52.2° Be'

283

60

11:25

290
297

0.767=52.9° Be'

0.729 = 62.6° Be'

0.770 = 52.2° Be'

65

11:29

306
312

0.773 = 51.5° Be'

0.732 = 61.8° Be'

0.776=50.8° Be'

70

11:34

320
328

0.779 = 50.1° Be'

0.736 = 60.7° Be'

0.781 = 49.6° Be'

75

11:41

336
348

0.784 = 48.9° Be'

0.739=59.9° Be'

0.788 = 48.0° Be'

80

11:46

362
371

0.793 = 46.9° Be'

0.742 = 59.2° Be'

0.797 = 46.0° Be'

85

11:53

388
406

0.801 = 45.1° Be'

0.746 = 58.1° Be'

0.808=43.6° Be'

90

11:59

428
460

0.815=42.1° Be'

0.749 = 57.4° Be'

0.823=40.4° Be'

95

12:05

492

0.832=38.5° Be'

0.754 = 56.1° Be'

Remarks: 36 cc. residuum; loss, M%.

242 BULLETIN NUMBER SIXTEEN OF

Formulae for Calculating the Cost of Manufacture of
Natural and Synthetic Gasoline.

Key to Symbols.

Be' = gravity of crude oil in degrees Baume'.
n = per cent of natural gasoline of 58 gravity in the crude,
c = value of crude oil at refinery in dollars per bbl.
f = value of fuel oil at refinery in dollars per bbl.
s = value of gas oil at refinery in dollars per bbl.
a = per cent of artificial or synthetic gasoline in crude.

(1) % artificial gasoline obtainable by commercial cracking.

[100 — n] [25 + 1.45 (Be — 10 — .3n)]

a = —

100
Total gasoline = n + a

(2) Cost of gasoline per gallon vi^hen made by skimming only =

c + 35 — f (.95 — .Oln)

.42 n

(3) Cost of gasoline per gallon when made by cracking and skim-

ming =
c + .40 + a (.0202 + .015 f ) — f (.95 — .01 n)

.42 (a +n)

(4) Cost of gasoline per gallon when made by cracking gas oil =

$2.02 + 1.41 s — .05 f

42
ILLUSTRATION OF ABOVE FORMULAE.

(1) Total gasoline from crude oils.

Gravity Natural Artificial Total

Mexia, Texas crude 37°Be' 5 68 73

Burkburnett, Texas 40 40 37 77

Ranger, Texas 38 25 49 74

Mexico, Panuco 12 5 34 39

Tuxpan, Mexico 17.5 15 32 47

(2) Cost of gasoline bv skimming only —

c = $2.00 per bbl.
n = 25% Be' = 37
f = $1.00 per bbl.

2.35— (.95 — .25)

= 15.7c per gallon

.42) (25)

(3) Cost of gasoline by skimming and cracking — using values given

above.
2.00 + .40 + 47.4 (.0202 + .015) — (.95 — .25)

= lie per gallon

.42 (47.4 + 25.0)

(4) Cost of gasoline made from gas oil.

With s = $1.25 and f = $1.00
Cost of cracked gasoline.
$2 02 + 1.75 — .05

^c— — 8 9c per gallon

42

KANSAS CITY TESTING. LABORATORY 243

Costs of Refining Petroleum.
(By Benner in "Petroleum," May, 1920)

COST
(Figured on Daily Basis)

2,000 barrels crude per day @ ?3.75 per barrel |7,500.00

Pipe line charges, 30c per barrel 600. no

Sala^ie^3 and labor . . 250.00

Fuel, power and water 200.00

Taxes and insurance 30.00

Incidentals 50 00

Plant depreciation 50.00

$8,680.00

OUTPUT
(Figured on Daily Basis Burkburnett Crude)

Gasoline, 34 per cent, 28,560 gals. @ 21c per gal. (wholesale) $ 5,997.60

Kerosene, 12 per cent, 10.080 gals. @ 14c per gal. (wholesale) 1,411.20

Fuel oil, 50 per cent, 1,000 bbls. @ $2.60 per bbl. (wholesale) 2,600.00

$10,008.80
Loss, 4 per cent.

Daily profit 1,328.80

Yearly profit 478,440 00

Profits from Petroleum Refining.

(By F. W. Freeborn in Oil & Gas Journal, 1920)

Profits of Skiinniing: Plant (191G)
Based on aiarket Price Aug., 1916, and Charg:ins 2,500 Bbls. of Crude Oil Per

34-Hour Day.

YIELD PER DAY.

Gasoline 30% 31,500 gal. @ $0.18 'i ^^•?"-^2

Kerosene W. W. 6% 6,300 gal. @ .OS ??iXn

Kerosene P. W. 9% 9,450 gal. @ .06 56(.00

Gas oil 5% 5,250 gal. @ .04% 236. 2»

Fuel oil 48% 50,400 gal. @ .04y2 2.268.00

Loss 2% 2,100 gal. 0.00

100% 105,000 gal. _^___

Total sales per day $9,402.75

COST PER DAY.

Crude oil run 2,500 bbls. @ $2.05 $5,125.00

pnael oil to burners & stills, 397 bbls. @ $1.89 7o0.33

Electric light & power for motors 10.00

Chemicals for treating oil and water 15.00

Salaries charged @ 2.7c per barrel 67.50

Total cost per day $5.967.83

Net profit per day ^'^■''''I'?^

Net profit per barrel '•^^c

Cost to refine one barrel of crude ■"'•'^

244 BULLETIN NUMBER SIXTEEN OF

Profits of Skimming Plant, 1920 (Freeborn)

Based on Market Prices April, 1920, and Charging 2,500 Barrels of
Crude Oil Per 24-Hour Day.

Yield Per Day.

GasoMne 30% 31,500 gals. @ $0.21 Vj % 6,77:; r,0

W. W. Kerosene 6% 6,300 gals. @ .12 756.00

P W. Kerosene 9% 9,450 gals. (S' .lOVj 992.25

Gts oil 5% 5,250 gals. (» .0^ 472.50

Fuel oil 48% 50,400 gals. @ .0725 3.654.00

Loss 2% 2,100 gals. 0.00

100% 105,000 gals.
Total sales per day $12,647.25

Cost Per Day.

Crude oil run, 2,500 barrels H |4.00 110,000.00

Fuel oil to stills & boilers, 397 bbls. @ $3.05 1,210.85

Light & Electric power for motors 13.00

Chemicals for treating oil & water 18.75

Sal-tries charged to operation 249.38

Total cost per day 11,491.98

Net profits per day $ 1,155 27

Net profit per barrel .47

Cost to refine one barrel crude .597

Profits From Lubricating and Paraffin Plant (1920).

Ba£e<l on market pricesof April, 1920, and h?ndling distillate from 2,500
barrels of crude oil per day. Distillate han^Jled 33% of crude run. (Freeborn.)

Yield Per Day.

Light lubricating oil 15% 8,347.5 gals. @ .$0.35 $ 2,92163

Medium lubricating oil 11% 6,121.5 gals. @ .35 2,142.52

Heavy lubrjcaiing oil 9% 5,008.5 gals. (S> .45 ...... .. 2.253.83

Heavy motor oil 5% 2,782.5 gals. @ .60 1.669.50

raraffin wax 6% 3.339 gals.

22.026 lbs. @ .08 1,762.08

T^Uf' "'• 48% 26,712 gals. @ .0725 1,936.62

J-"»» 6% 3,339 gals @ .00 0.00

100% 55,650 gals.
Total sale per day ^ 12, 868. 18

Cost Per Day.

Fuel oil 1,325 bnrrel.« @ $3.95 $4 nil "5

Fuel oil to boilers & stills 154 bbl. $3.05.. '4«'i'70

Klectric light & power iVoO

ChemlcaUs and fuller's earth "50 00

Salaries charged to operation .30o! 00

TotuI costs per day 77777777. 5.075.95

Ni t profit per day "^ T^eioTis

Net profit per barrel ' r 74

«'o.-l to refine one barrel.... -o

.Net profit per year on 80% operating Vinie.' .'.".' ■> 990 15716

KANSAS CITY TESTING LABORATORY 245

PROFITS OF COMPLETE REFINERY (FREEBORN).
Based on Market Price April, 1920, and Charging 2,500 Bbls. of Crude

Oil Per 24-Hour Day.
Yield Per Day.

Gasoline 30% 31,500 gals. r« $0.21V2 $ 6,772.50

AV. W. Kerosene, 45° 6% 6,300 gals. @ .12 756 00

P. W. Kerosene, 42° 9% 9,450 gals, (ffi .lOVs 992 25

Gas oil 5% 5,250 gals, ip' .03 472.50

Paraffin Dist. 25% 26,250 Return stock for lub. oils and wax

Flux 22% 23.100 gals. @ .0725 1,674.75

Loss 03% 3,150 gals. 000.00

100%

2,500 bbls. crude oil charged 100%

625 bbls. of paraffin distillate 25% off

Light lubricating oil 2S% 7,350 gals. @ SO. 35 '. 2.572.50

Medium lubricating oil 24% 6,300 gals. @ .35 2,205.00

Heavy lubricating oil 16% 4,200 gals. @ .45 1,890 00

Heavv motor oil 14% 3.675 gals. @ .60 2,205.00

Paraffin wax 12% 20,790 lbs. @ .08 1,663.20

3,150 gals.
Loss 6% 1,575 gals.

100% 26,250 gal.s.

Total sales $ 21,203.70

Total Costs.

Crude oil run 2,500 bbls. fi' $4.00 $10,000.00

P'uel oil to boilf-rs & stills, 432 bbls. @ $3.03 1,317.60

Electric light for power and motors 25.00

Chemicals and fuller's earth 265.00

Salaries charged to operation 550.00

Total costs 12.157 60

Net profits per day $ 9,046.10

Xet profit per barrel 3.61

Cost to refine one barrel .86

Net profit operating on S0% time basis 2,641,461.20

Profits From Filtering and Cold Settling Plant (Freeborn).

Filtering and Cold Settling Plant for rr.akm? Bright Stocks from Cylinder
Stock, installed in conjunction with Skimming Plants having a charging capicity
of 2.500 bbls. of crude per day. Yield of Cylinder stock from crude will average
from 10% to 20%. The following figures based on 15%:
15% of 2,500 — 375 bbls. or 15,750 gallons to he handled. Co'd settled

stock, 15% or 15,750 gal. @ $0.75 $11,812.50

Cost to produce:

Fuel oil— 375 bbls. @ $3.05 $1,113.75

Steam and electric power 10.00

Chemicals and fuller's earth 175.00

Salary charged to operation 95.00

Loss of 56" naphtha in mix and wash 141.00

General maintenance, etc IQiVOO $ 1,664.75

Total net profit per d.ay 10,147.75

Net profit per barrel 27.06

Cost to refine one barrel 1.39

Net profit per year figuring on operating 80% or 292 days 2,963,143.00

The nece.ssary equipment to be added to a skimming plant to make bright
stocks froiTi cylinder stocks, such as refrigerating plant, filtering plant, cold
.settling tanks and steam stills for reclaiming naphtha from cold settled stocks
and filter wash, will cost approximatelv $151,146.25.

Net profits per day $10,147. 75x292 diys. 80% time — $2,963,143.00.

Cost of Construction (Freeborn).

This represents a profit on the investment of much more than 1000%.

The question is often asked, what will a refinery cost? We are giving
below in a general way these costs. These include neither tank cars nor work-
ing capital but only cost of refinery ready to operate.

We have assumed a capacity of 2,500 barrels and will s.iy that a smaller
plant will co.st a little more and a larger one a little less per barrel.

Topping plant 2,500 bbl.«. @ $100 per barrel or $250,000.00

Complete refinery, 2,500 bbls. (» $300 per barrel or 750.000 00

Complete lubricating plant — Added to present topping plant of 2,500

bbls. would be ?S00 per bbl. of lubricants which is 625 bbls. or.. 500.000.00
Filtering and cold settling plant — .\dded to 2,500 bbl. topping pi »nt,

$400 per bbl. for 400 bbls. or 160.000.00

246 BULLETIN NUMBER SIXTEEN OF

c

COSTS OF REFINING IN 1922.

In 1922 (April) it may be assumed that a skimming plant will cost $100
per barrel ptr dav capacity including limited storage hut not including pipe
lines outside of refinery or tank cars. It costs approximately 50 cents to distill
a barrel of crude oil to coke. The cost of making 1 barrel of gasoline by
cracking is $2 to |5 and 1 H to 1% barrels of gas oil Is required to make it.
With ''as oil at $1.40 per barrel, the total cost of a barrel of cracked gasoline
is $3 75 to $10.00. With fuel oil at $1.00 and gas oil at $1.26 a plant in
Illinois is able to make 600 barrels of gasoline per day at a total cost of $:i.70
per barrel.
The profit derived from a refinery depends upon:

The price of crude oil.

The location of the particular refinery in respect to availability of crude oil
and the markets for the refined products.

The general market for refined products.

The quality of the crude oil available.

The amount of fuel oil, gas oil and unprofitable products.

The method of refining and refinery management.

The working and reserve capital.

The refinery making the most profit as a general rule is the one that
makes the greatest amount of gasoline and lubricating oils as they are the most
."table products of petroleum.

COST OF REFINING CALIFORNIA PETROLEUM.
(Report of Federal Trade Commission, 1921)

The cost of refining crude petroleum is shown in detail for five companies
named for the period 1916 — June 30, 1919, and for two companies from igi*
to the latter date. The cost of refining a barrel of crude petroleum including
the cost of the crude for all companies combined increased from $0,738 per
barrel in 1916 to $1,259 for the first half of 1919. The crude petroleum costs
ar<-- taken at the actual cost of production, or at purchase price, if bought. TTiere
was a wide range in the costs for individual companies. In 1916, the lowest
cost for a particular company was $0,602 and the highest $0.S45. In 1919, the
lowest cost was $0.95 and the highest $1,631. The companies showing high
costs are those purchasing a large proportion of the crude petroleum they refine.

The principal element of cost for a barrel of refined petroleum products is
the raw material — crude prtrcleum — even when the crude is charged to rhe
refinery at its cost of production plus transportation cost. On this basis, the
raw material represented 79.4% of the total cost in 1914 and ab'-ut 74%. in
1919. The refinery operating expense was about 13.5% in 1914 and 17.7% in
1919. while the general and administrative and depreciation combined were 7.1%
in 1914 and S.3% in 1919. The refining labor cost is a very small factor in
the cost of a barrel of refined petroleum products, and during the period cov-
ered, it varied from only $0,012 in 1914 to $0,046 in 1919.

Typical

Actual STANDARD STILLS. .,^.,^

Capacity Dimensions Weight Cost

III 1^11 22,000 $2,120.00

\M .V'll 24.000 2,250.00

m 10x30 2S,000 2,550.00

y^i IJ'^IO 36,000 3,225.00

B?ft WHl ^^'"^J" 3,685.00

fijX J2X30 36,000 2,810.00 K. D.

"" 12x30 36.000 3,580.00 Riveted

.i'Tf, AGITATORS. Tvpicai

i^apHouy Dimensions Weight Cost

ill \V^ll l^'SOO 2.085.00

Yil lO^^O 22,000 2.260.00

600 Ir'';^ '''•"OO 2,500.00

?nS VV^lt 36,000 2,680.00

innn 15x35 44,400 3 120 00

Wll ;^?« 55,000 3.845.06

""' ''Ox.fS 61.000 4,260 00

STANDARD CONDENSER BOXES.
si,p ^ Riveted Up. Seiung

Sxsi"-. Compartments Weight Price

10.000 $ 855.00

10,700 920.00

12,700 1,100.00

20x8x,io , Knocl^ed Down.

.lOxfx.'tO ? 22,600 1,450.00

J 32,400 2,040.00

■• 42,000 2,610.00

I 0x6x30
10x8x30

lOxHx.lO

KANSAS CITY TESTING LABORATORY

247

Gasoline.

Gasoline as now found.on the market is %"}i^ture of petroleum

hydrocarbons, having an initial boilmg point of f^^™/^ o^. ^'^./o^?.J'
anendboilingpointof from 360° F to 4bO°F, gravity of 55 to 61 Be.,

/9/e

/9/r

~J^ /9I4 1^/^ /^/'^

Fig 47 — The Demand for Gasoline.

a sweet to oily aroma, a water white color, specific heat of 0.50, and
heat of vaporization of 130 B.T.U. per pound.

The particular hydrocarbons composing it belong to a general
group'knoTn'rthe p'araffins. Other types of hydrocarbons are ^^c^^^

Name

1. Pentane

2. Hexane

3. Heptane

4. Octane

5. Nonane

6. Decane

7. Undecane

Boiling
point
97°F

156^

209"

258°

302=

343°F

383°F

'F

°F

'F

Specific
gravity
0 630
0.670
0 697
0.718
0 740
0.750
0.760

Baume' vaporization cal-

eravitv ories per gram

92.2° 84 0

78.9° 80.5

79.9° 74.0

65.0° 71.5

59.2° 67.5

56.7° 64.5

542° 61.5

248

BULLETIN NUMBER SIXTEEN OF

The following aromatic compounds are produced by pyrogenic de-
composition of heavy hydrocarbons and rarely exist naturally in crude
petroleum.

They are produced by the cracking of oil in the vapor phase
and at high temperatures and occur in artificial or what has been
called "synthetic" gasoline. Their chief origin is in byproducts from
the coking of coal.

Name Boiling Point Specific gravity Baume' gravity

Benzol (CoH«) 176 °F 0.880 29.1°

Toluol (CoH=CH3) 232 °F 0.872 30.6°

Xylene (C«H.(CH3)2 29rF 0.882 28.7°

A small amount of these hydrocarbons in commercial gasoline
very materially affects the gravity.

The character of gasoline is governed almost entirely by its
use for automobiles. It is also used to some extent for stove gasoline
and for cleaning purposes, in which case it has lower end point and
a higher Baume' gravity.

Gasoline originates from one or more of the following sources:

1. The natural product distilled from crude oil. This constitutes
about 70% of the total on the market (1921).

2. As a condensate from natural gas and known as casinghead
gasoline. This constitutes about 59f of all gasoline and is always in-
corporated with heavy hydrocarbons such as naphtha or with gasoline
distilled from a heavy crude or with gasoline made by cracking.

3. The light hydrocarbons produced by the pyrogenic decompo-
sition of heavy petroleum residua. This constitutes about 25% of the
market gasoline and tends to have a slight amount of aromatic com-
pounds.

/S'/i/ /9/9 /9eO'

I' IK. IS— Productior>, Consumption and Stock

s of Gasoline.

KANSAS CITY TESTING LABORATORY 249

The most desirable properties of gasoline are low end point and
a low initial boiling point, the usual refiner's practice being to call
everything gasoline which distills up to a temperature of 410°F. This
practice in a light crude gives a 58° Be' product, although in the un-
usually light crudes a 61° product is obtained and in heavy crudes a
gravity as low as 54° may be obtained. Light crudes such as those
from Mexia, Tex., give as high as 20';/c of naphtha without any gaso-
line but when this naphtha is blended with about 25% of casinghead
gasoline it gives a good motor gasoline.

Figure 39 shows the relation of the boiling point to the specific
gravity of ordinary market gasoline. Gasolines containing consider-
able olefins, aromatics or naphthenes have a higher relation of specific
gravity to boiling point than do gasolines composed entirely of par-
affin hydrocarbons.

Figure 49 shows the relation of the boiling temperature to the
percentage distilled over in ordinary commercial gasoline. These
curves show that the gravity alone is not a good measure of the
quality of a gasoline. For example, a 58° gravity gasoline in one
case has an initial boiling point of less than 100 °F and in another
case has an initial boiling point of 190 °F. A naphtha blended with
casinghead will have a very high gravity test, but will show a very
low initial boiling point and a very high end point.

COMPARISON OF GASOLINE SAMPLES COLLECTED BY BU-
REAU OF MINES.

January, 1921 and July, 1921.

First End Avg.

District Date Drop 20% 50% 90% Point B. P.

New York Jan., 1921 117 206 264 363 417 265

Julv, 1921 125 208 265 365 422 268

Difference " +8 +2 +1 +2 +5 +3

Washington Jan., 1921 118 201 259 385 439 270

July, 1921 130 204 263 387 442 274

Difference +12 +3 -|-4 +2 +3 +A

Pittsburgh Jan., 1921 92 171 248 391 430 244

July, 1921 112 181 247 382 435 259

Difference +20 +10 —1 —9 +5 +15

Chicago Jan., 1921 117 191 248 387 439 264

July, 1921 125 202 261 389 444 273

Difference +8 +11 +13 +2 +5 +9

New Orleans Jan., 1921 123 211 270 366 428 272

July, 1921 131 214 279 376 427 279

Difference +8 +3 +9 +10 —1 +7

St. Louis Jan., 1921 114 202 271 381 444 274

July, 1921 128 205 268 383 441 276

Difference +14 +3 —3 +2 —3 +2

Salt Lake City Jan., 1921 112 206 282 397 439 285

July, 1921 126 200 256 353 401 259

Difference +14 —6 —26 —44 —38 —26

San Francisco Jan., 1921 121 210 267 355 417 265

July, 1921 129 206 258 356 421 265

Difference +8 — 4 —9 +1 +4 Same

8 Districts Jan., 1921 113 197 261 378 431 265

July, 1921 125 201 261 376 432 269

Difference +12 +4 Same —2 +1 +4

Federal Specifications Nov. 25, 1919 140 221 284 374 437

250

BULLETIN NUMBER SIXTEEN OF

600

f/r^t /O 20 30 40 30 60 70 80

90 fr?a
Po/nf

FiK. 49— Di.stillation Curves of Gasoline Sold in 1921 (U. S. B. M.)

KANSAS CITY TESTING LABORATORY

THE COMBUSTION OF GASOLINE.

Average Results of Tests on Eleven 5-passenger Cars.

(See J. I. and E. Chem. Jan. 1921, Page 51.)

251

CONDITION
OF TEST

Engine racing

Engine idling

Three per cent grade (up)

15 miles per hour

10 miles per hour

3 miles per hour

Down 3'^c grade —

15 miles per hour

10 miles per hour

3 miles per hour

Level grade —

15 miles per hour

10 miles per hour

3 miles per hour

Miles

per
Gallon

13.2

12.7

6.2

24.5

22.8

9

16
16

7

Com-
pleteness
of Com-
bustion

70
69

75
75

72

70
70
72

76
72
72

Lbs. Air
per Lb.
of Gaso-
line

12.2-
11.8

12.6
13.0
12.2

12.3
12.3
12.9

14.4
12.7
12.6

Analysis of Exhaust Gas
Per Cent by Volume

CO2 O2 CO CH4 H

9.1
8.9

10.2
9.9
9.8

9.5
8.6
9.5

9.3
9.3
9.1

1.5

1.4

1.1
1.5
0.9

1.4
1.4
1.5

2.2
1.9
1.6

6.9
7.6

5.7
5.7
6.5

6.5
7.0
6.0

5.6
6.3
6.7

0.8
0.6

0.6
0.5
0.6

0.9
0.7
0.7

0.8
0.6
0.6

3.0
3.7

2.6
2.5
3.0

2.9
3.1
2.7

2.8
3.1
3.0

N2

78.8
77.8

79.8
79.8
79.2

78.8
79.2
79.6

79.3

78.8
79.0

EFFECT OF CARBURETOR ADJUSTMENT ON GASOLINE CON-
SUMPTION AND EXHAUST GAS COMPOSITION.

Four-cylinder roadster, engine 4% in. bore x 4% in. stroke;

Johnson carburetor; intake air and manifold heated; using gasoline

66.4°Be' distillation lO'/r, 127°F; 50%, 225°F, dry 441°F; average

239°F. Tests at 15 miles per hour ascending a 39''^ grade of asphalt

in good condition.

Gasoline consumption,

miles per gallon 14.9 13.9 10.6 8.8

Exhaust gas analyses, per
cent —

CO. 13.4 12.0 10.2 6.5

0. 1.7 1.4 0 3 1.2

CO 1.2 2.0 6.4 11 6

CH4 0.2 1.1 0.8 1.0

H. .... 0.0 0.0 24 6.4

N. ._. 83.5 83.5 79.9 73.3

Carburetor Adjust-
ment, lbs. air per lb.
gasoline 14.5 14.2 11.8 9.9

Per cent completeness of

combustion 95 85 74 56

Condition of exhaust clear clear slightly smoky smoky

Operation irregular smooth excellent poor povi^er

TABLES FOR COMPUTING AUTOMOBILE HORSE POWER.
(S. A. E. Horse Power Table.)

Four cycle Two cycle

Limit of error, .005 Limit of error, .005

D^'N D-N

HP = HP =

2.5 1-5151

D = diameter or bore of cylinder in inches.
N = number of cylinders.

252

BULLETIN NUMBER SIXTEEN OF

KANSAS CITY TESTING LABORATORY

IWc

AVERAGE COMPOSITION BY VOLUME OF EXHAUST GAS

FROM TESTS OF 23 CARS AT 15 MILES PER HOUR.

Level grade Ascending 3% grade

8.9 7o 9.6%

2.3 1.3

6.3 6 4

0.9 0.6

3.0 2 9

Carbon dioxide ...

Oxygen

Carbon monoxide

Methane

Hydrogen

Nitrogen 78.6

79 2

Total 100.0% 100.0%

Exhaust gas at 65 °F and 29.92 in Hg., level grade = 988 cu. ft.
per gallon of gasoline.

eO /9 /<? /T- /6 /5" M /7 /? // /O 9

V\S- 51 — Relation of Power and Combustion Efficiency in Gasoline

Engines.

ULTIMATE COMPOSITION OF GASOLINE.

Specific gravity 0.713

Carbon 84 3%

Hydrogen 15.7%

Calorific value, 21,300 B.T.U. per lb. = 130,000 B.T.U. per gal.

EXHAUST GAS FROM 1 GAL. GASOLINE ON LEVEL GRADE

TESTS CONTAINS:

988x6 3 = 62.2 cu. ft. CO
988x0.9= 9.1 cu. ft. CH.
988x3.0= 2.9 cu. f t. H^

254

BULLETIN NUMBER SIXTEEN OF

;

I

5v-
It*

/yv Exj^Auar Gas.

\

Fig. 52 — Relation of Car-
bon Monoxide to tlie Gaso-
line Mixture in Gasoline
Engines.

N.

tA r/O "aF'A/j^ ta CiASiii-iMii^iROUfJ&S

/6

TOTAL HEAT IN UNBURNED GASES PER GALLON GASOLINE.

62.2x320 =19,900 B.T.U.
9.1x1000= 9,100 B.T.U.
29.6X 332= 9,500 B.T.U.

38,500

Gross B. T. U. per cu. ft. at 65=
38,500
=29.6%

F. and 29.92 in Hg.

130,000
29.6% of the total heat of the gasoline goes out in the exhaust in the
form of combustible gases.

EFFICIENCY OF AUTOMOBILES MOVING ON LEVEL GROUND

AT 35 MILES PER HR.

Water radiator and engine radiation 40%

Exhaust gas heat and pipe resistance of pipe 36%

Engine friction 6%

Engine power — transmitted 18%

Transmission friction 3.5%

Rear tire friction 5.0%

Front tires and wheels 2.5%

Air resistance 7.0%

Total .18.0%

The apparent flexibility of the engine is governed largely by re-
ducing the last four items. This is largely accomplished by lubrica-
tion and tire inflation.

KANSAS CITY TESTING LABORATORY 255

U. S. Specifications for Gasoline.
(Technical Paper 298 Bureau of Mines.)

AVIATION GASOLINE, FIGHTING GRADE.
General :

1. This specification covers the grade of gasoline used by the
United States Government and its agencies as a fuel for fighting
planes where the highest efficiency is required.

2. The gasoline shall be free from undissolved water and sus-
pended matter.

Properties and Tests:

3. Color: The color shall be not darker than 25 Saybolt.

4. Doctor test: The doctor test shall be negative.

5. Corrosion test: One hundred cc of the gasoline shall cause
no gray or black corrosion and no weighable amount of deposit when
evaporated in a polished copper dish.

6. Unsaturated hydrocarbons: Not more than 1.09'c of the gaso-
line shall be soluble in concentrated sulphuric acid.

7. Distillation range:

When 5'^/c of the sample has been recovered in the graduated re-
ceiver, the thermometer shall not read more than 65°C (149°F) or
less than 50° C. (122° P.).

When 50 7f has been recovered in the receiver, the thermometer
shall not read more than 95 °C (203 °F).

When 90% has been recovered, in the receiver, the thermometer
shall not read more than 125°C (257°F).

When 96 7c has been recovered in. the receiver, the thermometer
shall not read more than 150°C (302°F). The end point shall not be
higher than 165° C. (329° F.).

At least 96% shall be recovered as distillate in the receiver from
the distillation.

The distillation loss shall not exceed 2% when the residue in the
flask is cooled and added to the distillate in the receiver.

8. Acidity: The residue remaining in the flask after the dis-
tillation is completed shall not show an acid reaction.

9. The United States War Department requires the fighting
grade to be colored red after inspection and acceptance.

All tests shall be made according to the methods for testing
gasoline adopted by the Interdepartmental Petroleum Specifications
Committee.

AVIATION GASOLINE. DOMESTIC GRADE.
General:

1. This specification covers the grade of gasoline used by the
United States Government and its agencies for aviation fuel where
the fighting grade is not required.

2. The gasoline shall be free from undissolved water and sus-
pended matter.

Properties and Tests: .,r n i n.

3. Color: The color shall be not darker than 25 baybolt.

4. Doctor test: The doctor test shall be negative.

256 BULLETIN NUMBER SIXTEEN OF

5. Corrosion test: One hundred cc of the prasoline shall cause
no gray black corrosion and not weighable amount of deposit when
evaporated in a polished copper dish.

6. Unsaturated hydrocarbons: Not more than 2.0% of the
gasoline shall be soluble in concentrated sulphuric acid.

7. Distillation range:

When 5% of the sample has been recovered in the graduated re-
ceiver, the thermometer shall not read more than 75°C (167°F) or
less than 50°C (122°F).

When 50% has been recovered in the receiver, the thermometer
shall not read more than 105°C (221°F).

When 90% has been recovered in the receiver, the thermometer
shall not read more than 155°C (311°F).

When 96% has been recovered in the receiver, the thermometer
shall not read more than 175°C (347°F).

The end point shall not be higher than 190° C. (374" F.).

At least 967o shall be recovered as distillate in the receiver
from distillation.

The distillation loss shall not exceed 2% when the residue in the
flask is cooled and added to the distillate in the heceiver.

8. Acidity: The residue remaining in the flask after the dis-
tillation is completed shall not show an acid reaction.

All tests shall be made according to the methods for testing gaso-
line adopted by the Interdepartmental Petroleum Specifications Com-
mittee.

MOTOR GASOLINE ("NEW NAVY").
General:

1. This specification covers the grade of gasoline used by the
United States Government and its agencies as a "fuel for automobiles,
motor boats and similar engines.

2. The color shall be not darker than No. 16 Saybolt.

3. A clean copper strip shall not be discolored when submerged
m gasoline for 3 hours at 122°F.

Properties and Tests:

4. Distillation range:

When the first drop has been recovered in the graduated re-
ceiver, the thermometer shall not read more than 60°C (140°F).

When 20% has been recovered in the receiver, the thermometer
fchali not read more than 105°C (221°F).

When 50% has been recovered in the receiver, the thermometer
Khali not read more than 140°C (284°F).

When 90% has been recovered in the receiver, the thermometer
shall not read more than lOO^C (374°F).

The end point shall not be higher than 225°C (437°F).

.u •^M^^^^^ ^'^''^" ^^^^^ ^'^ recovered as distillate in the receiver from
the distillation.

All tests shall be made according to the methods for testing
gasoline adopted by the Interdepartmental Petroleum Specifications
Committee. ^

KANSAS CITY TESTING LABORATORY 257

TURPENTINE SUBSTITUTE.
General:

1. This specification covers the grade of mineral spirits used
by the United States Government and its agencies for thinning paints
and varnishes and as a substitute for turpentine.

2. This material shall be free from undissolved water and sus-
pended matter.

Properties and Tests:

3. Color: The color shall be water white.

4. Spot test: It shall evaporate completely from filter paper
in 30 minutes.

5. Flash point: The flash point shall not be lower than 30°G
(86° F.). (Tag. Closed Tester.)

6. Sulphur: The sulphur test shall be negative.

7. Distillation range: Not over 59f shall distill below 130°C
(266°F).

Not less than 97Vc shall distill below 230°C (446°F).

8. Acidity: The residue remaining in the flask after the dis-
tillation is completed shall not show an acid reaction.

All tests shall be made in accordance with the methods for testing
gasoline adopted by the Committee on Standardization of Petroleum
Specifications.

Specifications for Natural Gasoline.
(Adopted by Association of Natural Gasoline Manufacturers.)

GRADE "A". GRADE "B".

Gravity Not below 72° Be' Not below 76° Be'

Not above 76° Be' Not above 80° Be'

End point Not over 375° F. Not over 375° F.

Color Water white Water white

Recovery Not less than 90% Not less than 85%

Vapor tension Not over 10 pounds Not over 10 pounds

GRADE "C." GRADE "D".

Gravity Not below 80° Be' Not below 80° Be'

Not above 84° Be' Not above 84° Be'

End point Not above 375° F. Not above 330° F.

Color Water white Water white

Recovery Not less than 85% Not less than 80%

Vapor tension Not over 10 pounds 12 pounds maximum

GRADE "E". GRADE "F".

Gravity Not below 84° Be' Not below 87° Be'

Not above 87° Be' Not above 90° Be'

Initial boiling point Not below 65° F. Not below 60° F.

End point Not above 330° F. Not above 330° F.

Color Water white Water white

Vapor tension 15 pounds maximum Under maximum required

by Bureau of Explos-
ives.
GRADE "G".

Gravity Specified by seller

Color Water white

Recovery Not less than 85%

Vapor tension Specified by seller

258 BULLETIN NUMBER SIXTEEN OF

Specifications for Motor Natural Gasoline.
(Adopted by Association of Natural Gasoline Manufacturers.)

GRADE "1".

Gravity Not below 60° Be'

Not above 62° Be'

Initial boiling point Not less than 87° F.

End point Not over 450° F.

Color Water white

Recovery Not less than 90%

Vapor tension Not over 6 pounds

GRADE "2".

Gravity Not below 62° Be'

Not above 66° Be'

Initial boiling point Not less than 80° F.

End point Not over 450° F.

Color Water white

Recovery Not less than 86%

Vapor tension Not over 8 pounds

GRADE "3".

Gravity Not below 66° Be'

- . . , ^ .,. Not above 70° Be'

Initial boiling point Not less than 70° F.

^"P point Not over 450° F.

^olor Water white

Recovery. Not less than 83%

Vapor tension Not over 10 pounds

GRADE "4".

P'";^>l'fY ;,. Specified by seller

FnH n °i "^ P°'"* Not less than 85° F.

^"f P°'"t Not over 465° F.

p3,_ Water white

VpTtion Sr/'^r"'"!"

'^ Not over 8 pounds

addit^o^nll^nrn"!^!'-*^^*^ ^""^^ determined by methods of A. S. T. M. with
additional provisions, condenser water temperature 32-34° F.

KANSAS CITY TESTING LABORATORY 259

Summary of Refined Oil Inspection Laws and Taxes.

ALABAMA.

Gasoline — The distillation test shall show an initial boiling point
of 140°F, 18% over at 250°F or below and an end point below
437° F. Tax on gasoline is l/20c per gallon.

Kerosene — Shall have a fire test of 120° F. or over. Tax on
kerosene is %c per gallon.

ARIZONA.

Has no requirements for quality of gasoline or kerosene, but
levies a road tax of Ic per gallon on gasoline.

ARKANSAS.

Gasoline — The gravity shall be taken at 60° F. and marked on
the container. The tax on gasoline is Ic per gallon, to be applied
on road improvements. Inspection tax of %c per gallon.

Kerosene — Shall have a fire test of 150° F. by Tagliabue open
cup. Tax on kerosene, Vhc per gallon.

CALIFORNIA.

Has no laws in regard to quality of gasoline or kerosene. Levies
no general tax.

COLORADO.

Gasoline — Gravity shall be taken. Gasoline shall contain not
more than 5% of solid matter. Road tax of Ic per gallon.

Kerosene — Shall have a flash point of not less than 90° F. by
Foster cup.

CONNECTICUT.

Has no gasoline laws. Levies a road tax of Ic per gallon on
gasoline.

Kerosene— Shall have a flash point of 110° F., fire test, 140° F.
by Tag. open tester.

DELAWARE.

Has no gasoline laws. Levies no tax on gasoline.
Kerosene — Shall have burning point of 115° F. by Tag. open
tester.

FLORIDA.

Gasoline — Gravity shall be placed on the label. Road tax of Ic
per gallon is levied on gasoline and an inspection tax of %c per
gallon on all petroleum products.

Kerosene — Shall be free from glue, water and suspended mat-
ter. The color shall be at least 21 Saybolt, flash point over 100° F.,
end point shall be below 600° F.

GEORGIA.

Gasoline — Container shall be properly labeled with the gravity
and name of the product. Road tax of Ic per gallon is levied. Gen-
eral tax of ^/4c per gallon for oil inspection.

Kerosene — Shall have flash point of over 100° F. by Elliott
closed tester.

260 BULLETIN NUMBER SIXTEEN OF

IDAHO.

Gasoline — Shall be of the quality standardized by the U. S.
Bureau of Mines and shall be labeled and sold as to true name and
grade. No tax levied.

Kerosene — Shall have fire test of over 120° F. by Tag. open
tester.

ILLINOIS.

Gasoline — Must be branded "Condemned for illuminating pur-
poses." No other requirements. No tax levied.

Kerosene — Shall have fire test of over 150° F. by Tag. open cup.

INDIANA.

Gasoline — Gravity shall not be less than 56° Be'.

Kerosene — Shall have flash point of over 120° F. by Foster cup.

IOWA.

Gasoline— Gravitv shall be between 70° Be' and 80° Be' and
shall distill from 150° F. to 210° F. All other products shall be
branded "substitute for gasoline." Shall show percentage boiling
below 135° F., from 135° F. to 210° F., from 210° F. to 302° F.,
percentage above 302° F. No tax levied.

Kerosene — Shall flash above 100° F. by Elliott closed tester,
tester.

KANSAS.

Gasoline — Shall be water white, contain no acid, shall be sweet
by the doctor test, have an end point of 450° F. or below, 20% shall
be distilled at 230° F., 50% at 325° F. Gravity test is required.

Kerosene — Shall flash at a temperature above 110° F. by Foster
cup. Tax levied on both gasoline and kerosene.

KENTUCKY.

Gasoline — No gasoline laws. Road tax of Ic per gallon is levied
on gasoline.

Kerosene— Shall have fire test of over 130° F. by Tag. open cup.
An inspection tax of l/20c per gallon is levied on all oil.

LOUISIANA.

Gasoline — No gasoline law except that Ic per gallon is levied
for roads.

Kerosene— Shall have flash point above 125° F. Any oil flash-
mg below this temperature shall be labeled "dangerous and explo-
sive."

MAINE.

Gasoline— Must be labeled "unsafe for illuminating purposes."
Kerosene- Must have a fire test above 120° F. by Tag. open

cup. No provision is made for state inspection of oil, this being in

charge of local government.

MARYLAND.

Has no laws governing quality of petroleum products.
MASSACHUSETTS.

Kerosene— Flash point of 100° F., fire test, 110° F. or more by
lag. open cup. No other petroleum requirements.

KANSAS CITY TESTING LABORATORY 261

MICHIGAN.

Gasoline — Must be correctly labeled.

Kerosene — Flash point 120° F. by Foster cup. Local laws in
Detroit and other cities are such as to accept Navy specification
gasoline.

MINNESOTA.

Gasoline — Shall have initial boiling point of 140° F., 20% over
at 221° F., 50% at 315° F., 90% at 420° F., end point not over 450°
F., residue not over 3%, 86% shall be recovered. Shall be marked
"unsafe for illuminating purposes." Test shall be placed on label.
Gasoline marked "high test" shall be a superior product.

Kerosene — Shall be water white, contain no glue, suspended
matter or water, residue at 600'' F. shall not be over 5%. Flash
point 100° F., fire test 120' F. by Tag. open cup. Certificate as to
quality shall be on package. Inspection tax of 5c per barrel is
levied on all refined petroleum.

MISSISSIPPI.

Has no laws governing quality of refined petroleum.

MISSOURI.

Gasoline — Gravity over 58° Be' is to be sold as gasoline Grav-
ity of 50° Be' to 58° Be' is to be sold as mixed gasoline or naphtha.

Kerosene — Shall be water white containing no water or tar.
Flash point over 120° F. by Tag. open cup. Gravity not less than
40° Be'. Not more than 4% residue at 570° F.

MONTANA.

Gasoline— Shall be free from water and other foreign matter
and shall be deodorized and contain no acid. Have initial boiling
point below 140° F., 20% between 158 and 221° F., 50% below
275° F., 90% below 390° F., end point below 460° F. Gasoline
acceptable if sum of 20% and 90% temperatures is below 611.

Kerosene — Flash point over 110° F. by Tag. open cup. Shall
contain no water or foreign matter. No fee for inspection and no
tax.

NEBRASKA.

Gasoline — Shall be water white and contain no water or impuri-
ties. Other requirements are new Navy specifications.

Kerosene — Shall be water white, free from water or tar. On
distillation shall have residue not over 7% at 570° F. Flash point
over 112° F. by Foster cup. Gravity over 40° Be'. Inspection fee
6c per barrel.

NEVADA.

No inspection laws.

NEW HAMPSHIRE.

Gasoline — No law.

Kerosene— Flash point 100° F., fire test 120° F. by open cup.
This law more specifically for liquid polishes.

NEW JERSEY.

Gasoline — Shall be properly labeled.

Kerosene— Flash po'nt on the label which shall be more than
100° F.

262 BULLETIN NUMBER SIXTEEN OF

NEW MEXICO. „ , X, , .

Gasoline — Gravity of over 46° Be . Road tax of Ic per gallon.
Kerosene — Flash point of over 120° F.

NEW YORK. ^ , ^ .T .,

Kerosene— Flash point of 110° F. by Tag. open cup. No other

laws.

NORTH CAROLINA.

Gasoline — Shall have initial boiling point of 140° F., 20Vc over
at 221° F., 50% over at 284° F., 907f over at 374° F. end point
below 437° F., loss not over 5%. Manufacturer must send notice of
shipment with full information to Commissioner of Agriculture,
Raleigh, N. C. Road tax, Ic per gallon, and inspection tax of V^c
per gallon.

Kerosene — Flash point of not over 100° F. by Elliott cup. Not
over 6% residue on distilling at 572° F.

NORTH DAKOTA.

Gasoline — Class I or household gasoline on distillation shall
yield less than 3% at 158° F. and not over 6% residue at 284° F.
Class I is not subject to tax. Class II gasoline on distillation shall
yield from 3% to 15% at 158° F. 96% shall distill over. End point
shall be below 428° F. Shall not be over 36% residue at 284° F.
Class II is taxed at ^ic per gallon. Class III comprises all other
gasoline and is taxed at Ic per gallon.

Kerosene— Flash point 100° F., fire test 125° F. by Elliott
closed cup. Shall be water white. Not over 6% shall be distilled at
310° F. and residue shall not be over 4%c at 570° F.

OHIO.

Gasoline — Shall be labeled "dangerous."

Kerosene — Flash point over 120° F. by Foster cup.

OKLAHOMA.

Gasoline — High grade or aero gasoline shall be water white,
free from acid, 5% distilled at 122° F., 97% at 350° F. Other
gasoline shall be labeled with the quality and brand "Motor fuel
oil."

Kerosene— First grade shall have gravity of 40 to 48° Be' flash
pomt above 120° F. A. S. T. M. tester. Second grade kerosene,
flash point above 110° F. A. S. T. M. tester.

OREGON.

Gasoline — Gravity shall be over 56° Be'. Road tax of 2c per
gallon on gasoline. No law on refined oil.

PENNSYLVANIA.

Gasoline — Road tax of Ic per gallon.

Kerosene— Fire test 110° F. by Tag. open cup.
RHODE ISLAND.

Kerosene— Flash point 110° F. by Tag. open cup.
SOUTH CAROLINA.

Gasoline— New Navy gasoline with an end point 225° C. Inspec-
tion tax Vsc per gallon.

^i.f ir^''"^?™'?,^^ P^'"^ 1^0° ^- with Elliott tester. Residue on
di.-5tilling at 570° F. shall be less than 6%.

KANSAS CITY TESTING LABORATORY 26J

SOUTH DAKOTA.

Gasoline — Gravity shall be recorded.

Kerosene — Shall be water white and contain no tar. Shall
distill not over 10% at 300° F., residue not over 4% at 570°. Flash
point above 105" F. with New York closed tester. Gravity shall be
over 41° Be'. Road tax of Ic per gallon on gasoline. Inspection tax
of 5c per barrel.

TENNESSEE.

Gasoline — Shall be labeled "unsafe for illuminating purposes."
Kerosene — Flash point shall be over 120° F. Tag. open cup.
Inspection fee on gasoline, 20c per barrel; 25c per barrel on kero-
sene.

TEXAS

Gasoline— Initial boiling point shall be 140° F., 20% at 221° F.,
45% at 275° F., 90%, at 356° F., end point 428° F., 95% shall be
recovered on distillation. Vapor tension shall be below 10 pounds
at 100° F.

Kerosene — No kerosene law.

UTAH.

Kerosene — No state laws. Salt Lake City requires that kero-
sene be water white, free from water or tar, flash point 110° F. by
Foster or Tag. cup.

Gasoline — Gasoline in Salt Lake City shall be the quality set
forth by specifications of Bureau of Mines. Products shall be
properly labeled.

VERMONT.

Kerosene — Fire test 110° F. by Tag. open cup.

VIRGINIA.

No law on petroleum products.

WASHINGTON.

Gasoline — Containers shall be branded with gravity. Road tax,
Ic per gallon.

Kerosene — Fire test 120° F. with Tag. open cup.

WEST VIRGINIA.

No law.

WISCONSIN.

Gasoline — Containers shall be marked with gravity. Inspection
tax, 5c per barrel.

Kerosene— Flash point 105° F., fire test 120° F. with Tag. open
cup.

WYOMING.

Gasoline — New navy gasoline containing not over 2'}c of un-
saturated hydrocarbons. End point 437° F.

Kerosene — Shall be water white, containing no water or tar.
Flash point 110° F. with Foster closed cup. On distillation shall
have a residue of not over 59f at 572° F.

264 BULLETIN NUMBER SIXTEEN OF

Possible Savings in Use of Gasoline.

The Bureau of Mines estimates that the following savings can be
effected daily: ^^^^^^^

Tank wagon losses _; .- -• oJ'^aa

Leaky carburetors, average 1/17 of a pint per car J^l't^jl

Poorly adjusted carburetors, V2 pint per car Tr^ nnn

Motors running idle, % pint per car ESS

Wasted in garages, 10 pints per day -.no'nnn

Saved by using kerosene m garages or a'^nn

Needless use of passenger cars, 1% pints per car 897,400

This makes a total of 1,500,000 gallons a day, or 561,000,000 gal-
lons a year, whereas our war needs were 350,000,000 gallons a year,
or less than two-thirds of what may be considered as wasted at the
present time.

SUGGESTIONS TO GASOLINE USERS.

The following important suggestions for avoiding waste will not
only save gasoline, but users of motor vehicles will be benefitted per-
sonally and individually through more efficient and more economical
operation of cars:

1. Store gasoline in underground steel tanks. Use wheeled steel
tanks with measuring pump and hose. They prevent loss by fire,
evaporation and spilling.

2. Don't spill or expose gasoline to air — it evaporates rapidly
and is dangerous.

3. Don't use gasoline for cleaning and washing — use kerosene or
other materials to cut grease.

4. Stop all gasoline leakages. Form habit of shutting off gas at
tank or feed pipe.

5. Adjust brake bands so they do not drag. See that all bearings
run freely.

6. Don't let engine run when car is standing. It is good for
starter battery to be used frequently.

7. Have carburetors adjusted at service stations of carburetor or
automobile companies— they will make adjustments without charge.

8. Keep needle valve clean and adjust carburetor (while engine is
hot) to use as lean mixture as possible. A rich mixture fouls the
engine and is wasteful.

9. Pre-heat air entering carburetor and keep radiator covered
in cold weather — this will insure better vaporization.

10. See that spark is timed correctly with engine and drive with
spark full advanced — a late spark increases gas consumption. ,

11. Have a hot spark, keep plugs clean and spark points properly
adjusted.

12. Avoid high speed. The average car is most economical at 15
to 25 miles an hour.

. 13. Don't accelerate and stop quickly — it wastes gas and wears
out tires. Stop engine and coast long hills.

14. Cut down aimless and needless use of cars. Do a number of
errands in one trip.

15. Know your mileage per gallon. Fill tank full and divide
odometer mileage by gallons consumed.

KANSAS CITY TESTING LABORATORY 265

Benzinum Purificatum (U. S. Pharmacopoeia).

Purified Petroleum Benzin.

Benzin. Purif. — Petroleum Ether.

A purified distillate from American petroleum consisting of hy-
drocarbons, chiefly of the marsh-gas series. Preserve it carefully in
well-closed containers, in a cool place, remote from fire.

Purified Petroleum Benzin is a clear, colorless, non-fluorescent,
volatile liquid, cf an ethereal, or faint, petroleum-like odor, and having
a neutral reaction. It is high'y inflammable and its vapor, w^hen
mixed with air and ignited, explodes violently.

It is pract'cally insoluble in water, freely soluble in alcohol, and
miscible with ether, chloroform, benzene, volatile oils and fixed oils,
with the exception of castor oil.

Specific gravity: 0.638 to 0.660 at 25°C.

It distills completely between 40°C and 80°C (104°F to 176°F).

Evaporate 10 mils of Purified Petroleum Benzm from a piece of
clean filter paper; no greasy stain remains, and the odor is not dis-
agreeable or notably sulphuretted. Not more than 0.0015 Gm. of res-
idue remains on evaporating 50 mils of Purified Petroleum Benzin at
a temperature not exceeding 40° C.

Boil 10 mils of Purified Petroleum Benzin for a few minutes with
one-fourth its volume of an alcoholic solution of ammonia (1 in 10)
and a few drops of silver nitrate T. S ; the liquid does not turn brown
(pyrogenous products and sulphur compounds).

Add 5 drops of Purified Peti'oleum Benzin to a mixture ofo 40
drops of sulphuric acid and 10 drops of nitric acid in a test tube, warm
the liquid for about ten minutes, set it aside for half an hour, and
dilute it in a shallow dish with water; no odor of nitrobenzene is
evolved.

Comparison of Gasoline and Benzol as Motor Fuel.

Heat of combustion: Benzol Gasoline

B. T. U. per gallon 132330 129060

B. T. U. per pound 18054 20750

Freezing temperature 41°F 50°F below Zero

Boiling temperature 170-180 130-400°F

Rate of evaporation ..: Slower Faster

Mileage per gallon (comparative) 110. 100.

Ignition temperature Higher Low

Pre-lgnition from carbon Less trouble More trouble

Carbon formed More Less

Relative volume of air required per

gallon 1.04 1.00

Relative volume of explosive gases

produced per gallon .92 1.00

Temperature of explosion Higher Lower

Rapidity of explosive force Less sudden More sudden

Benzol is most satisfactory if used mixed with gasoline or alco-
hol, preferably the latter.

266 BULLETIN NUMBER SIXTEEN OF

Kerosene, Coal Oil, Illuminating Oil, Burning Oil.

Kerosene in a general way may be defined as that fraction of
crude petroleum or oil made bv the pyrogenic decomposition of shales
or coal which distills at a temperature of from 302°F to 572°F, (150-
300°C) and contams no gasoline or residuum. Its flash point is al-
ways greater than 100°F and usually greater than 120°F. Its color
may be standard white, prime white, superfine white or water white.
Its gravity ranges from 31 to 48° Be'. Typical kerosene has a gravity
of 41 to 42''Be'. Sulphur is usually almost completely absent from
kerosene, being less than 0.03%. It consists chiefly of the paraffin
series, particularly when the gravity is greater than 38. The principal
constituents are nonane, decane, undecane, duodecane, tridecane, tetra-
decane, pentadecane, hexadecane and heptadecane. With lower grav-
ities it contains naphthenes and aromatic compounds. This is par-
ticularly true of Louisiana oils and California oils.

The quality of good kerosene has been found to be within the
following limits:

1. Specific gravity is between 0 760-0.860 (54.2-32 8°Be').

2. Flash point is over 100°F by closed tester.

3. Color is water white with no turbidity.

4. Cold test is below 10°F.

5. End point is below 600 °F.

6. Sulphur is below 0.05%.

7. Acid is absent.

8. It does not lose more than 1% on treatment with 66° sul-
phuric acid.

9. It burns without incrustation or smoking in an ordinary kero-
sene lamp.

The grades of burning oils are shown in the following table
with the relative value of each grade in cents per gallon at refinery.

North Texas.

40@42 prime white distillate 2%c

40@43 prime white kerosene 2i/^c

42@43 prime white kerosene 3 c

Oklahoma.

41@43 3%c

42(5)43 4 c

44@46 5 c

42(5)43 distillate 31/20

Pennsylvania.
45 prime white 6 c

45 water white 6%c

46 water white 7 c

47 water white 8 c

48 water white 9 c

30 mineral seal 6^/40

West Virginia.

45 water white 6 c

47 water white '^^!!"!!''"'!"!''!!!^^'^^'^8 c

Kerosene is produced in amounts that greatlv exceed the market
dornand so that the surplus is used for house ' heating and mixed
with gas oil for cracking stock. It is specially adapted for high
pressure (600 lbs.) cracking. ^ ^ f

KANSAS CITY TESTING LABORATORY 267

U. S. Specifications for Burning Oil (1921).

WATER WHITE KEROSENE.
General:

1. This specification covers the grade of kerosene used by the
United States Government and its agencies as an illuminating oil.
This oil may be used as fuel and for cleaning in case of necessity.

2. The oil shall be free from water, glue and suspended matter.
Properties and Tests:

3. Color: The color shall not be darker than No. 21 Saybolt.

4. Flash point: The flash point shall not be lower than 115°F
(closed tester-tag).

5. Sulphur: The sulphur shall not be more than 0.06%.

6. Floe: The floe test shall be negative.

7. Distillation; The end point shall not be higher than 600°F.

8. Cloud test: The oil shall not show a cloud at 0°F.

9. Doctor test: The doctor test shall be negative.

10. Burning test: The oil shall burn freely and steadily for
18 hours.

All tests shall be made according to the methods for testing
burning oils adopted by the Committee on Standardization of Petro-
leum Specifications.

SPECIAL NOTE COVERING KEROSENE FOR U. S. NAVY.

When specifically provided for, a representative sample of the
oil delivered will be tested photometrically after burning for one
hour in a lamp fitted with a No. 1 sun hinge burner. Five hours
later, another photometric test will be made to determine any change
in intensity of the light; the maximum allowable loss shall be 5%.
The flame shall show at least 6 candlepower when compared photo-
metrically with an incandescent lamp which has been standardized
by the Bureau of Standards.

Otherwise specifications enumerated above apply for United
States Navy Kerosene.

PRIME WHITE KEROSENE.
General :

1. This specification covers the grade of kerosene used by the
United States Government and its agencies where kerosene is re-
quired primarily as a fuel and for cleaning purposes. This oil can
be used as an illuminant in case of necessity.

2. The oil shall be free from water, glue and suspended matter.
Properties and Tests:

3. Color: The color shall not be darker than No. 16 Saybolt.

4. Flash point: The flash point shall not be lower than IIST
(tag closed tester).

5. Sulphur: The sulphur shall not be more than 0.09%.

6. Floe: The floe test shall be negative.

7. Distillation: The end point shall not be higher than 625°F.

8. Cloud test: The oil shall not show a cloud at 5°F.

9. Burning test: The oil shall burn freely and steadily for
8 hours.

All tests shall be made according to the methods for testmg
burning oils adopted by the Committee on Standardization of Petro-
leum Specifications.

268 BULLETIN NUMBER SIXTEEN OF

LONG TIME BURNING OIL.

General :

1. This specification covers the grade of burning oil used by
the United States Government and its agencies where a long time
burning oil is required.

2. The oil must be free from v^^ater, glue and suspended matter.
Properties and Tests:

3. Color: The color shall not be darker than No. 21 Saybolt.

4. Flash point: The flash point shall not be lower than 115°F
(tag closed tester).

5. Floe: The floe test shall be negative.

6. Cloud test: The oil shall not show a cloud at 0°F.

Note: Temperature of 0°F can be varied either up or down to
suit the climatic conditions in the territory in which the oil is to
be used.

7. Burning test: The oil must burn freely and steadily for
120 hours or until the oil is consumed.

All tests shall be made according to the methods for testing
burning oils adopted by the Committee on Standardization of Petro-
leum Specifications.

Oil for use by the Bureau of Lighthouses shall be as described
by the Department of Commerce, which specifications, etc., at the
present time are as follows:

1. The kerosene must have a flash point of not less than 140° F
and fire point of not less than 160°F (tag closed tester).

2. The kerosene must contain no free acids or mineral salts.
Litmus paper immersed in it for five hours must remain unchanged.

3. One hundred grams of kerosene shaken with 40 grams of
sulphuric acid (sp. gr. 1.73) must show little or no coloration.

4. When distilled from a still so jacketed as not to allow of
local heating at a rate of not over 10 % in ten minutes, the kero-
sene shall not distill below 350°F and 98';-'r shall distill under 515°F,
the temperature taken being that of the condensing vapor.

5. When burned for 120 hours in a lens lantern supplied with
a fifth order oil lamp, the kerosene must burn steadily and clearly
without smoking, with minimum incrustation of wick, slight discol-
oration of chimney and less than 10% loss of candlepower. A lamp
of this description will be loaned to successful bidder.

300 DEGREE MINERAL SEAL OIL.
General :

1. This specification covers the grade of oil used by the United
States Government and its agencies for lamps in passenger coaches
and for illuminating railroad equipment, and where a high flash
illummant is required.

ter.

2. The oil must be free from water, glue and suspended mat-

KANSAS CITY TESTING LABORATORY 269

Properties and Tests:

3. Color: The color must not be darker than No. 16 Saybolt.

4. Flash point: The flash point shall not be lower than 250°F
(Cleveland open cup).

5. Fire point: The fire point shall not be lower than 300° F
(Cleveland open cup).

6. Floe test: The floe test shall be negative.

7. Cloud test: The oil shall not show a cloud at 32°F.

8. Reaction: The oil shall be neutral.

9. Burning test: The lamp shall give a symmetrical flame,
free from smoke, when burned continuously without readjustment
until all of the oil is consumed.

All tests shall be made according to the methods for testing
burning oils adopted by the Committee on Standardization of Petro-
leum Specifications.

SIGNAL OIL.

General :

1. This specification covers the grade of oil used by the United
States Government and its agencies for railroad signal lamps.

2. The oil shall be free from water, glue and suspended matter.

3. The oil shall be compounded from 300 degree mineral seal
oil, as adopted by the Committee on Standardization of Petroleum
Specifications with pure prime winter strained lard oil or sperm
oil, or with a mixture of pure prime winter strained lard oil and
sperm oil.

Grade A shall not contain less than 30% of fatty oil by volume.
Grade B shall not contain less than 22% of fatty oil by volume.
Grade A shall always be furnished unless Grade B is specifically
ordered.

Properties and Tests:

4. Flash point: The flash point shall not be lower than 250 °F
(Cleveland open cup).

5. Fire point: The fire point shall not be lower than 300°
F (Cleveland open cup).

6. Cloud test: The oil shall not show a cloud at 32°F.

7. Free fatty acids: Grade A shall not contain over 0 60% of
free fatty acid calculated as oleic acid. Grade B shall not contain over
0.45% free fatty acid calculated as oleic acid.

8. Burning test: The oil shall burn 24 hours without trimming
or adjusting the wick.

All tests shall be made according to the methods for testing
burning oils adopted by the Committee on Standardization of Petro-
leum Specifications.

270 BULLETIN NUMBER SIXTEEN OF

GAS OIL.

Gas oil is that fraction of petroleum distillation coming off after
the kerosene or other illuminating oil. It is usually a destructive
distillation resulting in a distilled product carrying a considerable
amount of olefins and a residue having a lovi^er viscosity than would
be the case without a partially destructive distillation. When it is
desired to avoid a destructive distillation, steam may be used, giving
an oil suitable for absorption purposes sometimes known as straw oil.

Gas oil is used for making gas and for carbireting coal gas or
water gas. It is also used to make Blaugas, which is a product liqui-
fied under a pressure of about 1,500 pounds. It is also used for
Pintsch gas. A typical gas oil has the following properties:

Specific gravity 0.843 = 36.1°Be'

Flash point 90°C

Burning test \\%''C

Distillation test:

0°C-150°C - 0 0%

150°C-300°C - : 44.07c

300°C up : 55.3%

Coke - 0.7%

GAS OIL FOR DIESEL ENGINES (U. S. NAVY).

1. Flash point not lower than 150 °F (Abel or Pennsky-Mar-
ten's closed cup).

2. Water and sediment — trace only.

3. Asphaltum — none.

KANSAS CITY TESTING LABORATORY 271

STRAW OIL (U. S. BUREAU OF STANDARDS).

The characteristics of a straw oil for absorption of light oils from
gas as recommended by some operators and which are concurred in
by the committee of coal-tar products are substantially as follows:

1. Specific gravity not less than 0.860 (34°Be') at 15.5°C (60°F).

2. Flash point in open cup tester not less than 135°C (275°F).

3. Viscosity in Saybolt viscosimeter at 37.7° C (100°F) not more
than 70 seconds.

4. The pour test shall not be over 1.1°C (30°F).

5. When 500 cc of the oil are distilled with steam at atmospheric
pressure collecting 500 cc of condensed water, not over 5 cc of oil
shall have distilled over.

6. The oil remaining after the steam distillatioa shall be poured
into a 500 cc cylinder and shall show no permanent emulsion.

7. The oil shall not lose more than 10% by volume in washing
with 2V2 times its volume of 10091^ sulphuric acid when vigorously
agitated with acid for five minutes and allowed to stand for two
hours.

An additional set of specifications for wash oil which is used by
one Government department is as follows:

Specific gravity shall not be greater than thirty-five and nine-
tenths degrees (35.9°) Baume' at 60 °F, equivalent to specific gravity
0.844.

Viscosity shall not be more than 56 seconds in a Saybolt viscosi-
meter at 100° Fahrenheit.

The oil shall not thicken or cloud at 25°F in the cold test.

At least 95 ^r of the oil shall separate as a clear layer within 10
minutes after 100 cubic centimeters of oil and 100 cubic centimeters
of water have been shaken together vigorously for 20 seconds at a
temperature of 70 °F.

There shall not be more than 14';'^: of loss in volume of oil when
1 volume of oil and 2^/2 volumes of 1009f sulphuric acid are vigor-
ously agitated for 5 minutes and allowed to settle for 2 hours.

The oil shall not begin to distill below 240°C.

272 BULLETIN NUMBER SIXTEEN OF

Quality of Absorption Oil for Extracting Gasoline from Natural Gas
(Westcott "Casinghead Gasoline").

Gravity 35.6°

Initial boiling point 536 °F

End point 698 °F

Fire test 312.8°F

Saybolt viscosity@100°F 40.5

Distillation.

Initial 273 °C

5% 295 °C

10% 300 °C

20% 305 °C

30% 308.6°C

40% 311 °C

50% 316 °C

60% 322 °C

70% 329 °C

80% 336.5°C

90% 360 °C

KANSAS CITY TESTING LABORATORY 273

LUBRICATING OILS.

The principal source of lubricating oil is petroleum from which
the lighter components, naphtha, kerosene, solar oil and gas oil have
been removed by distillation, the residue thus obtained being used
directly as a lubricant or separated by distillation into various frac-
tions. By removing some of the fractions, as well as by mixing
others, a variety of products may be obtained with special properties
(viscosity, flash point, cold test and specific gravity).

This is the principle on which the industry is based. The sep-
arate fractions are further refined to remove odor, resinous materials,
etc., as well as to attain the desired lightness of color. This is ac-
complished by means of sulphuric acid, agitating with a stream of
air, the acid being later removed by washing with alkali or water;
the purification may also be brought about by filtration through ful-
ler's earth (see chapter on refining).

The oil may be distilled with superheated steam or with partial
vacuum, excessive direct firing being avoided to prevent decomposi-
tion. The temperature of the superheated steam is kept somewhat
higher than that of the still. Commercially, the distillates are cooled
and separated according to specific gravity, flash point and viscosity.

Direct firing is much used in separating the crude oil fractions,
thus increasing the yield of illuminating oils and producing a raw
wax distillate. The refining, however, is cai'ried on with superheated
steam.

ECONOMY OF LUBRICATION.

The economical transmission of power is largely dependent upon
the maximum reduction of friction.

The purpose of lubrication is to overcome friction in so far
as possible and to prevent wear and deterioration of adjacent mov-
ing parts.

It is claimed that from 40 9r to 80 '/r of all power produced by
machinery is lost in friction, and a very considerable part of this is
lost in avoidable friction due to improper lubrication.

THEORY OF LUBRICATION.

A lubricant should prevent direct contact between the bear-
ings and the moving parts of machinery, thus substituting for
metallic friction and wear the much smaller internal friction of the
lubricant. The more completely this result is attained under the
conditions of temperature, speed and pressure, the more valuable
the lubricant from a mechanical point of view. Whether the mechan-
ically most efficient lubricant is the most economical depends some-
what on the ratio of efficiency, the amount used and the price of
the material. Greases have a low mechanical efficiency compared
with liquid oils, but from the point of economy and cleanliness they
are far superior.

Only liquids with great tendency to adhere are suited for lubri-
cation, since only these have the property to penetrate by capillarity
where journal and bearings are the closest and where the danger of
contact and wear is the greatest. The lubricating oils prevent direct

274 BULLETIN NUMBER SIXTEEN OF

contact of the metal surfaces because of their adhesion to these sur-
faces and because their viscosity keeps them from being squeezed
out by the pressure on the bearing.

Experience has shown that the power to adhere to metals in-
creases with the viscosity of the oil. Since the danger that an oil
will be pressed out increases with the pressure on the bearings, it
is advisable for high pressures to use oils of considerable viscosity.

With low pressure and high speed there should be used a very
mobile oil, with higher pressure and low velocity more viscous oils.
If, for example, a spindle rotating with practically no pressure but
very rapidly were lubricated with a very viscous oil, it would mean
a lavish waste of power. But to lubricate a ti'ansmission gear with
a mobile oil would be a waste of lubricant, while the use of a heavy
grease would be entirely suitable. In fact, the use of a solid lubri-
cant, graphite, with heavy oils as a vehicle, has proven most de-
sirable in the case of very heavy bearings and transmission gears
with enormous pressures.

The oil should not lose its power of reducing friction by evapora-
tion, gumming or by acting chemically on the metal of the bearings
or journal.

The oil or gi'ease should not solidify or greatly change its vis-
cosity under conditions of use.

The qualities of various types of lubricating oils are as follows:

Light Heavj' Auto- Steam Large

Viscosity at — Spindle M'ch'n'y M'ch'n'y mobile Engine Cylinder Cylinder

70° F 75-500 375-750 1750-875 470-1100 300-400 2800-400

100° F 180-220 160-400 130-150 ...

122° F 75-90 ., 110-280 1100 300-560

210° F 40-50 45- 60 40- 55 44-47 120-150

Flash point, °F Min. 140 160 390 350 430 525 450

Cold test, °F 10 5 10- 40 10 25 45 40

Gravity, Be' 19 32 23-30 24-30

Flash and burning points of lubricants are the respective tem-
peratures at which the vapors arise in sufficient amount to ignite
and to burn continuously. They should be high enough to prevent
any danger of fire in using the oil and to be assured that a light
oil has not been added to a heavy oil to regulate viscosity. With the
same viscosity asphaltic base oils (Texas, California and Mexico)
has a lower flash point and a higher specific gravity than paraffin
base oils (Pennsylvania and West Virginia).

Specific gravity is the relation of the weight of a given volume
of 01 to the weight of the same volume of water. The oil trade
vsually u.ses the Baume' scale of gravity, which is entirely arbitrary.
ihe paraffm oils with the same viscosity are lighter (have a
higher gravity-Baume') than the asphaltic or semi-asphaltic oil. Grav-
ity IS not a measure of the quality of a lubricating oil.

_ Viscosity is a most important propertv for lubrication. The
viscosity IS expressed in the terms of the Savbolt Universal Viscosi-
Vni'iLT o^ '■i^""*''Y; ^he Engler in Germany and the Redwood in
i^ngland. Paraffin oils are said to lose their viscosity most readily
r!^mnf •" ^? ^7.Pl«sion cylinder by reason of the greater ease in de-
ho ,« ; • ^' 5t-''[ P^'Ofl^cts than do asphaltic oils. They tend to

vL,fn» ?"1 ^^^^y temperatures as asphalt base oils though less

viscous at atmospheric temperature.

KANSAS CITY TESTING LABORATORY

275

9^ SO 70 60 50 ^o JO eo /O

-^ " ' 10 ZO 30 ^O SO 60 70 80 90
Fig. 5 4 — Viscosity Blending- Chart for Lubricating- Oils.

276

BULLETIN NUMBER SIXTEEN OF

The residual carbon is a most harmful property in lubricants
for explosion motors, such as automobiles. High residual carbon is
found in poorly refined and blended oils. It is usually found in oils
that are not entirely made from overhead or distilled stock but part-
ly from cylinder or residual stocks or fatty oils.

Cold test determines the lowest temperature at which the oil
will flow. A low cold test is desirable for ease in circulating and
handling in cold weather. A low cold test for motor oils indicates the
absence of heavy ends that produce excessive carbon in the cylinder.

Color is not an index of the value of a lubricating oil. The light-
er the color, other things being equal, the purer the oil.

Free acid should be, and usually is, absent. It is an indication
of mineral acid that has not been neutralized and washed out in re-
fining or of the presence of naphthenic acids, or of the use of ani-
mal or vegetable oils.

A lubricating oil for use in internal combustion engines should
have a good viscosity at all temperatures under which the engine
will operate. This means that the oil should remain fluid in the
coldest weather and should have some decrree of viscosity up to
250°F. The piston walls of the engine attain temperatures as high
as 400 °F. At this high temperature, however, practically all oils
have the same viscosity. However, it is quite important that the
oils also have a good viscosity at the lower temperatures. An engine
motor oil should be a completely distilled oil and should contain no
residual or fatty matter. On evaporation in air at 500 °F it should
yield a minimum amount of pitch and by the Conradson carbon test
rhDuld have the minimum amount of carbon. The flash point is main-
ly of importance in that it md'cstes that the oil contains no light
oils. So far as operating conditions are concerned, it is of little
importance for the reason that a motor oil in a short time after
being used, has a very low flash point. After the oil has served its
purpose and gotten by the piston rings, then it should readily evap-
0 -ate and leave a minimum amount of carbonaceous matter. A motor
cil containing vegetable or animal oil produces acid on being sub-
jected to heat and pressure.

/so' TO 350'/=

HEfJT Of eycPL. OS/O/V 2000 " TO 3000 '^

P/STOfy/ MefiPS

300° ro /ooo */f

P/5TON IV/QLLS

zoo'ro ^-oo'f.

cet^fvk- g£fii?/NG o/

I'iO'TO iSO °P.

surtf o?L

90* 70 zoo '/=■

Fii

•porating: Temperatures of Various Tarts of a Gasoline
Engine.

KANSAS CITY TESTING LABORATORY 277

Summary of Tests of Motor Lubricants of Standard

Quality as Purchased on the Kansas City Market

in January 1922*.

1. Key Number 123456789

3. Retail price $1.20 SI. 20 SI. 20 SI. 20 SI. 00 SI. 00 $1.20 SI. 20 $1.00

4. Specific gravity 9325 .908 .912 .917 .896 .874 .920 .938 .S>03

5. Baume' Gra\'ity 20.2° 24.3° 23.6° 22.8° 26.4° 30.4° 22.3° 19.3° 25.1°

6. Color— N.P.A g E M M N 4^ OPS^PSeji E+ N 4}i

7. Color— lodimetric... 351 1480 52 51 70 247 219 2048 88

8. Flow test 15° F 47° F +5° F +3° F +4° F 35° F 28° F 27° F +10° F

9. Flashpoint— open... 355° F 430° F 360° F 365= F 250° F 300° F 365° F 325° F 350° F

10. Fire test 430° F 496° F 415° F 420° F 375° F 465° F 425° F 410° F 405° F

11. Viscosity— Say bolt —

Stand'd Univ. 70° F 2400 4410 710 810 336 720 1035 4775 505

100° F 650 1300 250 285 155 300 327 992 198

150° F 150 305 85 91 65 105 99 203 75

210° F 61 97 49 52 44 56 52 71 46

12. Carbon (ASTM) 0.48% 1.43% 0.08% 0.08% 0.09% 0.39% 0.18% 1.05% .085%

13. Gumming and Coking

(Pitcn) 18.4% 45.6% 10.8% 11.6% 14.0% 29.2% 12.8% 30.0% 12.8%

14. Heat-pressure tests —

Pressure— maximum. 2 1.5a 28.9 23.5 32.3 24.5 22.5 28.9 36.0 29 2

Gravity increase Be' . 4 . 6 6.3 4.3 6.4 4.1 6.9 5.3 5.1 4.5

Gasoline produced % 19.0 23.0 20.0 24.0 21.0 24.0 23.0 18.0 21.0

Gasoline gravity Be 56 7 60.0 57.2 58.5 56.8 60 5 58.2 57.2 59.1

Kerosene produced % 16.0 16.0 16.0 16.0 20.0 17.0 16.0 16.0 17.0

Kerosene gravity Be' 29.8 38.0 33.6 34.0 36.2 40.6 33.8 32.9 35,4

Residue% 65.0 61.0 64.0 60.0 59.0 59.0 61.0 66.0 62 0

Gravity residue Be' 17.0 19.2 22.0 17.1 20.9 27.0 16.7 16.1 19.5

Pitch in residue % 26.5 45.9 11.6 20.0 14.9 26.4 32.1 29.7 19.4

AcidityN/10% 8.0 3.5 7.0 4.5 4.5 4.5 4.0 9.0 4.0

*The tests include Mobiloil, Monogram, Polarine, Texaco, Enarco,
Vedol, Havoline and Sinclair brands.

278

BULLETIN NUMBER SIXTEEN OF

Summary of Tests of Motor Lubricants of Standard

Quality as Purchased on the Kansas City Market

in January, 1 922 — Continued.

1 10 11 12 13 14 1') 10 17 18 19 20

3 SI. 00 SI. 00 $100 .«0 'JO SO. 90 81.00 SI 00 SI 00 SI 20 Si 05 $1.50

4 915 915 .927 .897 .913 .8685 869 .922 .927 .902 .963

5 23.1° 23.1° 21.1° a*) 2° 23.5° 31 4° 31.4° 22.0° 21 1° 25.4° 15.4°

6 0-5 D IJ2I4' I.J2I4 E M-4 M-4 N 43-^ OPS^i P-6 G

7 152 749 15 13 1100 44 154 79 190 155 2

8 29° F 41° F — 21° F +24° F 43° F +23° F 34° F +5° F 5° F 40° F — 14° F

■9 370° F 390° F 360° F 380° F 410° F 380° F 390° F 330° F 355° F 395° F 530° F

10 420° F 475° F 420° F 435° F 470° F 460° F 475° F 395° F 420° F 460° F 590° F

11

856 ISOO 1835 556 2776 441 732 884 2345 655 5350

315 570 510 214 660 187 297 295 666 248 1365

105 157 127 79 173 76 106 91 159 86 320

52 65 62 47 68 47 56 50 63 48 104

'2 014% 0.72% 0.04% 0.06% 0.98% .044% 0 25% 0.12% 0 26% 0.08% 0.195%

'•■' '2.0% 25.6%. 10.4% 7.6% 30.4% 11.2% 20.0% 10.4% 21.2% 11.6% 67.0%

11

24.5 30 6 215 22.0 27.2 25.0 32.3 23.0 28.9 28 9 80.0

*^ '^0 48 5.6 5.9 5.9 51 5.8 48 11.4

18.0 220 20.0 20.0 21.0 25 0 26 0 19 0 20 0 21.0 25.0

57 0 58 9 57 9 607 59.8 61.1 61.9 59 1 59.4 60.1 56.7

'•^ " '"" "■'" 150 16.0 18.0 180 18 0 17 0 16.0 20.0

M.6 36.1 41.5 37 2 38.8 40 4 40.2 33.0 33.8 37.8 31.5

«»0 «10 64 0 65 0 63.0 57.0 56.0 63.0 63.0 63.0 55.0

'"" ■'- •'" 22.0 19.3 27.3 25.5 18.1 16.8 19.7 16.7

200 32.1 11.9 10.0 20.4 10.0 17 6 12 0 17 6 17.6 42.4

'"*" '•'* '" '^0 4.0 2.5 2.5 4.5 4 0 5 0 766.0

Sample No. 20 is castor oil.

KANSAS CITY TESTING LABORATORY

279

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KANSAS CITY TESTING LABORATORY 281

NATURAL HYDROCARBONS— VACUUM DISTILLED.

Table showing the properties of vacuum distilled hydrocarbons
and atmospheric pressure forced fire distilled hydrocarbons of a heavy
residuum from Mid-Continent oil.

Fraction

Gravitji

Viscosity

Sulphur

0 107c

0.868
31.3°Be

46

0.39 7o

10 20%

0.877
29.6°Be

60

0.35 7o

20—30%

0.895
26.4°Be

143

0.43 7o

30—40%

0.909
24.0°Be

293

0.537c

40 50%

0.920
22.1°Be

740

0.767c

50—60%

0.920
22.1°Be

745

0.687o

60 70%

0.920
22.1°Be

1058

0.707c

70 80%

0.920
22.rBe

2600

0.567c

HYDROCARBONS

FROM FORCED FIRE DISTILLATION OF

SAME OIL.

Fraction

Gravity

Viscosity

0 107c

0.864
32.1°Be'

51

10— 207o

0.877
29.6°Be'

69

20 30 7o

0.888
27.6°Be'

109

30— 407o

0893
26.7°Be'

141

40 50 7o

0.894
26.6°Be'

141

50—60 7<^

0.887
27.0°Be'

106

60 70 7o

0.878
29.4°Be'

75

70— 807o

0.877
29.6°Be'

69

EFFECT OF TEMPERATURE ON VISCOSITY OF NATURAL MID-

CONTINENT HEAVY OILS.

Av'ge Mid-Conti-

Heavy Kansas

nent Fuel Oil

Crude

26.8"Be'

19.6°Be'

60°F

:=z

294.

.........

70°F

^^

190.

3360.

100°F

^^

94.

1250.

120°F

^:

70.

680.

120°F

;;^

55.

328.

212°F

—

41.

105.

(Viscosity is expressed in terms of the Saybolt Universal)

282

BULLETIN NUMBER SIXTEEN OF

EFFECT OF CRACKING ON THE LUBRICATING QUALITIES OF

OIL.

In the cracking of petroleum by heat the paraffin hydrocarbons
are most readily decomposed into lighter hydrocarbons. The lubri-
cating hydrocarbonb remaining in cracked oil are therefore not par-
affin but consist chiefly of naphthenes and aromatics. In other words,
cracking reduces the viscosity of heavy hydrocarbon oils based on the
same gravity. This fact is set forth in the patent to Burton (U. S.
No. 1,167,884, Jan. 11, 1916) as follows:

Lubricating fractions made from Mid-Continent Crude Petroleum:

Baume' Gravity

Viscosity at 100°
(Saybolt Viscosimeter)

25.0

235

26.0

190

26.0

165

26.5

145

27.5

100

Lubricating fractions made from California Crude Petroleum:

Baume' Gravity

Viscosity at 100°

18.8

449

20.4

235

20.6

339

21.6

146

21.8

167

22.5

139

Lubricating fractions made

from

Cracked Petroleum Residua:

Baume' Gravity Viscosity

Gravity Viscosity

28.9 36

15.2 88

26.5 38

15.0 89

23.8 42

14.7 97

21.5 45

14.1 105

21.1 51

13.2 110

20.2 52

13.0 116

18.7 58

12.0 158

17.8 62

10.8 198

17.2 65

16.7 66

15.8 76

KANSAS CITY TESTING LABORATORY 283

U. S. Specifications for Lubricating Oils.

CLASS "A".
General :

1. This specification covers the grades of petroleum oil used
by the United States Government and its agencies for the general lub-
rication of engines and machinery where a highly refined oil is not
required. This oil is not to be used for steam cylinder lubrication.

2. Only refined petroleum oils without the admixture of fatty
oils, resins, soap or other compounds not derived from crude petro-
leum will be considered.

3. These oils shall be supplied in five grades, known as extra
light, light, medium, heavy and extra heavy.

Properties and Tests:

4. Flash and Fire Points: The flash and fire points of the five
grades shall not be lower than the following:

Flash Deg. F Fire Deg. F

Extra light _. 315 355

Light 325 365

Medium 335 380

Heavy , 345 390

Extra heavy 355 400

5. Viscosity: The viscosity of the five grades of oil at 100°F
shall be within the following limits:

Extra light 140-160 seconds

Light 175-210 seconds

Medium 275-310 seconds

Heavy 370-410 seconds

Extra heavy 470-520 seconds

6. Color: The color of the extra heavy grade shall not be
darker than No. 6 National Petroleum Association Standard, or its
equivalent. The color of the oth6r grades shall not be darker than
No. 5 National Petroleum Association Standard, or its equivalent.

7. Pour Test: The pour test shall not be above the following
temperatures:

Extra light :....35°F

Light : 35°F

Medium 40°F

Heavy 45 °F

Extra heavy 50 °F

8. Acidity: Not more than 0.10 milligram of potassium hy-
droxide shall be required to neutralize 1 gram of the oil.

9. Corrosion: A clean copper plate shall not be discolored when
submerged in the oil for 24 hours at room temperature.

10. All tests shall be made according to the methods for test-
ing lubricants adopted by the Committee on Standardization of Pe-
troleum Specifications.

284 BULLETIN NUMBER SIXTEEN OF

U. S. Specifications for Lubricating Oils.

CLASS "B"

GENERAL:

1. This specification covers the grade of petroleum oil used by
the United States Government and its agencies for the lubrication
of turbines, dynamos, high speed engines and other classes of ma-
chinery where an oil better than Class A is required. The oil shall
be satisfactory for use in circulating and forced feed systems.

2. Only refined petroleum oils without the admixture of fatty
oils, resins, soaps or other compounds not derived from crude petro-
leums will be considered.

3. These oils shall be supplied in five grades known as extra
light, light, medium, heavy and extra heavy.

4. Flash and Fire Points: The flash and fire points of the five
grades shall not be lower than the following:

Flash Deg.F Fire Deg.F

Extra light 315 355

Light 325 365

Medium 335 380

Heavy 345 390

Extra heavy 355 400

5. Viscosity: The viscosity of the five grades at 100 °F shall
be within the following limits:

Extra light 140-160 seconds

Light 175-210 seconds

Medium 275-310 seconds

Heavy 370-410 seconds

Extra heavy 470-520 seconds

6. Color: The color of the extra heavy grade shall not be
darker than No. 6 National Petroleum Association Standard or its
equivalent. The color of the other grades shall not be darker than
No. 5 National Petroleum Association Standard or its equivalent.

7. Pour Test: The pour test shall not be above the following
temperatures:

Extra light 35°F

Light , 35°F

Medium 40°F

Heavy 45°F

Extra heavy 50 °F

8. Acidity: Not more than 0.07 milligram of potassium hy-
droxide shall be required to neutralize 1 gram of oil.

9. Corrosion: A clean copper plate shall not be discolored when
submerged in the oil for 24 hours at room temperature.

^ 10. Emulsifying properties: The oil shall separate (see note)
m 30 minutes from an emulsion with 1 — Distilled water, 2 — 1% salt
solution, 3 — Normal caustic soda solution.

Note:— This means that there shall be only a slight cuff between
the water and the oil.

The demulsibility shall not be less than 300.

11. All tests shall be made according to the methods for test-
ing lubricants adopted by the Committee on Standardization of Pe-
troleum Specifications.

KANSAS CITY TESTING LABORATORY 285

Specifications for Lubricating Oils.

CLASS "C"
GENERAL:

1. This specification covers the grades of petroleum oil used
by the United States Government and its agencies for lubrication of
air compressors and international combustion engines, except aircraft,
motorcycle and Diesel engines; also for the lubrication of turbines
and other machinery where an oil better than Class B is required.
This oil shall be satisfactory for use in circulation and forced feed
systems.

2. Only refined petroleum oils without the admixture of fatty
oils, resins, soaps or other compounds not derived from crude pe-
troleum will be considered.

3. These oils shall be supplied in five grades, known as extra
light, light, medium, heavy and extra heavy.

PROPERTIES AND TESTS:

4. Flash and fire points: The flash and fire points of the five
grades shall not be lower than the following:

Flash Deg.F. Fire Deg.F

Extra light 315 355

Light 325 365

Medium -—335 380

Heavy 345 390

Extra heavy 355 400

Oil for use in oil compressors where the air leaving any stage or
cylinder has a temperature above 212 °F shall have a flash point not
lower than 400°F.

5. Viscosity: The viscosity of the five grades at 100 °F shall be
within the following limits:

Extra light 140-160 seconds

Light 175-210 seconds

Medium 275-310 seconds

Heavy 370-410 seconds

Extra heavy 470-520 seconds

6. Color: The color of the extra heavy grade shall not be
darker than No. 6 National Petroleum Association Standard or its
equivalent. The color of the other grades shall not be darker than
No. 5 National Petroleum Association Standard or its equivalent.

7. Pour test: The pour test shall not be above the following
temperatures:

Extra light 35^

Light ... 35 F

Medium 40 F

Heavy 45 F

Extra heavy 50 F

8. Acidity: Not more than 0.05 milligrams of potassium hy-
droxide shall be required to neutralize one gram of the oil.

286 BULLETIN NUMBER SIXTEEN OF

CLASS C— LUBRICATING OILS— Continued.

9. Corrosion: A clean copper plate shall not be discolored when
submerged in the oil for 24 hours at room temperature.

10. Emulsifying Properties: The oil shall separate (see note)
in 30 minutes from an emulsion with:

I Distilled water. 2 — I've salt solution. 3 — Normal caustic solution.

Note: — This means that there shall be only a slight cuff between
the water and the oil.

The demulsibility shall not be less than 300.

11. Carbon Residue: The carbon residue shall not exceed the
following :

Extra light 0.10%

Light 0.20%

Medium 0.30%

Heavy 0.40%

Extra heavy 0.60%

12. Further tests on oils of Class C may be required at th©
option of the Department of the Government using the oils.

13. All tests shall be made according to the methods for test-
ing lubricants adopted by the Committee on Standardization of Pe-
troleum Specifications.

AIRCRAFT MACHINE GUN OIL.

GENERAL:

1. This specification covers the grade of petroleum oil used by
the United States Government and its agencies for the lubrication of
machine guns on aircraft, for the c.c. interrupter gears and for gun
oil for cleaning and oiling machine guns and small arms.

2. The oil shall be a highly refined, filtered, straight-run pe-
troleum oil, suitable in every way for the uses specified in Paragraph
1. It shall be a pure petroleum product, without the addition of veg-
etable or animal oils or fats of any kind. It shall not contain any
material which might gum or corrode metals under any conditions.

PROPERTIES AND TESTS:

3. Flash point: The flash point shall not be less than 200°F.

4. Viscosity: The viscosity at lOO^F shall be within the follow-
ing limits: 80 to 115 seconds.

5. Pour test: The pour test shall be 45 degrees or more below
zero Fahr.

6. Acidity: Not more than 0.03 milligrams of potassium hy-
droxide shall be required to neutralize 1 gram of oil.

7. Carbon residue: The carbon residue shall not be more than
0.03%.

.8- All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
55pecifications.

KANSAS CITY TESTING LABORATORY 287

BUFFER OIL FOR RECOIL AND RECUPERATOR CYLINDERS

OF ALL BRITISH TYPES OF HOWITZERS

AND GUN CARRIAGES.

GENERAL:

1. This specification covers the grade of petroleum oil used by
the United States Government and its agencies for filling the recoil
and recuperator cylinders of all British type howitzers and gun car-
riages.

2. The oil shall be a pure refined petroleum oil.

PROPERTIES AND TESTS:

3. The flash point shall not be lower than 265 °F.

4. Viscosity: The viscosity at 100°F shall be within the follow-
ing limits: 65 to 75 seconds.

5. Pour Test: The pour test shall not be above 0°F.

6. Acidity: Not more than 0.05 milligrams of potassium hy-
droxide shall be required to neutralize 1 gram of the oil.

7. All tests shall be made according to the methods for test-
ing lubricants adopted by the Committee on Standardization for Pe-
troleum Specifications.

CUP GREASE.

GENERAL:

1. This specification covers the grades of cup grease used by
the United States Government and its agencies for the lubrication
of such parts of motor equipment and other machinery as are lubri-
cated by means of compression cups; S Vz and $1 to be used in spindle
cups or transmissions.

2. The grease shall be a well manufactured product, composed
of a calcium soap made from high grade animal or vegetable oils or
fatty acids, and a highly refined mineral oil.

3. The mineral oil used in reducing the soaps shall be a straight
well refined mineral oil with a viscosity at 100 °F of not less than
100 seconds.

PROPERTIES AND TESTS:

4. Soap Content:

(a) t V2 cup grease shall contain approximately 13% calcium soap

(b) f 1 cup grease shall contain approximately 14'/r calcium soap

(c) $ 3 cup grease shall contain approximately 18% calcium soap

(d) tt 5 cup grease shall contain approximately 24% calcium soap

5. Consistency: These greases shall be similar in consistency
to the approved trade standards for # V2, tf 1, S 3 and JJ 5 grease.

6. Moisture: The grease shall be a boiled grease, containing
not less than one or more than three per cent of water when finished.

7. Corrosion: A clean copper plate shall not be discolored when
submerged in the grease for 24 hours at room temperature.

8. Ash:

# V2 grease. The ash shall not be greater than 1.7%
Jf 1 grease. The ash shall not be greater than 1.8%
tf 3 grease. The ash shall not be greater than 2.3%
t 5 grease. The ash shall not be greater than 3.5%

288 BULLETIN NUMBER SIXTEEN OF

9. Fillers: The grease shall contain no fillers such as resins,
resinous oils, soap-stone, wax, talc, powdered mica or graphite, sul-
phur, clay, asbestos or any other filler.

10. All tests shall be made according to the methods for test-
ing lubricants adopted by the Committee on Standardization of Pe-
troleum Specifications.

TRANSMISSION LUBRICANT.

GENERAL:

1. This specification covers the grade of petroleum oil used by
the United States Government and its agencies for the lubrication
of transmission gears and bearings, differential gears, worm drives,
winch drives and roller and ball bearings used in connection with
such parts of the equipment of motor vehicles.

2. The lubricant shall be a refined petroleum product, without
the addition of any vegetable or animal oils or products derived from
them and be entirely free from fillers.

PROPERTIES AND TESTS:

3. Flash point: The flash point shall not be lower than 460°F.

4. Viscosity: The viscosity at 210°F shall be within the fol-
lowing limits: 175 to 220 seconds.

5. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

MARINE ENGINE OIL.

GENERAL:

1. This specification covers the grade of oil used by the United
States Government and its agencies for the lubrication of recipro-
cating steam engines in marine service where a compound engine
oil is required.

This oil must not be used in circulating or forced feed systems.

PROPERTIES AND TESTS:

2. The oil shall be a compounded oil made from refined pe-
troleum oil and 10% to 20% of blown refined rapeseed or blown re-
fined peanut oil; so compounded that it will not separate or break
down in any way either before or while in service.

3. Viscosity: The viscosity shall be:

65 to 75 seconds at 210°F.
Not over 700 seconds at 100 °F.

4. Pour Test: The pour test shall not be above 32°F.

5. Acidity: The oil shall not contain more than 1.50% of acid
calculated as oleic acid (equivalent to 3.0 mg K.O.H. per gram of
oil).

6. Corrosion: A clean copper plate shall not be discolored when
submerged in oil for 24 hours at room temperature.

7. Emulsifying Properties: The oil shall remain completely
emulsified for an hour from an emulsion with:

1. Distilled water. 2. 1% salt solution.

8. Wick Feed: The oil shall show a flow at the end of 14 days
of at least 30% of its flow at the end of the first 24 hour period.

9. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

KANSAS CITY TESTING LABORATORY 289

MINERAL STEAM CYLINDER OIL FOR NON-CONDENSING

ENGINES.

GENERAL:

1. This specification covers tlie grade of petroleum oil used by
the United States Government and its agencies for non-condensing
steam engine cylinder lubrication where a mineral oil is required;
also as a stock oil for compounding.

PROPERTIES AND TESTS:

2. The oil shall be a well refined petroleum oil without com-
pounding of any nature.

3. Flash point: The flash point shall not be lower than 475°F.

4. Viscosity: The viscosity at 210 °F shall be within the fol-
lowing limits: 135 to 165 seconds.

5. Cold test: The cold test shall not be above 45°F.

6. Precipitation test: When 5 cc of the oil is mixed with 95
cc of petroleum ether and allowed to stand 24 hours, it shall not show
a precipitate or sediment of more than 0,25 cc (5% by volume of the
original oil).

7. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

COMPOUNDED STEAM CYLINDER OIL FOR NON-CON-
DENSING ENGINES.

GENERAL:

1. This specification covers the grade of petroleum oil used by
the United States Government and its agencies for the lubrication
of steam cylinders of non-condensing engines and pumps where a
compounded oil is required.

PROPERTIES AND TESTS:

2. The oil shall be a well refined petroleum oil, compounded
with not less than 5 nor more than 7% of acidless tallow oil or lard
oil.

3. Flash point: The flash point shall not be lower than 475°F.
Viscosity: The viscosity at 210°F shall be within the following

limits: 120 to 150 seconds.

5. Cold test: The cold test shall not be above 45 °F.

6. Precipitation test: When 5 cc of the oil is mixed with 95 cc
of petroleum ether and allowed to stand 24 hours, it shall not show
a precipitate or sediment of more than 0.25 cc (5% by volume of the
original oil.)

7. Acidity: The oil shall not contain more than 0.40'/^ of acid
calculated as oleic acid (equivalent to 0.80 mg. KOH per gm. of oil).

8. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

290 BULLETIN NUMBER SIXTEEN OF

FLOOR OIL.

GENERAL:

1. This specification covers the grade of oil used by the United
States Government and its agencies for polishing and preserving
wooden floors.

2. The oil shall be a well refined straight petroleum oil.

PROPERTIES AND TESTS:

3. Flash point: The flash point shall not be lower than 300°F.

4. Viscosity: The viscosity at 100 °F shall be within the fol-
lowing limits: 60 to 100 seconds.

5. Color: The oil shall be pale or red in color. Black oil will
not be accepted.

6. Pour test: The pour test shall not be above 35°F.

7. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

GEAR CHAIN AND WIRE ROPE LUBRICANT.

GENERAL:

1. This specification covers the grade of petroleum oil used' by
the United States Government and its agencies for the lubrication
and protection of chains, wire ropes and gears of cranes, dredges,
steam shovels and all other heavy equipment, for the lubrication and
protection of the gears and ropes of balloon hoists; and for swabbing
the wires and cables of aircraft.

2. The oil shall be a petroleum product only, free from veg-
etable or animal oils or products derived from them. It shall be
entirely free from fillers, such as talc, resin, and all materials of
every nature not related to the original product.

PROPERTIES AND TESTS:

3. Viscosity: The viscosity at 210°F shall be within the fol-
lowing limits: 900 to 1,100 seconds.

4. Protection: When applied to a plate of polished steel the
lubricant shall protect the steel for a period of thirty days when im-
mersed in a 10% salt solution.

5. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

GUN AND ICE MACHINE OIL.

GENERAL:

1- .This specification covers the grade of petroleum oil used by
the United States Government and its agencies for cleaning and oil-
mg guns and small arms where Aircraft Machine Gun Oil is not re-
quired; also for lubrication of the cylinders of Ice Machines; for
lubrication of pneumatic tools and for hydraulic systems.

2 The oil shall be a straight-run, highly refined petroleum oil,
iree trom vegetable or animal oils or products derived from them;
sha be suitable in every way for the uses listed in Paragraph 1; and
snail not gum or corrode metals under any conditions.

I $12^ "'^^ ^^^^^ ^^ supplied in two grades known as # 100

KANSAS CITY TESTING LABORATORY 291

PROPERTIES AND TESTS:

4. Flash point: The flash point shall not be lower than 290 °F.

5. Viscosity: The viscosity at 100°F shall be within the fol-
lowing limits:

# 100 oil 95 to 110 seconds
t 125 oil 120 to 135 seconds

6. Pour test: The pour test shall not be above 5°F.

7. Acidity: Not more than 0.03 milligram of potassium hy-
droxide shall be required to neutralize 1 gram of the oil.

8. Emulsifying properties: The oil shall separate completely
in 30 minutes from an emulsion with:

1. Distilled water.

2. 19c salt solution.

9. Normal caustic soda solution.
The demulsibility shall not be less than 300.

9. All tests shall be made according to the methods for test-
ing lubricants adopted by the Committee on Standardization of Pe-
troleum Specifications.

RECOIL OIL.

GENERAL:

1. This specification covers the grades of petroleum oil used by
the United States Government and its agencies to fill the recoil
cylinders of gun carriages.

2. Only refined petroleum oils without the admixture of fatty
oils, resins, soap or other compounds not derived from crude petro-
leum will be considered.

3. These oils shall be supplied in three grades, known as light,
medium and heavy.

PROPERTIES AND TESTS:

4. Flash and fire points: The flash and fire points of the three
grades will not be lower than the following:

Flash Deg.F Fire Deg.F

Light 225 250

Medium 315 355

Heavy : 345 390

5. Viscosity: The viscosity of the three grades of oil at 100°F
shall be within the following limits:

Light 40- 45 seconds

Medium 140-160 seconds

Heavy 385-430 seconds

6. Color: The oil shail be pale or red in color. Black oil will
not be accepted.

7. Pour test: The pour test shall be 5 or more degrees below
zero F.

8. Acidity: Not more than 0.05 milligram of potassium hy-
droxide shall be required to neutralize 1 gram of the oil.

9. Corrosion: A clean copper plate shall not be discolored when
submerged in the oil for 24 hours at room temperature.

10. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petro-
leum Specifications.

292 BULLETIN NUMBER SIXTEEN OF

LIBERTY AERO AND MOTOR CYCLE OIL.

GENERAL:

1. This specification covers the grade of oil used by the United
States Government and its agencies for the lubrication of stationary-
cylinder air-craft engines and motor cycles.

2. The oil shall be made from pure, highly refined petroleum
products and must be suitable in every way for the entire lubrica-
tion of stationary cylinder air-craft engines and motorcycle engines
operating under all conditions. The oil shall not contain moisture,
sulphonates, soap, resin, or tarry constituents which would indicate
adulteration or lack of proper refining.

3. These oils shall be supplied in two grades, to be known as
Grade 1 and Grade 2.

PROPERTIES AND TESTS:

4. Flash point: The flash point of the two grades shall not be
lower than the following:

Grade 1— 400°F. Grade 2— 500°F.

5. Viscosity: The viscosity of the two grades at 210 °F shall
be within the following limits:

Grade 1 (Summer) 90-100 seconds

(Winter) 75- 85 seconds

Grade 2 125-135 seconds

6. Pour Test: The pour test of Grade 1 shall not be above tho
following limits:

Summer 45°F, Winter 15°F.

7. Cold Test: The cold test of Grade 2 shall not be above 35°]"'

8. Acidity: Not more than 0.10 mg. of potassium hydroxid*
shall be required to neutralize one gram of Grade 1 oil.

9. Emulsifying Properties: The oil shall separate completed
in one hour from an emulsion from distilled water at a temperatur*
of 180°F.

10. Carbon Residue: The carbon residue on Grade 1 shall not
be over 1.5%; on Grade 2, not over 2.00%.

11. Precipitation test: When 5 cc of the oil is mixed with 95 cc
of petroleum ether and allowed to stand 24 hours, it shall not show
a precipitate or sediment of more than 0.25 cc (5% by volume of the
original oil).

12. All tests shall be made according to the methods for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

KANSAS CITY TESTING LABORATORY 293

OIL AND GREASE USED IN RECOIL MECHANISM OF 75 AND
155 MM GUN CARRIAGE (French).

GENERAL:

1. This specification covers the grade of petroleum oil and
grease used by the Un'ted States Government and its agencies for
the recoil mechanism of 75 and 155 mm French gun carriages.
RECUPERATOR OIL:

2. Recoil oil (heavv) shall be used.
RECUPERATOR GREASE:

3. The grease shall be a well manufactured product composed
of a calcium soap made from high grade animal or vegetable oils or
fatty acids and a highly refined mineral oil.

4. The minei'al oil used in reducing the soap shall have a vis-
cosity at 100 °F of not less than 180 seconds.

PROPERTIES AND TESTS:

5. Soap Content: The grease shall contain approximately 18%
of a calcium soap.

6. Consistency: This grease shall be similar in consistency to
the approved trade standard for No. 3 grease.

7. Moisture: The grease shall be a boiled grease containing not
less than 1 nor more than 3% of water when finished.

8. Corrosion: A clean copper plate shall not be discolored when
submerged in the grease for 24 hours at room temperature.

9. Ash: The ash shall not be greater than 2.3%.

10. Fillers: The grease shall contain no fillers, such as rosin,
resinous oils, soapstone. wax, talc, powdered mica or graphite, sulphur,
clay, asbestos or any other filler.

11. All tests shall be made according to the methods for test-
ing lubricants adopted by the Committee on Standardization of Pe-
troleum Specifications.

PARAFFIN WAX.

GENERAL:

1. This specification covers the grades of paraffin wax used
by the United States Government and its agencies.

2. This wax shall be a highly refined petroleum product, free
from animal or vegetable wax or other adulterants.

3. This wax shall be supplied in three grades known as 130-132,
124-127, and 117-120.

PROPERTIES AND TESTS:

4. Color: The color shall be water-white.

5. Melting point: The melting points shall be as indicated:

Grade ^F °C

Melting point
130-132 130-132 approx. 55

124-127 124-127 approx. 52

117-120 117-120 approx. 48

All tests shall be made according to the methods for te.sting
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

294 BULLETIN NUMBER SIXTEEN OF

TRANSFORMER OIL.

GENERAL:

1. This specification covers the grade of petroleum oil used by
the United States Government and its agencies for oil switches, oil
circuit breakers and transformers.

2. The oil shall be made from pure, highly refined petroleum
products, free from animal or vegetable oils or fats of any kind and
shall be suitable in every way for the purpose listed in paragraph
one.

PROPERTIES AND TESTS:

3. Flash point: The flash point shall not be lower than 290 °F.

4. Viscosity: The viscosity at 100° F shall be within the follow-
ing limits: 95-110 seconds.

5. Pour test: The pour test shall not be above 20°F.

6. Acidity: Not more than 0.03 mg. of potassium hydroxide
shall be required to neutralize one gram of the oil.

7. Heat Test: The oil shall not show a deposit or any change
other than a darkening of color when heated to 450 °F.

8. Corrosion test: A clean copper plate shall not be discolored
when submerged in the oil for 24 hours at room temperature.

9. Break down test: The break down value shall not be less
than 23,000 volts.

10. Unsaturation test: The oil shall not contain more than 4.0%
of hydrocarbons soluble in concentrated sulphuric acid.

All tests shall be made according to the methods of testing lubri-
cants adopted by the Committee on Standardization of Petroleum
Specifications.

CAR OIL.

GENERAL:

1. This specification covers the grade of oil used by the United
States Government and its agencies as a lubricant on journals of all
cars, passenger coaches, steam and electric locomotives.

2. Only refined petroleum oils, without the admixture of fatty
oils or other compounds not derived from crude petroleum will be
considered.

PROPERTIES AND TESTS:

3. Flash point: The flash point of this oil shall not be lower
than 300^ F.

4. Viscosity: The viscosity at 210° F shall be within the foUow-
mg limits: 65-75 seconds.

5. Cold test: The cold test shall not be above 32°F,

6. Precipitation test: When 5 cc of the oil is mixed with 95 cc
of. petroleum ether and allowed to stand 24 hours, it shall not show
a precipitate or sediment of more than 0.25 cc (5% by volume of the
original oil).

7. All tests shall be made according to the method for testing
lubricants adopted by the Committee on Standardization of Petroleum
opacifications.

KANSAS CITY TESTING LABORATORY 295

LOCOMOTIVE ENGINE OIL.

GENERAL:

1. This specification covers the grade of oil used by the United
States Government and its agencies as a lubricant (by the Panama
Canal) for all locomotives, running gears of all locomotive cranes,
deck machinery of dredges (except engines) and for cold-saws in ma-
chine shops.

2. Only refined petroleum oils, w^ithout the admixture of fatty
oils or other compounds not derived from crude petroleum, will be
considered.

PROPERTIES AND TESTS:

3. These specifications are identical with those of Car Oil (Pan-
ama Canal).

4. Flash point: The flash point of this oil shall not be lower
than 300°F.

5. Viscositj": The viscosity at 210°F shall be within the fol-
lowing limits: 65 to 75 seconds.

6. Cold Test: The cold test shall not be above 32°F.

7. Precipitati'on test: When 5 cc of the oil is mixed with 95 cc
of petroleum ether and allowed to stand 24 hours, it shall not show a
precipitate or sediment of more than 0.25 cc (5% by volume of the
original oil).

8. All tests shall be made according to the method for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

CRANK PIN GREASE, DRIVING JOURNAL COMPOUND, ROD

CUP GREASE.

GENERAL:

1. This specification covers the grade of grease used by the
United States Government and its agencies for the lubrication of driv-
ing journal on locomotives (provided with gi-ease cellars) and for the
lubrication of cranks and rods on locomotives (provided with grease
cups).

2. The grease must be a well manufactured product, suitable
in every way for the purpose listed in paragraph No. 1. It shall be
composed of a soda soap (made from tallow) combined with a well
refined cvlinder stock petroleum oil.

PROPERTIES AND TESTS:

3. It shall be smooth, unifoi'm and must not crumble under
pressure.

4. Color: Driving Journal Compound shall be green or green-
ish in color. Rod Cup Grease and Crank Pin Grease shall be slightly
yellowish, in color.

5. Soap Content: The soap content shall not be less than the
following:

Driving Journal Compound 45%

Rod Cup Grease 40%

6. Free Alkali: Neither grade shall contain less than 0.50%
nor more than 2.5% of free alkali, calculated as NaOH.

7. The total water, glycerin and impurities present shall not ex-
ceed one-third of the total dry soap content.

8. All tests shall be made according to the method for testing
lubricants adopted by the Committee on Standardization of Petroleum
Specifications.

296 BULLETIN NUMBER SIXTEEN OF

PETROLEUM GREASE.

Petroleum grease is a sort of amorphous wax. It is obtained as
follows:

Wfien refining to cylinder stock, the residue in the still, which
is a cylinder stock, is mixed with naphtha. This mixture is then al-
lowed to settle, while being kept at a low temperature. The mixture
separates into two parts, the lower being the petroleum grease and
the upper part is drawn off. This upper part is then heated to drive
off the naphtha which can be used again and the remaining residue
is a low cold-test stock.

The petroleum grease may be filtered to produce the different
colored petrolatums. With some crudes, it is possible to obtain the
petrolatum stock by straight refinement; that is, it remains as a
residue in the still, after the lighter parts of the crude have been
distilled off. These crudes are very few, however, and come from
certain sections of Pennsylvania.

PETROLATUM.

Petrolatum consists of the higher members of the Paraffin series,
which settle from certain kinds of petroleum mixed and inseparable
from some of the oily constituents of the oil. Its uses for the light-
colored or filtered material are medicinal and for the toilet, or as
dark-colored material, it is used by makers of oiled paper and for the
purposes as outlined elsewhere.

Bacon & Hamor, "American Petroleum Industry" classify the
commercial varieties of petrolatum under two heads:

1. Those which are obtained as a ready-formed mixture of hy-
drocarbons of gelatinous consistency.

2. Those made by directly mixing solid paraffins of low melt-
ing-point with heavy lubricating oils. The latter varieties are less
homogeneous and are liable to deposit granules of paraffin on keep-
ing, and they are therefore not suited for the preparation of ointments
as is the true American petrolatum.

The viscosity of natural American petrolatum is given as:

45°C 50°C 80°C 100°C
Engler Vise 4.8 3.7 2.1 1.6

Petrolatum is also called petroleum jelly, petrolatum ointment,
petrolatum album and white petrolatum jelly, according to its degree
of refinement by the medical profession.

It is insoluble in water ^nd easily soluble in ether, chloroform,
oil of turpentine,, benzine, carbon bisulphide, petroleum benzine and
also most of the fixed or volatile oils.

The specific gravity ranges from about .820 to .865 at 60° F.

It does not oxidize on exposure to the air and is not readily acted
upon by chemical reagents.

KANSAS CITY TESTING LABORATORY 297

Some of the main types of greases and their uses are as follows:

(a) Axle Grease Carriage and wagon axles.

(b) Cup Greases Used in compression cups, funnel cups,

or in the bearing by packing.

(c) Gear Greases Tacky, waterproof grease for gears,

racks, etc.

(d) Curve or Track Greases Applied with brush or dauber to railway

track curves.

(e) Launching Grease Used on shipways.

(f) Tunnel-bearing Grease Made in small blocks, about 56 lbs.

Used in standard grease boxes to lubri-
cate shaft bearings of steam ships.

(g) Semi-fluid Grease Used in textile mills, high-speed ma-

chinery, etc., also in mine cars.

(h) Steel-mill Greases Cold-neck grease. Usually a cold-set

resin grease. For toll necks running at
ordinary temperatures.
Hot neck grease: An adhesive, high-
melting-point grease, waterproof.

(i) Elevator Greases Plunger grease: Waterproof, acid-less

. grease. Must not injure rod packings.

Slide grease: Used on elevator slides.

Usually No. 3 consistency graphited.

(j) Gear-shield Grease or Pinion

Glaze Usually made in 3 consistencies of dif-
ferent melting points. Used on steel
mills, etc., where gears are exposed to
intense heat. The grease in cooling
forms a cushion which adheres to the
gear. Usually the heavy grade re-
quires melting before application to
the gear.

(k) Railroad Grease Rod grease. Usually hard. Used in driv-
ing rod cups.

Driving-journal compound: hard. Made
to fit the grease boxes.

Wool-mixed grease: Made of long-fibre
woolen yarn and a small percentage of
cotton waste, impregnated with a
high-melting-point grease. Used for
journal lubrication, instead of usual
oil and waste.

Air-brake grease: Usually a graphited
waterproof grease.

(1) Paper-mill Greases Usually fiber type. High melting point.

Bearings are very hot, due to steam
passing through them. Wool-mixed
grease often used, or box is packed with
wool, and from time to time fresh
grease is added.

298

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY 299

PETROLEUM LIQUIDUM, U. S. P.
Liquid Petrolatum.

Petrolat. Liq. — Liquid Paraffin, Mineral OiL

A mixture of liquid hydrocarbons obtained from petroleum. Pre-
serve it in well closed containers, protected from light.

Heavy Liquid Petrolatum. — Heavy Liquid Petrolatum has a vis-
cosity of not less than 3.1 when determined by the test given below.

Light Liquid Petrolatum. — Light Liquid Petrolatum has a vis-
cosity of not more than 3 when determined by the test given below
and vaporizes freely.

Each variety conforms to the following description and tests:

Specific gravity for Liquid Petrolatum, 0 828 to 0.905 at 25°C.

A colorless, transparent, oil liquid, free or nearly free from fluo-
rescence, odorless and tasteless when cold and possessing not more
than a faint petroleum odor when heated.

When cooled to 10 °C Liquid Petrolatum does not become more
than opalescent (solid paraffins).

Insoluble in water or alcohol; soluble in ether, chloroform, petro-
leum benzin or in fixed or volatile oils. Camphor, menthol, thymol
and many similar substances are dissolved by Liquid Petrolatum.

Boil 10 mils, of Liquid Petrolatum with an equal volume of al-
cohol, the alcoholic liquid is not acid to litmus (acids).

Introduce into a glass-stoppered cylinder which has been pre-
viously rinsed with sulphuric acid 5 mils, of Liquid Petrolatum and
5 mils, of colorless sulphuric acid, heat in a water bath during 10
minutes, shaking well at intervals of 30 seconds; the oil remains un-
changed in color and the acid does not become darker than pale
amber (carbonized impurities).

Prepare a clear, colorless saturated solution of lead oxide in an
aqueous solution of sodium hydroxide (1 in 5) and mix 2 drops of
this solution with 4 mils, of Liquid Petrolatum and 2 mils, of de-
hydrated alcohol; the mixture does not darken after heating for 10
minutes at 70 °C and cooling (sulphur compounds).

Viscosity. — Make a permanent mark about 2 cm. below the bulb
of a 50 mil. pipet of the usual type and note the time in seconds
required at 25'C for the level of distilled water to fall from the
upper to the lower mark as the liquid flows from the pipet. The
time should not be less than 25 seconds nor more than 30 seconds
for the pipet selected.

Draw the Liquid Petrolatum to be tested into this pipet, which
should be clean and dry, and note the time in seconds required at
25 °C for it's level to fall from the same upper to the lower mark as
above determined. The quotient indicates the viscosity. Distilled
water at 25°C is taken as 1.

Average Dose. — Metric, 15 mils.; apothecaries, 4 fluidrachnis.

300 BULLETIN NUMBER SIXTEEN OF

PETROLATUM, U. S. P.

Petrolat. — Petrolatum Ointment, Petroleum Jelly.

A purified mixture of semi-solid hydrocarbons obtained from
petroleum.

Petrolatum is an unctuous mass, varying in color from yellowish
to light amber, having not more than a slight fluorescence even after
being melted. It is transparent in thin layers, completely amorphous,
free or nearly free from odor or taste.

Petrolatum is insoluble in water, almost insoluble in cold or hot
alcohol or in cold dehydrated alcohol, freely soluble in ether, chloro-
form, carbon bisulphide, oil of turpentine, petroleum benzin, benzene
or in most fixed or volatile oils.

Specific gravity, 0.820 to 0.865 at 60°C.

It melts between 38° and 54°C.

Heat about 2 gms. of Petrolatum in an open porcelain or platinum
dish over a Bunsen burner flame. It volatilizes without emitting an
acrid odor and on incineration not more than 0.05 '/c of ash remains.

Shake melted Petrolatum with an equal volume of hot distilled
water; the latter remains neutral to litmus (acid or alkalies).

Digest 10 grams of Petrolatum at 100 °C for half an hour with
10 grms. of sodium hydroxide and 50 mils, of distilled water, then
separate the aqueous layer and supersaturate it with sulphuric acid;
no oils or solid substance separates (fixed oils, fats or rosin).

PETROLATUM ALBUM, U. S. P.

White Petrolatum.

Petrolat. Alb.— White Petroleum Jelly.

Petrolatum wholly or nearly decolorized.

White Petrolatum is a white or faintly yellowish unctuous mass,
transparent in thin layers even after cooling to 0°C, completely
amorphous.

In other respects White Petrolatum has the characteristics of
and responds to the tests for identity and purity under Petrolatum.

KANSAS CITY TESTING LABORATORY 301

Paraffin Wax.

After the gasoline, kerosene, naphtha and gas oil have been
removed from crude petroleum by distillation, the residue is run in-
to a special still. This may be the ordinary cylindrical horizontal
still or the tower still. In the horizontal still, the entire distillate
is generally collected for the wax distillate. In the tower still, the
distillate is usually taken off in three portions, a light distillate,
an intermediate distillate and a heavy distillate, coke only remain-
ing in the still.

The heavy distillate contains the wax and is generally known
as "wax distillate," and contains from 596 to 12% of wax and has
a gravity of about 30 to 35° Be'. The amount of paraffin wax in
the usual crude petroleum varies from nothing up to 29c. In rare
instances, petroleum has been found containing as much as 109c of
wax. In the crude petroleum, the wax exists in the amorphous form
known as protoparaffin which is converted into pyroparaffin or
crystalline wax by the action of high temperature.

Distillate carrying the crystalline wax is pumped to the chill-
ing machine in which it is passed through cylinders, inside of
which are inner cylinders containing brine at a very low tempera-
ture. These inner brine cylinders are revolved to get good distri-
bution of the heat. On the outside of the revolving cylinders are
scrapers which prevent the oil flow from becoming sluggish, due to
the solidification of the wax. The chilled wax distillate is pumped
from the chilling machines to the wax press. In the wax press the
cylinders and the plunger push the plates against each other and
the iron rings around the outer edge of the plates form a tight leak
proof joint. The pump pressure on the oil forces it through a can-
vas sheet on which the wax collects. The oil drips down into a trough
where it is collected and pumped into the lubricating stock. The
wax collected on the canvas plates is removed with chipping chisels
or "spuds" and falls into a conveyor which carries it to the slack
wax tank. This slack wax is about 509'f pure, wax and 509c oil. The
slack wax is now melted and pumped into a sweating pan. Each
pan is equipped with a coil of pipe near the bottom. The melted
wax is run into the pans and is chilled by water running through
the pipe coils until it is solid. The temperature of the solid mass
is now slowly raised and under these conditions the oil is gradually
squeezed from the wax and flows away. Most of the color in the
slack wax is carried away with the oil in sweating. The wax that
is obtained from the first process of sweating is commonly spoken
of as paraffin scale. The wax that is re-sweated is spoken of as
sweated wax. The yellow sweated wax is now melted and filtered
through bone meal or fuller's earth. The product ordinarily is col-
orless, odorless and tasteless. The fuller's earth absorbs all tarry and
asphaltic compounds and is used in the proportion of about one ton
of fuller's earth to five tons of wax. The filtration and decoloriza-
tion of the wax is usually carried on by gravity in large upright
cylinders. The fuller's earth may be used over and over again if
burned out to remove coloring matter and residual waxy and oily
material. The oil taken from the slack wax in sweating is com-
monly spoken of as foot's oil. (See also p. 197.)

302 BULLETIN NUMBER SIXTEEN OF

Paraffin wax is usually sold according to melting point. Differ-
ent methods of determining melting point are used. Paraffin wax
is marketed according to the melting point which varies from 105 °F
for what is known as match wax to 140 °F which is the highest grade
wax such as is used for wax paper for packing edible articles. Most
of the high melting point wax is imported and comes from East In-
dian crude petroleum.

Chemically, paraffin wax consists of paraffin hydrocarbons hav-
ing a general formula of CnH2n-h2 and ranging from C23H48 to C3oH72-

Uses of Paraffin Wax.— "Crude Wax": This product is sold
to match factories as "Match Wax" for use on the heads of matches.
It is also used in leather tanneries as a stuffing or loading for the
leather. It is sometimes used for burning in special lamps used
by miners and for marine bunker lights. It is useful also for wax-
ing yarn in the textile industry, to act as a softener and lubricant
for the yarn during winding. The customarv melting ranges for
the two regular grades of wax are 117°F— 119°F and 124°F— 126°F.
Crude wax may be used for any purpose where a petroleum taste
and odor are not objectionable. It is shipped either in slabs or sold
in barrels. The slabs are packed in cases of about 250 pounds, or
in jute bags of about 225 pounds.

"Refined Wax." This product should be free from taste and
odor. It is used for such purposes as a coating for cheese, elec-
trical insulation, coating for beer vats, artificial flower manufacture,
coating vinegar and cider barrels, lining butter tubs, coating butter
cartons, coating paper milk bottle tops, coating paper dinnking cups
and milk bottles, sealing preserves and jams, coating the necks of
drug bottles, etching, also for coating meats, sausages and any pro-
duct which must be prevented from drying out and losing weight.
Some other uses are: Coatings for whisky, alcohol, molasses and
sour kraut barrels, polishing wooden handles, spokes and wooden
ware, saturating paper used in waterproof signs, oyster and ice
cream pails.

It is usually shipped in 20-pound slabs and packed either in
jute bags or wooden cases. A brief description of the method of
using wax to coat cheese is as follows: The wax is used to improve
the appearance of the cheese and to prevent the accumulation of
the green mold which may appear on cheese that is not frequently
handled. It also prevents shrinkage and evaporation of the cheese.
The wax is melted in a large vat, which is heated by steam pipes or
hot water baths. A direct flame cannot be used, because of the
danger of charring the wax. The cheese is immersed in the melted
wax for a few seconds and it is then placed on a rack for cooling.
Usually the cheese is waxed when it is received at the storage ware-
house and when it is from one to two weeks old. This coating for
cheese boxes and butter tubs permits them to be shipped dry, im-
proving their appearance and preventing burst hoops from water-
stocked staves. (J. R. Battle.)

Paraffin wax is valued by the color, melting point and the spe-
cific gravity. The price of the crude wax having a melting point
of from 120°F to 126°F is about 2c p4r pound, while the highly
refined wax having a melting point of up to 140°F is worth about
7c per pound. (1922.)

KANSAS CITY TESTING LABORATORY

303

Paraffin wax is ordinarily obtained from petroleum; also from
shale oil and ozocerite. Paraffin exists in crude petroleum in the
form of protoparaffin, in which condition it does not crystallize out
and cannot be expressed from oil at low temperatures. In order
to obtain it in condition for refrigeration and filtration, the heavy
oil is subjected to a destructive distillation, thereby producing the
crystalline pyroparaffin.

I Grams per lOO ce

f &.

o'r wr aoT sot ^ot jot 6o°r

Fig. 56 — Solubility of Wax.

70'r

Pennsylvania petroleum furnishes from 1%% to 2'/f paraffin
wax, some petroleum such as one in Roumania giving as much as
10%.

The wax distillate from which paraffin is obtained contains ordi-
narily about 10% of wax. This distillate has a gravity of from
33° Be' to 35° Be' and distills over at a temperature of 500 1< to
700 °F. The paraffin is freed from oil by the sweatmg process alter
filtration.

304 BULLETIN NUMBER SIXTEEN OF

PARAFFINUM, U. S. P.
Paraffin,

A purified mixture of solid hydrocarbons usually obtained from
petroleum.

Paraffin is a colorless or white more or less translucent mass,
crystalline when separating from solution, without odor or taste
and slightly greasy to the touch.

It is insoluble in water or alcohol, slightly soluble in dehydrated
alcohol, freely soluble in ether, petroleum benzine, benzene, carbon
disulphide, volatile oils or in most warm fixed oils.

Specific gravity, about 0.900 at 25 °C.

It melts between 50° and 57 °C.

When strongly heated it ignites, burns with a luminous flame
and deposits carbon.

Heat about 0.5 gm. of paraffin in a dry test tube with an equal
weight of sulphur; the mixture becomes black from separated car-
bon and hydrogen sulphide gas is evolved.

Paraffin is not acted upon or colored by concentrated sulphuric
or nitric acid in the cold.

Shake melted paraffin with an equal volume of hot alcohol; the
separated alcohol does not redden moistened blue litmus paper (acids).

KANSAS CITY TESTING LABORATORY 305

Miscellaneous Oils and Their Uses.

Recoil Cylinder Oil or Hydroline Oil is used to fill the recoil
cylinders of gun carriages. It should have a viscosity (S. U.) of
less than 145 at 32 °F and over 43 at 100 °F with a cold test below
0°F. Loss at 212°F for 2 hours, under 57c.

Recuperator Oil is used for the recoil mechanism of 75 and 155
mm French gun carriages. Free from saponifiable matter, flash
point over 345°F, viscosity lOO'F, 385 to 430. Pour test, below
— 5°F.

Recuperator Grease consists of 18% of lime soap; of tallow
oil, neatsfoot oil, lard oil or equivalent, and 82% mineral oil of 180
viscosity at 100°F; maximum water content, 3%; ash, below 2.3%.

Air Compressor Oil quality varies according to the character
of the compressor. In single stage compressors the maximum tem-
perature developed per stroke without cooling by air or water varies
from 145 °F for 10 pounds to 750 °F for 250 pounds pressure. For
a compressor operating at 125 pounds pressure, the lubricating oil
for air cylinders should have the following properties: Viscosity
at 100 °F, 270-350; flash point over 375 °F. For higher pressure, a
high viscosity oil is required. Oils should be distilled or of paraffin
base.

Oxygen Gas Compressors. Oil cannot be used for this purpose.
Water solutions of soft soap (potassium linolate) or glycerin is used.

Carbon Dioxide Compressors. Glycerin is commonly used, but
same oils as for air compressors are satisfactory but must not give
a flavor to the carbon dioxide.

Ammonia Compressors. A pure mineral oil, cold test — 5°F,
flash 365 °F, viscosity 100 at 100 °F.

Airplane Oil (see special specifications). Castor Oil was orig-
inally used and first grade had following properties: Pale yellow,
clear, specific gravity .964, flash point 550°F, fire test, 618°F, cold
test — 10°F, Saybolt Universal Viscosity 100°Fi=1440, 150°F = 308,
200°F=:117, 210°F = 95, 250°F = 64. Acid value 1, free acid 0.5,
iodine value 88.3.

Brick Oil, Repress Oil or Brockie is oil used on the die through
which the plastic clay is pressed for forming the brick. The oil
covers the clay column when it leaves the die and prevents sticking
to the steel plate over which it travels. The column is again oiled
before entering the cutting machine to prevent stickmg to the cut-
ting wires and again to the wire cut sides. About 90% of 27 Be
distillate with 10% of De Gras oil is commonly used for this purpose.

Car Oil, Axle Oil, Summer Black Oil are used for saturating
waste for packing the journal boxes of car axles. It should be suf-
ficiently viscous not to readily drip from the waste. A flash test
of 380°F and cold test of 5°F is usually required.

306 BULLETIN NUMBER SIXTEEN OF

Thread Cutting Oil, Bolt Oil is a compounded product used as a
combination of a lubricant and cooling agent. It is usually com-
posed of a water insoluble metallic soap such as calcium stearate,
copper oleate, zinc oleate which acts as an emulsifying agent, and
a viscous neutral oil about 200 viscosity. A small amount of am-
monia or alkali greatly aids the emulsion. Instead of the metallic
soap, sulphonated oils, naphthenic acids and agitator sludge oils
may be used to produce the emulsions.

Quenching Oils are used for slower cooling of steel than is ac-
complished with water. It must be a pure mineral oil with a high
flash point.

Condenser, Compounded and Blown Oils are mixtures of min-
eral lubricating oils with seed oil, the seed oil usually being blown
to increase the viscosity.

Cylinder Oil or Cylinder Stock is the residue obtained from dis-
tilling special grades of light crude oils with a very large amount
of steam, avoiding cracking as much as possible and from which
the wax distillate has been removed. Cylinder oils vary in gravity
from 20° to 27°Be', flash point from 475°F to 650°F, viscosity at
210°F Saybolt, 100 to 350, cold test 30 to 60°F. They usually are
not filtered but may be refined by filtering through Fuller's earth
or bone black.

Core Oil is 36° gravity mineral oil compounded with boiled lin-
seed oil or china wood oil.

Cream Separator Oils are nonviscous oils of about 30° to 34°Be'
cavity, 70 to 200 viscosity at 70 °F.

Cup Greases are mixtures of petroleum oil and lime soap with
or without rosin oil.

Floor Oil is a light non-viscous neutral oil.

Gear Case Oil or Transmission Oil is a steam refined cylinder
oil with a gravity of about 25°Be', flash point 600 °F, cold test of
30 F, Saybolt viscosity at 210°F of 240.

Harness Oil is a compounded oil or a mineral oil of 175 viscosity
at 100 F and about 25°Be' to 30°Be' gravity containing petrolatum,
leather oil and wax and some fatty oils.

Ichthyol is an artificial preparation obtained by the distillation
of certain bituminous shales and subsequent sulphonation and neu-
tralization with ammonia or soda. It comes on the market under

u ?™al "a"ie of Ammonii Icythyo-sulphonas or Ammonium Sul-
pho-ichthyolate. The specific gravity of the preparation is ap-
proximately 1.0, and it has a viscosity of 17.7 (Engler). A typical
preparation contains 15% to 16% of sulphur, and it is to the sul-

fJu rL-,J^^^^ ^* *^^ preparation is largely due. On account
01 the dilficulty in duplicating exactly the original product and the
scarcity of the original product, it has now attained a very high
price. '' ^

KANSAS CITY TESTING LABORATORY 307

Knitting Machine Oil is a spindle oil of 70-200 viscosity@70°F.

Leather Oil is a non-viscous neutral oil of low viscosity.

Motor-Cycle Oil is a high viscosity lubricating oil similar to
aeroplane oil.

Neutral Oils are oils obtained from pressed distillate.

Non Viscous Neutral Oil is neutral oil having a viscosity be-
low 135 Saybolt at 100 °F.

Viscous Neutral Oil is neutral oil having a viscosity above 135
at 100°F.

Mazout is the term applied to residual fuel oil in Russia.

Mineral Seal Oil is heavy burning oil obtained in the distilla-
tion for cylinder stock.

Oildag is a compound of deflocculated graphite suspended in
petroleum lubricating oil covered by U. S. Patent No. 911,358 by
Acheson.

Paraffin Oil is the wax-free oil obtained by pressing wax dis-
tillate.

Petrolatum is a semi-solid paraffin oil or wax composed of suf-
ficient varieties of petroleum hydrocarbons to give an indistinct melt-
ing point. It has a flow point of about 105 °F (see Petrolatum Mol-
lum).

Petroleum Coke is the residue in coking or tar stills and usually
constitutes about 5'7f of the crude oil. Mid-Continent crude leaves
a residue ordinarily about 6 inches thick in the still and Mexican
crude petroleum leaves a residue about 30 inches thick in the bot-
tom of the still. One ton of Panuco (Mexico) crude oil gives 365
pounds of coke.

Roll Oil for tin, copper and brass rolls has the same qualities
as engine oil.

Sewing Machine Oil is light neutral oil with a viscosity of 75
at 70°F, cold test 20°F or below, fire test 400°F, flash point 340°F
and gravity of 34.5°Be'.

Spindle Oil is the lighter lubricating oil usually of a gravity
of 25-35'Be', flash point^300-450°F, viscosity 40-400 at 70°F, cold
test at 0°F-40°F, colorless to dark red.

Stitching Oil is a light non-viscous neutral oil used in stitching
shoes.

Summer Black Oil is a black lubricating oil of about 500-600
fire test and is used for tempering and for concrete waterproofmg.

Tempering Oil is a viscous neutral oil frequently the same as
hammer oil and summer black oil.

308

BULLETIN NUMBER SIXTEEN OF

mmt.

._^ ^^vr^jTf^r

{?. Of so

.S£iLM-&lLJllj:l—Of^ Wi^yrfT

_/*- ■ /gc T^OL f= ^ a:^

-aoti^

Thickened Oil is a mineral oil in which the viscosity is increased
by the addition of unvulcanized rubber, aluminum soap or blown
vegetable oil.

Turbine Oil is a non-emulsifyins: oil of about 150 viscosity at
70°F and a flash point of about 420°F.

Watch Oil is usually a non-petroleum oil and is ordinarily Dol-
phin oil. Good watch oil is, however, made from petroleum and
is a close distillation cut just above kerosene with a very low cold
test.

Wool Oil is a sun bleached neutral oil sometimes compounded
with lard oil and with a viscosity of 140-160- Saybolt, gravity of
about 32°Be' and flash paint of 375°F. It is used to aid in carding
the wool fibers.

Transformer Oils are

used for cooling transfor-
mer coils used for chang-
ing the voltage of electric
currents. Oil serves in
distributing the heat and
conducting it to the
radiating surfaces. It
prevents oxidation and
hardening of the wire in-
sulation. Transformer oil
must be a poor conductor
of electricity (a high
dielectric strength) for
which reason, it must
contain no moisture, acid,
soaps, suspended matter,
dissolved salts or sapon-
ifiable matter. The effect
of moisture on the dielec-
tric strength is shown in
Fig. 59. Coils of copper
are most satisfactory for
circulating water to cool
transformer oil. Lead
coils have been known to
react with pure mineral
oil to form lead soap.
P r e s u m ably sufficient
oxygen dissolves in the

Wi^i w

WSi

■&i>t4C

■a

t3:i?/«(?

M

o.o/oo '•

r^rff y^

/O so 30 fO

Fig. 57— Solubility of Water in Petroleum,
oil to allow this reaction to take place.

(t '^'iu ^^i^oyi"g method is used to test the dielectric strength
(lor other tests see general methods of testing lubricants).

KANSAS CITY TESTING LABORATORY

309

Method of Testing the Dielectric Strength of Transformer Oils.

The apparatus used for this test is shown in Figure 58, and
is manufactured by the Westinghouse Electric and Manufacturing
Company for this purpose. It consists of a graduated glass cylinder
in which is placed two testing terminals, each a brass sphere V2 in.
in diameter. The lower sphere is fixed and the upper sphere is
adjustable in its distance from the lower sphere. In making the
test, the cylinder is filled with the oil and the gap between the two
terminals is adjusted. The oil is allowed to stand for 10 minutes so
that any air bubbles may escape. The testing voltage is now ap-
plied, beginning low and gradually inci'easing and without opening
the circuit until the breakdown occurs. The oil is then shaken up
and the test is repeated until at least five breakdowns have occurred.
The average of these breakdowns is taken as the dielectric strength.

Instead of having a fixed distance between the terminals a con-
stant voltage may be used and the grap decreased by adjusting the
upper terminal with a slow motion screw until the breakdown occurs.

As a general thing, the dielectr'c strength is proportional to the
amount of moisture in the oil. It is also effected by the presence
of saponifiable oil.

I

m

ur

\NeST/NOHOUS£ T£ST//V(5 3eT

\

Fig. 58 — Apparatus for Te.sting Dielectric Strength.

310

BULLETIN NUMBER SIXTEEN OF

^ ,e/C SrjP/TA'GT/i - /C/COVOLT

Fig. 59— Relation of Water Content to Dielectric Stength of Trans-
former Oils.

KANSAS CITY TESTING LABORATORY

311

Fuel Oil.

Liquid fuel is chiefly crude petroleum and its residues. Shale
oil, coal tars, wood tars and vegetable and animal oils are also used
as fuel to a very limited extent. Petroleum as a fuel for use in
steam or power plants has considerable variations. Its most dis-
tinctive chemical features are the practical absence of mineral mat-
ter, water and light gasoline and the presence of a large amount
of hydrogen. Ordinarily when fuel oil is mentioned, reference is
made to the residue from petroleum distillation, the gasoline and
kerosene having first been removed.

r^/fi j^fdu/eerrcNrs n £(?c//\//ii£/vrj/vjp/92/

ACTUAL

COAL
£(3UIVAL£NT3

COAL

7454^

eso.ooQOooTo/vs 6so,ooo,oooro/vs

The chief properties making fuel oil available for use are the
ease with which it flows, the low cost of handling and the absence
of residue. Fuel oil has a remarkably constant heat of combus-
tion. The heat of combustion in terms of B. T. U. per pound of oil
is higher with lighter oils but is lower in B. T. U. per gallon with
lighter oils, therefore it is obvious that the heavier oils are cheaper
for fuel at the same price per gallon, which is the unit of measure-
ment. Ordinarily, fuel oil
obtained from petroleum
when dry and free from
sediment has a very defi-
nite heating value in rela-
tion to gravity as is shown
by the accompanying
tables on page 318.

The chief impurities
found in fuel oil are water
or brine and asphaltic
sediment. The asphaltic
sediment or tarry matter
has almost as great heat-
ing value as the dry oil
itself but the brine or
water very greatly dimin-
ishes the heating value as
well as interferes with the
mechanical use of the oil.
Feel oil is ordinarily only
used under conditions of
its greater convenience
than coal. In so far as
the cost of heat obtained
from fuel oil is concerned
it is in most localities

Fig-. 60 — Fuel Requirements of tlie United much higher than coal.
States. The price of coal is the

governing feature in the

price of fuel oil. In general practice, three barrels of fuel oil are

equivalent to one ton of coal screenings.

f£TeOL£l/Ai

nnrse/vw£^

NATaeAiaAs

//■^^■^

J6CiOOO, OOO SBLS. /OO.OOO, OOO rOAfS

efSoo.oooH.r:

ss, OOO, OOO roivs

.00/ 7,

eo, OOO, 000 coeps ■^o, 000. 000 to/us

27000,00070/^3

/z.sooroi's

goo a/LLioA/ ca.rr

£S.OOOrOA/S

312 BULLETIN NUMBER SIXTEEN OF

The gravity varies according to the character of the oil and the
amount of light constituents that have been distilled out of it. The
following table shows typical gravities of fuel oil from different
sources:

Gravity

Mexican fuel oil 12.6°Be'

Paraffin base fuel oil 27.5°Be'

California fuel oil 15.5°Be'

Towanda fuel oil 26.0°Be'

Mid-Continent heavy fuel oil 23.5°Be'

Typical Mid-Continent oil 26.5°Be'

Garber, Oklahoma fuel oil 31.3°Be'

The viscosity of fuel oil is not proportional to the gravity as
is indicated by the following tables:

Viscosity and Gravity of Fuel Oils. (See Pages 313-4.)

Gravity Viscosity at 70 ° T

California Crude 16.9°Be' 5400

Residuum from same after cracking 15.5 414

Heavy Kansas Crude 19.7 3360

Residuum from same after cracking 21.2 178

Heavy Mid-Continent fuel oil : 23.5 810

Residuum from same after cracking 21 2 135

Garber, Okla., fuel oil 31.3 183

Residuum from same after cracking 28.0 70

Heavy Mexican flux oil 10 8 14500

Residuum from same after cracking 12. 6 530

Average Mid-Continent fuel oil 27.5 272

Residuum from same after cracking. ...23. 7 88
As compared with other sources of heat, the theoretical amount

of heat obtainable from petroleum or fuel oil as determined when

the combustion is complete and the absorption of heat is complete
IS as follows:

!'Snn'2^n ^- '^- ^- "^ Petroleum at $1.00 per bbl. costs ...$0,165

1,000,000 B. T. U. of good slack coal at S3.00 per ton 0.136

! n^n'^^^ 5 Z: U- °^ natural gas at $0.30 per 1,000 cu. ft 0.33

1,000,000 B. T. U. of coal gas at $0.50 per 1,000 cu. ft 0.79

1,000,000 B. T. U. of electricity at Ic per k. w. hour 2 93

^*^®n^^?7^ '^ ^^^^^ "PO" the following: Fuel oil of specific
^?9i*^,r,2-^^^Tf^^'^°^^'' ^^'ght Pe^ ga"on 7.5 lbs., weight per bar-
i^/onn Ibs^ B. T. U. per lb. = 19,225, per ton = 38,450,000, per gallon=
144,200, cubic foot = 1,078,500, per barrels 6,056,000.

Slack coal = 11, 000 B. T. U. per pound.

Natural gas = 900 B. T. U. per cubic foot.

Theoretical Equivalents.

1 ton of coal = 36 bbls oil=24,500 cu. ft. of natural gas.

wl^ °M ""nf.^c?-^ '^"- ^«al = 160 cu. ft. of natural gas.

ba re o. =0278 ton coal = 6806 cu. ft. of natural |as.
1 pound 011 = 1.75 lbs. coal = 21.3 cu. ft. of natural gas
1 pound coal = 0.763 gallon oil = 12.2 cu. ft. of natural gas.

KANSAS CITY TESTING LABORATORY

313

As to the actual heating value of fuel oils from various sources
the table on page 315 is representative:

KEY TO FIGURE 61.

Curve
No.

a
b
c
d
e
f

g

h

i

J

J'

k

1

r

m

n
n'
o
P

q

r

s
t
u

V

w
w'

X

y

z
z'

A.
B
C
D
E
F
G

TYPE OF OIL

SOLID CURVES

Mexican residue

"Toltec fuel oil," Inter-Ocean Oil Co., N. Y

"Toltec or Panuco oil," Inter-Ocean Oil Co

"No. 102," Union Oil Co., Bakersfield, Cal

"No. 18," Union Oil Co., Bakersfield, Cal

"Standard" Mexican crude (lot 2)

"No. 25," Union Oil Co., Bakersfield, Cal

Mexican crude, Texas Co

Sample No. 3, Angol-Mex. Pet. Products Co

"Gaviota Refinery," Associated Oil Co., Cal

Mexican oil, Atlantic torpedo flotilla, March, 1914. .

Standard Mexican crude (lot 1)

Mexican oil, U. S. S. Arethusa

"Nos. 1, 2, 3," Anglo-Mexican Pet. Products Co.. . .

Producers Crude No. 1 fuel oil. Union Oil Co., Cali-
fornia

"Coalinga Field," Associated Oil Co., Monterey, Cal

"Avon Refinery," Associated Oil Co., Avon, Cal. . . .

Richmond, California

Sun Co., Louisiana

"Standard," Illinois

Gulf Refining Co., Navy standard oil, U. S. S. Per
kins

"Standard," Indiana

"Standard Star," California

"Standard," Illinois (lot 4)

"Standard," Indiana (lot 4)

Gulf Refining Co., Navy contract

"Standard," Lima, Ohio, crude

Camden Chemical Co., by-product of coal tar.

"Star," California

Gulf Refining Co., Navy standard oil, U. S. S. Roe

Standard Mexican gas oil

Indicates test results.

DOTTED CURVES

Panuca crude, Inter-Ocean Oil Co

Mexican petroleum, Texas Co

Associated Oil Co., California

Bakersfield, Cal., pipe line to Port Costa

California Standard Oil Co., steamer Santa Barbara

Beaumont, Tex., Gulf Refining Co

Navy standard oil, Texas Co

GRAVITY

Specific

1.000
.988
.986
.980
.980
.964
.978
.952
.952
.953
.947
.954
.950
.955

.959
.957
.953
.953
.936
.893

.892
.880
.912
.893
.880
.882
.876

.912
.885
.856

.975
.938
.971
.970
.962
.907
.911 to .900

°Be'

Plash
Point,

o p

10.0

11.7

12.0

12

12

13

13

17

17

17

18.

17.0

17.6

16.8

16.1
16.5
17.1
17.1
19.8
27.3

27.5
29.6
23.9
27.3
29.6
29.3
30.4

23.9

28.7
34.2

13.7
19.5
14.2
14.4
15.7
24.8
24 to 26

374
220
124
280
285
202
262
126
164
230
182
145
182
188

174
186
168
228
275
146

180
144
180
146
144
170
149

180
182
151

146
234
257
260
282
222
195 to 220

From "Oil Fuel Handbook."

314

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY

315

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The advantages of the use of fuel oil are as follows:

1. Handling costs are reduced; fewer firemen, coal passers,
helpers, etc., are required, the reduction being approximately in the

ratio of 5 to 1. . . , , .

2. Ease of fire control, ignition, regulation. In an emergency
such as, for instance, a failure in water supply, the oil fire can be
promptly extinguished. Much time is saved in bringing up the steam
pressure; 150 pounds can be secured from cold water in a half hour.

3. Since combustion is nearly perfect, much higher capacities
and efficiencies obtain. Excess air is held to a minimum. The
opening of furnace doors for cleaning or working of fires is dis-
pensed with; furnace temperatures are accordingly almost constant.

4. Smaller storage space is required and this may be at a much
greater distance from furnace.

5. Oil in storage does not diminish in calorific value as does
coal, and there is little danger from spontaneous combustion.

6. The refuse from the combustion of fuel oil is insignificant
and easy of disposal. The boiler room is free of ashes and dust.
Annoyance and damage to surrounding property is minimized. Tubes
do not collect ashes.

7. No banking of fire occurs with the consequent loss.

8. Smoke can be practically eliminated.

9. The heat is largely isolated to the furnace and the boiler
room temperatures are much lowered.

10. Since there is less excess air, the stack area may be slight-
ly less than that required for coal. Stacks having insufficient draft
with coal may with oil, be sufficient.

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V\k. 63— Relative Cost of Coal and Fuel Oil.

f:SV"'^.0O

KANSAS CITY TESTING LABORATORY

321

11. In oil burning furnaces the heat is more uniformly dis-
tributed. There is less burning out of boiler tubes. Firing tools
are unnecessary.

The disadvantages of the use of fuel oil are:

1. The fire and explosion hazard. Oil must have a flash point
of 140°F or more. Some city ordinances prohibit the use of oil be-
cause of the fire risk, and require the tanks to be under ground and
many feet from the nearest building.

2. Cost of oil storage.

3. A more intense temperature due to smaller excess of air with
consequently increased cost of maintenance of furnace and boiler.

4. The noise in combustion and the odor is sometimes objec-
tionable in home furnaces as well as apparent danger of fire or
explosion with complicated method of burning.

5. The liability of leakage and wastage.

6. The deposition of carbon or soot on tubes and furnace walls.

REQUIREMENTS FOR BURNING FUEL OIL.

In the successful combustion of fuel oil, certain conditions must
be complied with as follows:

1. A burner which gives proper atomization of the oil must be
used.

2. Following atomization, the oil must be correctly mixed with
air in order to give complete combustion. Air is introduced through
the checker work under the burners. The quantity so admitted is
varied with the amount of oil being fed; 225-250 cubic feet of air
is good practice.

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322

BULLETIN NUMBER SIXTEEN OF

3. Unless the combustion is complete before the gases reach
the boiler heating surfaces, it will not be completed at all until
after oil and air reach the stack, when it will be wasted. To pre-
vent this occurrence, large combustion spaces are necessary so that
there is a gas travel of sufficient length.

4. Proper selection and location of burners will prevent local-
ization of heat. Otherwise, blistering from overheating may result.

The oil burner atomizes or vaporizes the fuel so that it may be
burned like a gas. There are the following types:

1. The Spray Burner. In this type the oil is atomized by
compressed air or steam.

2. The Vapor Burner. In this type the oil is vaporized and
passed into the furnace.

3. The Mechanical Burner. In this type, the oil is subjected
to high pressure, then vaporized by forcing through a small nozzle.

The first and third types are in use in power plants, the second
or carburetor type is extensively employed in Europe and in house-
heaters using distillate fuel oil.

Stationary boiler plant engineers prefer spray burners over me-
chanical burners. Marine engineers prefer mechanical burners.

Steam spray burners are divided into two groups; outside mixers
and inside mixers. Preference for the mechanical obtains where feed
water is difficult or expensive to secure. The steam spray atomizer
has certain advantages of flexibility, superior range of capacity and
lower installation cost, notwithstanding the fact that both oil and
steam lines are required, whereas the mechanical needs only the
oil line. The spray burner is more easily installed in and removed

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FiK. G.",— Relative Cost of Gas and Fuel Oil.

:90"

•'/OO

KANSAS CITY TESTING LABORATORY

323

from the coal-burning furnace. It requires a lower oil pressure than
the mechanical. The steam required for atomization runs from 2
to 4 per cent of the boiler output. The spray burner may be oper-
ated to induce a suction on the oil supply for small installations.

OPERATION OF BURNERS.

From 25 to 50 pounds pressure is adequate where steam spray
atomizers are used. The mechanical burners require pressures rang-
ing from 50 to 250 pounds. A preferred pressure is about 200
pounds. Whatever the pressure, it must be steady with all oil burn-
ers. In the case of the mechanical, large air chambers on the oil
line are a necessity if duplex reciprocating pumps furnish the pres-
sure. There air chambers are an inconvenience in vessels where
floor space is limited and the navy has overcome their need by using

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U.sed to CO.
Fuol Oil.

in Stack Combustion of

324 BULLETIN NUMBER SIXTEEN OF

rotary and screw pumps which give a steady pressure of oil with
little or no air cushioning.

Fuel oil is heated to decrease the viscosity. The steam spray
atomizer has the advantage over the mechanical in that it will
handle oils of greater viscosity. Exhaust steam passed through
coils is sufficient to raise the temperature to 12.5 °F which is usu-
ally satisfactory. With the mechanical burner, the oil must be more
mobile and a temperature of from 120 to 180 °F is required. A spe-
cial oil heater may be used.

In burning oil a bright, intense white flame ordinarily indi-
cates an excess of air. The air should be regulated until the light
brown haze just disappears at the top of stack.

In lighting of fires a lighted torch is placed directly under the
burner pit and then the oil is turned on. This order of operation
must never be reversed. If the spray is started before the torch
is lighted, the oil will be injected into a dark furnace and an ex-
plosive mixture is likely to be formed by the time the torch has
been lighted.

The usual feeding system consists of an installation of steam-
driven pumps in duplicate. These deliver the fuel from the supply
tank to the burner under pressure. Either pump may be shut
down for repairs without interfering with the operation of the boil-
er, due to a by-passing of the piping.

In using exhaust steam to heat oil, care must be taken that
the oil temperature is not raised above its flash point. A strainer
should be placed on the suction line between storage tank and oil
pressure pump, to keep foreign matter from stopping up the burner.
A relief valve set at a maximum oil pressure should be provided
between the pumps and burners to relieve excessive pressure.

A meter may be installed to record the oil consumption of each
boiler. The oil piping system should be installed so that the oil
can be drained back to the storage tanks when necessary. Many
plants doubly insure their continuous operation by installing the
equipment in duplicate sets. The supply of steam and oil may be
regulated by hand to meet the requirements of the individual burner.

Standpipe pressures provide satisfactory means of operating
low-pressure systems. The steam pump which runs continuously
draws the oil from an underground storage tank and keeps the stand-
pipe supplied.

The design of the oil-burning furnace is highly important. In-
candescent brickwork around the flame is desirable but where this is
impossible, a flat, broad flame, burning close to a white-hot check-
crwork floor through which the air is continuously admitted is ad-
visable. The flame should not impinge directly on the heating sur-
faces and an even heat distribution should be the aim.

The flame should never extend into the tubes. Where the fur-
nace is located under the first pass of the boiler, the heating sur-
faces of the boiler easily absorb radiant energy from the incan-
(k'.scent firebrick. Such constructions as arches, target walls and
the like are of questionable value; by localizing the heat, tubes may
be burned out and the capacity of the boiler limited.

The burning of oil results in a fluffy soot deposit with a trace
of oil and adheres to the tubes. If this deposit is not regularly

KANSAS CITY TESTING LABORATORY

325

removed, it crystallizes and carbonizes on the tubes and is difficult
to scrape off. The frequent use of steam jets will result in clean
tubes, the soot being easily removed in the early stages of its de-
position.

Since the soot deposits which result from the combustion of
oil are in the nature of pure carbon and are very adhesive their
insulating effects are much increased over those from coal. With
coal, the deposits settle on the top of the tube, leaving the balance
of the circumference comparatively free. Oil burning causes deposits
which are more evenly distributed, covering rather uniformly the
entire firing areas.

Prices of Fuel Oil (U. S. G. S.)

0.

1915—

January

Ftbruary

March

April

May

June

July

August

September

October

Xo\ ember

December

1916 —

January 1

February 1

March 1

April

May

June

July

August

September

October

November 1

December 1

1917 —

January 1

40@0.50
40@ .50
30@ .40
35@ .40
35@ .40
35@ .40
35@ .40
50@ .55
50@ .55
60@ .65
75@ .80
90@1.00

00@1.05
05@1.10
10@1.20
S.T@ .95
60@
60@
55@
55@
55@
60@
,00@1.25
,00@1.25

.80
.80
.75
.75
.75
.80

i.oo@2.on

February 1.00@2.00

March 1.00@2.00

April 1.00@2.00

May 1.00@2.00

June 1.25@1.50

July 1.25@1..';0

August 1.25@1.50

September 1.25@1.5n

October 1.60@2.00

November 1.25@2.25

December 1.25@2.25

1918 —

January 1.25@2.2

Februarv 1.25@2.2

March 1.25@2.2

April 1.75@2.2

May l.T5(g2.2

The following table gives the
United States from 1909 to 1920,
U. S. Geological Survey:

Barrels

1920 41,772,000

1919 35,225,000

1918 36,713,667

1917 42,238,565

1916 38,208,516

1915 32,830,187

June 1

July 1.

August 1

September 1

October 1.

November 1.

December 1.

1919 —

January 1.

February

April

May

June

July

August

September

October

November 1.

December 1.

1920 —

January 2.

February 2.

March 2.

April 3.

May 3.

June 3.

July

.\u.gust 3.

September 3.

October 2.

November 2.

December 1.

1921—

January 1.

February

March

April

May

.Tune

July

August

September

October

November

Deci mber

75@2.25
75@2.25
85@1.90
S5@1.90
S5@1.90
85@1.90
7o@1.90

15@2.00

90@1.00

1.00

.90

.90

.80

80@ .85

S0@ .90

S0@ .90

00(n>1.50

50@2.50

20@2.55
15(n2.20
25@2.80
00(53.25
3 5 (ft' 3. 50
15(?'3.50
3.20
25@3.35
00(<f3.30
50@'2.S5
,15(Si2.30
,70@2.05

25(n>1.70

55(S)1.00

60(a) .85

70(n'

•10(.i>

40(0)

35(n>

4 0(ft'

45(S)

75(<i)1.10

90(riil.25

S0(S1.10

.80
.70
.50
.45
.50
.55

fuel oil consumption of railroads of the
figures prior to 1919 being those of the

Barrels

1914 31,093,266

1913 33,004.815

1912 33,605,598

1911 29,748,845

1910 :: 23,187.346

1909 19,905 335

326

BULLETIN NUMBER SIXTEEN OF

Miscellaneous Facts Concerning Heating By Oil.

Good practice in the atomization of fuel oil requires an average
of 0.3 pound of steam per pound of oil burned.

One pound of fuel oil requires 14 to 15 pounds or 200 cubic
feet of air for complete combustion; 225 cubic feet is good practice.

The stack gases from an oil furnace for the highest efficiency
should not contain less than IS^-f of carbon dioxide (over 13% is
good).

The temperature of an oil flame with complete combustion and
without an excess of air is about 3,750° F. (Natural gas flame,
3,250° F.)

One pound of oil will yield on combustion 16 to 17 pounds of
gases of combustion or 400-500 cubic feet at a temperature of 400° F.

Oil is successfully used in melting iron and steel scrap. For this
purpose it is much superior to coal on account of the absence of
mineral matter and the very much smaller amount of sulphur.

One barrel of oil will melt one ton of steel in the reverberatory
furnace, with the furnace walls already hot.

A typical malleable ii'on foundry by the changing of the fur-
naces from coal to oil fuel increased the strength of their castings
lOO'/f and increased the output 209'c

Diesel engines consume from .45 to .7 pound of heavy oil per
brake H. P. per hour.

Oil requires 60 7f of stack area needed for coal firing.

Oil gives a fuel efficiency at least 10% greater than coal.

The advantages of oil fuel installations for locomotives and boats
have been found to be as follows:

(a) Economy of space reserved for carrying fuel; 507f more fuel
value per unit space.

(b) Ease in filling tanks.

(c) Rapidity of time in meeting a varying load on boiler. Fires
may be instantly lighted.

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TEMPERATURE - DEGREES CENTIGRADE
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T.'icr CI rri c TEMPERATURE - OF'^PFES FAHRENHEIT

A ig. 1,^— Jhc Specific Hc-at of Flue Gases, (G, F. Gebhardt.)

KANSAS CITY TESTING LABORATORY

327

(d) Ability to force boiler to extreme duty in case of emergency.

(e) Short height of stack.

(g) Superior personnel available for the operation of the burners.

(h) Ability to secure and maintain higher speed with oil fuel
than with coal. No deterioration in storage.

In the distillation of crude oil in which 50% of the crude is dis-
tilled off as benzine and kerosene, in good practice, 2.8 barrels of fuel
oil are used per 100 barrels of crude oil treated.

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jTheoretical draft with various flue gas and air temperatures, for % chimney 100 feet high and assuming an area
•uiBcient that friction in the chimney may be neglected. For a chimney of any other bagbt, multiply the tabular hgure Dy

i where H is 'the height of the chimney in feet

FiK. 6<S — Influence of Temperaturo.s of Stack on Draft.'! In- oil Furnaces

Based Upon 100-Foot Stack.

328 BULLETIN NUMBER SIXTEEN OF

For all refining purposes in the production of gasoline, naphtha
and kerosene only, from 6 to 7 barrels of fuel oil are required for each
100 barrels of crude treated, assuming that 50% of the lighter hydro-
carbons are distilled from the crude.

One-fourth of a gallon of fuel oil is required to produce one
gallon of 58° Baunie' gasoline by cracking according to a pressure
distillation process now extensively used.

The specific heat of petroleum is about 0.5 (.49-.53), the heat of
vaporization averages about 130 B. T. U. per pound and the heat of
fusion 63 B. T. U. per pound (Paraffin).

For Natural Dry Petroleum of Paraffin or Semi-Paraffin Base
the following relation of gravity (Baume'-U. S.) and heating value
holds:

B. T. U. per pound = 18700 -f 40 (Be'-lO).

Of the world's total tonnage of vessels of 100 tons and upward
on Lloyd's Register, an approximate division as to the fuel motive
power is as follows, according to Westgarth Brown, president of the
South Wales Institute of Engineers:

Per Cent
1919 1920

Using coal as fuel 76 82

Fitted to use oil as fuel for boilers 16.3 10.5

Using oil in internal combustion engines 1.7 1.5

Using sail power only 6 6

3% bbls. oil (42 gallons per bbl.) is the equivalent of 5,000 pounds
hickory or 4,550 pounds white oak.

6 gallons oil equals 1.000 cubic feet of natural gas of calorific
value of 1,000 B.T.U. per cubic foot.

3^4 gallons oil equals 1,000 cubic feet of commercial or water gas
of calorific value of 620 B.T.U. per cubic foot.

2V4 gallons oil equals 1,000 cubic feet by-nroduct coke-oven gas
at 440 B T.U. per cubic foot.

0.42 gallons oil equals 1,000 cubic feet blast-furnace gas at 90
B.T.U. per cubic feet.

SAMPLING FUEL OIL.

The accuracy of tests depends upon the care with which an aver-
age representative sample of fuel oil delivery has been taken and the
importance of obtaining such a sample cannot be over-estimated. Top,
middle and bottom samples should be taken with a standard "car thief"
and these samples should be combined and thoroughly mixed to form
one sample for car deliveries. Where oil is received in tanks or
reservoirs the swing pipe should first be locked at a position well
above the level of the water and sediment usually found in the bottom
of such tanks. Tanks should be sampled every foot for the first five
feet above the bottom of the swing pipe, and at five-foot intervals
from there to the surface of the oil. This sampling should be done
with a standard tank thief, the samples tested individually, and
deductions for impurities made on the separate volumes which these
samples represent. If the tank is a large one, it should be sampled
through at least two hatches. In receiving large deliveries of the
more viscous oils it is necessary to take many samples in order to
insure fair and average impurity (M. & B. S) deductions. This is
because water and sediment do not readily settle out of such oils.

KANSAS CITY TESTING LABORATORY

329

S 6 7 8 9 /O // /^ IJ /^ /5

Fig. 69 — Heat Losses in Flue Gases From Oil Furnaces.

330

BULLETIN NUMBER SIXTEEN OF

Natural and Producer Gas Costs.

The following table of Producer Gas Costs includes fuel, power,
repairs and maintenance, labor and supervision, interest and deprecia-
tion; in fact, every item of cost except the interest and taxes on the
land occupied. (Courtesy of Steere Engr. Co., Detroit, Mich.)

Producer Gas Costs per

Costs at Which Other Fuels Must be Bought to Obtain the

1000 Cu. Ft. for Coal

Same Number of B. T. U.

as When Buying

Producer

Costs Given

Gas With Coal at the Price Given

Coal Gas or

Carburetted

Water Gas per

Hot

Natural Gas

Fuel Oil

Blue Gas per

Raw

Clean

per 1000 Cu. Ft.

per Gallon

1000 Cu. Ft.

1000 Cu. Ft.

Cost of

Pio-
ducer

Cold
Pro-

One

Ton of

Gas at

ducer

Hot

Clean

Hot

Clean

Hot

Clean

Hot

Clean

Coal

Offtake

Gas

Raw

Cold

Raw

Cold

Raw

Cold

Raw

Cold

Gas

Gas

Gas

Gas

Gas

Gas

Gas

Gas

$2.00

3.13c

4.15c

23.7c

31.5c

2.91c

3.86c

12.6c

16.72c

6.45c

8.59c

2.50

3.55

4.57

26.9

34.67

3.3

4.25

14.3

18.40

7.34

9.45

3.00

3.96

4.98

30.1

37.84

3.69

4.64

16.6

20.09

8.20

10.32

3.50

4.38

5.40

33.3

41.01

4.08

5.03

17.65

21.77

9.07

11.18

4.00

4.79

5.82

36.3

44.18

4.46

5.42

19.3

23.45

9.92

12.05

4.50

5.21

6.24

39.5

47.35

4.85

5.81

21.

25.13

10.78

12.91

5.00

5.63

6.66

42.7

50.52

5.24

6.20

22.7

26.82

11.65

13.78

5.50

6.05

7.08

45.9

53.69

5.63

6.59

24.35

28.50

12.5

14.64

6.00

6.46

7.49

49.1

56.85

6.01

6.97

26.0

30.18

13.36

15.50

HEATING VALUES USED.

Producer Gas 145 B. T. U. per cu. ft.

Natural Gas 1,100 B. T. U. per cu. ft.

Fuel Oil 135.000 B. T. U. per gallon

Coal Gas or Carburetted Water Gas 585 B. T. U. per cu. ft.

Blue Gas 300 B. T. U. per cu. ft.

Note: These costs are based on the plant operating with a 100%
load factor; that is, operating at rated capacity 24 hours per day, 365
day-s per year. Comparatively few plants have a lOO^c load factor;
therefore, it is necessary to take this very important point into con-
sideration when estimating the cost of gas.

The cost of Producer Gas, with a i-easonable degree of accuracy
may be estimated for any load factor by applying the formula:

K400R \ T

Where C = Cost of Producer Gas per 1000 cu. ft. under conditions
specified.
A = Number of feet of gas used per day.
B = Days per week plant is in operation.
T = Cost figures shown in table at 100% load factor.
R = Rated hourly capacity of plant in cubic feet.
It also must be kept in mind that furnace efficiencies have a very
great bearing on the cost of the finished product. Without regenera-
tion or recuperation Producer Gas cannot be used as efficiently as the
more concentrated fuels.

The expense of the distribution system and the furnaces also
have an important bearing on the total cost of doing the work.

KANSAS CITY TESTING LABORATORY 331

Colloidal Fuel.

So-called Colloidal Fuel is a mixture of fuel oil and powdered
coal. The coal is suspended in the oil to an extent of as much as
65% by weight and yet remains sufficiently fluid that it may be
pumped and atomized. The usual amount of coal is about 40% with
possibly 1% of some emulsifying agent.

The suspended matter may be low grade pulverized combustible
matter. This incorporated with fuel oil makes possible the use of
low grade coals of the high fixed carbon or high ash types which have
not heretofore been successfully burned.

This colloidal fuel has a specific gravity of 1.00 to 1.25, a weight
of 8.3 to 11.0 pounds per gallon, a flash point the same as the fuel oil,
a heating value of from 14,500 to 17,000 B.T.U. per lb.

Some practical advantages are:

(a) It is about 20% more valuable in thermal efficiency in all
types of boilers, on account of clean combustion.

(b) It can be handled by pumping.

(c) It can be fired by atomization.

(d) It can be stored indefinitely without deterioration, or fire
hazard.

(e) The same volume has nearly twice the power value of coal
and 10% more than fuel oil.

(f) Labor costs are reduced (70% for boats).

(g) It can be covered with water and sinks in water, thus reduc-
ing the fire danger for boats.

The following table summarizes the principal properties of vari-
ous fuels compared with colloidal fuel. Essentially, colloidal fuel is
nothing more than powdered coal, the voids in which have been filled
with fuel oil. It is quite obvious that such a mixture will be suffi-
ciently stable that the coal particles will not settle out.

COMPARISON OF VARIOUS FUEL PRODUCTS.

Ratio of
Heating
Weight B.T.U. Lbs. B.T.U. Value
Spec. Voids per per per per per

Grav. % Cu. Ft. Lb. Gal. Gal. Cu.Ft.

Bituminous Coal, crushed 1 . 33 39 . 7 50 1 3,000 6 . 685 86,900 1 000

PowderedCoal, 85%, 200-mesh . . 1.35 52.5 40 14,000 5,35 '4,900 0.862

FuelOil 0.90 0.0 56.14 19,500 7.51 146,400 1.685

Mixture — Powdered Coal with voids „,„

filled with fuel oil 1.115 0.0 69.6 16,200 9.30 151,800 1.747

332 BULLETIN NUMBER SIXTEEN OF

U. S. Specifications for Fuel Oils (1921).

FUEL OIL FOR DIESEL ENGINES.

General:

1. This specification covers the grade of oil used by the United
States Government and its agencies as a fuel for Diesel engines.

2. Fuel oil shall be a hydrocarbon oil, free from grit, acid, and
fibrous or other foreign matters likely to clo^ or injure the burners
or valves. If required, it shall be strained by being drawn through
filters of wire gauze of 16 meshes to the inch. The clearance through
the strainer shall be at least twice the area of the suction pipe, and
the strainers shall be in duplicate.

Properties and Tests:

3. Flash Point: The flash point shall not be lower than 150°F
(Pensky-Martens closed tester).

4. Water and Sediment: Water and sediment combined shall
not amount to more than 0.19f.

5. Carbon Residue: The carbon residue shall not exceed 0.5'/c.

6. Precipitation Test: When 5 cc of the oil is mixed with 9.5 cc
of petroleum ether and allowed to stand 24 hours, it shall not show a
precipitate or sediment of more than 0.25 cc (5% by volume of the
original oil).

All tests shall be made according to the methods for testing fuel
oils adopted by the Committee on Standardization of Petroleum Speci-
fications.

FUEL OIL (NAVY STANDARD).
General :

1. This specification covers the grade of oil used by the United
States Government and its agencies where a high grade fuel oil is
required.

2. Fuel oil shall be a hydrocarbon oil, free from grit, acid and
importanc of obtaining such a sample cannot be over-estimated. Top,
fibrous or other foreign matters likely to clog or injure the burners
filters of wire gauze of 16 meshes to the inch. The clearance through
the strainer shall be at least twice the area of the suction pipe and
the strainers shall be in duplicate.

Properties and Tests:

3. Flash Point: The flash point shall not be lower than 150°F
(Pensky-Martens closed tester). In case of oils having viscosity
greater than 30 seconds at 150 °F (Saybolt Furol Viscosimeter) (8°
Engler) the flash point shall not be below the temperature at which
the oil has a viscosity of 30 seconds.

4. Viscosity: The viscosity shall not be greater than 140 seconds
at 70°F (Saybolt Furol Viscosimeter). (40° Engler.)

5. Sulphur: Sulphur shall not be over 1.59?.

6. Water and Sediment: Water and sediment combined shall
not amount to over 1.07^.

All tests shall be made according to the methods for testing fuel
oils adopted by the Committee on Standardization of Petroleum Speci-
fications.

KANSAS CITY TESTING LABORATORY 333

BUNKER FUEL OIL "A."
General:

1. This specification covers the grade of fuel oil used by the
United States Government and its agencies where a low viscosity oil
is required.

2. Fuel oil shall be a hydrocarbon oil, free from grit, acid and
fibrous or other foreign matters likely to clog or injure the burners
or valves. If required, it shall be strained by being drawn through
filters of wire gauze of 16 meshes to the inch. The clearance through
the strainer shall be at least twice the area of the suction pipe and
the strainers shall be in duplicate.

Properties and Tests:

3. Flash Point: The flash point shall not be lower than 150°F
(Pensky-Martens closed tester). In case of oils having viscosity
greater than 30 seconds at 150°F (Saybolt Furol Viscosimeter) (8°
Engler) the flash point shall not be below the temperature at which
the oil has a viscosity of 30 seconds.

4. Viscosity: The viscosity shall not be greater than 140 seconds
at 70°F (Saybolt Furol Viscosimeter) (40° Engler).

5. Water and Sediment: Water and sediment combined shall
not amount to over 1.0%.

All tests shall be made according to the methods for testing fuel
oils adopted by the Committee on Standardization of Petroleum
Specifications.

BUNKER FUEL OIL "B."
General :

1. This specification covers the grade of fuel oil used by the
United States Government and its agencies where a more viscous oil
than Bunker Oil "A" can be used.

2. Fuel oil shall be a hydrocarbon oil, free from grit, acid and
fibrous or other foreign matters likely to clog or injure the burners
or valves. If required, it shall be strained by being drawn through
filters of wire gauze of 16 meshes to the inch. The clearance through
the strainer shall be at least twice the area of the suction pipe, and
the strainers shall be in duplicate.

Properties and Tests:

3. Flash Point: The flash point shall be not lower than 150° F
(Pensky-Martens closed tester).

4. Viscosity: The viscosity shall not be greater than 100 seconds
at 122°F (Saybolt Furol Viscosimeter).

5. Sediment and Water: The sediment and water combined
shall not amount to over 1.0%.

All tests shall be made according to the methods for testing fuel
oils adopted by the Committee on Standardization of Petroleum
Specifications.

BUNKER FUEL OIL "C."
General:

1. This specification covers the grade of fuel oil used by the
United States Government and its agencies where a high viscosity oil
is satisfactory.

334

BULLETIN NUMBER SIXTEEN OF

2. Fuel oil shall be a hydrocarbon oil, free from grit, acid, and
fibrous or other foreign matters likely to clog or injure the burners
or valves. If required, it shall be strained by being drawn through
filters of wire gauze of 16 meshes to the inch. The clearance through
the strainers shall be at least twice the area of the suction pipe and
the strainers shall be in duplicate.

Properties and Tests:

3. Flash Point: The flash point shall be not lower than 1.50°F
(Pensky-Martens closed tester).

4. Viscosity: The viscosity shall not be greater than 350 sec-
onds at 122 °F (Saybolt Furol Viscosimeter).

5. Water and Sediment : Water and sediment combined shall
not amount to over 1.0%.

All tests shall be made according to the methods for testing
fuel oils adopted by the Committee on Standardization of Petroleum
Specifications.

Air Supply Required for Different Grades of Fuel.

(William Kent)

Pounds air per pound coal = 1.0.5 [11.52 C + 34.56 (H- -) ]

8

ULTIMATE COMPOSITION OF FUELS.

Ultimate analysis of coal dried at 105°C.

KIND OF COAL

Anthra-
cite

Semi-
Anthra-
cite

Semi-
Bitum-
inous

Bitum-
inous,
Pa.

Bitum-
inous,
Ohio

Lig-
nite,
Tex.

Crude
Oil,
Tex.

Carbon

76.86
2.63
2.27
0.82
0.78

16.64

78.32
3.63
2.25
1.41
2.03

12.36

86.47
4.54
2.68
1.08
0.57
4.66

77.10
4.57
6.67
1.58
0.90
9.18

75.82
5.06

10.47
1.50
0.82
6.33

64.84
4.47

16.52
1.30
1.44

11.43

84.8

11.6

1 \

Hydrogen

Oxygen

Nitrogen.
Sulphur. .

0.8
1.7

Ash

Pounds of Air Required for Combustion.

Per Lb. Dry Coal. . . .
Per Lb. Combustible .
Per Lb. Carbon

14.50
17.39
18.86

15.27
17.42
19.50

17.12
17.96
19.40

15.26
16.81
19.65

15.04
16.05
19.84

12.45
14.06
19.21

20.60
24.29

fv, ^^'^'"^ ^^^ proximate analysis only, a close approximation to
the number of pounds or air required per pound of combustible, in
order to have the air supply SO'/r in excess, is as follows:

A iu • Pounds

Anthracite and semi-anthracite 17.4

Semi-bituminous •_ , Ig 0

Bituminous, Pennsylvania ' 17 0

Bituminous, Ohio 16 0

Lignite, Texas 140

Crude Oil, Texas 20 6

KANSAS CITY TESTING LABORATORY 335

Total Heat Losses Due to Chimney Gases.

L' + U + v.

Loss From Unburned Carbon Monoxide.

101.5 m c

Lt =

m + d
Li = heat lost in B.T.U. per lb. of fuel due to incomplete combustion

of carbon in flue gases,
m = percent carbon monoxide in flue gas.
c = percent carbon in fuel,
d = percent carbon dioxide in flue gas.

Loss From Specific Heat of Gases.

L. = 0.24 W (T.-T,)

Lj = heat lost in B.T.U. per lb. of fuel due to temperature of stack

gases.
T2 = stack temperature.
Ti = air temperature.
W : weight of flue gases per pound of fuel as found by flue gas

analysis or = A + 1, A being pounds air used per one pound

of fuel.

Loss From Water Vapor.

L, =: V (Ti-T.) + 965. (V-Va).

Lt = Loss due to water vapor in the flue gases per pound of fuel.
V = Pounds water vapor in flue gas per pound of fuel used.
Va = Pounds water vapor in air per pound of fuel used.

Fuel Loss in Ashes.
H a,
L4 = or = A P.

H = heating value of ashes or refuse per pound of fuel.

a, = percent mineral matter or ash in fuel used.

as = percent mineral matter or ash in i-efuse.

P = pounds of ashes or refuse per pound of fuel used.

A = B.T.U. per pound of refuse.

hi = loss in B.T.U. per pound of original fuel.

336

BULLETIN NUMBER SIXTEEN OF

Properties and Requirements of One Pound of Various

Fuel Elements.

Carbon (C)

Hydrogen (H)

Sulphur (S)

Carbon

Water

Sulphur

Product

Dioxide

Dioxide

CO2

H,0

SO2

B. T. U. per pound burned

14,600

62,000

4,050

Oxygen consumed, pounds

2.67

7.94

0.998

Nitrogen in air, pounds

8.89

26.59

3.342

Air used, pounds

11.56

34.53

4.34

Oxygen consumed, cu. ft

29.9

89.0

11.2

Nitrogen in air, cu. ft

113.3

338.7

42.6

Air used, cu. ft., 32° F

143.2

427.7

53.8

Flue gas, pounds

12.56

35.53

5.34

Flue gas at 32° F., cu. ft

143.2

338.7

53.8

Flue gas at 525° F., cu. ft

286.4

1033.0

107.6

Total amount of flue gas at 525° F per lb. of fuel:

In cubic feet z= 2.86 C + 10.33 H 4 25 N + 1.07 S — 1.30

In pounds = .126C + .355H 4- .01 N + .053S — .0550

C = Vf Carbon, H = % Hydrogen, N = % Nitrogen, S = % Sul-
phur, 0 = % Oxygen.

Pounds water vapor in flue gas per pound of fuel = .0894 H.

B.T.U. lost per lb. fuel on account of water vapor in flue gas at
525°F = 117. H.

Heating value of fuel (Dulong I'ormula adopted by A.S.M.E.)

B.T.U. per lb. = 146 C + 620 (H--) + 40 S.

8

Pounds air required per lb. fuel = .116 C+ .345 (H--) +.438.

8

Cu. ft. air at 100°F per lb. fuel = 1.63 C + 4.87 (H--) + .628.

8

used.

Add 50% to these values for practice in which 50% excess air is

KANSAS CITY TESTING LABORATORY

337

Fuel Losses in Practice.

Heat Absorbed
and Losses Itemized

Heat absorbed by boiler

Loss due to free moisture in
coal

Loss due to water vapor

Loss due to heat in dry flue
gases

Loss due to carbon monoxide . .

Loss due to combustible in ash
and refuse

Loss due to heating moisture in
air

Loss due to unconsumed hydro-
gen, hydrocarbon, radiation
and unaccounted for

Calorific value of coal .

Highest
Attain-
able
Efli-
ciency

89.86

0.50

4.20

5.33
0.00

0.00

0.11

0.00

100.00%

Excel-
lent

Prac-
tice

80.0

0.5

4.2

10.0
0.2

1.5

0.2

3.4

100.0

/c

Good
Prac-
tice

75.0

0.6
4.3

13.0
0.3

2.4

0.2

4.2

Aver-
age

Prac-
tice

65.0

0.6
4.3

17.5
0.5

^••
4.5

0.3

7.3

100.07c 100. 07f

Poor
Prac-
tice

60.0

f

0.7

4.4

20.0
1.0
It

5.5
rpi
0.4

8.0

100.0%

ZO^J^^.TU S,OpO

laoo

/5,000

eoooo

e% 4 7o ex &% /ox. /e% mz /^ -. 's-.
Fig. 70 — Heat Losses in Oil Furnaces Due to Excess of Air.

338

BULLETIN NUMBER SIXTEEN OF

Radiant Heat.

With poorly installed setting where insulation is not properly at-
tended to, radiation losses may amount to as much as from 6 to 87c.
Whatever the extent of the loss may be, it is usually neglected in
the average plant and it is an actual fact that in 9 plants out of
10 it can be cut in two with a comparatively small expenditure
for insulating material and careful attention to the work.

^^ff//)r/^<f mmr^mm^^m^

/,000 £,000 3,000 -^,000
Kir. 71- II. at Transmission of Iladiant Heat in Fuel Oil

Furnaces.

KANSAS CITY TESTING LABORATORY 339

Stack Design for Oil Furnaces.

Stacks for oil-burning equipment differ considerably from those
for solid fuels as relatively slight drafts are required.

The following table prepared by Weymouth is based on actual
test data. Centrally situated stacks, short flues, average operating
efficiencies and a permissible overload of 50 per cent are assumed.

STACK SIZES FOR OIL FUEL.

Height Above Boiler-room Floor, Feet

Stack Diameter,

80

90 100

120

140

160

Inches

Nominal Rated Boiler, Horsepower

33

161

206

233

270

306

315

36

208

253 295

331

363

387

39

251

303 343

399

488

467

42

295

359 i 403

474

521

557

48

399

486 ' 551

645

713

760

54

519

634

720

847

933

1,000

60

657

800

913

1,073

1,193

1,280

66

813

993 1,133

1,333

1,480

1,593

72

980

1,206 1,373

1,620

1,807

1,940

84

1,373

1,587

1,933

2,293

2,560

2,767

96

1,833

2,260

2,587

3,087

3,453

3,740

108

2,367

2,920 3,347

4,000

4,483

4,867

120

3,060

3,660 4,207

5,040

5,660

6,160

340 BULLETIN NUMBER SIXTEEN OF

Heat of Combustion of Various Substances.

Acetylene

Alcohol, grain

Alcohol, wood

Asphalt, 60° penetration

Asphalt, hard, from petroleum . .
Asphalt, blown, from petroleum .

Benzol

Cane sugar

Carbon or coke

Carbon Monoxide (CO)

Cellulose

Coal, Penn. Anthracite

Coal, West Va. Bituminous

Coal, Wyo. Lignite

Coal, No. Dak. Lignite

Coal, Kansas Bituminous

Coal, Illinois Bituminous

Coal, cannel (Missouri)

Coal, peat

Coke (from bituminous coal) . . . .

Coke, Petroleum

Cottonseed oil

Fuel oil

Gas, coal, min

max

Gas, methane

Gas, water

Gas, hydrogen

Gasoline, average

Gilsonite

Glycerin

Graphite

Hydrogen (Ha)

Iron

Methane (CHJ ....'.

Naphthalene

Oil Gas

Paraffin wax

Producer gas

Shale oil

Shale (Bituminous — Colorado)

Shale (spent)

Starch

Stearic acid

Sulphur

Tallow ....
Wood

Calories

B. T. U.

per Gram

per Lb.

Combustible

of Combustible

Matter

Matter

11,527

20,749

7,054

12,697

5,330

9,594

9,532

17,159

9,989

17,980

10,210

18,380

10,030

18,054

3,961

7,130

8,137

14,647

2,435

4,383

4,208

7,575

8,266

14,880

8,778

15,800

7,444

13,400

6,411

11,540

8,461

15,230

8,056

14,500

8,980

16,165

5,940

10,692

8,047

14,485

8,017

14,503

9,500

17,100

10,833

19,500

4,440

7,990

7,370

12,266

13,344

24,019

2,350

4,230

34,462

62,032

11,528

20,750

9,944

17,900

4,316

7,769

7,901

14,222

34,500

62,100

1,582

2,848

13,343

24,017

9,690

17,442

10,800

19,440

11,140

20,050

773 +

1,391 +

10,970

19,750

4,430

7,975

1,080

1,944

4,228

7,610

9,374

16,873

2,241

4,034

9,500

17,100

4,750

8,550

KANSAS CITY TESTING LABORATORY

341

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KANSAS CITY TESTING LABORATORY

343

Melting Point and Heat of Fusion of Various

Substances.

MELTING POINT

Heat of Fusion

NAME

Calories
per Gram

B. T.U.
per Lb.

Acetic acid

3 °C= 37.4° F
—75 ° C= 103.0° F
—7 ° C = +19.4° F 1
62 ° C= 143.6° F
2 °C= 35.6° F
266.8° C= 514.0° F
— 7.3°C= 18.8° F
321 ° C= 610.0° F
774 °C=1426.0°F
—56.3° C= 133.4° F
1221 °C=2330.0°F
1093 °C=2000.0°F
—103.5° C= 154.0° F
1055 °C=1930.0°F
34 °C= 93.2° F
13 °C= 55.4° F
13 °C= 55.4° F
0 ° C = 32 ° F
325 ° C= 617.0° F
38.7° C- 37.7° F
79.2° C= 175.0° F
— 9.2°C= 15.4° F
1500.0° C =2732.0° F
50.0° C= 122.0° F
25.4° C= 77.9° F
27.4° C= 81.4° F
1779.0° C =3234.0° F
58.0° C= 136.4° F
360.4° C= 681.0° F
999.0° C =1830.0° F
1750.0° C =3183.0° F
96.5° C= 206.0° F
804.0° C =1479.0° F
992.0° C =1818.0° F
318.0° C= 604.0° F
45.0° C= 113.0° F
64.0° C=- 147.0° F
115 0° C= 239.0° F
290.0° C= 554.0° F
228 0° C= 442.0° F
415.3° C= 780.0° F

43.7
108.1

21.0 1
42.3

29 . 1
12.64
16.2
13.7
54.6
43.8
23.0 ;
32.0 :
22.96
43.0
26.3
19.1
42.5
80.0

5 86
2.75
35.5
22.3
36.3
35.1
24.9

4.74

27.2

15.7

28.6

21.1

258.0

31.7

123.5

186.1

40,0

37.0

47.6

9.37

7.2

13.3

28.1

78.7

Ammonia (NH3)

Anilin

194.6

37.8

Beeswax

76.1

Benzol

52.4

Bismuth

22.7

Bromine

29.2

Cadmium

Calcium Chloride (CaCl^;
Carbon dioxide

24.7
98.3
78.8

Cast Iron — gray

white

Chlorine

41.4
57.6
41.4

Copper

77.4

Cresol ....

47.3

Gallium

34.4

Glycerin

76.5

Ice

144.0

Lead

10.5

Mercury

4.95

Naphthalene

63.9

Nitrobenzol

40.1

Palladium

65.3

Paraffin

63.3

Phenol

44.8

Phosphorus

^^

Platinum

49.0

Potassium

28.3

Potassium Hydroxide . . .

Silver

Silica

51.5

38.0

464.5

Sodium

57.1

Sodium Chloride

Sodium Fluoride

Sodium Hydroxide

Spermeceti .

222.3

335.0

72.0

66.6

Stearic Acid

85.7

Sulphur

16.9

Thallium

12.9

Tin

23 9

Zinc

50.6

344

BULLETIN NUMBER SIXTEEN OF

Heat of Vaporization and Boiling Point of Various

Substances.

NAME

Temperature of Boiling
(Pressure not given)

Heat of Vaporization

Calories
per Gram

B. T. U.

per Lb.

Acetic acid

Acetone

Alcohol (ethyl)

Alcohol (methyl, wood)
Ammonia (1 atmos.) . . .

Ammonia

Ammonium Chloride . .

Amyl Alcohol

Amyl Chloride

Amylene

Aniline

Benzol

Butyl Alcohol

Butyric Acid

Carbon Dioxide

Carbon Bisulphide ....
Carbon Tetrachloride. .

Chloroform

Cresol

Chlorine

Decane

Ether

Ethyl Acetate

Formic Acid

Gasoline

Heptane

Hexane

Hexylene

Hydrogen Sulphide. . . .

Iodine

Mercury

Methyl Acetate ^ . . . . .

Nitric Acid

Nitrogen

Nitrous Oxide

Nitrobenzol

Octane

Oxygen

Pentane

Propyl Alcohol . . . .

Sulphur

Sulphur Dioxide

Sulj)huric Acid

Sulphur Trioxide.

Toluol

Turpentine. . .

Xylol....

Water

40

110

56

70

64

-33

17

350

131

107

12

183

80

83

163

46
76
60

201
-22

159
34
73

100

-150

90

68

-61

174

350

57

86

-195

-20

151

120

-188

30

90

316

0

326

18

110

160

139

108

.0°

.6°

.0°

.5°

.5°

.0°

.0°

.0°

.0 '

.5°

.0°

.0°

.0°

.0°

.0°

.2°

.2°

.9°

.6°

.0°

.6^
.6=
.5^

5° C
9° C

.1°
.0°
.0°
.0°
.0°
.0°
.4°
.0°
.0°

.1°

.0°
.6°
.0°
.5°
.0°
.0°
.0°
.0°
.0°
.0°
.0°
.0°
.8°
.0°
.9°
.0°

= 230.0°

= 133.8°

= 158.0°

= 148.2°

= —28.3°

= 62.6°

= 662.0°

= 268.0°

= 224

= 54

-- 360

= 176.0'

= 181.4'

= 325.4'

= 32.0'

= 115.2'

= 169.2'

= 141.6'

= 395.0'
7.6'

= 319.0"

= 94.8'

= 163.6'

= 212.0'
=104-300'

= 194.0'

= 154.4'

= 32.0'

= 78.5'

= 345.0'

= 662.0'

= 134.8'

= 186.8'

= 320.0'

= —4.0'

= 305.0'

= 248.0'
= —306.0'

= 86.0'

= 194.0'

= 601.0'
32.0'

= 619.0'

= 64.4=

= 231.0'

= 320.0'

= 284.0'

= 226.0'

92.8
155.2
208.92
267.5
341.0
297.0
709.0
120.0
56.3
75.0
104.2
93.45
130.4
114.0
56.25
86.67
46.4
58.49
100.5
67.4
60.8

91

84

120

.11
.3

.4

75.00

77.8

.4

.7

79.
92.

132.0
23.95
62.0
97.0

115.1
47.65
67.0
79.2
71.4
58.0
85.8

169.0

362.0
91.7

.1

.4

122.

147.
84.0
74.0
82.0

535.9

167.0
279.3
376.0
481.5
614.0
534.6
1276.0
216.0
101 3
135.0
187.5
168.2
234.7
205.2
101.25
156.0

83.5
105.30
180.9
121.3
109.4
164.0
151.7
216.7
135.0
140.0
142.9
166.8
237.6

43.10
111.60
174.6
207.2

85.8
120.6
142.5
128.5
104.4
154.4
304.2
651.5
165.0
219.8
265.3
151.2
133.2
147.6
964.6

KANSAS CITY TESTING LABORATORY

345

Specific Heat of Various

Acetic acid— solid 0 . 627

liquid 0 . 502

Acetone 0 . 528

Alcohol Methyl— absolute 0 . 600

Alcohol Ethyl— 95 % 0 . 700

Alumina 0.197

Aluminum 0.2185

AUyl Alcohol 0.665

Ammonia (0° C) 0.876

(20° C) 1.190

(70° C) 1.233

Ammonium Nitrate (64%) 0.610

Amyl Alcohol 0 . 455

Amylene 1 . 060

Anilin 0.512

Antimony 0 . 495

Asphalt 0 . 550

Benzol— fluid 0 . 407

solid 0.397

Beeswax 0.820

Bismuth 0.305

Bismuth— liquid 0 . 0308

Brass 0.0939

Brick work and masonry . 0 . 200

Brine, 25% 0.8073

Cadmium 0.1804

Carbon bisulphide 0.240

Carbon (diamond) 0 . 145

Carbon dioxide 0 . 215

Carbon (graohite) 0 . 186

Carbon tetrachloride 0.2C3

Calcium chloride sol.(407c) 0 . 636

Cast Iron O.ISO

Cellulose 0 . 33

Chalk 0.215

Charcoal 0.214

Chlorine— solid f 108° C).. 0.1446
Chlorine— liquid (0° C).. . 0.2230

Coal, average 0 . 220

Coke 0.203

Copper 0.0933

Concrete 0 . 20

Corundum 0.198

Cresol 0.553

Ether 0 . 5034

Flint and rocks in general. 0.200

Fuel oil 0 . 550

Fusel oil 0 . 5640

Gallium— solid 0 . 079

Gallium— liquid 0 . 80

Gasoline 0.475

Gas oil 0 . 500

Glass— plate 0.186

Glass — common 0.117

Substances Solid and Liquid

Glycerin 0.576

Gold 0.316

Granite 0.190

Graphite 0.202

Gypsum, sulphate of lime. 0.197

Heptane 0.487

Hexane 0 . 504

Hexadecane 0.496

Ice 0.505

Iodine 0.057

Iron 0.1130

Kerosene 0 . 490

Lead— liquid 0.0402

Lead 0.0315

Limestone 0 . 210

Manganese 0 . 1217

Magnesium 0.245

Marble 0.208

Mercury 0 . 0331

Naphthalene 0.314

Nickel 0.1091

Nonane 0 . 503

Octane 0.505

Paraffin Wax 0 . 563

Pentane 0.476

Petroleum 0 . 505

Phenol 0.561

Phosphorus (red) 0 . 1698

Phosphorus (yellow) 0 . 202

Platinum 0.0323

Quartz and sand 0 . 190

Quicklime 0.217

Rubber 0.481

Selerium (cryst.) 0.084

Seler.ium (amorph.) 0 . 112

Seawater 0 ^51

Silver 0.0568

Soda Ash 0.231

Solium chloride (26%). . . 0.780
Sodium nitrate (47%).... 0.708
Sulphuric acid (solid) .... 0.2349
Sulphuric acid (liquid). . . 0.3315
Sulphuric acid (85%,). ... 0.406

Sulphur chloride 0.202

Sulphur 0.1844

Sulphur liquid 0.2340

Sulphuric acid (sp. gr. 1.87) 0 . 3350

Tin 0-.0559

Toluol 0.363

Turpentine 0 472

Wood (dry) 0.327

Wood (wet) 0 . 500

Zinc Chloride (68%).... 0.437
Zinc 0.0938

346

BULLETIN NUMBER SIXTEEN OF

Specific Heat of Gases and Vapors.

Acetone

Acetic acid

Air

Alcohol

Ammonia

Argon

Benzol

Blast furnace gas

Carbonic acid, CO2

Carbon monoxide CO

Chlorine

Chloroform

Ether

Flue Gas, 10%, CO2

Hydrogen

Hydrogen chloride

Methane, CH., ]][

Nitrous Oxide

Nitrogen

Olefiant gas, C2H4 (ethylene) .................

Oxygen

Sulphur dioxide (SO2)

Superheated steam (water vapor) (atmospheric

pressure

Helium

Carbon bisulphide (CS2)
Nhric oxide

Constant
Pressure

0 . 3740

0.4125

0.23751

0.4534

0.508

0.123

0.332

0.2277

0.217

0.2479

0.124

0.1567

0.4797

0.318

3.40900

0.194

0.5929

0.224

0.24380

0.404

0.21751

0.1553

0.4805
1.250
0.1596
0.2317

Constant
Volume

0.16847

0.399

0.299

0.171
0 . 1758

0.3411
'2. 41226

0.4683

0 . 17273
0.332
0.15507
0.1246

0.346

KANSAS CITY TESTING LABORATORY 347

Thermal Units.

The BRITISH THERMAL UNIT (B. T. U.) is the heat required
to raise the temperature of one pound of water, one degree Fahr.
(average between 32° and 212° F). As one kilogram is equal to
2.20462 pounds and one degree Cent, is equal to 9/5 degrees Fahr. the
large calorie is 3.96832 (2.20462 X 9/5) times as great as the Brit-
ish Thermal Unit, the small calorie being 0.00396832 times the Brit-
ish thermal unit.

The SxMALL CALORIE is the amount of heat required to raise
the temperature of one gram of water one degree Cent, (from 0° to
1°, 4° to 5°, or 15° to 16° being used, giving slightly different
values.)

The LARGE CALORIE is the amount of heat required to raise
the temperature of one kilogram of water one degree Cent. It is
therefore one thousand times as large as the small calorie.

The HEAT OF COMBUSTION of a substance is the number of
small or large calories of heat evolved during the combustion of a
gram or a kilogram of the substance.

Using the English weights and measures, it is the number of
B.T.U. of heat evolved during the combustion of one pound of the
substance. To convert the former into the latter value the number
of calories must be multiplied by 1.8 (3.96832 -^ 2.20462).

The HEAT OF FORMATION of a substance is the number of
calories of heat evolved or absorbed when a gram molecular weight
of the substance is formed. When heat is absorbed, the value found
is negative.

The MELTING POINT of the substance is the temperature at
which the solid or liquid forms are capable of existing together in
equilibrium.

The BOILING POINT of a liquid is the highest temperature at
which the liquid and its pure vapor can exist together in equilibrium.
This temperature varies with the pressure.

The SPECIFIC HEAT of a substance is the ratio of the number
of thermal units necessary to raise the temperature of a substance
one degree, divided by the number of thermal units necessary to raise
the same weight of water at 60 °F one degree. It may also be de-
fined as the number of thermal units required to raise the tempera-
ture of one gram of a substance one degree Centigrade.

The HEAT OF FUSION of a substance is the number of thermal
units required to change a unit mass of the solid at its melting point
into liquid at the same temperature.

The HEAT OF VAPORIZATION of a liquid is the number of
thermal units required to change a unit mass of the liquid at its boil-
ing point into vapor at the same temperature.

TEMPERATURE UNIT. or thermal intensity is measured in
degrees Centigrade (Celsius)' or degrees Fahrenheit. One degree
Cent, is one one-hundredth of the fliffcrence of temperature between
the freezing point of water and its boiling point at 760 millimeters
pressure as indicated by the expansion of mercury. A degree Fahr.
is one one-hundred eightieth of the difference of temperature between
the freezing point of water and the boiling point of water.

MECHANICAL EQUIVALENT OF HEAT— 779.4 ft. pounds = 1
B.T.U.

348

BULLETIN NUMBER SIXTEEN OF

^ ^ BAUhfE' ^n

AVtTY

S i$ K K Gi

01

\

s

\

o

\

N

y

\

TO

\

s.

\

L

55
^1 ui

\

\

\

\

V

\

\

\

\

\

\

\

\

\

>

\

\

J

\

\

So.

%

Or

\

V

\

\

\

o
-J

01

%

^

i

P)-

01

OvfV

•

^

Fit,'. 72- SI. ale Oil Fractional Gravity Before and After Cracking.

KANSAS CITY TESTING LABORATORY 349

Distillation Products of Coal and Oil Shale.

Oil shale is a stratified sedimentary rock in which are found
numerous fragments of fossil plants and animals, principally aquatic
form. Oil shale in its natural form does" not contain any oil what-
ever but it does contain on the average about 35% of organic matter.
The mineral base of oil shale presents a suggestion as to the origin
of the organic matter. The mineral is a hydrous silicate of alumina
and as a general rule hydrous silicates of alumina have great ab-
sorptive power for hydrocarbons of large molecular weight. A typical
one, Bentonite, as well as Fuller's Earth, has the property of decol-
orizing and removing complex matter from hydrocarbon oils. Oil
shale may then be compared with Fuller's Earth which has turned
black or greenish black after absorbing a large amount of coloring
matter from petroleum. This may readily have taken place while
the petroleum was vaporizing. This organic matter when subjected
to pyrogenic distillation forms the following products:

Fuel oil or shale oil, 20.25% equal to 405 lbs. or 54 gal. per ton.

Water, 4.08% equal to 83 lbs. or 10 gal.

Combustible gas 8.86% equal to 1,605 cubic cubic feet.

Ammonia as ammonium sulphate, 0.90% = 34 lbs. ammonium
sulphate.

Mineral matter and carbonaceous residue 66.0%.

With a low temperature distillation, larger amounts of heavier
fuel oil are obtained. With the higher temperature distillation,
smaller amounts of shale oil containing more or less naphtha and
burning oil are obtained.

A typical distillation of oil shale is as follows:
Commercial Fractions :

Naphtha (410°F) "gasoline" 10.0% (46° Baume')

Burning oil 18.2%

Gas and lubricating oil 61.8%

Residue 10.0%

Fractional Distillation of Oil:

Fraction Boiling point Gravity (25°C)

0- 10 100°C 0.794 = 46.3°Be'

10- 20 194 0.822 = 40.3°Be'

20- 30 230 0.846 = 35.5°Be'

30- 40 255 0.867 = 31.5°Be'

40- 50 285 0.885 =: 28.2''Be'

50- 60 309 0.899 = 25.7°Be'

60- 70 328 0.912 = 23.5°Be'

70- 80 337 0.900 = 25.5°Be'

80- 90 345 0.910 = 23.8°Be'

90-100 350 0.910 = 23.8°Be'

This product in many respects resembles ordinary crude petro-
leum and for this reason the shale oil industry has aroused great
interest on account of its possible substitution for petroleum. Shale
oil, however, is utilized in only a few countries, chiefly Scotland,
though oil shale is very widely distributed throughout the world. The
oil shale resources of the United States are so extensive as to fur-
nish an effective guarantee for the future when the underground
reservoirs of petroleum are exhausted. The cost of obtaining the

350 BULLETIN NUMBER SIXTEEN OF

shale oil, however, will in all probability far exceed the present cost
of obtaining- petroleum. It is possible that the mining of petroleum
by shafts will be resorted to before it is necessary to depend upon
oil shale as a source of fuel oil. Many difficulties of mining, pro-
duction, refining and marketing of shale oil must be overcome. Much
of the known oil shale is remote from routes of transportation in a
territory difficult of access and is far removed from points of fuel
oil consumption. Methods of mining and transportation must be
developed; processes of extracting the oil from the shale must be
perfected; improved methods of refining which do not entail large
losses must be worked out. Present methods of refining crude oil
cannot be profitably applied to the refining of shale oil on account of
the different chemical character. Most oil shale is a tough, brown-
ish to black fine grained rock. It is riot an article of commerce ex-
cept possibly as a road building material and it cannot be transported
any great distance from the point where it is mined. The mineral mat-
ter is the greater portion of its content and is essentially a disin-
tegrated feldspar impregnated with the organic matter. The com-
position of the mineral ash of a shale found in Colorado is as follows:

Loss on ignition 11.05%

Silica (SiO.) 37.10%

Alumina (AKOs) 20.30%

Iron Oxide (Fe.Os) 9.20%

Lime (CaO) 12.05%

Magnesia ,..(MgO) 5.10%

Sulphur (SO3) 4.80%

Alkalies and difference 0.40%

100.00%

It is estimated that in Colorado alone there is enough shale to
produce 20,000 million barrels of oil and 300 million tons of am-
monium sulphate.

Oil shale is mined somewhat like coal and is then crushed to con-
venient size and roasted in retorts, in which its volatile constituents
are driven off. In Scotland and France, the only countries where
the oil shale industry has yet been established, the shale is fed by
gravity from a storage hopper into the top of a vertical cylindrical
retort; in which it is allowed to move slowly downward while it is
being roasted until it is discharged from the lower end as waste. The
heat is applied externally in such a manner that the temperature in-
creases downward in the retort. The temperature in the upper third
\. n^!^o^ where all the oil gases are driven off does not rise
above 900 F; the temperature in the lower part of the retort is
raised to about 1600°F in order to convert the maximum amount of
nitrogen in the shale into ammonia. The gases and vapors formed in
the retort are conveyed through condensing and scrubbing apparatus
to separate and clean the oil and ammonia. The oil is then refined
by methods similar to those used in refining petroleum and the am-
monia IS converted into ammonium sulphate by treatment with sul-
phuric acid.

KANSAS CITY TESTING LABORATORY

351

TEMP.

5 § 8 g g g

TAHFf.

(X
H

\

o
ft

\

v

\

\

\

\,

\

\,

0^

s

\,

N

\

o

)0i

\

\

V

X.

N

\

:5

\

^,

!8

ay

I'\

Ul

O

cS-

Fig. 73 — Shale Oi! Distilling Temperature Before and After Cracking.

352 BULLETIN NUMBER SIXTEEN OF

Occurrence and Distribution. — Oil shale, like coal, occurs in beds
that range in age from Devonian to Tertiary. The principal beds
of oil shale in Scotland, France and Canada are in the older forma-
tions, but the richest and largest deposits in the United States are in
the Green River formation, of Eocene (Tertiary) age.

Shale from which oil can he distilled probably occurs in nearly
all countries but it has been reported in comparatively few, either
because it is so similar in appearance to ordinary carbonaceous shale
or because there has been so little demand for it while petroleum
has been plentiful that no special search has been made for it.

In North America, oil shale occurs in both Canada and the United
States but is commercially undeveloped. The richest shales in the
Rocky Mountains region of the United States are of Tertiary age but
large areas in the eastern part of the United States and eastern
Canada are underlain by dark shales of Paleozoic age that are in
many places as rich in organic matter from which oil can be dis-
tilled as those that are mined commercially in Scotland and France.

Comparatively little is known about oil shale in South America
though it is said to occur in Argentina, at several localities in Brazil
and in Chile. Unsuccessful attempts have been made to distill oil
profitably from oil shale in eastern Brazil but the failure is reported
to have been due to mismanagement rather than to the poor quality
of the shale.

In Africa, thin beds of shale capable of yielding oil when dis-
tilled are reported from Angola, the Belgian Congo, Natal and the
Transvaal but the shale is mined in none of these countries and the
thickness, richness and extent of most of the deposits are not re-,
ported. Perhaps the largest area underlain by oil shale is in the Bel-
gian Congo.

In Europe, the commercial development of the oil shale industry
began early in the nineteenth century before the rise of the modern
petroleum industry. In 1913, the world's output of oil shale was
3,591,810 metric tons of which 3,573.810 tons were mined in Europe.
About 91 per cent was produced in Scotland, 8 per cent in the Autun
and Aumance districts in France and the remainder in Australia,
Germany and Italy. In Scotland, the oil shale industry has been
able to compete successfully with the petroleum industry because of
the output of valuable by-products made in connection with the oil
and because of the remoteness of Scotland from the principal sources
of petroleum — southern Russia and the United States. Large de-
posits of oil shale are reported to occur in northern Russia.

Oil shale in Asia is not mentioned in reports but valuable de-
posits may nevertheless exist there even in areas that have been cov-
ered by geologic studies.

In Oceanica some oil shale has been mined and distilled at sev-
eral places in Australia (most of them in New South Wales) and in
New Zealand, but the total shale of oil produced in all these places
has been less than one per cent of the world's output and in none
of them is oil shale now mined. In all the areas where oil shale is
reported the beds are thin.

KANSAS CITY TESTING LABORATORY 353

Position of the United States. — When petroleum was discovered
in quantity in the United States in 1859, oil was being distilled from
cannel coal (whence the term "coal oil") but no record has been
found of large production of oil from shale in this country. There
are, however, extensive reserves of material sufficiently rich to justify
the hope that it may form the basis of a great industry and during
the last ten years progress has been made in perfecting processes
for the commercial distillation of oil from domestic oil shale. The
valuable deposits of oil shale in North America are widely distributed
and include beds ranging in age from Devonian to Eocene. Local
conditions such as remoteness from, a supply of petroleum and near-
ness to a sufficient market, have heretofore made it possible to de-
velop an oil shale industry in Scotland, France, Australia and New
Zealand and in view of a possible shortage in the world's supply of
petroleum in the near future, it seems probable that an oil shale in-
dustry may be developed even in such countries as the United States
where petroleum is now abundant. The largest foreign deposits of
oil sTiale are apparently in Brazil and Russia but the most valuable
deposits in the world are probably those of Colorado, Utah and Wy-
oming.

While shale unquestionably is an enormous reserve for fuel oil,
it is not so valuable for gasoline. Shale oil holds a position between
petroleum and coal tar. Coal, tar is not yet satisfactorily treated or
cracked for the production of gasoline. Shale oil makes a very poor
naphtha in that it contains a very large per cent of olefins. The ole-
fins are (decreased materially by cracking at high pressures particu-
larly in the presence of hydrogen. The accompanying graphs show
the effect of high pressure cracking in the character of the hydro-
carbons in shale oil.

Refining Practice for Shale Oil.*

In refining Scotch shale oil a loss of about 22 per cent is in-
curred, chiefly in the form of compounds with chemicals used in the
treatment. This is over four times the average loss incurred in re-
fining American petroleum. Products made from the crude oil are
naphtha, including scrubber naphtha, 9.9 per cent; burning oils, 24.7
per cent; gas and fuel oils, 24.4 per cent; lubricating oils, 6.6 per cent;
paraffin wax, 9.5 per cent; still coke, 2 per cent. Satisfactory mo-
tor fuels, burning oils and fuel oils are produced. The lubricating
oils are not particularly viscous and are not, thercfoi'e, adapted for
heavy duty work, such as use in internal combustion motors, high
pressure bearings, and the like. A very good quality of paraffin wax
is produced which is used chiefly for candle making. The still coke
is of rather poor quality, being contaminated with the chemicals used
in refining the oils, and on this account does not bring a very good
price. Some oil is recovered from the compounds or sludges formed
in chemical treatment of the oils, and this recovered oil is used as
part of the fuel in the refinery. At the same time considerable acid
is recovered from the sludges, and is used either in treating other
oil or in the production of ammonium sulphate.

At the present time it is imposnble to accurately estmiate the
cost of producing shale oil from American oil shales, and therefore im-

354 BULLETIN NUMBER SIXTEEN OF

possible to arrive at any satisfactory estimate of possible profit. By
basing our calculations on Scotch practice, however, it is possible
to give an idea of some of the requirements for an oil shale
industry in this country. Assume that an industry producing and re-
fining 50,000 barrels of shale oil per day had been developed in the
State of Colorado. This could hardly be termed a large industry nor
would it go far in supplying the demands of the nation, which at
the present time is using nearly ] ,250,000 barrels of petroleum per
day, but if we assume that the shale yielded forty-two gallons of oil
to the ton, 50,000 tons of shale would have to be mined each day. I
will not venture to predict how many tons of shale a man can mine
in this country per day, but in Scotland each man produces about
four and one-half tons. Knowing that the American coal miner is
a better producer than the British coal miner, for the sake of mak-
ing an illustration, assume that the American miner will produce ten
tons per day. The assumed industry would then require at least
5,000 miners, nearly half as many miners as are employed in pro-
ducing coal in Colorado at the present time.

If Scotch shale i-etorts were used the retorting plant investment
necessary for the 50,000-barrel industry would be over $160,000,000,
based on present estimates of the cost of Scotch retorts, and the
refining equipment necessary would require another $50,000,000, if we
base estimates on the capital required for building refineries for the
complete refining of petroleum. Of course, these figures may not
apply to American shales and practice, but they give an idea of the
capital required by an oil shale industry.

In addition to the large capital required for an oil shale industry^
there are many serious technical and economic problems to be solved
before the industry can hope to succeed in a large way. As yet we do
not know what type of process will be required to handle our shales
successfully and at a profit, and we know very little regarding the
methods of refining these oils or what quality of finished products
can be made from them. A large oil shale industry will require a
large quantity of labor, and this labor must be obtained and housed.

Starting with shale, adding heat and steam, and treating the
water and gas removed, there has now been produced spent shale of
no value, gas which is burned in the retort furnaces to supply heat
for the distillation operations, sulphate of ammonia which is ready
for the market, and a crude oil which requires refining to yield mar-
ketable products. A ton of Scotch oil shale, in the treatment of which
about 100 gallons of water have been used, produces at the present
time about 24.5 gallons of crude oil, 36 pounds of ammonium sul-
phate, 10,000 cubic feet of gas of about 240 B. T. U. heat value and
about 1,600 pounds of spent shale.

In general Scotch shale oil refining is similar to petroleum re-
tming, but because shale oil contains a greater percentage of ob-
jectionable compounds than ordinary petroleum the refinery operation
^ more complicated and more costly than average petroleum refining,
briefly stated, Scotch shale oils are subjected to more distillation
ami more chemical treatments than is petroleum when the latter is
refined.

*For complete references on oil shale see Reports of Investiga-
tions of Bureau of Mines No. 2256, 2176.

KANSAS CITY TESTING LABORATORY

355

FRACTIONAL GRAA^ITY DISTILLATION ANALYSIS OF
SHALE OIL BEFORE CRACKING.

Laboratory Number 46258, Original Shale Oil.

Specific Gravity, 0.920; °Be' U. S. 22.1°; °Be' Tag. 22.3°.

Color, Brownish Black; Sulphur=0.49% B.T.U.%18,425.

%

Temp. °F.

Gravity of Fract on

Gravity of
Total Over

Gravity of
Stream

0.790=47.6° Be'

5

330
368

0.790 = 47.6° Be'

0.790=47.6° Be'

0.802=44.9° Be'
0.814=42.3° Be'

10

378
398

0.814=42.3° Be'

0.802 = 44.9° Be'

0.823=40.4° Be'
0.833 = 38.3° Be'

15

413
426

0.833=38.3° Be'

0.812=42.7° Be'

0.839=37.1° Be'
0.845=35.9° Be'

20

446
464

0.845=35.9° Be'

0.820 = 41.0° Be'

0.853=34.4° Be'
0.861=32.8° Be'

25

479
494

0.861 = 32.8° Be'

0.828=39.4° Be'

0.869 = 31.3° Be'
0.876=30.0° Be'

30

516
530

0.876=30.0° Be'

0.836=37.7° Be'

0.883=28.7° Be'
0.890=27.5° Be'

35

543
552

0.890 = 27.5° Be'

0.844=36.1° Be'

0.895=26.6° Be'
0.900=25.7° Be'

40

576
586

0.900 = 25.7° Be'

0.851 = 34.8° Be'

0.905=24.8° Be'
0 909=24.1° Be'

45

599
604

0.909 = 24.2° Be'

0.857 = 33.6° Be'

0.910 = 24.0° Be'
0.911=23.8° Be'

50

613

0.911=23.8° Be'

0.867 = 31.7° Be'

0.916=23.0° Be'
0.922=21,9° Be'

55

Gas

0.922=21.9° Be'

0.872=30.7° Be'

0.928=21.0° Be'
0.934=20.0° Be'

60

Gas

0.934 = 20.0° Be'

0.877=29.8° Be'

0.937 = 19.5° Be'
0.940 = 19.1° Be'

65

Gas

0.940 = 19.0° Be'

0.882 = 28.9° Be'

0.943 = 18.5° Be'
0.947 = 17.9° Be'

70

Gas

0.947 = 17.9° Be'

0.887=28.0° Be'

0.950 = 17.4° Be'

Summary:

Water 2.1%

42.7° Benzine or Naphtha 12.9%

31° Illuminating oil, unrefined 25.0%

24° Gas, Oil or Distillate 10.0%

18.5° Wax Distillate 30.0%,

Residue 20.0%

Olefins

Aromatics

Naphthenes and Paraffins .

58.0%

27.0%,
15.0%

Ammonia in water portion = 0.422% as NHs.

356

BULLETIN NUMBER SIXTEEN OF

FRACTIONAL GRAVITY DISTILLATION ANALYSIS OF
SHALE OIL AFTER CRACKING.

Laboratory Number 46258, Shale Oil Residue Cracked
at 800 lbs. Pressure.

Specific Gravity, 0.896; °Be' U. S. 26 2; °Be' Tag. 26.4.
;, ,f Color, Dark Red;

%

Temp. °F.

Gravity of Fraction

Gravity of
Total Over

Gravity of
Stream

0

119

0.681=76.3° Be'

5

210

0.681 = 76.3° Be'

0.681 = 76.2° Be'

0.690 = 73.6° Be'
0.699 = 70.9° Be'

10

281

0.717=65.8° Be'

0.699=70.9° Be'

0.710=67.8° Be'
0.721 = C4 7°Be'

15

334

0.765 = 53.5° Be'

0.721 = 64.7° Be'

0.730 = 62.3° Be'
0.740 = 59.7° Be'

20

368

0.798 = 45.8° Be'

0.740=59.7° Be'

0.748=57.7° Be'
0.757 = 55.4° Be'

25

395

0.823 = 40.4° Be'

0.757=55.4° Be'

0.764 = 53.7° Be'
0.771 = 53 0°Be'

30

435

0.846=35.7° Be'

0.771 = 52.0° Be'

0.777 = 50.6° Be'
0.784 = 49.0° Be'

35

454

0.861=32.8° Be'

0.784 = 49.0° Be'

0.790 = 47.6° Be'
0.796 = 46.2° Be'

40

486

0.881 = 29.1° Be'

0.796=46.2° Be'

0.801=45.1° Be'
0.807 = 43.8° Be'

45

518

0.898=26.1° Be'

0.807 = 43.8° Be'

0.812 = 42.7° Be'
0.818 = 41.5° Be'

50

543

0.911=23.8° Be'

0.818 = 41.5° Be'

0.823 = 40.4° Be'
0.828 = 39.4° Be'

55

582

0.930 = 20.7° Be'

0.828=39.4° Be'

0.833 = 38.3° Be'
0.838=37.3° Be'

60

623

0.945=18.2° Be'

0.838=37.3° Be'

0,844 = 36.1° Be'
0.855 = 34.0° Be'

65

651

0.959 = 16.0° Be'

0.855 = 34.0° Be'

0.859 = 33.2° Be'
0.862 = 32.6° Be'

70

679

0.965 = 15.1° Be'

0.862 = 32.6° Be'

0.865 = 32.0° Be'

Naphtha in oil charged . . . None

Synthetic Oil-
Naphtha 30.0%

Illuminants 25 0%

Olefins 27.5%.

KANSAS CITY TESTING LABORATORY

357

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359

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360

BULLETIN NUMBER SIXTEEN OF

Products of Distillation of Coal — (a)

PRODUCT

1917

Quantity

Value

1918

Quantity

Value

Gas (M cubic feet)-

Coal gas

Water gas

Oil gas

By-product gas. .

Coke (short tons) , b-
Coal gas

Tar (gallons) —

Coal gas

Water gas

Oil gas

By-product gas.

Ammonia Sulphate or equivalent
(lbs.)—

Coal gas

By-product gas

Light oils (gals.), d-

Coal gas

Water gas

Oil gas

By-product gas. .

Naphthalene (Ibs.)-

Coal gas

Water gas ......

By-product

Retort carbon (short tons)-

Coal gas

Water gas

By-product

42,927,728
153,457,318

14,739,508
131,026,575

$38,324,113

131,876,065

13,470,911

11,360,335

42,630,448
175,431,370

14,100,601
158,358,479

$43,016,085

156,150,576

13,619,264

13,699,515

342,151,129

1,857,248
c22,439,280

$195,031,424

$10,953,693
cl38,643,153

390,520,898

1,813,660
025,997,580

$226,485,440

$14,022,818
cl93,018,785

24,296,528

53,318,413

59,533,208

727,556

221,999,264

$149,596,846

$1,774,326

1,258,683

32,682

5,566,302

27,811.240

48,522,987

53,419,753

550,006

200,233,002

$207,041,603

$1,886,629

1,731,714

15,967

6,364,972

335,578,441

88,547,975
560,792,322

$8,631,993

$1,362,125
17,903,864

302,725,748

56,900,464
697,308,770

$9,999,282

$1,453,070
26,442,951

649,340,297

770,298

6,420,717

205,475

54,427,266

$19,265,989

$448,855

1,655,204

74,035

28,655,204

754,209,234

12,292,026

20,376

59,564,376

$27,896,021

$6,978,281

4,274

25,688,446

61,823,756

399,897
17,276,044

$30,833,298

$9,687
569,449

71,876,778

508,202
15,890,447

$32,671,001

$14,282
650,229

17,675,941

252
1,068

$579,136

$ 2,733
12,067

16,398,649

1,007
251
655

$664,511

$13,275
2,230
2,732

Lampblack and carbon residue
(Hhort tons) —
Oil gas

1,320
31,205

$14,800
$169,425

1,913
17,678

$18,237

$95,211

. ./f„^ 0*,^^.'" products not included in this table, valued at $807,147
in 1J17 and $1,808,515 in 1918 were: From coal-gas plants, creosote,
tar, distillery products, pitch, coke breeze and spent iron oxide. From
oil-gas plants: Sodium ferrocyanide. From by-product coke oven
plants: Coke breeze, sodium ferrocyanide, residue, drip oil, spent
oxide and pyridin oil.

KANSAS CITY TESTING LABORATORY

861

Products from One Ton of Dry Coal at Different

Temperatures.

(COAL WITH 35% VOLATILE AND 7% ASH.)

Coke or Carbonized Coal

Coke Oven

(1700° F)

66%

(1% Volatile)

Low Temperature
Carbonization

68%
(3% Volatile)

Gas, cubic feet per ton

Light oil from gas, gallons per ton . . .
Ammonium sulphate, pounds per ton

Tar oils, gallons per ton

Pitch, gallons

10,000
3
20
3.8
8.2

9,000

2

20

15

0

Fuel Consumed or Lost in Coking.

BEE HIVE

BY-PRODUCT

Millions
of B. T. U.

Millions
of B. T. U.

Gas

11,000 cu. ft. = 6.160

9 gallons= 1.401

4 gallons= 0.527

100 pounds= 1.300

4,300 cu. ft. = 2.480

Tar

none

Light oil

none

Coke

none

Total coal equivalent ....

671 pounds=9.388
33.55%

172 pounds=2.408
8.6%

One ton of coal tar may yield:

Pitch 1,000

Naphthalene 112

Anthracite oils 34

Creosote oils : 20

Cresylic acid ■ 2

Carbolic acid 2^ gals

Heavy naphtha 1 gal.

Solvent naphtha IH gals.

Toluol 3 gal.

Benzol h gal.

lbs.

lbs.
gals,
gals,
gals.

362 BULLETIN NUMBER SIXTEEN OF

Composition of Pitch:

Carbon

Hydrogen

B. T. U. per pound

Moisture

Volatile

Fixed carbon

Ash

Specific gravity

Hard

Soft

93.2 %

91.8%

4.4 %

4.6%

15,930

0.05%

66.85%

32.55%

0.60% •

1.35

Yield from Distillation of Eastern High Grade Coals.
(Howard N. Eavenson in Coal Age.)

Kentuck}- Coals, 24 Samples:

Average

Ash, per cent 4 . 78

Sulphur, per cent 0 . 75

Phosphorus, per cent 0 . 006

By-product yield per net ton —

Tar, gallon 7.8

Benzol, free, gallon 2.6

Ammonium sulphate, pound 28 . 1

Surplus gas, cu. ft 5,068

Yield of coke, per cent 69 . 5

Fusing point of ash, degrees F 2654

West Virginia Coals, 31 Samples:

Ash, per cent 5.29

Sulphur, per cent 0 . 99

Phosphorus, per cent 0.006

By-product jield, per net ton —

Tar, gallon 8.0

Benzol, free, gallon 2.6

Ammonium sulphate, pounds 24 . 5

Surplus gas, cu. ft 5,069

Yield of coke, per cent 72 . 8

Fusing point of ash, degrees F 2743

Pennsylvania Coals, 20 Samples:

Ash, per cent 7 27

Sulphur, per cent 1 18

Phosphorus, per cent 0 012

By-product yield, per net ton-
Tar, gallon 7 8

Benzol, gallons 22

Ammonium sulphate, pounds 25 1

Surplus gas, cu. ft 5^497

Yield of coke, per cent [ ] // 67 5

Fusing point of ash, degrees F. . . ! . . . . . . 2366

Maximum

Minimum

9.32
1.78
0.027

1.56
0.44
0.001

10.2

3.2
34.1

5,520
75.0
2940

5.4

2.3

22.4

4,740
67.0
2430

9.09
2.76
0.019

2.59
0.63
0.002

10.6

3.3
31.0

5,340
76.8
2970

5.8

2.1
21.2

4,770
68.2
2610

10.44
2.14
0.018

5.32
0.77
0.005

10.1

5.8

29 .'8 "
5,654

70.0
2390

22 .'8*'
5,304

64.2
2350

KANSAS CITY TESTING LABORATORY 363

Gas-Manufacturing Processes in Use in the United

States.

The manufactured gas distributed in the United States is of three
principal kinds: Coal gas, carbureted water gas and oil gas.

The manufacture of water gas consists essentially of an inter-
mittent process in which a bed of anthracite coal or coke is brought
to a high temperature by an air blast and then steam under pressure
is blown through the fuel, forming carbon monoxide, hydrogen and
a small amount of carbon dioxide by reaction with the carbon in the
fuel. The resultant gas, called blue water gas, has a heating value of
approximately 300 B.T.U. per cubic foot and almost no luminosity
when burned in an open flame. It is conducted into a fire-brick-lined
chamber called the carburetor, which contains staggered rows of fire
bricks, called checker brick, heated to incandescence during the blow
period. Gas oil or fuel is sprayed into the carburetor while the gas is
passing through, forming an oil gas which enriches the blue water
gas to any desired heating value or candlepower. Another checker-
brick-filled chamber, called the superheater, converts most of the oil-
gas vapors into permanent gases, which will not condense again upon
cooling. During the formation of the oil gas certain portions of the
hydrocarbons which compose the oil are changed in their composition
to form benzol, toluol and related hydrocarbons called aromatic com-
pounds. Considerable tar is formed at the same time. This is con-
densed, scrubbed and washed out of the gas by various means, but
usually at a temperature which permits most of the aromatics to go
forward with the gas. The sulphur in the gas is removed by iron-
oxide purifiers and the gas is metered and leaves the plant at or
slightly above atmospheric temperature.

The manufacture of coal gas is essentially different from that of
water gas. In this process certain classes of bituminous coals are
distilled in fire clay or silica retorts or ovens and the resulting gases
are condensed, scrubbed, washed and purified to remove water vapor,
tar, ammonia and sulphur. As in the water gas process, certain of
the hydrocarbons given off by the coal are transformed by the heat of
the retort to aromatic compounds. A small part of these aromatics
is washed out of the gas by the wash water and tar, but the larger
part remains in the gas. In fact, the cooling of the gas is usually so
regulated that most of these substances will remain in the gas to
increase its heating value and candlepower. Coal gas retorts take a
variety of forms. Among these are coke ovens, chamber ovens, hori-
zontal D-shaped retorts, vertical retorts, inclined retorts, etc. Even
those of a given class differ among themselves in details of construc-
tion. In most of them the distillation is an intermittent process, but
some continuous methods are used. In all these processes the gas
produced consists of the same constituents in somewhat different pro-
portions. The form of apparatus used in a given case depends largely
upon economic considerations or is governed by certain special quali-
ties which are desired in one or more of the products produced. In all
of these coal gas processes coke remains in the retort after distilla-
tion. In some of them, as for example in coke ovens, coke is the prin-
cipal product, but in city gas plants gas is the chief product. The
operation is carried out in any case to give most satisfactory qualities

364

BULLETIN NUMBER SIXTEEN OF

to the principal product and at the same time obtain as high yields
and good quality as possible of the secondary or by-products.

Mixed gas is usually understood to be a mixture of carbureted
water gas and coal or coke-oven gas. It is supplied in many cities
in the United States where the requirements permit of a mixed gas
being supplied. The manufacturing installation for mixed gas is
practically two complete installations, one for coal gas and one for
carbureted water gas, with their auxiliary scrubbing, condensing, puri-
fying, and metering apparatus entirely independent and separate.
The manufactured mixed gas, however, is stored in common holders
and delivered through a single distribution system. The coal and
water gas thus supplement each other. The uniform but more cum-
bersome coal-gas. production furnishes coke as fuel for the water-gas
plant. This in turn takes care of the irregularities of the output, and,
where necessary, increases the quality of the gas production, especially
where a high candlepower standard is in force.

The oil gas process is at present confined chiefly to the Pacific
Coast States, where comparatively cheap oil and expensive coal make
the coal and water gas processes less feasible. In oil gas manufac-
ture oil alone is used as fuel for heating the checker bricks of the fix-
ing chambers and oil is sprayed by steam into the chambers where,
in contact with the bricks, lampblack and permanent gases are formed.
In this process also aromatic compounds are included among the con-
stituents of the gas.

Note. — See Bulletin of Bureau of Standards.

Products of Refining of Light Oil of Gas Works.

Carbon
Disul-
phide

Benzene

Toulene

M-zylene

Naph-
thalene

Molecular weight

76.12
10.57
1.2921
1.2773
1 . 2698
1.2623
1 2473
.00125
46.2

.041
127.9
198 5
244.1
298.0
434.6
.202
3.42

.3480
.4420
.6260
66.100
11 550
.1.300
0.240
83.8
.219
.765
—108.6

78.05
7.36
.8999
.8883
.8839
.8786
.8679
.0012
80.36
.043
26.63
45.68
58.90
75 21
119.34
.209
3 54

.9960
.8805
17.930
132 100
33 . 600
.3780
0 419
92.9
.072
.241
+ 5.4

92.. 06
7.27
.8845
.8757
.8714
.8659
.8573
.0010
110.3
.047
7.20
13.02
17.22
22.53
37.46
.244
4 14

10.150
.8850
18.270
132 600
40 150
.4.500
0.440
83 55
Insol.
Insol.
—92.4

106.08

7.26
.8823
.8738
.8697
.8655
.8574
.00095
139.1
.052

1.75

3.45

4.74

6.43
11.43
.281

4.76

10.230
.8910
18.410
133,500
46.500
.5210
0,383
78.25
Insol.
Insol.
—54.8

128.06

Pounds per United States Gal. (60° F)

Specific Kravity ( 0°C/4°C)

9.60

Specificgravity (10°Cy4°C).., . . ..

Specific gravity ri5°C/4°C) . ,

Specific gravity (20°C/4°C)

"i:i517'

Specific gravity (30°C/4°C)

Change of Specific Gravity per 1° C

Boiling point at 760 mm.Hg. {°C)

217.7

Increase in boiling point (°ram.Hg.)

.059

Vapor pressure mmHg ( 0°C)

.022

Vapor pressure mrnHg (10°C)

.047

Vapor [)res.sure mniHg (I5°C)

.062

Vapnr pressure mmHg (2U°C)

.080

\'ai)or |)rc,ssure mmHg (3n°C")

.135

I'ounils Dcr cu ft. vapor (60° F = 30 in.)

Kil prr cu. m, vapor 10° C-760 mm.). . . .

.339
5.72

Heat comliustion (net) 1.5°C-760 mmHg.
Calorics per kil. liriuid

.9700

Calories per liter, li(|uid

11.170

B. T. U. per pound, liquid

17.460

B. T. U. per U. S. gal., linuid

167.300

C;alori(s per cu. meter, vapor

B. T. U. per cu. ft, vapor

52.400
.5910

Specific h«it (calorics per kil.)

0 314

I cat of vaporii. (calorics per kil.).

Sol. in waUT (22°(;) grm subs, in 100 gHjO. . .
(irains HjO in lOOg subs

Insol.
Insol.

Melting point (°C)

+80.0

KANSAS CITY TESTING LABORATORY

365

Average Content of Light Oils in Various Gases.

The amount of benzol and toluol formed in any one of these
processes is bj' no means definite. It depends upon the operating
conditions and the quality of the raw materials (coal or oil). It
would therefore be impossible to predict exactly what the yield of
products in a given case would be, but an extensive inquiry into the
operation of a number of typical plants has given the following tabula-
tion as the usual range of figures for the various processes. Individual
results may vary widely from them in a particular case.

TABLE 1, — Approximate Yields of Crude Light Oil and Pure Products
and Approximate Composition of Crude Light Oil.

APPROXIMATE YIELD OF CRUDE LIGHT OIL.

Coal gas —

Horizontal retort 3.0-4.0 gallons per short ton coal carbonized

Continuous vertical retort . .1.5-2.5 gallons per short ton coal carbonized

Inclined retort 1.8-2.3 gallons per short ton coal carbonized

Coke-oven gas, run of oven. . .2.6-3.6 gallons per short ton coal carbonized

Carbureted water gas 8-10 per cent of vol. of gas oil used

Oil gas 0.2-0.3 gal. per 1000 cu. ft. of gas.

APPROXIMATE COMPOSITION OF CRUDE LIGHT OIL.

Solvent
Naphtha,
Wash Oil,
Benzol Toluol, Naphthalene,
Coal gas: Per Cent Per Cent Per Cent

Horizontal retort 50 13-18 35

Continuous vertical retort 30 10-15 55

Inclined retort 45 13-18 40

Coke-oven gas, run of oven 50 14-18 35

Carbureted water gas 40 20-25 37

Oil gas 80 8-10 10

APPROXIMATE YIELD OF PURE PRODUCTS.

Gallons per short ton coal carbonized: Benzol Toluol

Coal gas —

Horizontal retort 15 ^ • J"^ ■ ^

Continuous vertical retort .6 o" a

Inclined retort -9 ' q~ ' c

Coke-oven gas, run of oven 1-5 . 3- . 5

Gallons per 1000 cubic feet of gas:

Carbureted water gas 15 • 06- . lU

Oil gas 25 .02-. 03

Degrees
Boiling
Point in
Paraffins Specific Gravity Centigrade

N— heptane 0.712, at 16° C 97

Triethylmethane 689, at 27° C 96

N-octane 708, at 12.5° C 125

Diispbutyl 714, at 0° C 108.5

366 BULLETIN NUMBER SIXTEEN OF

Yields of Oil from Distillation of Cannel Coal.

Yield of Crude Oil
Locality Per Ton, Gallons

England:

Derbyshire °^

Wigan cannel 74

Newcastle 48

Scotland:

Boghead cannel 120

Scotch cannel 40

Lesmahago cannel 96

iCtew Brunswick:

Albertite 110

American:

Breckenridge, Ky., cannel 130

Erie R. R., Pa 47

Falling Rock cannel 80

Pittsburgh 49

Kanawha semi-cannel 71

Elk River semi-cannel 60

Cannelton, Ind. cannel 86

Coshocton, Ohio 74

Darlington, Pa. (Cannelton) 56

Camden lignite, Ark. 64

Missouri, Cooper Co 75

The coke resulting from cannel coal is not of satisfactory quality
for ordinary purposes. However, it is satisfactory for making pro-
ducer gas or burning as a domestic fuel in hard coal burners, provided
a small amount of bituminous matter remains in it.

KANSAS CITY TESTING LABORATORY 367

Refining of Oil for Road Building and Paving

Purposes.

The various methods of refining which yield residues adaptable
or used for road building and paving purposes are as follows:

Sedimentation.

Dehydration.

Fractional distillation by direct fire.

Forced fire distillation with direct fire.

Steam distillation.

Inert gas distillation.

Air blowing.

In the types of oil which are ordinarily used for making asphalt
or road binders, water is one of the most common impurities. The
water is ordinarily salt water and may contain more or less other
mineral matter than the salt. These impurities are insoluble in the
bitumen proper and as they differ from the bitumen in specific grav-
ity, they may be removed wholly or in part by the process of sedi-
mentation or separation by gravity. In the more fluid petroleums,
sedimentation occurs during storage in the large tanks and the water
is ordinarily automatically drawn off from the bottom of the tank by
reason of the different heads produced by the salt water and by the
oil. However, a small amount of emulsified water nearly always
remains in all petroleums, so that there will always be a small amount
of sediment. If the petroleum is very heavy and viscous, approxi-
mately equal in gravity to water, then the water will remain emulsi-
fied and will not separate by gravity. This type of oil happens to be
the most suitable in quality for producing asphalt and special means
of removing this water is necessary before the oil can be reduced to
the desired consistency. The dehydration processes are designed
primarily for removal of the water in the bituminous material which
will not completely separate by sedimentation. It is desirable to do
this before distillation because of the fact that the presence of the
water will cause foaming when the mixture is heated to the tempera-
ture of boiling water. Dehydrating plants vary considerably in design,
but those more commonly used for petroleum in California are spoken
of as topping plants. In this sort of plant the oil is pumped with or
without pressure through a length of pipe containing many bends
and turns, so that the oil is considerably stirred. The pipe coils are
set in furnaces, so that they may be suitably heated to a tempera-
ture above that of boiling water. This pipe discharges the foam into
a large expansion chamber, where the water and more volatile con-
stituents separate in the form of vapor which is condensed in an ordi-
nary condenser for the recovery of the light products. This sort of
plant is commonly spoken of as a pipe still. From the pipe still, the
oil passes through another line, direct to a large batch still, where it
is subjected to the ordinary fractional distillation.

The essential principle in the distillation of an oil for road pur-
poses is that it shall distill at a temperature sufficiently low to pre-

368 BULLETIN NUMBER SIXTEEN OF

vent the decomposition of the hydrocarbons. Since asphalt hydrocar-
bons begin to decompose at a temperature of 600 °F or slightly below,
it is desirable that the fire distillation be carried only to that tem-
perature After this temperature has been reached, the usual method
is to blow superheated steam, which mechanically carries over the
more volatile hydrocarbons at a temperature much below the actual
boiling point.

This distillation has a special action in removing the paraffin
compounds which are particularly undesirable in that they have very
little ductility and cementation value. The distillate will contain any
light oils such as are used as spindle oils and for general lubrica-
tion, as well as any paraffin wax. It is particularly desirable m this
distillation to prevent the formation of free carbon or coke. The dis-
tillation with steam may be carried down until the residue shows a
penetration of about 10 millimeters.

A method of distillation which gives very great yields of solid or
semi-solid asphalt even from semi-paraffin base oils is that of blow-
ing the oil at moderately high temperature with air. The amount of
air and rate in blowing is usually about 300 cubic feet per barrel of
oil per hour (see p. 375). For delivering air to an asphalt blowing
still with the oil at a temperature of 400°F and producing about
2.50 bbls. per day, 100 H. P. is required. Air blowing in many Mid-
Continent oils gives much more asphalt than naturally exists in the
oil. The action of the air is to produce a more viscous product which
is very much less susceptible to temperature changes than the nat-
ural asphalt. It is strictly a chemical fransformation process formed
from the hydrocarbons in the oil which are ordinarily not useful for
asphalt making purposes. It has been found from practical experience
that this type of asphalt is not sufficiently cementitious and ductile
to be used for ordinary paving purposes in producing first class
asphalt pavement. It can, however, be successfully used and is in
great demand for water-proofing purposes, for filler in brick and wood
block pavement, for roofing purposes and for fluxing ductile asphalt.

The best types of petroleum for asphalt paving purposes are those
from California, Mexico, Trinidad and Texas.

ASPHALT PAVEMENT.

Asphalt is a black non-oxidized bituminous hj'drocarbon, semi-
fluid to hard in consistency, the heavy residuum from petroleum or
occurring naturally. The residua from petroleum are known as oil
asphalts and come most largely from California, Mexican, Texas and
Mid-Continent petroleums. The most commonly used natural asphalts
are Trinidad, Bermudez, Cuban and Gilsonite.

The term asphalt is commonly applied to bituminous pavements,
being mixtures usually of oil asphalt with dust, sand, gravel or rock
in varying proportions from 6% to 20%. The terms "bitumen" or
"asphaltic cement" are commonly applied to the pure asphalt material.

The types of asphalt construction now commonly used are:
1. Asphaltic concrete. This mixture is very common in localities
where Joplin chats are available. It is known also as "Topeka Specifi-

KANSAS CITY TESTING LABORATORY

369

cation Pavement" and "Bituminous Concrete," but it might be called
bituminous gravel. The stone it carries is of V2" and %" size. (Fig.
76.)

2. Sheet asphalt is the original type of asphalt pavement laid in
two courses, the bottom one with coarse stone, the top with sand
mixed with the bitumen. (Fig. 77.)

3. Bituminous concrete (Warren) is laid with coarse stone in
the wearing surface. (Fig. 78.)

4. Bituminous earth is laid without an appreciable amount of
sand or rock. (Fig. 79.)

There are two different basic principles involved in proportioning
the mineral matter of an asphalt pavement. One is to so grade the
coarse mineral particles that they support each other and intex'lock.
The other is to produce a mastic of bitumen and finely divided earthy
material that is rigid and self-supporting because of surface tension
action. This mastic fills the voids in the coarse material and has a
much higher melting point than the pure bitumen and does not so
readily allow softening or movement of the pavement.

COMPOSITION OF NATURAL ASPHALT.

Natural
Trinidad

Bitumen 56.0%

Mineral Matter 36.8%

Specific Gravity 1.400

Fixed Carbon 11.0%

Melting Point, °F 190

Penetration 0.5

Free Carbon " 6 0%

Sulphur (ash free basis).... 6.5%
Petroleum ether soluble .... 65.0%
Total Carbon (ash free).... 82.6%

Hydrogen (ash free) 10.5%

Nitrogen (ash free) 0.5%

Ber-
mudez

94.0

%

2.0%

1.085

13.5%

180

2.5

4.0%

5.6%

70.07o

82 5%

10.3%

0.7%

Gilsonite
99.4%
0.5%
1.045
13.0%
300
0

0.1%

1.3%

30.0%

Gra-

hamite

94.1%

5.7%

1.171

53.3%

Cokes

0

0.2%
2.0%
0.4%
87.2%
7.5%
0.2%

Cuban

75.1%
21.4%

1.305
25.0%
240

0

3.5%

8.3%
41.1%

COMPOSITION OF OIL ASPHALTS.

Mexican

Bitumen 99.5%

Mineral Matter 0.3%

Specific Gravity 1.040

Fixed Carbon 17.5%

Melting Point, °F 140

Penetration 55

Free Carbon 0.0%

Sulphur (ash free basis) 4.50%

Petroleum Ether Soluble 70.0%

Cementing Properties good

Ductility 45 cm

Loss at 325°F 5 hrs 0.2%

Heat Test adherent

Mid-Con-
tinent Air

Blown

99.2%
0.7%
0.990

12.0%
180

40
0.0%
0.60%

72.0%
poor

2 cm
0.1%

smooth

Stanolind
(cracked-
pressure tar
California residue)

99.5%
0.3%
1.045
15.0%
140
60
0.0%
1.65%
670%'
good
70 cm
0.2%
adherent

99 8%
0.3%.
1060

17.5%
135

50
0.0%
0.35%

70.0%

good

1004-
0.
scaly

.1%

370

BULLETIN NUMBER SIXTEEN OF

Composition of Rock Asphalt. Buckhorn,

Ragusa, Seyssel, Mons, Cass Co., Okla-

Sicily France France Missouri homa

Bitumen 9.9% 5 9% 8.9% 6.9% 5.9%

Passing 200 mesh 37.1 44.1 53.1 20.0 9.0

80 mesh 23.0 15.0 13.0 21.0 8.4

50 mesh 14.0 9.0 7.0 17.0 9.0

40 mesh 4.0 7.0 5.0 6.0 9.9

30 mesh 2.0 7.0 3.0 6.5 15.0

20 mesh 5.0 6.0 5.0 5.1 8.8

10 mesh 5.0 6.0 5.0 7.5 8.0

4 mesh 0.0 0.0 0.0 10.0 26.0

Calcium carbonate 89.0 91.3 90.0 92.9 96.0

ASPHALTIC SANDSTONES.

Breckenridge Higginsville,

County, Ky. Oklahoma Missouri

Bitumen 9.2% 9.2% 7.9%

Passing 200 mesh 5.2 1.5 25.7

80 mesh 45.5 56.5 71.3

40 mesh 36.3 30.4 3.0

10 mesh 3.8 2.4 0.0

Calcium carbonate 0.0 0.0 0.0

SHEET ASPHALT PAVEMENT.

Sheet asphalt is the standard asphalt pavement. Specifications
call for two courses of the following composition and properties:

BINDER OR BOTTOM COURSE.

Limits Standard

Bitumen 51/2%— 8% 6.0%

Mineral passing 200 mesh 7 12 8.0

Mineral passing 80 mesh 10 20 12.0

Mineral passing 40 mesh 10 20 15^0

Mineral passing 10 mesh 7 20 13.0

Mineral passing 4 mesh 10 20 17!o

Mineral passing 2 mesh 10 20 16.0

Mineral passing 1 mesh 10 20 13!o

Thickness \i/^ in

Density "ZZZZZZZ^er 2.30

TOP COURSE.

,-,., Limits Standard

Bitumen 9.75%— 11.0% 10.0%

Mmeral passing 200 mesh 12 18 13.0

Mineral passing 80 mesh 20 34 23!o

Mineral passing 40 mesh 20 40 27!5

Mineral passing 10 mesh 12 35 26!5

Mineral passing 4 mesh 0 0.0

Mineral passing 2 mesh 0 0 0

Mineral passing 1 mesh '.' 0 0.0

rru- 1 100.0

Thickness 1^ in,

Density o^er 2.17

KANSAS CITY TESTING LABORATORY

371

Composition of Asphalt Pavements.

The following table gives a comparison of a typical composition
and properties of good mixtures representing the various types of
asphalt wearing surface pavements:

Bituminous Bitumi-

Concrete nous Bitumi-

(Topeka Concrete Sheet nous

Spec.) (Warren) Asphalt Earth

Asphaltic cement 8.0% 6.0% 10 0% 20.0%

Dust passing 200 mesh screen 12.0 5 5 12.0 62.0

Dust passing 80 mesh screen 12.0 2.8 16.0 15.0

Dust passing 40 mesh screen 20.0 6.7 38.0 3.0

Dust passing 10 mesh screen 20.0 24.5 24 0 0.0

Dust passing 4 mesh screen 18.0 15.3 0.0 0.0

Dust passing 2 mesh screen 10.0 13.3 0.0 0.0

Dust passing 1 mesh screen 0.0 25 0 0.0 0.0

100.0 100.0 100.0 100.0
Weight per sq. yd. 2 in. surface,

lbs 215 225 205 185

EFFECT OF MINERAL MATTER 0^^ THE PENETRATION OF
ASPHALTIC CEMENT (Typical Case).

% Dust Penetration Melting Point

0 200 100

35 . 128 110

55 92 120

70 34 150

In a general way, 1% of dust in asphaltic cement decreases the
penetration 2 points with A. C. of ordinary penetration. This will vary
somewhat according to the character of the asphaltic cement. A pave-
ment having a relation of 2 parts dust and 1 part bitumen cannot
soften or flow in hot weather.

FLUXING OF HARD ASPHALT.

As a general rule, 30% of 10-12° Be' asphaltic flux is required to
bring Trinidad asnhalt to a penetration of 50. Less of paraffm flux is
required. For each 1% of asphaltic flux added to about 50° asphalt
the penetration is raised 3 points. For exact results a test should be
made with the actual materials in question.

MATERIALS REQUIRED FOR 1000 YARDS OF ASPHALTIC CON-
CRETE PAVEMENT ARE AS FOLLOWS (Typical):

For wearing surface:
"Chats" or Gravel = 32 tons
Sand (Coarse) = 32 tons

Sand (Fine) = 32 tons

Dust = 7 tons

Asphaltic Cement = SVi tons

For concrete base:
(6 inches of 1:3:6 mix.)
Cement - 732 sacks = 183 bbls.
Sand — - 77 cubic yards —
Rock = 155 cubic yards
Water = 7,000 gallons

372 BULLETIN NUMBER SIXTEEN OF

RELATION OF THE DEFECTS OF AN ASPHALT PAVEMENT TO
ITS PHYSICAL PROPERTIES.

Cracking is- caused by asphaltic cement without sufficient ductility,
with too low penetration, insufficient in quantity or that has
been over-heated; Imperfections in the base, such as a cracking
in the base or the lack of a rigid base or lateral support; Insuf-
ficient compression when laid; Lack of traffic.

Disintegration and Hole Formation are caused by asphaltic cement
with poor ductility and cementing value, or insufficient to coat
mineral aggregate and fill voids; Dirty sand; Non-uniform thick-
ness of surface mixture; Weak foundations in spots; Water from
beneath.

Scaling of the Surface Mixture is caused by asphaltic cement lacking
in cementing power, insufficient in quantity or subject to decom-
position by the weather; Improper grading of mineral, particularly
insufficient dust; Dirt conglomerates in sand; Insufficient density.

Waviness and Displacement are caused by asphaltic cement without
cement power, too soft or in too large quantity; Irregularity of
surface thickness, or of composition of asphaltic surface mixture;
Insufficient dust or filler; Non-rigid base or expansion of the
base; Street with heavy grade.

Marking is caused by asphaltic cement that is too soft or in too large
quantity; and that is too uniform; Insufficient dust or filler;
Insufficient density.

FUNCTIONS OF VARIOUS CONSTITUENTS OF ASPHALTIC

SURFACE MIXTURE.

Gravel and Coarse Sand in proper relation diminish voids, insure
greater stability and increase density, allow the use of less
asphaltic cement, decrease tendency to displacement, waviness
and marking, increase susceptibility to damage by erosion and
abrasion.

Sand in proper relation increases stability by filling voids in stone,
increases capacity to resist abrasion, diminishes tendency to
raveling.

Filler or Very Fine Dust in proper relation increases density and
stability by filling voids in sand, increases capacity to resist
abrasion, allows wider range in penetration of A. C, diminishes
or overcomes tendency to marking, displacement and waviness,
increases cementation of mixture, increases capacitv for A. C,
increases the need for much compression and softer A. C. in lay-
ing mixture, eliminates lakes of A. C, decreases brittleness of
pavement.

A. C. in proper quantity and relation cements mineral particles to-
gether, keeps out water, imparts pliabilitv, resiliency and noise-
lessness, prevents erosion and disintegration of coarse mineral o*
pavement,

KANSAS CITf TESTING LABORATORY 373

Specifications for Asphaltic Cement for Asphalt

Surface Mixture.

Impurities.

The asphaltic cement shall contain no water, decomposition prod-
ucts, granular particles or other impurities, and it shall be homo-
geneous.

Ash passing the 200-mesh screen shall not be considered an im-
purity, but if greater than 1% corrections in gross weights shall be
made to allow for the proper percentage of bitumen.

Specific Gravity.

The specific gravity of the asphaltic cement shall not be less than
1,000 at 77°F.

Fixed Carbon.

The fixed carbon shall not be greater than 18%.

Solubility in Carbon Bisulphide.

The asphaltic cement shall be soluble to the extent of at least
99% in chemically pure carbon bisulphide at air temperature and
based upon ash free material.

Solubility in Carbon Tetrachloride.

The asphaltic cement shall be soluble to the extent of at least
98.5% in chemically pure carbon bisulphide at air temperature and
based upon ash free material.
Melting Point.

The melting point shall be greater than 128° F and less than
160°F (General Electric method).
Flash Point.

The flash point shall be not less than 400°F by a closed test.

Penetration.

The asphaltic cement shall be of such consistency that at a tem-
perature of 77 °F a No, 2 needle weighted with 100 grams in five
seconds shall not penetrate more than 9.0 nor less than 5.0 milli-
meters. For asphaltic cement containing ash 0.2 millimeter may be
added for each 1.0% of asli to give the true penetration.

Loss by Volatilization.

The loss by volatilization shall not exceed 2%, and the penetra-
tion after such loss shall be more than 50% of the origmal penetra-
tion. The ductility after heating as above shall have been reduced
not more than 20%, the value of the ductility in each case bemg the
number of centimeters of elongation at the temperature at which the
asphaltic cement has a penetration of 5.0 milhmeters. The volatiliza-
tion test shall be carried out essentially as follows:

Fifty grams of the asphaltic cement in a cylindrical vessel 55 mil-
limeters'in diameter and 35 millimeters high shall be placed in an
electrically heated oven at a temperature of 325 °F and so maintained

374 BULLETIN NUMBER SIXTEEN OF

for a period of 5 hours. The oven shall have one vent in the top 1
centimeter in diameter, and the bulb of the thermometer shall be
placed adjacent the vessel containing the asphaltic cement.

Ductility.

When pulled vertically or horizontally by a motor at a uniform
rate of 5 centimeters per minute in a bath of water, a cylinder of
asphaltic cement 1 centimeter in diameter at a temperature at which
its penetration is 5 millimeters shall be elongated to the extent of not
less than 10 centimeters before breaking.

EPITOME OF THE PURPOSES OF CERTAIN SPECIFICATIONS
FOR ASPHALTIC CEMENT.

Impurities are a measure of the care with which the asphaltic ce-
ment has been refined and handled. Usually the presence of impuri-
ties in large quantities indicates a poor grade of asphalt. Water as an
impurity would act as a diluent and would cause foaming in the kettle.
Ash or mineral matter is not considered an impurity if it is a natural
constituent of the asphaltic cement, but the mix and cementing value
must be figured on the bitumen alone.

Specific Gravity of the asphaltic cement should be over 1.000. The
advantage of a specific gravity more than 1.000 is that there will be
less tendency for water to float out the asphaltic cement. The specific
gravity is raised by the presence of mineral matter. Asphaltic oils of
a penetration satisfactory for paving purposes always have a specific
gravity greater than 1.000. Paraffin base oil and air -blown products
usually have a specific gravity less than 1.000.

Fixed Carbon is a measure of the chemical constitution of an
asphalt to some extent. Certain types of asphalt such as Mexican
have naturally a constitution that yields a large amount of fixed car-
bon. Fixed carbon is largely used for determining the source and
uniformity of an asphalt. Fixed carbon is not free carbon, but in-
cludes free carbon, which is practically absent in asphaltic cements.

Solubility in Carbon Bisulphide is a measure of the purity of an
asphaltic cement. The cementing value, other things being equal, is
proportional to the carbon bisulphide solubility. Any carbonaceous
material such as coal tar or pitch is detected by the carbon bisulphide
solubility test.

Solubility in Carbon Tetrachloride is very nearly the same as the
solubility in carbon bisulphide. It is claimed that an asphalt having
more than 1%% difference in the solubility in carbon bisulphide and
carbon tetrachloride has been subjected to excessive heat in refining.

Melting Point is the temperature at which the asphaltic cement
will flow readily. The melting point desired is dependent upon the mix-
ture. If the amount of fine dust in the mineral aggregate is low, the
asphalt should have a melting point higher than the highest tempera-
ture to which the pavement is subjected.

Flash Point is a measure of the amount of volatile hydrocarbons
that are present in the asphalt and its readiness to decompose by heat.

KANSAS CITY TESTING LABORATORY

375

Penetration is a measure of the consistency of the asphaltic ce-
ment. It is merely a quick, convenient test for checking up numerous
individual samples. The penetration is expressed in degrees and in
accordance with the method of the American Society for Testing Ma-
terials, each degree representing 1-10 of a millimeter or 1-250 of an
inch. The penetration, then, is the number of degrees that a No. 2
sewing needle when weighted with 100 grams will pass vertically
into the A. C. at a temperature of 77°F (2o°C) in 5 seconds. The pene-
tration to be desired will depend upon the climate, the nature of the
traffic, the grading of the mineral particles, the amount of \oids, the
amount of compression attainable, the ductility and cementing strength
of the A. C. and the amount of dust filler.

Loss of Volatilization is a measure of the amount of light hydro-
carbons that are present in asphalt and is also a measure of the tend-
ency of an asphalt to oxidize and to lose its ductility and penetra-
tion. Asphalt cement which has no ductility after this volatilization
test will not be satisfactory for paving purposes. '.

Ductility is the measure of the ability of an asphaltic cement to
expand and contract without breaking or cracking. The same asphalt

at a higher pene- __^ ,i

tration should ^ssniisaigfciN^-^^^^-^-'issd- ,:-.^'zJ '.t ■ i,

have a higher
ductility, so all
ductility tests
should be based
on a certain defi-
nite penetration
regardless of the
temperature, or
should be based
upon a tempera-
ture of 32 °F.
Ductility is also
a measure of the
cementing
strength.

Viscosity is a
measure of abil-
ity of the asphal- , ,„. ., . - . x,, •

tic cement to im- of Asphalt Produced by A.r Blowing

part plasticity and malleability.

- P^G^^ycirc a-y^:ii

"■■'-.' J

Fij

.•OC too zoo ^^O i^O ^OO ^90

20 *0 00 6Q '00 /2Q /-^O

Relation of Penetration tq^ Melting Point

i '

Typical Specifications for Wearing Surface of
Asphaltic Concrete

The wearing surface shall be composed of a properly prepared
mixture of bitumen, dust, sand and chats, gravel or trap rock.

The amount of asphaltic cement, dust, sand and chats shall be
so regulated that the average mixture shall be within the following

ts by weignt:

Size of

Opening,

Lower

Upper

Average

Bitumen ....--.

In. Square

Limit
7.0 7f)

Limit
lO.OVc

Typical

8.0%

Dust passing

200

mesh ...

." 0 0029

8.0

18.0

12.0

Sand passing

80

mesh .

. 0.0068

100

20.0

12.0

Sand passing

40

mesh .

. 0.0150

15.0

25.0

20.0

Sand passing

10

mesh .

. 0.065

15.0

40.0

20.0

Sand passing

4

mesh .

. 0.185

10.0

22.0

200

Sand passing

2

mesh .

. 0 380

0.0

10.0

8.0

Ordinarily this mixture is to be obtained by the use of rock,
coarse sand, fine bank sand and limestone dust or cement.

All of the mineral ingredients except the dust shall be heated and
mixed in a suitable drier to a temperature of from 300 to 350 °F. The
bin containing the mineral shall be permanently equipped with a re-
cording or an observation thermometer.

The asphaltic cement shall be added after it has been heated to a
temperature not exceeding 360 °F. The heating of the asphaltic ce-
ment must be by steam or if by direct fire vigorous mechanical stir-
ring must be used. A recording thermometer should be used in the
A. C. kettle and the aggregate.

The dust shall be added dry to each batch separately prior to
the addition of the A. C. All materials shall be weighed.

The mixing shall be for a sufficient time to thoroughly and uni-
formly mix all materials and for a period of not less than one minute.

The temperature of the mixture shall be between 270°F and 350°F
when it leaves the plant.

It shall be between 250°F and 350°F on the street (preferably
300°F).

The surface of the concrete shall be dry and clean at the time the
surface mixture is applied.

Tbe mixture shall be applied and raked to a uniform thickness,
none being allowed to remain at the point of dumping and all lumps
being thoroughly raked out.

The amount of hot mix applied shall be at least 210 pounds per
square yard and shall be of a uniform thickness of 2 inches after
rolling.

The compression shall be applied with a 5-torI roller until com-
plete and sufficient in the judgment of the inspector and as indicated
by the tests of the preceding day's laid surface. Hydraulic cement
may be dusted over and rolled into the finished pavement.

The specific gravity of the compressed surface mixture shall
average 2.20 or more and shall not at any time be less than 2.16. A.
piece of the compressed surface mixture after being placed in water
for 24 hours shall not have absorbed water and shall not have become
crumbly or weakened.

KANSAS CITY TESTING LABORATORY

377

Table for Calculating Voids in Sand and Limestone.

Weight in

Weight' in

Pounds per

Pounds per

Cubic Foot

% Voids

Cubic Foot

% Voids

60

63.9

61

63.3

96

42.2

62

62.6

97

41.6

63

62.1

98

41.0

64

61.5

99

40.4

65

60.9

100

39.8

66

60.3

101

39.2

67

59.6

102

38.6

68

59.1

103

38.0

69

58.5

104

37.4

70

57.9

105

36.7

71

57.3

106

36.2

72

56.7

107

35.6

73

56.0

108

35.0

74

55.4

109

34.4

75

54.8

110

33.8

76

54.2

111

33.2

77

53.6

112

32.5

78

53.0

113

32.0

79

52.4

114

31.4

80

51.8

115

30.7

81

51.2

116

30.2

82

50.6

117

29.6

83

50.0

118

28.9

84

49.4

119

28.3

85

48.8

120

27.8

86

48.2

121

27.2

87

47.6

122

26 6

88

47.0

123

26.0

89

46.4

124

25.4

90

45.8

125

24.7

91

45.2

126

24.1

92

44.6

127

23.5

93

44.0

128

22.9

94

43.4

129

22.3

95

42.8

130

21.7

Grams per 100 cc X .6243 - pounds per cubic foot.
% voids - 100 — (0.376 X grams per 100 cc).

378 BULLETIN NUMBER SIXTEEN OF

Specifications of the National Paving Brick Mfgrs.

Assn.

Oil Asphalt Filler,
(Squeegee Method.)

Section 1. Description: Asphalt filler shall be homogeneous,
free from water and shall not foam when heated to 200°C (392°F).
It shall meet the following requirements:

(a) Flash point— Not less than 200°C (392°F).

(b) Melting point— (Ring and Ball) Not less than 65°C
(149°F).

(c) Penetration: At 0°C (32°F) 200 gms. 1 min. not less than
10. At 25°C (77°F) 100 gms. 5 sec. (30-50). At 46°C (115°F) 50
gms. 5 sec. not more than 110.

(d) Loss on evaporation: 163^C (325°F) 5 hrs. less than 1%.

(e) Ductility — Not less than 3.

(f) 9c total bitumen (soluble in carbon tetrachloride) not less
than 99%.

(g) 7c total bitumen (soluble in carbon bisulphide) not less
than 99%.

(h) Reduction in penetration — At 25 °C (77 °F) due to heating
specified under loss on evaporation, not more than 50%.

Section 2. Tests: Tests for the above requirements shall be
made according to the following methods:

(a) Flash point — (open cup). U. S. Department of Agricul-
ture Bulletin 314, page 17.

(b) Melting point — American Society for Testing Materials,
Standard Method, Serial Designation D 36-19.

(c) Penetration — American Society for Testing Materials,
Standard Method, Serial Designation D 36-19.

(d) Loss on evaporation — (Volatilization). U. S. Department
of Agriculture Bulletin 314, page 19, 50 gram sample.

(e) Ductility — American Society of Civil Engineers, Transac-
tions. Vol. LXXXII, 1918, page 1460.

(f) Total Bitumen — U. S. Department of Agriculture Bulletin
314, page 25.

(g) Percent of Total Bitumen — (Carbon Tetrachloride). U. S.
Department of Agriculture, Bulletin 314, page 29.

(h) Reduction in Penetration: See test for Penetration.

Section 3. Samples: The contractor shall submit with his bid
a one (1) pound sample of the asphalt filler proposed to be used in
the work, together with a statement as to its source and character.

KANSAS CITY TESTING LABORATORY 379

Section 4. Heating: Filler shall be heated to a temperature
not exceeding 200 °C (392°F). It shall be applied at a temperature
of not less than 150° C (300° F). The heater shall be equipped with
a thermometer capable of registering at all times the temperature
of the filler.

Section 5. Cleaning the Surface: Brick shall be clean and dry
when the filler is applied. Immediately before filling the joints, the
surface of the brick shall be swept clean. All brick shall be filled
and a surface dressing applied on the day of laying. Filler shall not
be applied if the brick are wet nor if air temperatures are such that
the filler will not flow freely to the bottom of the joints.

Section 6. Filling and Squeegeeing: Filler shall be removed
from the heater and applied promptly to the pavement before cool-
ing. Filler shall be worked into the joints by means of hot iron
squeegees operated slowly backward and forward at an angle with the
joints. Squeegee irons shall be kept hot and every precaution taken
completely to fill the joints. Squeegeeing shall continue until the
joints are full and a thin coating of asphalt remains upon the sui'-
face of the brick. Filler shall be applied and squeegeed until the
joints remain full.

Section 7. Surface Dressing: Immediately after the joints are
filled, a thin coating of dry stone screenings, sand or granulated
slag shall be spread upon the surface of the pavement, provided the
wearing surface of the brick is wire-cut. Top dressing shall be of
such sizes that all will pass a number 4 sieve. As soon as the dress-
ing is spread the surface of the pavement shall be rolled thoroughly
to bed the dressing into the asphalt coating.

Section 8. Opening to Traffic: The brick roadway may be
opened to traffic immediately upon completion of the surface dress-
ing.

380

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY

383

Properties of Typical Road Oils.

Viscosity

Loss

No.

Gravity and

210° F

Viscosity

As-

Character

350° C

Weight

Uni-

Furol

phalt,

of Asphalt

24 hrs.,

per Gallon

versal

104° F

%

%

1

.933=20.2° Be'
7.77 lbs.

46.0

20.8

55.0

waxy

50.2

2

.933 = 20.2° Be'

7.77 lbs.

126.0

172.0

65.0

ductile

22.2

3

.951 = 17.3° Be'
7 . 92 lbs.

80.0

79.0

66.0

granular

30.8

4

.973=13.9° Be'
8.10 lbs.

47.0

25.0

51.5

ductile
excellent

60.2

5

1.028= 6.1° Be'
8.57 lbs.

124.0

430.0

66.0

ductile
excellent

27.0

6

1.005= 9.3° Be'
8.38 lbs.

99.0

72.0

60.0

ductile
excellent

33.0

7

0.953 = 17.0° Be'

7.93 lbs.

139.0

252.0

75.0

waxy

15.0

8

0.940=19.0° Be'
7 . 83 lbs.

122.0

182.0

69.0

ductile
good

29.6

9

0.940=19.0° Be'
7.83 lbs.

127.0

183.0

69.0

ductile
good

29.5

10

0.950=17.5° Be'
7.91 lbs.

135.0

252.0

75.0

waxy

15.0

11

0.935=19.8° Be.

7.79 lbs.

99.0

117.0

63.5

ductile
good

32.6

12

0.931 = 20.5^ Be.
7.75 lbs.

115.6

159.0

66.0

ductile
good

26.4

Open Specifications for Road Oil.

Water None

Specific gravity Over .940

Soluble in carbon bisulphide 99.5%

Per cent asphalt O^^"" ^^

Ductility of 100° asphalt at 77° F Over 5 cm.

Viscosity S. U. at 210° F= 100-150 (must be under 100 if for cold

application).
Viscosity Furol at 104° F= 100-500 (must be under 199 if for cold
application).

384 BULLETIN NUMBER SIXTEEN OF

Illinois State Highway Specification for Road Oil.

SPECIFICATION SI.
(Heavy Oil, Hot Application.)

HEAVY OIL FOR SURFACE TREATMENT OF BITUMIN-
OUS OR WATERBOUND MACADAM ROADS. The road oil shall
be homogeneous, free from water and shall not foam when heated
to 150°C (302°F). It shall conform to the following requirements:
Specific gravity 25"C/25°C (77°F/77°F), not less than 0.980.
Flash point, not less than 150°C (302^F).
Specific viscosity at 100°C (212°F), 30.0 to 70.0.
Float test at 50°C (122° F), 100 seconds to 200 seconds.
Loss at 163°C (325°F) 5 hours, not over 5.0%.
Float test of residue at 50 °C (122°F), 120 seconds to 240 seconds.
Total bitumen, not less than 99.5%.

Per cent of total bitumen insoluble in 86° Be' naphtha, 10 to 25%.
Fixed carbon, 7 to 15%.

SPECIFICATION S2.

(Medium Oil, Hot Application.)

MEDIUM OIL FOR SURFACE TREATMENT OF BITUMIN-
OUS OR WATERBOUND MACADAM ROADS. The road oil shall
be homogeneous, free from water and shall not foam when heated
to 100°C (212°F). It shall conform to the following specifications:
Specific gravity 25°C/25°C (77°F/77'F), 0.960 to 1,010.
Flash point, not less than 100°C (212°F).
Specific viscosity at 100°C (212°F), 5.0 to 15.0.
Float test at 32°C (90°F), 30 seconds to 90 seconds.
Loss at 163°C (325°F) 5 hours, not over 15.0%.
Float test of residue at 50°C (122°F), 90 seconds to 180 seconds.
Total bitumen, not less than 99.5%.

% total bitumen insoluble in 86° Be' naphtha, 7.0% to 20.0%.
Fixed carbon, 5.0% to 10.0%.

SPECIFICATION S3.

(Light Oil, Cold Application.)

LIGHT OIL FOR SURFACE TREATMENT OF BITUMINOUS
OR WATERBOUND MACADAM OR OF GRAVEL ROADS: The
road oil shall be homogeneous and free from water. It shall conform
to the following requirements:

Specific gravity 25°C/25°C (77°F/77'F), 0.920 to 0.970.
Specific viscosity at 25°C (77°F), 30.0 to 70.0.
Loss at 163°C (325°F) 5 hours, 20.0% to 30.0%.
Total bitumen, not less than 99.5%.

% total bitumen insoluble in 86° Be' naphtha, 5.0% to 20.0%.
Fixed carbon, 4.0% to 10.0%.

KANSAS CITY TESTING LABORATORY

385

10

12

14

le 15 to 22 24

Wid+h of Road, Fee+

ee

GAI.LONS OF ROAD OIL REQUIRED PER MILE OF ROAD
AT GIVEN WIDTH AND RATE

j,-ig. 75 — Amount of Road Oil Required

Application.

£oi

Different Rates ot

386 BULLETIN NUMBER SIXTEEN OF

Bituminous Acid-Proof Coatings for Acid-Proofing
Concrete Surfaces. (Bureau of Standards.) ,

Acid-Proof Black.

This material shall be composed of a high grade of bitumen
thinned with suitable volatile solvents to furnish a smooth, black
product which shall dry in twenty-four hours and be unaffected by
mineral acids of specified concentration.

It must contain at least 40% of non-volatile, shall not settle, liver
or thicken in the container and shall conform to the following re-
quirements.

(a) When flowed on a piece of clean sheet iron approximately
4x6 in. and 0.016 in. thick and allowed to dry for one week at room
temperature the film must withstand bending double quickly over a
rod of 5 mm. in diameter without cracking or flaking.

(b) A test piece prepared as above and dried for one week at
room temperature shall be laid flat and in different places several
drops each of sulphuric acid, specific gravity 1.3, nitric acid, specific
gravity 1.23 and hydrochloric acid, specific gravity 1.09 shall be al-
lowed to remain on the surface of the film for six hours. On exam-
iiiation. the film shall show only slight dulling and the metal beneath
shall show no corrosion.

Bituminous Enamel.

The enamel shall consist of a homogeneous mixture of a bitumen
of relatively high melting point and finely powdered siliceous min-
eral filler. The total amount of mineral filler as determined from
the ash, shall not exceed 40% nor be less than 15% by weight. Within
the above limits the satisfactox-y working qualities of the enamel shall
control the quantity of mineral filler to be used. The mineral filler
must be resistant to hydrochloric, sulphuric and nitric acids, and must
pass a sieve the openings of which are not greater than 0.14 mm.
(0.0055 in.) (This corresponds to about 100 mesh sieve).
Bituminous Primer.

The primer shall consist of a like bituminous material containing
no added mineral matter, thinned with a solvent to a satisfactory
brushing consistency. It shall dry to a tacky state in thirty minutes
and shall not flash "below 30 °C by the Abel closed tester. The solvent
used shall have a minimum toxic effect upon workmen appljnng the
primer within an enclosed space.
Bituminous Acid-Proof Mastic.

The bituminous mastic shall be composed of asphalt cement, clean,
sharp grained sand, and fine absorbent siliceous dust. These ma-
terials shall be mixed in the proper proportions and shall be applied
hot to the concrete surface, which shall be dry and free from dust
and shall have been previously coated with a priming or bonding
solution which has just reached the tacky state.
Asphalt Cement.

The asphalt cement must be of refined- asphalt and shall be homo-
geneous and free from water.

It shall meet the following requirements:

Melting point (ring and ball) 150 to 180 °F.

Penetration at 25°C, 100 g. 5 sec. 15 to 40.
Total bitumen .=oluble in carbon bisulphide, not less than 90%.

The sand shall be clean, hard grained and moderately sharp, and
shall be free from clay, silt and organic matter.

KANSAS CITY TESTING LABORATORY 387

It shall be well graded from coarse to fine, and when tested by
means of the laboratory sieves, shall meet the following requirements:

Passing 4 mesh sieve, 100%.

Total passing 20 mesh sieve, 50 to 80%.

Total passing 50 mesh sieve, not more than 30%.

Passing 100 mesh sieve, not more than 5%.

Mineral Filler.

The mineral filler shall be any finely powdered acid-resistant
siliceous material, 85% of which shall pass a 100 mesh screen.

Priming Solution.

The priming solution shall consist of an asphaltic base similar
to the asphalt cement and shall be thinned to a good brushing consist-
ency with a suitable volatile solvent.

Mixing.

The sand or the mixture of the sand and mineral matter and the
asphalt cement shall be heated separately to about 300 °F. When
the asphalt cement is completely fluid, the hot dry aggregate is
stirred in and thoroughly mixed until the mass is homogeneous and
sufficiently fluid for pouring. The temperature of pouring should
be between 350 and 400 °F. The aggregate if dry may be stirred in
without previous heating but in that case a longer period of heatmg
and stirring will be required.

Laying.

The concrete surface shall be primed and allowed to dry to the
tacky state. The hot mixture, prepared as above, shall then be poured
spread on, soothed out and worked into place with suitable tools.
After the surface has begun to set, it shall be sprmkled with hard-
grained sand and a little mineral dust and rubbed down until it is
smooth. The finished layer should be at least 1 in. thick.

Approximate Formula.

The composition varies within narrow limits according to the
service required of the material, and when ready for laying should
be as follows: "^

Asphalt cement 12 to 15%

Mineral filler 20 to Zb/c

Sand or other aggregate - b" to w /o

388

BULLETIN NUMBER SIXTEEN OF

Vig. 76— Topeka Bituminous Concrete.

Fig-. 77 — Sheet Asphalt.

KANSAS CITY TESTING LABORATORY

389

Fig. 7S — ^Asphaltic Concrete (Warrenite.)

Fig. 70 — Bituminous Earth Pavemont.

390

BULLETIN NUMBER SIXTEEN OF

Fig-. SO — Brick Pavement With Asphalt Filler.

Fig. 81 — Wood Block With Asphalt Filler.

KANSAS CITY TESTING LABORATORY

391

Fig. 82 — Asphalt Macadam Pavement.

Fig. 83— Two-Course Concrete Pavement.

392 BULLETIN NUMBER SIXTEEN OF

Fig. 84 — Oil Treated Macadam Pavement.

KANSAS CITY TESTING LABORATORY 393

Natural Gas.

Natural gas is an ideal domestic fuel and an almost equally ideal
industrial fuel. It is a large item in interstate but not in interna-
tional trade. About one-fourth of the natural gas consumed in
the United States is used for generating power, and its use af-
fects international industry and commerce, for it supplements the
supply of coal and oil.

As it saves man power, is especially adapted to certain indus-
trial processes and is cheap, natural gas is used as fuel in many
glass works, cement plants, brickyards, factories and metallurgical
plants. It is also used in large quantities as raw material in mak-
ing carbon black, 30 per cent of the natural gas consumed indus-
trially in West Virginia in 1917 having been used in the carbon black
industry.

Some natural gas is valuable because of its content of gaso-
line, and the extraction of gasoline from natural gas is now an in-
dustry of increasing magnitude. Some of the gasoline thus obtained
is so light that it must be blended with naphthas and other distillates
obtained from crude oil before it can be used as a motor fuel. A re-
cently developed process is that of extracting the gas helium from
natural gas. It is used in balloons as a non-inflammable substitute
for hydrogen.

Natural gas is now used by about 16,500 industrial consumers
of whom more than 10,000 employ it for generating power and by
about 2,500,000 domestic consumers. The field operations undertaken
to exploit natural gas have been accompanied by enormous waste,
which will hasten the exhaustion of this fuel.

Character and Occurrence — Pure natural gas is odorless and col-
orless, burns with a luminous flame and is highly explosive when
mixed with air. Its chief constituent is marsh gas, or methane, a
member of the paraffin series. Besides methane, it may contain
ethane, a closely related gas and varying amounts of ethylene or
defiant gas, carbon monoxide, carbon dioxide and nitrogen as well
as a little oxygen and helium.

Natural gas is classified as either "wet" or "dry" according to
its content of gasoline. Wet gas is commonly associated with oil in
oil fields and is generally obtained from the same sand or formation
that yields the oil or even from the same well. It contains not only
ethane, propane, butane and pentane, the lighter members of the
methane series, which predominate in the dry gas, but some heavier
hydrocarbons. Dry gas contains chiefly methane or marsh gas, the
lightest known hydrocarbon, which has a specific gravity of 0.559.
It is usually not associated with oil in the sand and is generally un-
der high pressure.

The close association of oil and gas in both occurrence and ori-
gin makes it difficult to consider the two re.sources separately. Gas
invariably accompanies oil wherever the conditions arc favorable to
its accumulation but it is also found in places far removed from oil
fields. Many of the natural gas fields coincide areally with oil fieUls
and the production of oil and that of natural gas are closely related.

394

BULLETIN NUMBER SIXTEEN OF

The gas being lighter usually accumulates in the upper parts of the
oil and gas bearing deposits. The accumulation of natural gas is
governed by features of geologic structure similar to those that gov-
ern the accumulation of oil and the origin of natural gas is accounted
for by the same theories that account for the origin of oil. Natural
gas is found in rocks that range i.i geologic age from Cambrian to
Recent, but most of the vi^orld's supply of natural gas is derived from
beds of Devonian, Carboniferous and Tertiary age.

Geographic Distribution — The chief natural gas fields of the United
States are the Appalachian field, comprising parts of the States of
West Virginia, Pennsj^lvania, New York, Ohio, Kentucky and Ten-
nessee; the Mid-Continent field, including parts of Kansas and Okla-
homa; and isolated fields in the states of Louisiana, Texas, Arkan-
sas, California, Illinois and Indiana. Gas is also found in small
quantities in Wyoming, Washington, Colorado, Oregon, South Dakota,
North Dakota, Montana, Idaho, lov/a, Michigan, Missouri, New Mex-
ico, Utah and Alabama. In foreign countries, natural gas is found
in considerable quantities in the provinces of Ontario, Alberta and
New Brunswick in Canada and in Great Britain, Italy, Rumania,
Galicia, Hungarj', Russia, Persia, India, Japan, Mexico, Peru and
Argentina. Undoubtedly as the search for petroleum is continued,
productive gas fields will be discovered in foreign countries even in
countries where natural gas is not now supposed to be present in
great quantities.

Production — The commercial production of natural gas is re-
stricted almost wholly to the United States, the available statistics
showing that about 95 per cent of the world's output is produced
in this country. Canada stands second in rank. The United States
is likely to lose this remarkable predominance, for she has already
apparently passed her maximum production. (See U. S. Geol. Survey.)

The table on page 395 shows the production of the principal
natui'al gas producing countries in the woi'ld in 1913 and 1917:

Typical Composition of Commercial Gases.

Me-

thane

Ethyl-

Hydro-

Carbon

Carbon

Nitro-

Oxy-

B.T.U.

CnHjn

enes

gen

monox.

diox.

gen

gen

per

+ 2

CnHsn

H2

CO

CO2

N2

02

cu. ft.

Coal gas, Germany

34.02

5.09

46.20

8.88

3.01

2.15

0.65

700

Coal Gas, United States.

40.00

4.00

46.00

6.00

0.45

2.05

1.50

755

Li^ite gas

15.59

3.25

45.16

17.24

11.51

5.49

1.76

500

Wood distillation gas. . . .

21.70

6.00

18.30

31.50

17.40

5.10

0.00

Cannel coal gas, low tem-

perature

Cannel coal gas, high

60 10

6 30

21 20

temperature

34 20

3 50

54 50

Water gas

2.00
91.58
73.92

0.00

0.00

10.43

45.00
0.00
9.30

45.50
0.00
0.45

4.00
0.00
0.22

2.00
7.95
5.46

1.50
0.00
0.22

350

Natural gas

970

Pressure still gas

Oil gas

57.70
1.20
0.5

77.0

38.10

"3:5"

3.40

12.00

3.00

0.50
27.00
26.00
16.5

0.30
2.50
9.5
3.0

1390

Producer gas

57.30
56.0

154

Blast furnace gas

*Still gases from lub stills
*Still ga-ses from coking

stills

71.0

17.0

5.0

5.0

1.0

KANSAS CITY TESTING LABORATORY

395

NATURAL GAS PRODUCED BY PRINCIPAL COUNTRIES
1913 AND 1917 IN THOUSANDS OF CUBIC FEET.

Countrv— 1913

United States 581.898,239

Canada 20,487,000

Austria 250,000

Italy 210,525

Great Britain 87

Japan Small Amount

Russia - Small Amount

World 603,000,000

1917
795,110,376
27,408,940

6,750,000
85

829,000,000

REPORT OF BUREAU OF LABOR STATISTICS ON PRICE OF

1,000 CUBIC FEET OF GAS USED FOR HOUSEHOLD

PURPOSES IN VARIOUS CITIES.

Natural Gas.

Buffalo $0.35

Cincinnati 35

Cleveland 35

Columbus 30

Dallas 45

Kansas City $0.80

Little Rock 45

Louisville 648

Pittsburgh Co 35

Manufactured and Natural Mixed.
Los Angeles $0.75

;^*v;

Ma

1919.

Atlanta $1

Baltimore

Birmingham

Boston Co. — A 1

Boston Co.— B 1

Boston Co. — C

Bridgeport 1

nufactured Gas.

1919.

Mobile $1-

Buffalo

Butte

Charleston (S. C).

Chicago

Cleveland

Denver

Detroit

Fall River

Houston

Indianapolis

Jacksonville

Manchester

Memphis

Milwaukee

Minneapolis

,00

.75

.95

.00

.10

.95

.10

.45

.485

.10

.88

.80

.95

.79

.95

.00

.60

.25

.10

.00

.75

.95

New Haven 1

New Orleans 1

Newark

New York

Norfolk 1

Omaha 1

Peoria

Philadelphia l

Pittsburgh 1

Portland, Me 1

Portland, Ore

Providence |

Richmond ^

Rochester

San Francisco

Scranton |

Seattle ^

St. Louis

St. Paul

Washington

35

10

.30

.97

.80

.20

.15

.85

.00

.00

.40

.779

.30

.00

.95

.90

.30

.25

.75

.85

.95

396 BULLETIN NUMBER SIXTEEN OF

Natural gas is found trapped in the various strata of the earth,
principally in sandstone formations of loose texture, in shale seams
and in cavities. It is usually associated with petroleum or coal and
occurs in the carboniferous strata or in more recent formations. In
coal mines it constitutes what is known as fire damp, being given
off from the exposed seams of coal. It is most commonly associated
with peti'oleum in petroleum bearing sand and occupies the space in
the sand above the oil. Occasionally it occurs in strata without any
oil being present, in which case it is of a slightly different composi-
tion than the gas which is found in contact with the oil. In many
cases it appears that the gas has been obtained from the atmosphere,
the oxygen having been removed by its combination with reducible
substances such as sulphides, leaving a residue of nitrogen. This
gives to such natural gases the peculiarity of having a very large
amount of nitrogen. Associated with the nitrogen there occasionally
is found a small amount of helium which is also an ordinary con-
stituent of air in small quantities. It may be that the difference of
solubility of the different gases of the air in water may account for
the tendency of accumulation of helium in such instances. As a rule,
however, natural gas consists of hydrocarbons of the same type as
petroleum and identical with the hydrocarbons which are given off
by the cracking of petroleum.

The proportions in which the different hydrocarbons exist in ordi-
nary gas such as is delivered to Kansas City, Missouri, is something
like the following:

Methane 84.7%

Ethane 9.4%

Propane 3.0%

Butane 1.3%

Nitrogen 1.6%

This gas has the greater portion of the heavy hydrocarbons con-
densed out on account of the high pressure in the pipe lines. Such a
gas is a mixture of methane with a varying amount of the other gases.
As shown by the above table, the gases ethane, propane and butane
furnish much of the heating value of the gas. A gas with a consider-
able amount of gasoline vapor in it will have a considerably higher
heating value than one from which it has been removed, or known as
a dry gas.

The compositions of the natural gas used in eight cities in the
United States are as follows:

Methane, Ethane, Nitrogen,

City Percent Per Cent Per Cent

Pittsburgh, Pa 79.2 19.6 1.2

Louisville, Ky 77.8 20.4 1.8

Buffalo, N. Y 79.9 15.2 4.9

Cincinnati, 0 89.8 19.5 .7

Cleveland, 0 80.5 18.2 1.3

Springfield, 0 80.3 14.7 5.0

Columbus, 0 80.4 18.1 1.5

Chelsea, Okla 75.4 17.7 6.6

These analyses were made by the ordinary combustion method
and hence show only the two predominating paraffin hydrocarbons.

KANSAS CITY TESTING LABORATORY 397

The composition of gases found in Kansas and Oklahoma as given
by Allen and Lyder are shown by the following table:

,. , B.T.U. per

Location Methane Ethane Nitrogen Cubic Foot

Augusta, Kas 10.54 1 64 87.69 129

Cowley County, Kas 16.27 3.01 80.23 209

Chautauqua County, Kas 42.38 1.85 55.29 441

Chautauqua County, Kas 49 01 3.89 46.67 541

Elsworth, Kas 61.09 1.09 37.20 609

Ponca City, Okla 44.60 14.86 40.10 688

Kay County, Okla 57.91 9.89 31.65 735

Chautauqua County, Kas 85.53 0.15 12.95 839

Chautauqua County, Kas 79.13 7.79 11.39 894

Butler County, Kas 62 15 18.38 18.64 930

Montgomery County, Kas. ..83.04 8.54 "^.95 970

Blackwell, Okla 70.69 18.65 9.32 1025

Cushing, Okla 70.74 2164 7.49 1059

Bartlesville, Okla 70.50 24.60 3.21 1125

The presence of such a large amount of nitrogen in some cases
makes the gas almost valueless unless some process is used whereby
the nitrogen may be adapted to chemical processes.

While natural gas has a very high heating value in comparison
with water gas, water gas has the advantage in that it gives a more
intense flame. The comparison of various commercial gases is shown
in the following table:

Natural gas may have its origin from a sand which is entirely
separated from sand containing oil or it may come from above the oil
in the same sand as oil.

In the latter case the lighter portions of the oil will have been
volatilized and carried into the gas. Such a gas is known as a "wet"
gas. In other words, the wet gas is composed of the usual constitu-
ents of dry gas; that is, methane, ethane, propane and butane, and in
addition pentane, hexane and heptane. These last three are liquid at
ordinary temperatures and are the most desirable components of
gasoline.

Gas coming from a sand containing no oil is "dry" gas and does
not contain the pentane, hexane and heptane.

A "wet" gas coming from an unknown sand indicates the presence
of oil in that sand.

In the ordinary oil well the gas is allowed to escape between the
casing of the well and the tube which has been inserted for withciniwal
of the oil. The gas so collecting in the casing is known as casinghoan
gas and may be used or allowed to escape.

This gas collecting in the casinghead of an oil well is "wet" gas
and contains some of the gasoline from the oil. The gasoline which
may be compressed from it or refrigerated from it is then known as
"casinghead" gasoline.

398

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY 399

The lighter the oil with which the casinghead gas has been asso-
ciated, the greater ordinarily will be the amount of gasoline contained
in the gas.

Ever since natural gas has been conducted in pipe lines it has been
known that gasoline could be separated by pressure and much has been
incidentally so produced. More recently the great demand for gasoline
has encouraged the design of hundreds of special plants for the extrac-
tion of gasoline from natural gas.

In 1904, at Titusville, Pennsylvania, Fasenmeyer made casinghead
gasoline by pumping the gas under pressure through a coil under
water.

In the early methods pressures of about 50 pounds per square inch
were used. Later condensing with a pressure of 400 pounds per
square inch was found to produce too "wild" a gasoline or one that
escaped too easily on handling. A pressure of 250 pounds per square
inch is now used, and the pressure of the condensed liquid is con-
trolled by absorbing it directly into heavier naphtha.

At first the compression was done in one stage, but it is the cus-
tom now to do it in two stages. The gravity of the product is from
80 to 100° Baume'.

The amount of casinghead gasoline present in a gas well depend
upon the character of the oil associated with it, the temperature, the
pressure, the compactness of the sand and the condition in the sand
at the point tapped.

The amount of gasoline obtained from casinghead gas in the Mid-
Continent field varies from % to 8 gallons per 1,000 cubic feet. A
typical gas yields 2y2 gallons per 1,000 cubic feet. Many yield 3 to 4
gallons -per 1,000 cubic feet.

The total production of casinghead gasoline in the United States
is shown on page 400.

The cost of plants for producing casinghead gasoline has varied
from $12 to $25 per thousand cubic feet of gas handled, and the oper-
ation of the plants has been uniformly successful and highly
profitable.

While the type of plant ordinarily constructed is for compression
methods, it is probable that the absorption method will be more gen-
erally adopted. The operation of the absorption method is similar to
that of extracting toluol from coal gas and may be applied to a natural
gas capable of yielding 1 pint of gasoline per 1,000 cu. ft. By the use
of the absorption process 50 million cu. ft. of natural gas wou d be
available per day and 100 million gallons of light gasoline would be
made.

400

BULLETIN NUMBER SIXTEEN OF

Natural Gas Gasoline Produced in the United States,

1911-1920.

Prepared by U. S. Geological Survey, Department of the Interior.

GASOLINE PRODUCED

Number
of

Number
of

Av. Yield

YEAR

Gasoline per

Operators

Plants

Quantity

Average Price

M Cu. Ft.

(Gallons)

per Gallon
(Cents)

(Gallons)

1911

132

176

7,425,839

7.16

3.00

1912

186

250

12,081,179

9.60

2.60

1913

232

341

24,060,817

10.22

2.43

1914

254

386

42,652,632

7.28

2.43

1915

287

414

65,364,665

7.88

2.57

1916

460

596

103,492,689

13.85

.496

1917

750

886

217,884,104

18.45

.508

1918

503

1,004

282,535,550

17.83

.63

1919

611

1,191

351,535,026

18.26

.73

1920

577

1,151

383,311,817

18.7

.772

1921 (Est.)

600

1,200

410,000,000

Unblended Natural Gas -Gasoline Produced in the
United States in 1920. (By States).

No. of
Oper-
ators

No. of
Plants

GASOLINE PRODUCED

Perc.

Prod, of

State

STATE

Quantity
(Gallons)

Av.
Price

(Cts.)

Av.
Yield
(Gals.)

%
Total

Oklahoma

141

74

29

20

207

14

32

4

38

6

8

4

312

210

70

42

306

31

59

4

92

9

10

4

177,424,824

58,941,488

48,207,976

32,956,028

21,151,135

10,609,629

10,015,638

8,711,037

6,054,916

4,497,320

4,330,748

411,078

18.0
22.0
17.3
18.0
21.0
16.1
22.0
20.0
22.0
24.0
19.0
18.4

2.10

.34

1.10

2.10

.35

.28

.25

1.81

2.09

.24

.37

2.53

91.7
27.0
73.3
91.5
52.0
57.3
23.0
94.0

100.0

4.0

36.4

100.0

46.3

West Virginia

15.4

California

12.6

Texas

8.6

Pennsylvania

5.5

Louisiana

2.8

Ohio

2.6

Wyoming

2.3

Illinois

1.6

Kentucky

1.2

Kansas

1.1

New York

.1

Totals, 1920

577

1,149

383,311,817

18.7

.772

73.0

100.0

KANSAS CITY TESTING LABORATORY 401

Charcoal is now used for the absorption of the gasoline from
natural gas at atmospheric pressure. Activated charcoal with the gas
passing at the right velocity will absorb all of the gasoline and
22-25% of its weight in gasoline. The gasoline is distilled from the
charcoal by means of superheated steam. Bentonite or similar hydrous
silicates of alumina have somewhat the same absorption qualities as
charcoal.

References for Casinghead Gasoline: Auerswald, Mech. Engr.,
43,601, 1921. Oil & Gas Journal, 20, 74, 1921. U. S. Patent 1402340,
Jan. 3, 1922.

FORMULA FOR THE CAPACITY OF ABSORPTION TOWERS OF
CASINGHEAD GAS PLANTS.

C=2d^h s p

C = capacity in cubic feet of gas per day.

d= diameter of tower in inches

h = height of tower in feet— baffled portion

s=fraction of unobstructed cross section

p=pressure of gas in pounds

With S = .50

C=d=h p

Amount of Absorption Oil required.
O = .02 C G

0=gallons of oil necessary to circulate per day
C = capacity in cu. ft. of gas per day
G=gallons of extractable gasoline per 1000 cu. ft.

Azz2 g

A = area of condenser in square feet

g=: gallons of gasoline to condense per hour.

402

BULLETIN NUMBER SIXTEEN OF

Properties of Hydrocarbons Found in Natural Gas and

Casinghead Gas.

01

c.
o

3

n

c

»

»

Formula

Molecular Weight

Specific Gravity of Liquid.

Specific Gravity of Gas. . .

Boiling point at atmospheric
pressure

Pressure to liquefy at 60° F
lbs

CH4
16.03

0.555

-165° C
=265° F

Vapor pressure 70° F in per
cent of atmosphere

100+

Gallons per 1000 cu. ft. at
B. P. reduced to 60° F...

Weight 1000 cu. ft. vapor at
B. P. reduced to 60° F, lbs.

Shrinkage in volume by 1 gal.
liquid removed per 1000
cu. ft

42

CjHe

30.05

.432 =
194° Be'

1.049

-93° C
=135° F

475

100+
4.13

79.7

CjHa!

44.07

.515 =
142° Be'

1.526

-45° C
=49° F

105

100+

7.17

116

CiHio

58.08

.585=
109° Be'

2.008

+ 1°C
34=° F

35

100+
10.72
152.6

Max. possible removable gal.
per 1000 cu. ft. at 70° F,

Heating value in B. T. U. per
cu. ft

B. T. U. per lb

Cu. ft air to burn 1 cu. ft. gas
Carbon per cent

Explosive mixture per cent in

air, maximum

Minimum

1065
25360
9.57
75.0

14.5
5.6

1861
23350
16.72
80.0

5.0
3.0

2685
23150
23.92
81.8

3.5
2.1

3447
22590
31.10

82.8

3.0
1.6

CiHij

72.10

.630=
92.2° Be'

2.496

36.3° C
=97° F

6.5

00

14.35

189.7

7.0%

7.8

4250
22400
38.28
83.3

2.5
1.3

CeHu

86.12

.670=
78.9° Be'

2.982

69° C=
156° F

1.8

10
18.22
226.6

5.5%

1.8

5012
22120
46.46
83.7

2.2

CtHh

100.13

.697 =
70.9°

3.467

98.4° C
=200° F

0.5

2.7
22.05
263.5

4.5%

0.6

5780
21935
53.6
84.0

1.9

CsHit

114.15

.718=
65.0°

3.952

125.5° C
=258° F

0.15

0.7

25.86

300

3.9%

0.18
6542

kin

21807

m

60.8

84.2

1.6

KANSAS CITY TESTING LABORATORY 403

About Natural Gas and Its Usefulness.

An average sample of natural gas has 950 B.T.U. per cubic foot.
1 lb. mill coal will evaporate 9 lbs. water.
1 gal. oil will evaporate 100 lbs. water.
1 cu. ft. gas will evaporate 0.85 water.
1 ton coal used under boilers = 18,500 cu. ft. of gas.
1 bbl. oil (42 gal.) under boilers = 5,000 cu. ft. of gas.
40 to 50 cu. ft. of gas = 1 boiler H.P.
Gas Engines:

Highest grade gas engines develop a brake H.P. on 8,500 B.T.U.

Average engine develops a H.P. on 10^500 B.T.U.

Oil well engine develops a H.P. on 20,000 B T.U.

In a steam turbine plant of over 500 K.W. capacity 30 cut. ft. gas

per K.W. is a fair average.
It requires 40,000 cu. ft. of gas to pump one million gallons of
water against 200-foot head.
Brick Plants — Gas Used per Thousand Brick Made:
1,800 cubic feet for power.
1,800 cubic feet for drying.
15,000 cubic feet for kilns.
Ice Plants:

2,000 feet gas per ton of refrigeration.
Zinc Plants:

15,000 cubic feet for roasting per ton of metal produced.
65,000 cubic feet for smelting per ton of metal produced.
20,000 cubic feet for power and miscellaneous uses per ton of
metal produced.
Cement Plants:

60 to 100 cubic feet per barrel for power.
80 to 100 cubic feet per barrel for roasters.
1,800 to 2,600 cubic feet per barrel for kilns.
Salt Plants:

Direct-fire pans, 9,000 cubic feet per ton.
Steam pans, 10,000 cubic feet per ton.
Single-effect vacuum pan, 15,000 cubic feet per ton.
Double-effect vacuum pan, 10,000 cubic feet per ton.
Triple-effect vacuum pan, 6,000 cubic feet per ton.
Flour Mills:

200 to 400 cubic feet per barrel.
Gas Compressors: , , • ^

Horsepower required to compress 1,000 cu. ft. of gas per mmute.
To 15 lbs. 50 H.P.

To 30 lbs. 85 H.P.

To 45 lbs. Ill H.P.

To 60 lbs 134 H.P.

To 80 lbs' 117 H.P. (2 stages)

To 100 lbs' 151 H.P. (2 stages)

To 200 lbs' 212 H.P. (2 stages)

Horsepower required to compress 1,000 cu. ft. of gas per hr.
To 15 lbs. 1 ^^ H.P.

To 30 lbs. 1-75 H.P.

To 45 lbs. 8.25 H P.

The specie hea^of average natural gas is 0.60 B.T.U. per pound,
or 0.028 BT.U. per cubic foot at 32 F.

404 BULLETIN NUMBER SIXTEEN OF

Gasoline, Natural Gas and Coal Dust Elxplosions. .

An explosion or a detonation is a chemical reaction which goes
on with increasing velocity and is accompanied by a rise of tempera-
ture. The lowest temperature at which combustion or explosion of a
mixture may take place is called the ignition temperature. This
varies greatly with different kinds of gas, about 650°C. The vapors
of some substances such as carbon bisulphide and hydrogen sulphide
are capable of ignition at much lower temperatures, even as low as
100 °C. Some gases even inflame spontaneously at room temperature.
These are phosphorus tri-hydride, boron and silicon hydride and caco-
dyl. Ordinarily, explosive mixtures are ignited by the presence of a
flame or spark at any point in the mixture ordinarily greater than
.2 of a millimeter in length. In order that the gaseous mixture ex-
plodes it is necessary that the heat generated by the local combustion
be greater than the heat absorbed by the surrounding gases. This
means of course that if the mixture is heated to a high temperature
it will be more readily explosive though the pressure will exert ver5'
little influence. An excess of either the combustible agent or the
oxidizing agent in the mixture will have the sam.e cooling effect tha*"
is exerted by any inert gas. The result is that the limits of explosi
bility of various mixtures of combustible gases and air are depend-
ent upon the heat generated by the combination and by the heat ab-
sorbed jn raising the temperature of the gases.

In the same manner that mixtures of gas or vapor and air will
explode, coal dust, oil m.ists and dusts of other combustible materials
will explode. As a general fact, these explosions will not take place
at ordinary room temperature unless there is over one-half pound of
dust of suspended matter per 500 cubic feet of air.

For ordinary gases the following limits hold as to the range of
combustion with combustible mixtures when air is the oxidising agent:

Limits of Explosibility of Mixtures of Combustible Gases and Air.

Gasoline vapor 1.5- 6.0% by vol. of mixture

Methane 5.5-14.5% by vol. of mixture

Ethane 2 5- 5.0% by vol. of mixture

Natural gas 5.0-12.0% by vol. of mixture

Acetylene 3.0-73.0% by vol. of mixture

Artificial illuminating gas 7.0-21.0% by vol. of mixture

Hydrogen 5.0-72.0% by vol. of mixture

Carbon m.onoxide 15.0-73.0% by vol. of mixture

Blast furnace gas 36.0-65.0% by vol. of mixture

Water gas 9.0-55.0% by vol. of mixture-
Coal gas 6.0-29.0%) by vol. of mixture

Ethylene 4.0-22.0% by vol. of mixture

Coal dust + 1 lb. per 500 cu. ft. of air

The striking back of a flame in a burner is caused by the pres-
ence of an explosive mixture in the burner. While the usual rate of
striking back of the flame or the propagation of an explosion is over
6,000 feet per second and about seven times the rate of sound in the
same medium, this rate exists only when there is no retardation of
the explosive wave caused by the cooling effect of the orifice or tube
through which it passes.

KANSAS CITY TESTING LABORATORY 405

Chemical Products from Natural Gas.

Natural gas offers peculiar opportunities for research on the de-
velopment of various oxidized and chlorinated products of methane
and ethane. It is well known that the ordinary natural gas burner
if not properly adjusted will emit great quantities of formaldehyde
gas probably according to the following reaction: CH4 + O2 = CH2O
+ H2O. The conditions governing the quantitative production of for-
maldehyde by partial oxidation of natural gas are those of proper
mixing, exact temperature and catalysis. Many different methods
have been attempted in the production of formaldehyde but most of
them will not produce more than 25 7f of the theoretical yield. Other
remote possibilities in the controlled oxidation of natural gas include
the production of alcohol and acetone.

The greatest success in the manufacture of chemical compounds
has resulted from the chlorination of natural gas. The commercial
preparation of mono-chloro-methane or methyl chloride CHsCl is now
being carried out successfully by a firm of manufacturing chemists.
This compound is used largely as a refrigerant and in the dye stuff
industry. Other chlorination products such as chloroform, CHCb
and carbon tetrachloride CCU are not yet made cheaply enough from
natural gas to compete with other established ways of making them.
They are however successfully made. These chlorination processes
are ordinarily carried out by the slow action of chlorine on the nat-
ural gas at carefully regulated temperatures and with a proper cata-
lyzer. Catalyzers that have been successfully used are finely di-
vided tin, nickel, copper, lead, dense charcoal, palladium, platinum
and the like. Unless low temperatures are used, the chlorine reacts
explosively forming only hydrochloric acid and carbon.

Hydrogen may also be made by the heating of natural gas at
very high temperature. However, this method of manufacture has
always been a method of convenience rather than a commercial method
where the making of hydrogen is a business. Amyl acetate may also
be indirectly made from natural gas by means of a chlorination pro-
cess but it is not yet done in competition comni3:-cially with other
methods of making this chemical.

406 BULLETIN NUMBER SIXTEEN OF

Methods of Manufacture of Carbon Black.

The processes of manufacturing carbon black now in use or con-
templation are as follows:

(1) Channel Process. This process consists in the use of steel
channels carried on trucks above gas flames burning from lava tips.
The lava tips are fitted so that they bum without sufficient air giv-
ing a yellow smoky flame. This flame impinges upon the bottom of
the channel bars which are moving slowly so as to present a cool
surface to the flame. The channel bars usually are about seven
inches wide and weigh about twelve pounds per foot. Scrapers are
adjusted to the bottom of the channels to take off the carbon as col-
lected. The carbon falls as the channel passes over the scraper and
is conveyed to the packing department. Each lava tip burns from
four to fourteen cubic feet of gas per hour and one tip produces about
3-5 grams of carbon per day. Thirteen tips produce one pound of car-
bon per day. A sixty barrel plant or one making 3,000 pounds of
•'arbon black per day requires 38,400 lava tips.

(2) Disc Process. This process was invented by Blood in 1883
and in principle is the same as the channel process except that the
cold surface on which the gas flame impinges is a cast iron disc
about 40 inches in diameter. The disc rotates at the rate of about
four revolutions per hour. The carbon is scraped off in much the
same manner as the channel process.

(3) Plate Process. This is known also as the Cabot Process.
This consists in perforated circular plates about 24 feet in diameter
and is essentially the same in principle as the disc and channel
processes. The spent gas passes through the perforated or ven-
tilator holes whereas in the disc process, they pass out over the edge
of the disc and in the channel process, between the channel bars.

(4) Roller or Cylinder Process. In this process, the face of the
cylinder is exposed to the gas flame. The cylinders are from three
to eight feet long and about eight to nine inches in diameter, each
weighing about 100 pounds. The cylinder rotates on a horizontal
axis.

(5) Thermal Decomposition Methods. In this, the primary ob-
ject has been to produce hydrogen. There is no o;:idation of the gas
and the carbon is produced purely by cracking. The carbon in this
method is comparatively poor, being rather hard and containing some
bituminous matter. The temperature of cracking usually is about
1500°F.

(6) Explosion Method. This method is not operated at present
on a commercial scale but has the advantage of being highly efficient
and giving a good grade of carbon. A charge of the gas mixed with
either air or oxygen is compressed into a heavy metal cylinder and ig-
nited by a spark. The explosion wave goes through the whole cylin-
der. The cylinder is opened and the carbon brushed out and a new
charge placed in. This is repeated indefinitelv.

KANSAS CITY TESTING LABORATORY

407

YIELD OF CARBON BLACK IN DIFFERENT FIELDS.

Plant No.

State

Process

Lbs. of Carbon Black
per 1000 Cu. Ft. Gas

1

Louisiana

Channel, 2-table

Channel, 1-table

Channel, 1-table

Large plate

Large plate

Rotary disc

Roller

Rotary disc

Channel, 2-table....

Channel, 1-table

Rotary disc

Channel

0 78

2

Louisiana . . .

0 95

3

Louisiana ....

0 80

4

Louisiana. . . .

0 80

5
6
7
8
9

10
11
12

West Virginia
West Virginia
West Virginia
West Virginia
West Virginia
West Virginia
West Virginia
Oklahoma . . .

1.10
0.95
0.80
1.00
1.12
1.30
1.40
1.20

13

Wyoming

Channel

1.40

COMPARISON OF DIFFERENT METHODS.

Plant
No.

Location

Louisiana

Louisiana

West Virginia.
West Virginia .
West Virginia .
West Virginia
Oklahoma . . . .

Method

*Sq. ft. per

Burner

Tip

2-table.
1-table.

Channel
Channel

Roller

Large plate

Channel, 2 table

Small disc

Channel. 1-table

0.21
0.26

Sq. ft. per Lb. | Sq. ft. per 100
of Carbon Cu. ft. of

Black Gas Burned

4.87

3.73

4.23

4 04

9.10

7.33

6.53

7.16

5.05

6.75

3.10

2.90

3.70

3.50

*Square foot of depositing surface.

The total quantity of carbon black produced from natural gas in
the United States in 1920 was 51,320.892 pounds, according to E. G-
Sievers of the U. S. Geological Survey, a decrease of 1.4 per cent
from 1919, notwithstanding an increase in the number of plants. In
1919, the plants were still operating at or near full capacity on ac-
count of the war, but since normal conditions have been restored the
production has decreased. The output in 1920 was made by 39 plants
operated bv 19 producers. The total value was $4,032,286 as com-
puted from' the prices received by the producers. The prices ranged
from 4 cents to 27 cents a pound. The average daily production in
1918 was 120,830 pounds, in 1919 it was 144,600 pounds, and m IJ^d
it was 140,608 pounds.

About 40,600,000 cubic feet of natural Kfs was consumed in the
manufacture of carbon black in 1920. I" 1919, the ^"^^"tty con-
sumed was 49,896.200,000 cubic feet and in 1918 it was estimated at
45,000,000,000 cubic feet. In 1920 the productiori of carbon black
per thousand cubic feet of gas consumed ranged from 0 45 to ^
pounds, but the average production during the year foi all states was
about 1.26 pounds.

408 BULLETIN NUMBER SIXTEEN OF

Range in Production of Carbon Black at Plants in the United States

in 1919 and 1920.
Production Plants

1919 1920

Less than 1 pound 6 6

From 1 to 1.2 pounds 17 19

From 1.3 to 1.6 pounds 11 . 6

From 1.7 to 2.0 pounds 2 8

Totals 36 39

The daily capacity of the plants in volume of gas treated ranges

from 172,000 to 20,350,000 cubic feet and in quantity of carbon black

produced from 90 to 23,250 pounds.

Production in 1919.

State Plants Pounds

West Virginia 23 29,925,614

Louisiana 7 14,024,606

Wyoming and Montana 2 4,868,947

Oklahoma and Kentucky 2 2,922,274

Pennsylvania 2 315,500

Totals 36 52,056,491

Gas = 49.9 X 10' cu. ft.

Production in 1920.
State Plants Pounds

West Virginia 19 26,659,469

Louisiana 15 18,565,498

Wyoming 1 1

Montana 1 j" 5,850,313

Kentucky 1 J

Pennsylvania 2 246,612

Totals 39 51,321,892

Gas = 40.6 X 10" cu. ft.

Uses of Carbon Black.

The uses of carbon black are, in order of importance: (1) the
manufacture of printing inks, (2) incorporation with rubber, (3)
varnishes and black points, (4) the blackening of ironware, (5) phono-
graphic records, pencils, carbon paper, typewriter ribbons, Chinese
inks, artificial stones, insulators and crucibles for steel.

The quantities employed in 1918 were: Printing ink, 5,000 to
6,000 tons, rubber, 10,000 tons, ironware, 2,000 to 3,000 tons and
other uses, 500 tons. In regard to printing inks, lamp black has
been used since the invention of the printing press and was used ex-
clusively up to 1864. For certain qualities, where a very fine grain
of black was required, much trouble was taken to purify it, but after
the discovery of carbon black in 1864 and the lowering of the price
of the latter in 1880, the use of the former diminished and at the
present day very small quantities of lamp black are being used.

Before 1914, the use of carbon black in the rubber industry was
scarcely known, and no differentiation was made between it and lamp

KANSAS CITY TESTING LABORATORY

409

black. The rise in price of zinc oxide then led to the employment of
carbon black as a filler in rubber and its valuable properties were
for the first time realized. It increases resistance to abrasion, gives
softness and in the opinion of many chemists has a favorable ef-
fect upon the aging of the rubber. From the economic point of
view, carbon black is cheaper than zinc oxide. Its density is 1.8, that
of zinc oxide is 5.8, so taking equal volumes and the price of carbon
black at 10c per pound, the black costs 33 per cent less than the zinc
oxide.

By reason of its fine state of division, carbon black constitutes
an ideal filling material for rubber, because it can be so intimately
mixed with the plastic rubber. It also protects the rubber against
the destructive effects of light and it possibly retards oxidation. Car-
bon black for the rubber industry is usually required to comply with
the following specifications:

(1) Moisture, less than 4 per cent.

(2) Acetone soluble matter, less than 0 5%.

(3) Ash, less than 0.25 '/f.

(4) No gritty particles to be present.

SPECIFIC HEAT OF GASES ENCOUNTERED IN NATURAL GAS

AND "CRACKED" GAS.

(H. L. Payne, J. A. & Appl. Chem.)

B.T.U.perlb. B.T.U.
perl°F

Air 0.234

Carbon dioxide 0.234

Carbonic oxide 0.245

Hydrogen 3.41

"Illuminants" 0.404

Methane 0.593

Nitrogen 0.244

Oxygen ^'^on

Aqueous vapor 0.480

per cu. ft.
perl°F
0.018
0.027
0.019
0.019
0.040
0.027
0.019
0.019

CALORIFIC VALUE OF NATURAL AND OIL GASES IN BRITISH
THERMAL UNITS PER CUBIC FOOT.

Name Symbol

Hydrogen H:

Carbonic oxide CO

Methane CH,

Illuminants

Ethane C-H„

Propane n u

Butane n w'"

Pentane Cr,Hi;

Hexane ^U'*

Ethylene C^H^

Propylene CsHb

Benzene ru

Acetylene C^H:

60°F

Initial

326.2

323.5

1009.2

1764.4

2521

3274

1588
2347.2
3807.4
1476.7

From and Ignition
to32°F Point "F

345.4
341.2
1065.0
2000.0
1861.0
2657.0
3441.0
4255.0
5017.0
1674.0
2509.0
4012 0
1477.0

1085
1200
1230

ii'4b

1015

1400

1010

940

788

410 BULLETIN NUMBER SIXTEEN OF

NATURAL GAS PRODUCED IN THE UNITED STATES IN 1916.

Quantity Price, cents

State M. cu. ft. per M. cu. ft. Value

West Virginia 299,318,907 15.90 47,603,396

Pennsylvania 129,925,150 18.74 24,344,324

Oklahoma 123,517,358 9.70 11,983,774

Ohio 69,888,070 22.32 15,601,144

Louisiana 32,080,975 8.29 2,660,445

Kansas 31,710,438 15.31 4,855,389

California 31,643,266 17.19 5,440,277

Texas 15,809,579 18.89 3,143,871

New York 8,594,187 29.37 2,524,115

Illinois 3,533,701 11.22 396,357

Arkansas 2,387,935 10.13 241,896

Kentucky 2,106,542 35.73 7.52,635

Indiana 1,715,499 29.34 503,373

Wyoming and Colorado 575,044 14.97 86,077

Montana 213,315 18.21 38,855

Dakotas and Alabama 77,478 40.75 31,573

Missouri 69,236 25.41 17,594

Tennessee 2,000 57.50 1,150

Michigan 1,298 73.04 948

Iowa ._ 275 100.00 275

Totals 753,170,253 15.96 120,227,468

Testing of Capacity of Casinghead Gas Wells.

To use the orifice well tester the specific gravity of the gas must
be taken. This is fully described on page 419.

To test a well, close all openings but one or if the well is shut
in at the casinghead, blow off the well before inserting the orifice well
tester. Allow the well to blow into the atmosphere for half an hour
or until there is no appreciable decrease in the volume of the gas
flowing from it. Screw in the orifice well tester, which carries a
two-inch thread, and allow the gas to flow into the atmosphere
through the proper size of orifice.

Connect a syphon gauge to the nipple on the side of the orifice
well tester, using a short piece of common three-eighths-inch rubber
hose. The syphon gauge should be filled with water up to the zero
mark on the scale. If the well appears to be large use the large-sized
orifice. To correctly determine the proper size of orifice it is neces-
sary to read the gauge and note the height of the water in the glass.
Read both sides of the scale and add them together. In other words,
measure the difference between the two water levels which is the true
pressure in inches of water. By referring to tables that accompany
each instrument, or as found on pages 420-424, the flow of a well
for a twenty-four hour period will be found under the proper gravity
and opposite the pressure.

The specific gravity bottle can be used to take the water pressure
of the gas flowing through the orifice in place of the syphon gauge.
In this case measure the difference between the two levels of the
water.

Use as large an orifice as possible so as not to permit the gas
to create a back pressure in the well. A back pressure in the well
will decrease the flow of the gas.

KANSAS CITY TESTING LABORATORY

411

Pitot Tube for Testing Open Flow of Gas Wells.

The most accurate way of testing the flow of a gas well is by
means of the Pitot tube, which is an instrument for determining the
velocity of flowing gas by means of its momentum. The instrument,

a

Fig. 85 — Pitot Tube.

as shown in figure usually consists of %,^"^J,"^^t''.af iusrinsTdo
bent at right angles, which is inserted in the flowing gas, just ins.cit

412

BULLETIN NUMBER SIXTEEN OF

the pipe or tubing a, at a point between one-third and one-fourth
of the pipe's diameter from the outer edge of the pipe. The plane
of the opening in the tube is held at right angles to the flowing
gas. At a convenient distance, varying from 1 to 2 feet, an inverted
siphon or U-shaped gage, usually half filled with mercury or water,
is attached to the other end. If the pressure of the flow is more
than 5 pounds per square inch, a pressure gage is required.

In small-sized wells with a flow of not more than 4,000,000 cubic
feet per 24 hours, a 12-inch U-gage with water can be used for flows
ranging from 4,000,000 to 15,000,000 feet, mercury in a 12-inch U-
gage; for 15,000,000 to 35,000,000 feet, a 50-pound spring gage, and
for more than 35,000,000 feet, a 100-pound spring gage should be
used. The foregoing figures are based on a 6-inch hole.

For convenience, a scale graduated from the center in inches
and tenths of an inch is attached between the two limbs of the U-
gage. The distance above and below this center line at which the
liquid in the gage stands should be added, the object being to de-
termine the exact distance between the high and low side of the fluid
in inches and tenths of an inch.

The top joint of the tubing or casing should be free from fittings
for a distance of 10 feet below the mouth of the well where the test
is made. The test should not be made in a collar or gate or at the
mouth of any fitting. The well should be blown off at least three
hours prior to making the test.

After the velocity pressure of the gas flowing from the well
tubing has been determined in inches of water, inches of mercury, or
pounds per square inch, as outlined above, the corresponding flow
may be obtained from the following table*. The quantities of gas
stated in the table are based on a pressure of 4 ounces above atmos-
pheric, or 14.65 pounds per square inch absolute pressure, a flowing
temperature of 60°F., a storage temperature of 60°F., and a specific
gravity of 0.60 (air = 1). If the specific gravity is other than 0.60 the

/

0.60

flow should be multiplied by

/-

V specific gravity of gas

*Westcott, H. P.: Handbook of Natural Gas, 1915, pp. 176, 177.
For pipe diameters other than those given in the following table,
the following multipliers should be applied to the figures for 1-inch
tubing given in the table.

Multipliers for Pipe Diameters Ranging from V/z to 12 Inches.

Diameter of

Multi-

Diameter of

Multi-

Diameter of

Multi-

Pipe, Inches

plier

Pipe, Inches

pUer

Pipe, Inches

plier

1^

2.25

5

25

8

64

2M

6.25

5^

31.64

8H

68

AH

18

6

36

9

81

^Vs

21.39

en

39

10

100

GVs

43.9

12

144

KANSAS CITY TESTING LABORATORY

413

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414 BULLETIN NUMBER SIXTEEN OF

Flow of Gas in Pipes — Low Pressure.

The following formulae are intended for low pressure distribution
of gas, with comparatively small differences between the initial and
final pressurp'?*

Pole's Formula Q = 1350 y

Molesworth's Formula Q — 1000 a ,

Gill's Formula Q = 1291 ,, ,. , ,.

^ V s (1 + d)

Where Q = quantity of gas discharged in cubic feet per hour,
d = inside diameter of pipe in inches,
h = pressure in inches of water,
s = specific gravity of gas, air being 1.
1 = length of main in yards.

Oliphant's Formula. A formula determined by F. H. Oliphant for
the discharge of gas when the specific gravity is 0.60 is

/

d-h

si

/

d^h

si

/

d'h

/Pi'— P2=

Q = 42a y l

Where Q = discharge in cubic feet per hour at atmospheric pressure.

Pi = initial pressure in pounds per square inch (absolute)

Pj = final pressure in pounds per square inch (absolute).

L = length of main in miles.

a = coefficient (see table below).

For gas of any other specific gravity, s, multiply the discharge by

/ 0.60
■y . for temperature of flowing gas when observed above 60 °F

* s

deduct 1 per cent for each 5° and add a like amount for temperatures
less than 60°F.

According to Oliphant, the discharge is not strictly proportional to

/ 1

^.| . Using a coefficient of unity for 1-inch pipe he gives

V d'

/ 1

d"' 30

KANSAS CITY TESTING LABORATORY

415

Inside

diameter

inches

%
1

11/2
2

2%

Values of Coefficient "a'

Inside
diameter
inches a

.0317
.1810
.5012

1.00

2.93

5.92
10.37

3
4
5

5%
6
8
10

16.
34.
60
81
95
198
350

Inside

diameter

inches

12
16
18
20
24
30
36

For 15 inch outside diameter pipe, 14% inches inside dia. a
For 16 inch outside diameter pipe, 15^/4 inches inside dia. a
For 18 inch outside diameter pipe, nVi inches inside dia. a
For 20 inch outside diameter pipe, 19 Vi inches inside dia. a

a

556
1160
1570
2055
3285
5830
9330

= 863

= 1025

= 1410

= 1860

Capacity of Pipe Lines.

(Metric Metal Works.)

Tables to Find the Cubic Feet, Per Day of 24 Hours, of Gas of .6

Specific Gravity at Certain Pressure in Pipe Lines

of Various Diameter and Lengths.

Select in table A the number opposite the gauge pressures, in
pounds, then from table B select the number opposite the length of
line in miles. Multiply these two numbers together and result is the
cubic feet that a 1-inch line will discharge for the pressures and
length named in twenty-four hours. If the diameter of the pipe is
other than one inch, select the number in table C which corresponds
with the diameter and multiply this number by the discharge for one
inch already secured. The result is the quantity in cubic feet in
twenty-four hours discharged by a line whose diameter was selected.

If there are other pressures and lengths not given in the table
they can be secured by interpolation. Example— Suppose it is re-
quired to find the discharge per day of twenty-four hours of a pipe
line having an intake of 200-pound gauge pressure and 2i) pounds at
the discharge end, the length being 20 miles, and the il''>n\^'ter «
inches. In table A we find opposite 200 and 25 the number 21.i5.
and in table B opposite 20 miles, 22.5, multiplying these two numbers
the result being 47.637 cubic feet that under the above condition ot
pressure and length a 1-inch pipe would convey, but the required
diameter is 8 inches. Under this number in table ^' "t ^\;' .' '^^' ';"' ,
that 198 corresponds; therefore 47,637 X 198 = 9,433,120. which is
the cubic feet discharged in 24 hours.

If the pressure were twenty pounds instead of twenty-five at the
discharge end it would be found very closely by »;>;''"»^'thc figures
opposite 15 and 25 and dividing by 2. the result would be 9,4(.fi.1.. «•

416

BULLETIN NUMBER SIXTEEN OF

TABLE A.

Dis-

Dis-

Dis-

Intake,

charge,

Re-

Intake,

charge,

Re-

Intake,

charge,

Re-

Lbs.

Lbs.

sultant

Lbs.

Lbs.

sultant

Lbs.

Lbs.

sultant

1

H

4.7

40 •

5

51,2

110

75

86.8

1

14

3.9

40

10

49,0

110

85

75,0

2

Vi

6.9

40

15

46.1

110

100

49,0

2

1

4.7

40

20

42.4

125

5

138.6

2

IJ^

4.0

40

25

37.8

125

15

136.8

3

1

8.1

40

30

31.6

125

25

134,2

3

2

5.8

40

35

22.9

125

35

130,8

4

1

10.1

50

5

61.8

125

50

124,0

4

2

8.4

50

10

60,0

125

75

107.2

4

3

6.0

50

15

57,7

125

100

79,8

5

1

11.8

50

20

54,8

125

110

63,1

5

2

10.4

50

25

51,2

135

5

148.7

5

3

8.6

50

30

46.9

135

15

147,0

5

4

6.2

50

35

41,5

135

25

144,6

6

1

13.4

50

40

34,6

135

35

141,4

6

3

10.6

50

45

25,0

135

50

135,2

6

5

6,3

60

5

72,3

135

75

120,0

7

1

14.9

60

10

70,7

135

100

96,3

7

3

12.5

60

15

68,8

150

5

168,3

7

5

9.0

60

20

66,3

150

15

163,3

7

6

6:5

60

25

63,4

150

25

160,1

8

1

16.3

60

30

60,0

150

40

155,6

8

3

14.1

60

40

51,0

150

50

151,7

8

5

11.2

60

50

37,4

150

75

138.3

8

7

6,6

60

55

26,9

150

100

118.3

9

1

17.6

70

5

82,6

150

120

94.9

9

3

15.6

70

10

81,2

175

5

188.9

9

5

13.1

70

20

77.5

175

15

187.6

9

8

6.8

70

30

72,1

175

25

185.7

10

1

19.2

70

40

64,8

175

35

183.3

10

2

18.3

70

50

54,7

175

50

178.5

10

4

16.3

70

60

40,0

175

75

167.3

10

6

13.6

80

5

92,8

175

100

151.2

10

8

9.8

80

10

91,6

175

150

94.2

10

9

7.0

80

20

88,3

200

5

214.1

12

1

21.8

80

30

83,7

200

15

212.9

12

3

20.1

80

40

77,5

200

25

211.3

12

6

17.0

80

50

69.2

200

35

209.1

12

8

14.1

80

60

58.3

200

50

204.9

12

10

10.2

80

70

42.4

200

75

195.3

15

1

25.4

90

5

103.1

200

100

181.7

15

3

24.0

90

10

102.0

200

125

163.2

15

6

21.4

90

20

99.0

200

150

137.9

15

9

18.0

90

30

94.9

200

175

100.6

15

12

13.1

90

40

89.4

200

190

64.8

20

1

31.1

90

50

82.5

220

5

234.2

20

4

29.4

90

60

73,5

220

15

233.1

20

8

26.4

90

70

61,6

220

25

231.6

20

10

24.5

90

80

44,7

220

35

229.6

20

15

18.0

100

5

113,3

220

50

225.8

20

18

11.7

100

10

112,3

220

75

217.1

25

1

36.7

100

15

111 0

220

100

204.9

25

3

35.7

100

20

109,5

220

125

188.8

25

6

34.0

100

25

107.8

220

150

167.3

25

10

31,2

100

35

103.6

220

175

138.3

25

15

26,5

100

50

94.9

220

200

94.9

25

18

22,6

100

75

71.6

230

5

244.1

30

1

42.1

100

85

56.8

230

15

243.2

30

3

41,2

100

95

33.5

230

25

241.7

30

6

39,8

110

5

123.4

230

35

239.8

30

10

37,4

110

15

121.4

230

50

236.2

30

15

33,5

110

25

118.4

230

75

227.9

30

20

28.3

110

35

114.6

230

100

216.3

30

25

20,0

110

50

106.8

230

150

181.5

KANSAS CITY TESTING LABORATORY

An

TABLE A— Continued.

Dis-

Dis-

Dis-

Intake,

charge,

Re-

Intake,

charge,

Re-

Intake,

charge,

I Re-

Lbs.

Lbs.

sultant

Lbs.

Lbs.

sultant

Lbs.

Lbs.
225

sultant

230

200

117.5

325

250

213.0

400

338.6

230

215

84.4

325

275

177.5

400

250

319.4

250

6

264.2

325

285

160.0

400

275

296.9

250

15

263.3

325

300

128.0

400

300

270.2

250

25

262.0

350

5

364.5

400

325

238.0

250

35

269.2

350

15

363.8

400

350

197.5

250

50

256.9

350

25

362.8

400

375

141.9

250

75

249.3

350

35

361.6

425

5

439.6

250

100

238.3

350

50

359.2

425

15

439.0

250

125

225.0

350

75

353.7

425

25

438.2

250

150

207.4

350

100

346.4

425

35

437.2

250

175

184.7

350

125

337.1

425

50

435.2

250

200

154.9

350

150

325.6

425

75

430.7

250

230

101.0

350

175

311.7

425

100

424.7

275

5

289.3

350

200

295.0

425

125

417.1

275

15

288.4

350

225

275.0

425

150

407.9

275

25

287.2

350

250

251.0

425

175

396.9

275

35

285.7

350

275

221.6

425

200

383.9

275

50

282.6

350

300

184.4

425

225

368.8

275

75

275.7

350

325

132.8

425

250

351.3

275

100

266.2

375

5

389.5

425

275

330.9

275

150

238.5

375

15

388.8

425

300

307.2

275

200

194.6

375

25

387.9

425

325

279.3

275

250

117.8

375

35

286.8

425

350

245.7

300

5

314.4

375

50

384.6

425

375

203.7

300

15

313.6

375

75

379.5

425

400

146.2

300

25

312.5

375

100

372.7

450

5

464.6

300

35

311.0

375

125

364.0

450

15

464.0

300

50

308.2

375

150

353.4

450

25

463.3

300

75

301.9

375

175

340.6

450

35

462.3

300

100

293.8

375

200

325.4

450

50

460.4

300

125

282.2

375

225

307.4

450

75

456.2

300

150

268.3

375

250

286.1

450

100

450.5

300

175

251.3

375

275

260.8

450

135

443.4

300

200

230.2

375

300

230.0

450

150

434.7

300

250

170.3

375

325

191.1

450

175

424.4

300

275

123.0

375

350

137.4

450

200

412.3
398.3

325

5

339.4

400

5

414.5

450

225

325

15

338.7

400

15

413.9

450

250

382.1
363.5
342 . 1
317.2
288.1
263.2
209.8
150.4
486.7
610.0

325

25

337.6

400

25

413.1

450

275

325

35

336 3

400

35

412.0

450

300

325
325
325
325
325
325

50
75
100
125
150
175

333.7
327.9
320.0
309.8
297.3
281.9

400
400
400
400
400
400

50
75
100
125
150
175

409.9
405.1
398.8
390.2
380.8
369.0

450
450
450
450
450
475

325
350
375
400
425
50
50

325

200

263.4

400

200

355.0

500

418

BULLETIN NUMBER SIXTEEN OF

TABLE B.

Miles

Multipliers

Miles

Multipliers

Miles

Multipliers

h

2880.

19

231.2

61

129.1

H

2016.

20

225.5

62

128.1

Vs

1652.4

21

220.1

63

126.9

Yi

1419.7

22

214.9

64

126.0

il

1275.9

23

210.0

65

125.1

M

1158.6

24

205.7

66

124.1

Vi

1083.7

25

201.6

67

123.1

1

1008.0

26

197.6

68

122.2

Wi

826.2

27

193.8

69

121.3

IM

763.6

28

190.5

70

120.4

2

714.9

29

187.0

72

118.7

2J^

638.0

30

183.9

74

117.2

2M

607.2

31

181.0

76

115.6

3

582.7

32

178.0

78

114.2

^Vi

539.0

33

175.6

80

112.7

4

504.0

34

172.9

82

111.2

Wi

475.5

35

170.3

84

109.9

5

450.0

36

168.0

86

108.7

5.4

428.9

37

165.8

88

107.5

6

411.4

38

163.6

90

106.2

6J^

395.3

39

161.3

92

105.1

7

380.4

40

159.5

94

103.9

•7M

367.9

41

157.5

96

102.9

356.2

42

155.6

98

101.8

8H

345.2

43

153.7

100

100.8

9

336.0

44

152.0

102

99.8

9J^

327.3

45

150.2

105

98.3

319.0

46

148.7

107

97.5

311.1

47

146.9

110

96.0

11

303.6

48

145.4

112

95.3

11 K

297.3

49

144.0

115

93.9

J2

I2H

291.3

50

142.6

118

92.8

284.7

51

141.2

120

92.0

13

276.4

52

139.8

122

91.2

13J^

274.6

53

138.5

125

90.2

14

269.5

54

137.1

130

88.4

14H

264.6

55

135.8

135

86.8

15

260.5

56

134.8

140

85.2

15J^

255.8

. 57

133.5

145

83.7

16

252.0

58

132.3

150

82.3

17

244.7
237 . 5

59
60

131.2
130.1

18

TABLE C.

Multipliers for diameters other than 1 inch.

M

inch

=

.0317

Vz

inch

.1810

%

inch

=r

.5012

1

inch

=

1.0000

Wi

inch

=

2.9300

2

inch

=

5.9200

21/2

inch

=

10.3700

3

inch

= 16.50

4

inch

= 34.10

5

inch

= 60.00

5%

inch

= 81.00

6

inch

= 95.00

8

inch

= 198.00

10

12 inch = 556

16

inch

=

1160

18

inch

3Z

1570

20

inch

2055

24

inch

r=

3285

30

inch

ZIZ

5830

36 inch = 9330

inch = 350.00

For wrought iron pipes greater than 12 inches in diameter the
measure is taken from outside, and for pipes of ordinary thick-
ness the corresponding inside diameters and multipliers are as follows:
Outside dia. of 15-inch pipe gives 14^/4 in. inside dia. = 863
Outside dia. of 16-inch pipe gives 15^4 in. inside dia. = 1025
Outside dia. of 18-inch pipe gives 17% in. inside dia. = 1410
Outside dia. of 20-inch pipe gives 19% in. inside dia. = 1860

KANSAS CITY TESTING LABORATORY

419

Measuring the Flow of Natural Gas.

ORIFICE METER.

An instrument known as the orifice meter, for testing small flows
of natural gas, is shown in the figure. This instrument is simple in
construction, consisting of a short 2-inch nipple, b, with pipe thread
on one end and a thin
plate disk on the other.
The disk carries a 1-
inch orifice, a, and a
hose connection, c, for
taking the pressure.
The meter is especially
intended for testing
small gas wells and
"casinghead" gas from
oil wells. As a rule
the flow of gas from
an oil well is rather
small, and it is not ad-
visable to test the flow
with a Pitot tube such
as is used in testing
large gas wells. In
using the orifice tester,
it is necessary to know
the specific gravity of
the gas in order to ob-
tain the flow.

Before the. orifice
well tester is attached
to the casinghead the
well should be per-
mitted to blow into the
atmosphere until the
head of the gas is re-
duced and the flow has
become normal. Then
the tester is attached
by simply screwing it
into the end of a 3-foot
length of 2-inch pipe
and the pressure is
read in inches of water
on the siphon gage, d.
In the tables * on pages
420-21, the flow of the . . . -„„,,-if,. the

well with values for the gas of different gravities _ is opiK)siU the

ig. The orifice in \
uninjured; otherwise the page

(I

Fig. 86— Orifice .Meter.

'. S. Bureau "f Pi Miidards.)

well with values lor tne gas ui uixx^i'^wv ^--•■-■~-, ,'\ , „,,,!
gage reading. The orifice in the instrument should be kept dr> and
nnfniured; otherwise the page reading will not be coiroct.

^Westcott H. P.: Handbook of Natural Gas, 1915. pp. 545-548.

420

BULLETIN NUMBER SIXTEEN OF

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KANSAS CITY TESTING LABORATORY

421

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422

BULLETIN NUMBER SIXTEEN OF

Orifice Capacity.

Diameter, Inches

Cubic Feet per Hour

Area

Morse
Drill

Gage

Coal Gas,

Water Gas,

Natural Gas

Frac.

Decimal

Square Inch

Size

0.32 sp. gr.
2" Press

0.62 sp. gr.
2" Press

0.62 sp. gr.
43^-cz. Press

0.0135

0.000143

80

1.04

0.86

1.67

0.0145

0.000165

79

1.16

0.97

1.89

1/64

0.0156

0.00019

1.26

1.05

2.05

0.016

0 . 00020

■ 7g--

1.32

1.10

2.14

0.018

0.00025

77

1.35

1.13

2.20

0.020

0.00031

76

1.62

1.35

2,63

0.021

0.00035

75

1.80

1.52

2 96

0.0225

0 . 00040

74

2.16

1.80

3.51

0.024

0.000.45

73

2.29

1.90

3.70

0.025

0.00049

72

2.46

2.05

4.00

0.026

0.00053

71

2.70

2.25

4.38

0.028

0.00062

70

2.79

2.33

4.54

0.0292

0.00067

69

3.08

2.57

4.97

0.031

0.00075

68

2.23

2.70

5.26

1/32

0.031

0.00076

3.26

2.73

5.32

0.032

0.00080

67 '

3.42

2.85

5.56

0.033

0.00086

66

3.53

2.94

5.73

0.035

0.00096 ^

65

3.69

3.08

6.00

0.036

0.00102

64

3.86

3.23

6.30

0.038

0.00108

63

4.05

3.38

6.60

0.038

0.00113 I

62

4.11

3.51

6:84

0.039

0.00119 ►

61

4.50

3.75

7.31

0.040

0.00126

60

4.95

4.12

8.04

0.041

0.00132

59

5.22

4.35

8.48

0.042

0.00138

58

5.40

4.50

8.67

0.043

0.00145

57

5.67

4.71

9.2

0.0465

0.00170

56

6.57

5.47

10.6

3/64

0.0469

0.00173

6.75

5.63

11.0

0 . 0520

0.0021

'55"

8.9

6.75

13.2

0.0550

0.0023

54

9.0

7.50

14.6

0.0595

0.0028

53

10 8

9.0

17.5

1/16

0.0625

0.0031

11.7

7.7

19.0

0.0635

0.0032

52 "

11.9

9.9

19.3

0.0670

0.0035

51

12.6

10.5

20 5

0.070

0 . 0038

50

13 5

11.2

21.8

0.0730

0 . 0042

49

14.4

12 0

23.4

0.076

0.0043

48

15.3

12 7

24.8

6/64

0.0781

0.0048

15.7

13.1

25 5

0.0785

0.0018

■■■47' ■'

15.8

13.2

25 7

0.081

0.0051

46

16

13.5

26

0.082

0.0053

45 ■•

17

14.3

28

0.086

0.0058

44'

18

15

29

0.089

0.0062

43'

19

16.5

32

0.0935

0 . 0069

42

20

17

33

3/32

0.0937 i

0 . 0069

21

18

35

0.096

0.0072

■ 41"

22

19

37

0.098

0.0075

40

23

20

39

0.0995

0.0078

39

24

20.5

40 :

0.1015

0.0081

38

25

21

41

0.104

0.0085

37

26

22

43

0.1065

0.0090

36

27

22.5

44

7/64

0.1093

0 . 0094

28

23

45

0.110 =,

0.0095

"35

29

24

47

0.111

0.0097

34

30

25

49

0.113

0.0100

33

31

26

51

0.116

0.0106

32

32

27

53

KANSAS CITY TESTING LABORATORY

423

ORIFICE CAPACITY— Continued.

Diameter, Inches

Cubic Feet per Hour

Area,

Morse
Drill

Square Inch

Gage

Coal Gas,

Water Gas.

Natural Gas,

Frac.

Decimal

Sizej

0.43 sp. gr.
2" Press

0.62 sp. gr.
2" Press

0.62 sp. gr.
434-oz. Press

0.120

0.0113

31

33

28

55

1/8

0.125

0.0123

36

30

58

0.1285

0.0130

30

39

32

62

0.136

0.0145

29

43

35

68

0.1405

0.0155

28

44

37

72

9/64

0 . 1406

0.0155

45

38

74

0.144

0.0163

27

47

39

76

0.147

0.0174

26

48

40

78

0.1495

0.0175

25

51

42

82

0.152

0.0181

24

52

43

84

0.154

0.0186

23

53

44

86

5/32

0.156

0.0192

54

45

88

0.157

0.0192

22

55

46

90

0.159

0.0198

21

57

47

91

0.161

0 . 0203

20

58

48

95

0.166

0.0216

19

60

50

97

0.1695

0.0226

18

62

52

101

11/64

0.1719

0.0232

63

53

103

0.173

0.0235

17

65

54

105

0.177

0.0246

16

68

56

109

0.180

0 . 0254

15

69

58

113

0.182

0.0260

14

71

59

115

0.185

0.0269

13

72

61

119

3/16

0.1875

0.0276

75

62

121

0.189

0.0280

i2

76

63

123

0.191

0.0286

11

77

64

125

0.1935

0.0294

10

79

66

129

0.196

0.0302

9

80

67

131

0.199

0.0311

8

83

69

134

0.201

0.0317

7

84

70

136

13/64

0.203

0.0324

86

71

138

0.204

0.0327

6

87

72

140

0.205

0 . 0332

5

89

74

144

0.209

0.0343

4

93

77

150

0.213

0.0356

3

95

79

154

7/32

0.2187
0 221

0.0375
0 0384

2 '"

97
99

80
82

156
160

0 228

0.0408

1

104

86

168

15/64

1/4
17/64

9/32
19/64

5/16
21/64
11/32
23/64

3/8
25/64

0.2344

0.250

0.2656

0.2812

0.2969

0.3125

0.3281

0.3437

0.3594

0.375

0.3906

0.0442
0.0491
0.0554
0.0621
0.0692
0.0767
0.0845
0.0928
0.1014
0.1104
0.1198

108
119
131
142
163
164
176
187
198
209
221
231
241
254
264
277
286
299
309
320
331
340
353

90
99
109
119
128
136
146
155
165
174
184
193

175
193
212
232
260
166
285
302
322
340
360
376

■ 13/32

0.4062

0 . 1296

9ni

392

27/64

0.4219

! 0.1398

211

412

7/16

0.4375

0.1503

220

430

29/64

0.4531

0.1612

230

448

15/32

0.4687

0.1725

239

466

31/64

1/2

0.4844
0.500

0.1843
0.1963

249
267

486
600

33/64

0.5156

0 . 2088

267

620

17/32

0.5312

0.2216

276

639

35/64

0.5469

0.2349

285

656

9/16

0.5625

0.2485

296

676

37/64

0.5781

0.2625

■jna

690

19/32

0.5937

0.2769

1

424

BULLETIN NUMBER SIXTEEN OF

ORIFICE CAPACITY— Continued.

Diameter, Inches

Area,
Square Inch

Morse
Drill
Gage

Size

Cubic Feet per Hour

Frac.

Decimal

Coal Gas,

0.43 sp. gr.

2" Press

Water Gas

0.62 sp. gr.

2" Press

Natural Gas,
0.62 sp. gr.
4K-OZ. Press

39/69

5/8
41/64
21/32
43/64
11/16
45/64
23/32
47/64

3/4
49/64
25/32
51/64
13/16
53/64
27/32
25/64

7/8
57/64
29/32
59/64
15/16
61/64
31/32
63/64
1

0.6094

0.625

0.6406

0.6562

0.0719

0,6875

0.7031

0.7187

0.7344

0.750

0.7656

0.7812

0.7969

0.8125

0.8281

0.8438

0.8594

0.875

0.8906

0.9062

0.9219

0.9375

0.9531

0.9687

9.9844

1.0000

0.2917
0.3068
0.3223
0.3382
0.3546
0.3712
0.3883
0.4057
0.4236
0.4418
0.4604
0.4794
0.4988
0.5185
0.5386
0.5591
0.5801
0.6013
0.6229
0.6450
0.6675
0.6903
0.7134
0.7371
0.7611
0.7854

376
387
399
410
421
431
443
454
466
476
488
499
510
520
532
543
554
565
576
588
599
510
620
632
644
655

313
323
333
341
350
369
370
378
387
397
406
415
424
433
443
453
461
472
480
490
500
507
517
526
536
545

610
630
650
665
682
720
722
737
755
774
792
810
827
845
865
884
900
920
938
955
976
985
1010
1025
1047
1062

NOTE: — The above table is based upon data obtained from gas
orifices that are ordinarily used in gas appliances such as the ones
used in Hale Gas Mixers.

ARTIFICIAL GAS:— The above figures are based upon 2-inch
pressure; for higher pressures these figures should be increased by
a percentage as shown below:

3-inch
4-inch
5-inch
6-inch
7-inch

25
50
62.5

75
87.5

%

10-inch
12-inch
16-inch
20-inch

120 %
140
180
210

NATURAL GAS: — The above figures for natural gas are based
on a gas under 4% oz. pressure having a specific gravity of 0.62,
which is the ordinary gravity of natural gas sold in cities supplied by
gas from the Mid-Continent. Pennsylvania and West Virginia fields.
When the pressure is greater than 4V2 oz. the figures in the table
should be increased as shown below:

5 oz. = 10%

6 oz. = 20

7 oz. = 30

8 oz. = 39 %

9 oz. = 47.5
10 oz. = 60

KANSAS CITY TESTING LABORATORY 425

Outline of Methods of Analysis of Petroleum Products.

1. Specific Gravity and Baume' Gravity.

(a) With hydrometer. (d) By fluid suspension.

(b) With picnometer. (e) By displacement.

(c) With Westphal balance. (f) Asphaltic Cement.

2. Color of Petroleum.

(a) Saybolt Chromometer. (d) lodimetric.

(b) Lovibond Tintometer. (e) Union Colorimeter.

(c) Potassium Bichromate.

3. Odor of Oil.

4. Transparency.

5. Viscosity or Fluidity.

(a) Saybolt Universal, Engler and Redvfood Viscosimeters.

(b) Furol Viscosity for fuel oil and road oil.

(c) Ubbelohde Viscosimeter for thin petroleum products.

(d) MacMichael Disk Friction Viscosimeter.

(e) Float test for viscosity of road oils.

(f ) Zero Viscosity for semi-solid petroleum products.

(g) Petrolatum.

6. Melting Point.

(a) Ring and Ball.

(b) Cube method.

(c) "General Electric" method.

(d) Wax.

7. Cold Test.

(a) Cloud test.

(b) Pour test.

(c) Cold test.

8. Water and Bottom Settlings.

(a) By centrifuge.

(b) By distillation.

9. Distillation Tests for Petroleum.

(a) End point distillation.

(b) Fractional— Gravity distillation analysis.

(c) Proximate distillation for water, gasolme, kerosene and re-
siduum.

(d) Fractional — Sample distillation.

10. Flash and Burning Points.

(a) Illuminating oils with closed tester (lag.).

(b) All types of petroleum products with the Elliott or New York
closed tester.

(c) Lubricants and asphalt with Cleveland open cup.

(d) Fuel oil with Pensky-Martens.

11. Pressure— Heat Tests. f^,^r,^rMfiirP

(a) Cracking test under high pressure and temperature.

(b) Vapor pressure test at high pressure. . . „„j nrp<»<»ure

(c) Motor oil lubricant test for stability under heat and pressure.

(d) Vapor pressure of light gasohne.

12. Carbon residue.

(a) Conradson carbon test.

(b) Fixed carbon and ash m asphalt.

(c) Asphaltic carbon in lubricating oils.

426 BULLETIN NUMBER SIXTEEN OF

13. Emulsification test of lubricating oils.

14. Heat of combustion.

(a) By bomb calorimeter.

(b) By calculation from gravity.

15. Sulphur in Petroleum Products.

(a) By bomb calorimeter.

(b) By Eschka method.

(c) By chemical bomb.

(d) In illuminating oils by lamp method.

(e) For Naphtha and turpentine substitute, white lead test.

16. Ultimate Analysis.

(a) Carbon and Hydrogen.

(b) Nitrogen.

17. Doctor Test for Refined Distillates.

18. Olefins, Ethylenes or Unsaturated Hydrocarbons.

(a) Babcock method.

(b) Cylinder method.

(c) Refining loss.

19. Aromatic and Paraffin Hydrocarbons in Petroleum.

(a) Nitrating method.

(b) Distillation method.

20. Acid.

(a) Free acid in petroleum products.

(b) Combined fatty acid.

21. Floe Test.

22. Corrosion and Gumming Test of Gasoline.

23. Penetration or Consistency of Asphalt.

24. Ductility of Asphalt.

25. Resistance of Asphalt and Oil to Evaporation.

26. Determination of Natural Asphalt or Semi-Solid HydrocarboM in

Petroleum. Oxidation of Lubricating Oils.

27. Solubility of Petroleum and Asphalts.

(a) In petroleum ether —

(1) A.S.T.M. precipitation number of lubricating oils.

(2) Tar in lubricating oils, asphaltenes in asphaltic cement.

(b) In carbon bisulphide — total bitumen.

(c) In carbon tetrachloride — carbene free bitumen.

28. Resistance of asphalt to oxidation.

29. Paraffin wax or scale determination.

30. Bitumen and Grading of Asphalt-Mineral Mixtures.

(a) By burning.

(b) By extraction.

31. Tensile and Cementing Strength of Asphaltic Surface Mixtures.

32. Specific Gravity of Gas.

(a) Effusion or viscosity method.

33. Gasoline Determination in Gas.

(a) By absorption test.

(b) Freezing test.

34. Complete Chemical Analysis of Gas with Preparation of Reagents.

35. Heat of Combustion of Gas.

(a) By the calorimeter.

(b) By oxygen consumption.

(c) By calculation from chemical analysis.

KANSAS CITY TESTING LABORATORY

427

Index to Applications of Methods of Analysis.

, PRODUCT

Routine Test

Occasional Tesi

Rarely Used

A. Crude Petroleum ...

lA, 2D, 3, 4,
8, 9B, 9C, 15

7C,9D,10,5A,
9C, 14, 26, 29

2D, 7B, 9D,
12, 16, 18

B. Gasoline, Benzine and

Naphtha

1, 2, 3, 4, 9A,
17, 18, 22

9B, 14, 19,20,
IID

5B, 7A, 15, 16
20

C. Kerosene and Illumi-
nating Oils

1,2ABC,3,4,
5B, 7, 9B,
lOA, 15. 17,
21

lOB, 14, 18,
20,22

9C,11B, 16,19

D. Gas Oil, Straw Oil,
Absorption Oil. . . .

1, 2, 3, 4, 7,
9C, 10, 14, 15

5, llA, 12A,
13, 17, 18

16, 19, 20, 21

E. Lubricants, Paraffin
Oils

1, 2, 3, 4, 5A,
7, 10, 12A, 13,
15, 20, 27A

14, 17, 18, lie.
12C

16, 19, 21

F. Fuel Oil, Diesel En-
gine Oil

1,5C, 7, 8, 10,
14, 15

5, 11,26,27A,
29

2D,3, 9, 12, 16
18, 19

G. Road Oil, Flux Oil . .

lAB, 5AD, 8,
10, 12, 25, 26,

27

7B, 14, 15,29

2D, 11, 16

H. Asphalt and Pitch . . .

IDF, 5F,
6ABC, IOC,
12, 23, 24, 27

8B, 15, 28.
29

2D, 3, 14, 16.
25

I. Wax

1, 2, 3, 6D

4,25

llA, 12A, 14,
15, 16, 17, 18,
19,20

J. Grease

1, 2, 3, 4,
5DE, 8, 12B,
27

20,25

16

K. Asphalt Surface Mix.

IE, 30, 31

L. Gas

32. 33, 34, 35

16

Note— See special specifications for other tests of Petroleum
Products.

428 BULLETIN NUMBER SIXTEEN OF

1. Specific Gravity and Baume' Gravity (General Discussion).

Specific gravity is the relation by weight of the same volume of
oil and of water. Unless some other temperature is specifically men-
tioned the gravity refers to 60 °F. Specific gravity is determined by
means of the hydrometei', the Westphal balance, the picnometer and
by displacement methods. The absolute specific gravity scale is not
commonly used in the oil industry. Instead, the Baume' gravity
scale, an entirely arbitrary standard is used. Two Baume' gravity
scales are in use in the oil industry; one is that adopted by the U. S.
Bureau of Standards and its relation to specific gravity is indicated
by the following formula:

140

Specific Gravity = for liquids lighter than water.

130 + Baume'

Another scale possibly more commonly used is that of the Amer-
ican Petroleum Association, which is based upon the following rela-
tion to specific gravity:

141.5

Specific Gravity = for liquids lighter than water.

131.5 + Baume'

The difference between the two readings varies from nothing
with very heavy oils to as much as 0.5° Be' for ordinary gasoline.
When the oil is heavier than water a different formula is used
for calculating the Baume' gravity, the following being in general
use:

145

Degrees Baume' — 145 for liquids heavier than

water. Specific Gravity

Oils heavier than water are not commonly encountered. The
method of using the hydrometer is the same in all cases whether its
reading is in terms of the U. S. Bureau of Standards Baume' Scale,
the Petroleum Association Baume' Scale, Baum.e' Scale for liquids
heavier than water, or for direct specific gravity. The ideal instru-
ment for all purposes is, of course, that reading directly in specific
gravity. By the use of tables these readings can be converted into the
Baume' reading desired and without any misunderstanding as to which
scale is intended.

Tables for the correction of the specific gravity of oils are to be
found on pages 538 to 542. Tables for the correction of the Baume'
gravity of oils to the basis of 60°F are to be found on pages 529 to 537.
Baume' values are extended to lower than 10° on page 529.

KANSAS CITY TESTING LABORATORY 429

1.00

100 200 300 400

TEMPERATURE-DEGREES FAHRENHEIT

500

600

Fig. 87 — Effect of High Temperatures on the Specific Gravity of Oil.

430 BULLETIN NUMBER SIXTEEN OF

lA, Specific Gravity and Baume' Gravity With the Hydrometer.

The correct method of reading the hydrometer is illustrated in
Fig. 88, page 432. The sample of oil is placed in a clear jar or cylinder
and the hydrometer carefully immersed in it to a point slightly below
that to which it naturally sinks and is then allowed to float freely.
The reading should not be taken until the oil and the hydrometer are
free from air bubbles and are at rest.

In taking the reading the eye should be placed slightly below the
plane of the surface of the oil and then raised slowly until this surface,
seen as an ellipse, becomes a straight line. The point at which this
line cuts the hydrometer scale should be taken as the reading of the
instrument.

In case the oil is not sufficiently clear to allow the reading to be
made as above described, it will be necessary to read from above the
oil surface and to estimate as accurately as possible the point to which
the oil rises on the hydrometer stem. It should be remembered, how-
ever, that the instrument is calibrated to give correct indications when
read at the principal surface of the liquid. It will be necessary, there-
fore, to correct the reading at the upper meniscus by an amount equal
to the height to which the oil creeps up on the stem of the hydrometer.
The amount of this correction may be determined with sufficient ac-
curacy for most purposes by taking a few readings on the upper and
the lower meniscus in a clear oil and noting the differences.

In the case of thick viscous oils after the hydrometer has appar-
ently sunk to a stationary position it is well to determine if it will rise
to the same position when pushed down into the oil.

A specific gravity hydrometer will read too low and a Baume'
hydrometer too high when read at the upper edge of the meniscus.
The correction for meniscus height should therefore be added to a
specific gravity reading and subtracted from a Baume' reading.

The magnitude of the correction will obviously depend upon the
length and value of the subdivisions of the hydrometer scale and must
be determined in each case for the particular hydrometer in question.

Specific gravity and Baume' gravity readings of oils are con-
veniently taken at room temperature and these readings must be con-
verted to the gravity at 60 °F. As a general rule it may be said that
petroleum oil expands with heat so that 0.0004 must be added as a cor-
rection to the specific gravity readings for each degree Fahr. that the
oil is above 60 °F or must be subtracted for each degree Fahr. below
60 °F. On the Baume' scale 0.1° Be' may be subtracted for each degree
Fahr. above 60 °F or added for each degree Fahr. below 60 °F. For
exact temperature corrections for specific gravity, see pages 538 to
542. For exact temperature corrections for Baume' gravity, see pages
529-537. For conversions of Baume' to and from specific gravity, see
pages 523-528.

The followins table is based on the data contained in Bureau of Standards
Technologic Paper No. 77 and upon which are based the tables contained in
Bureau of Standards Circular No. 57. United States Standard Tables for Petroleum
Oils. It differs from Table 3 of Circular No. 57 in that the specific gravity of the
oil la known as 60°/60of Instead of at the temperature at which the voluine
meaeurements are made,

KANSAS CITY TESTING LABORATORY

431

Volume at 60 F Occupied by Unit Volume of Oil at Various

Temperatures.

Observed
Temperature,

Specific Gravity at 60760° F.

Degrees Fahr.

0 60

0 65

0.70

0 75

0.80

0.85

0.90

0.95

1.00

30

32.

0.000971

1.0288

1.0269

1.0251

1.0232

1.0213

1.0194
1.0174
1.0155
1.0136
1.0116

1.0097
1.0078
1.0059
1.0040
1.0020

1.0000
0.9981
0.9962
0.9942
0.9923

0.9903
0.9884
0.9864
0.9845
0.9825

0.9806
0.9786
0.9767
0.9748
0.9728

0.9708
0.9688
0.9669
0.9649
0.9629

0.9610
0.9591
0.9572
0.9552
0.9533

0.9514
0.9495
0.9476
0.9456
0.9437

0.9418

0.00081'

1.0240

1.0224

1.0208

1.0193

1.0177

1.0161
1.0145
1.0129
1.0113
1.0098

1.0082
1.0065
1.0048
1.0032
1.0016

1.0000
0.9984
0.9968
0.9952
0.9936

0.9919
0.9903
0.9887
0.9871
0.9855

0.9839
0.9823
0.9807
0.9790
0.9774

0.9758
0.9741
0.9725
0.9708
0.9692

0.9676
0.9660
0.9643
0.9626
0.9610

0.9594
0.9578
0.9562
0.9545
0.9529

0.9513

0.00069>

1.0208

1.0194

1.0180

1.0167

1.0153

1.0139
1.0125
1.0111
1.0097
1.0084

1.0070
1.0056
1.0042
1.0028
1.0014

1.0000
n.9986
0,9972
0.9958
0.9944

0.9930
0.9916
0.9902
0.9888
0.9875

0.9861
0.9847
0.9833
0.9819
0.9805

0.9791
0.9777
0.9763
0.9749
0.9735

0.9721
0.9707
0.9693
0.9679
0.9665

0.9651
0.9637
0.9623
0.9609
0.9595

0.9581

0.00059'-

1.0178

1.0166

1.0154

1.0142

1.0130

1.0118
1.0106
1.0095
1.0083
1.0071

1.0059
1.0048
1.0036
1.0024
1.0012

1.0000
0.9988
0.9976
0.9964
0.9952

0.9940
0.9928
0.9917
0.9905
0.9893

0.9881
0.9869
0.9857
0.9845
0.9833

0.9821
0.9809
0.9798
0.9786
0.9774

0.9762
0.9750
0.9738
0.9726
0.9714

0.9702
0.9690
0.9678
0.9606
0.9654

0.9642

0.000511

1.0151

1.0141

1.0131

1.0121

1.0111

1.0101
1.0091
1.008U
1.0070
1.0060

1.0050
1.0040
1.00.30
1.0020
1.0010

1.0000
0.9990
0.9980
0.9970
0.9960

0.9950
0.9940
0.9930
0.9920
0.9909

0.9899
0.9889
0.9879
0.9868
0.9856

0.9848
0.9838
0.9828
0.9818
0.9808

0.9797
0.9787
0.9777
0.9767
0.9757

0.9747
0.9736
0.9726
0.9716
0.9706

0.9696

0.000451

1.0135

1.0126

1.0117

I.OIOS

1.0099

1.0090
1.0081
1.0072
1.0063
1.0054

1.0045
1.0036
1.0027
1.0018
1.0009

1.0000
0.99S1
0.9982
0.9973
0.9964

0.9955
0.9946
0.9937
0.9928
0.9919

0.9910
0.9901
0.9892
0.9883
0.9875

0.9805
0.9856
0.9847
0.9838
0.9829

0.9820
0.9811
0.9802
0.9793
0.9784

0.9776
0.9767
0.9758
0.9749
0.9740

0.9731

0.000411

1.0123

1.0115

1.0107

1.0099

1.0091

1.0082
1.0074
1.0066
1.0058
1.0050

1.0041
1.0033
1.01325
1.0017
1.0000

1.0000
0.9992
0.9984
0 9976
0.9967

0.9959
0.9951
0.9943
0.9935
0.9927

0.9918
0.9910
0.9902
0.9893
0.9855

0.9877
0.9869
0.9860
0.9852
0.9844

0.9836
0.9828
0.9820
0.9812
0.9804

0.9796
0.9788
0.9780
0.9772
0.9764

0.0756

0.000381
1.0116

1.0108
1.0100
1.0092
1.0085

1.0077
1.0069
1.0062
1.0054
1.0046

1.0038
1.0031
1.0023
1.0015
1.0008

1.0000
0.9992
0.9985
0.9977
0.9970

0.9962
0.9954
0.9947
0.9939
0.9931

0.9923
0.9915
0.9908
0.9900
0.9893

0.9885
0.9878
0.9870
0.9863
0.9850

0.9848
0.9841
0.'.iS33
0.9826
0.9819

0.9811
0.98(t4
0.9796
0.9788
0.9781

0.9774

0.000371

1.0111

1.0103

1.0095

1.0088

1.0080

1.0073
1 0066

34

36

38

40

42

44

1.0059
1 0051

46

48

50

1.0044
1 0037

52

1 0029

54

1.0021

56

1.0014

58

1.0007

60

1.0000

62

0.9992

64

0.9985

66

0.9978

68

0.9971

70

72

0.9963
0.9956

74

0.9948

76

0.9941

78

0.9934

80

0.9927

82

0.9920

84

0.9912

86

0.9905

88 .

0.9898

90

0.9891

92

0.9884

94

0.9877

96

0.9870

98

0.98li2

100

0.9855

102

0.9848

104

0.9S41

106

(1.9834

108

0.9827

110

:0.9SHt

112

0.9812
0.9SO,'>

114

116

0.9798
0.9791

118

120

0.9784

—

1 These
nologic Pap
been compu
from the values
column headings

approximate volume co-offioion.s art- o>-rlve.l 'ro"' J"' ^ '' i*^,^,,^."; ,
per No. 77, by using the A term only. The t«ble a.s k'),^" ''J''';,'' ,,,',\'I
uted by using both the A and B terms and •ho'•e^_.re OKf. r» »1 KhU
alues that ^vould be obtained by u.sing the .•o-efflelent.M n.s kIx-" In

432

BULLETIN NUMBER SIXTEEN OF

t^ 3£

W:f,

r;-

E--

\^:

Fig. 88 — Method of Reading the Hydrometer.

KANSAS CITY TESTING LABORATORY

433

IB. Specific Gravity "With the Picnometer.

Various types of picnometers may be
used for this purpose, each of which has
special advantages. Some are plain bottles
with capillary openings in a well made
ground glass stopper; others have grad-
uated tubes in the stoppers, vacuum walls
and inserted thermometers. The Sprengel
picnometer is particularly adapted to the
handling of very viscous oils as it prevents
including air bubbles in the instrument.
With any of the various types the perfectly
dry and clean picnometer is weighed at 60 °F
to the nearest 0.0001 gram. It is filled with
distilled water at 60 °F and weighed. It is
then dried completely and filled with the
oil to be tested at 60 °F. The net weight of
the oil divided by the net weight of the dis-
tilled water gives the specific gravity of
the oil. For conversion into degrees Baume'
the formulae given on page 428 or the
tables given on pages 523 to 528 are used.

Fig. 9 0 —
Pi cnometer
W i t h o u t
Therm o -
meter.

Fig. 9 1 —
Picnometer
With Ther-
mometer.

Fig-. 89—
B a u me'
Hydro-
meter

434

BULLETIN NUMBER SIXTEEN OF

IC. Specific Gravity With the Westphal Balance.

"il (Tji '*^^ This is a very convenient instrument

w^here a great variety of petroleum products
are to be tested as it covers any range of
specific gravity and can be used for prac-
tically any type of liquid. Its character is
shown by the figure 92. The oil is put into
the jar and the weights or riders are ad-
justed on the beam until the pointer is in
exact poise. The readings are in specific
gravity based on a v/ater temperature of
60°F at which temperature the instrument
is standardized. The specific gravity may
be converted to Baume' scale with the tables.

Fig. 92 — Westphal Bal-
lance.

ID. Specific Gravity of Semi-Solid Petroleum Materials.

A convenient method of taking
the specific gravity of asphaltic
cement and similar semi-solid
petroleum materials is the follow-
ing. (See Fig. 93.) Roll up a ball
of the asphalt about 1 cm. in di-
ameter, being careful that no water
or air is inclosed. Place this in a
cylinder of cold distilled water
from which the air has been re-
moved by previous boiling. If the
ball of asphalt floats, denatured
alcohol is added until it shows no
tendency to go either up or down
when placed in the middle of the
cylinder. The specific gravity of
the liquid is then taken with the
Westphal balance or with the
hydrometer. If the ball of asphalt
sinks a saturated solution of so-
dium chloride or common salt is
added until the asphalt when placed

11,
(HP

I I

t — I

L__J

Fig. 93 — Specific Gravity of As-
plialtic Cement by Fluid Sus-
pension.

m the center of the cylinder shows no tendency to go either up or down.
The specific gravity is taken with a hydrometer for liquids heavier
than water or with the Westphal balance. It is necessary in per-
forming this test that the bubbles of air which tend to adhere to the
surface of the asphalt be occasionally removed, and that the solution
be thoroughly mixed. All air bubbles and water must be thoroughly
kneaded out of the asphalt. The usual temperature required for the
gravity of this material is 77°F or 25°C.

KANSAS CITY TESTING LABORATORY

435

IE. Specific Gravity of Solid Asphaltic Materials.

A fragment of bituminous material is suspended by means of a
thread from a hook of one pan support of the balance and about one-
half inch above the pan and weighed. This weight is "a." It is then
immersed in water at 25 °C and suspended, the water container not
being allowed to touch the balance and is weighed again. This weight
is "b."

The specific gravity is

a-b

(See Fig. 94.)

The sample of asphaltic surface mixture for this test should be
cut out of the street after the pavement has been rolled and cooled.
This test is a very good measure of the all around quality of the work.
The sample is weighed in the air and in water, the weight in air divided
by the loss of weight in water gives the specific gravity. This times
62.4 gives the weight per cubic foot and times 93.6 gives the weight
per square yard of 2-inch surface.

Fig-. 1)4— Specific Gravity by Displaccmeiil

L

436

BULLETIN NUMBER SIXTEEN OF

IF. Method of Determining the Specific Gravity of Asphaltic Cement.

Specific Oiri^vi-ry af

Fig. 95 — Capsule for Specific Gravity of Asphaltic Cement.

When considerable accuracy is required, the specific gravity of
asphaltic cement may be done in the following manner:

For a receptacle, use a short glass tube as shown in the accom-
panying figure. This may be a half-inch test tube that has been cut
off to a length of about two inches.

Enough of the dry asphalt is put in the tube to fill it about one-
half full. The tube is placed in an air oven at a temperature of from
105° to 150 °C so that the asphalt melts down compactly in the tube.

The record for determining specific gravity is as follows:
Ci = Weight of the tube in air.
Ci =: Weight of the tube in water.

Ai — Weight of the tube -h the asphaltic cement in air.
A:; = Weight of the tube + asphaltic cement in water.

These weighings are cairied out with the water at a temperature
of 77° F. The specific gravity then is equal to:

A,— C,

(A:-C:) — (A,-C.)

KANSAS CITY TESTING LABORATORY

437

2A. THE COLOR OF REFINED PETROLEUM (KEROSENE,

NAPHTHA, GASOLINE).

The Saybolt apparatus consists of two color comparison tubes, one
being arranged for insertion of a standard yellow glass in the bottom,
the other being graduated for different lengths of oil column. (See
Fig. 96.)

The yellow glass discs are supplied with each Chromometer.

Two glasses are used to determine color shades up to and includ-
ing + 15, and only one glass from 4-16 to +25.

An excess of oil is filled into the graduated tube so that in draw-
ing off the excess the color of the oil becomes lighter.

The apparatus should be set at a window having a one-light sash
so that a good light is reflected from the mirror, but not in the direct
rays of the sun, and care should be taken that no colored light is
reflected toward the instrument from surrounding buildings, tanks
or other objects.

Clean the Chromometer before making a new
test, by allowing some of the oil to be tested to
run through the graduated tube.

After using, do not let the instrument stand
with the light reflecting up the tubes.

When not in use, put the color glasses in the
pockets prepared for them on the back of the
upright stand.

For the purpose of most easily determining
color shades, the color of the column of oil when
nearing the color of the standard glass discs, is
lowered shade by shade by use of the pet cock.
Now lower the column of oil one shade more
and if it appears whiter than the standard glass
disc, the color of the oil is recorded one shade
above this last whiter point.

It is evident that no oils are to be compared
with one disc unless they positively show whiter
at 10 4/8 inches with two discs.

Moreover, a full tube (20 inches) of white oil
that shows whiter than one (1) disc must rate
over +25.

ONE DISC

Inches of Oil

in Tube Color Shades

Fig^. 96 — Saybolt
Chromometer.

20

+ 25

18

+ 24

16

+ 23

14

+ 22

12

+ 21

Water

10 6/8

+ 20

white

9 4/8

+ 19

8 2/8

+ 18

7 2/8

+ 17

6 2/8

+ 16 J

438

BULLETIN NUMBER SIXTEEN OF

TWO

DISCS

Inches of Oil

in Tube (

Color Shades

10 4/8

+ 15]

9 6/8

+ 14

9

+ 13

8 2/8

4-12

7 6/8

+ 11

C!t'

. 7 2/8

+ 10

(■ ,

6 6/8

+ 9

6 4/8

+ 8

6 2/8

+ 7

6

+ 6

5 6/8

+ 5j

white

5 4/8

+ 4

5 2/8

+ 3

0

+ 2

•

4 6/8

+ 1

4 4/8

0

4 2/8

— 1

4

— 2

. Standard

3 6/8

— 3

white

3 5/8

— 4

3 4/8

— 5

3 3/8

— 6

3 2/8

— 7

3 1/8

— 8

3

— 9

2-B. Color by Lovibond Tintometer.

The Lovibond color units and divisions are shown below, together
with the color, series and number of each glass. These slides are used
for determining the color of the refined products — gasoline, naphtha
and kerosene.

Lovibond color units with specifications for the slides

Slide Color Series Number

Water white Yellow 510 2.3

Red 200 1.6

1 to 12.0 Amber 500 0.1 to 12 0

If the oil is darker than the water white glass, slides are added to
the slot containing the standard water white until the color of the oil
is matched. When the .2 slide is added in this manner, the color is
reported as W.W. — 0.2 the minus sign indicating that the oil is darker
than the standard water white. If the color of the oil is lighter than
that of the water white glass, additional slides are placed in the slots
in front of the oil and should the color be matched in this manner
with, say the .5 slide and the .2 slide, the color is reported W.W. + 0.70.

The color equivalent of water white, the standard color for gaso-
line and naphtha, has been defined as the equivalent of a column
404.6 mm. long of a 0.000279f acidulated solution of potassium
chromate.

The most practical adaptation of the tintometer for the color of
lubricating oils is in the Union Colorimeter covering the National
Petroleum Association standards as shown in paragraph 2-E.

Fig 97 — JL,ovibond
Tintometer.

KANSAS CITY TESTING LABORATORY

439

2-C. Color With Potassium Bichromate Solutions.

In the absence of an instrument, standard acidulated solutions
may be prepai-ed to correspond with the solutions indicated in the
following table. Each of these solutions when placed in four-ounce
sample bottles and marked with the equivalent Saybolt value may be
used to match samples. Solutions prepared in four-ounce bottles as
indicated below are much more convenient and more easily read than
in the case of using the Saybolt Chromometer.

Milligrams

of

Milligrams of

potassium bichi

'omate

potassium bichromate

Saybolt

per

lOOcc of 1%

Saybolt

per

lOOcc of 1%

Color

sulphuric acid s

olution

Color

sulphuric acid solution

25

...0.20

9. ...

....1.95

24

0.30

8

...2.05

23

0.37

7

....2.17

22

0.45

6

....2.30

21...

0.55

5

....2.40

20

0.65

19...

0.75

4

....2.55

18.-

0.85

3

....2.65

17

0.95

2

....2.75

16....

1.10

1

....2.85

15...

1.25

0

...3.00

14...

1.35

13...

1.50

12...

1.65

11...

1.75

10...

1.85

^ —

'ca'

Kig. 98 — Color Tubt

440 BULLETIN NUMBER SIXTEEN OF

2-D. Color of Oil by Iodine Method.

This method may be applied to all dark colored petroleum prod-
ucts. In determining the color by the iodine method a solution is
made containing in one liter of very pure distilled water, ten grams
of iodine and twenty grams of potassium iodide. This is kept in a
glass stoppered bottle. The apparatus necessary is that indicated
in Fig. 98 which may be a set of carbon color tubes or two tubes
such as are required in the determination of manganese in steel.
For crude oil, road oil, fuel oil and other black oils a dilution of
1/1000 in colorless benzol is made by diluting Ice to lOcc of benzol
and then Ice of this to lOOcc with benzol. This is thoroughly
mixed in one of the glass stoppered color tubes. 1 cc of the
standard iodine solution is put into the large color tube which holds
250cc. It is diluted with distilled water until its color matches that
of the oil under test. The color is calculated as follows: I = milli-
grams of iodine in lOOcc of water in the tube containing the diluted
iodine.

d = The number of cc of benzol to Ice of oil.
Color = I (d + 1).

For gas oil, lubricating oils and yellow oils, a dilution of 1/100
with benzol is sufficient. For gasoline, naphtha, kerosene and
illuminating oils there is no dilution with benzol, the comparison
being made directly. The union colorimeter may be used for com-
parison purposes.

The descriptive terms applied in the color of crude oil are black,
brownish black, blackish brown, brown, reddish brown, green, greenish
brown, brownish green and bluish green. The kerosene is spoken of
as being water white, superfine white, prime white, standard white,
prime light straw, light straw, and straw. Other colors are designated
by yellow, dark yellow, reddish yellow, brownish yellow, yellowish
brown, brown red, blood red, and yellowish red.

KANSAS CITY TESTING LABORATORY

441

2-E. Color of Lubrication Oils.
(Union Colorimeter)

The color of lubricating oils is determined by placing a 4-ounce
bottle of the oil under examination in the right-hand circular com-
partment of the instrument. In the compartment behind the slot
place a 4-ounce bottle of water white gasoline or distilled water.
Then place one of the standard glasses in the slot and close the slide.
The instrument should be directed toward a window so that the
observer can compare the color of the oil with the standard glas?

Fig. 99 — Union Colorimeter.

In the case of cylinder stocks (filtered) fifteen cubic centimeters
are mixed with 85cc of water white gasoline or benzol and the color
is determined as in the case of lighter lubricating oils, (for darK
cylinder stocks use method 2D.)

The following are the NATIONAL PETROLEUM ASSOCIATION
STANDARDS for Engine, Machinery and Cylinder Uils:

Tagliabue-Robinson

Colorimeter

Equivalent

A Cylinder— Extra Light Filtered.

D Cylinder— Light Filtered.

E Cylinder— Medium Filtered

G Lily white

H Cream white ....

I Extra Pale

J Extra lemon pale

K Lemon pale

L Extra orange pale

M Orange pale..

N Pale

O Light red ....

P Dark red

Q Claret red . . .

N. P. A. No. 1. . .
N. P. A. No. l}-i
N. P. A. No. 2

N. P. A. No. 3

N. P. A. No. 4

N. P

N. P. A. No. 5
N. P. A. No. 6

20 3^
IVA
12M
10

9

SH

2

1^

442

BULLETIN NUMBER SIXTEEN OF

Equivalents

of the

above colors in

Lovibond

slides

and in iodine

colors expressed

in mill

igrams of iodint

; per lOOcc of solution are as

follows :

N. P. A.

Lovibond

•

Standard

Red

Yellow

Blue

lodimetric

A

10.2

29.0

0

50 (diluted)

D

21.0

31.0

0

100 (diluted)

E

89.0

56.0

0

500 (diluted^

G

0.12

2.4

0

2.8

H

0.6

8.0

0

5.7

I

2.5

26.0

0

10.8

J

4.6

27.0

0

20.1

K

6.9

32.0

0

32.1

L

7.8

39.0

0

38.4

M

14.0

50.0

0.55

70.7

N

21.0

56.0

0.55

112.0

0

35.0

93.0

0

195.0

P

60.0

60.0

0.55

300.0

Q

60.0

106.0

1.8

460.0

3. Odor of Oil.

The odor of oil may be spoken of as sweet, ethereal, aromatic,
tarry, fatty, creosotic, acid, sour, sulphurous, sulphuretted hydrogen,
pyridine and pungent.

The sour or cracked odor is characteristic of benzine or incom-
pletely refined gasoline. The aromatic odor or odor of benzene
(benzol) is characteristic of high temperature cracking or aluminum
chloride refining. Sweet ethereal odors are characteristic of naphthas
made from low sulphur paraffin base crude oils. Tarry and creosotic
odors are characteristic of cracked residues. Fatty odors are often
noticed in illuminating oils. Acid and sulphurous odors are found in
sludge oils from agitator treatment. Sulphuretted hydrogen and
pungent odors come from high sulphur crude oils, such as Mexican.
Pyridine odors come from oils containing a large amount of nitrogen
(California) and from shale oils.

Odors may be intensified in some cases by mild treatment of the
oil with acid or with caustic.

4. Transparency of Oil.

Transparency may be expressed by the thickness of oil in centi-
meters through which the filament of a fifty watt Mazda electric
lamp is visible. It may be also noted whether the oil is fluorescent
and the character of the fluorescence, whether bluish, greenish or yel-
lowish by reflected light; also whether any turbidity is of a smoky,
granular or flocculent character.

Transparency is usually closely related to color. Transparency is
often affected by the blending of oils, the mixing of light crude with
heavy crude oil or of paraffin base with asphaltic base crude oil often
produces a turbidity.

KANSAS CITY TESTING LABORATORY 443

5-A. Viscosity of Liquid Petroleum Products.

(SAYBOLT UNIVERSAL.) (A. S.T. M.)

The apparatus is shown in figure 100.

To make the test, heat the iaath to the necessary temperature
and clean out the standard oil tube with the plunger, using some of
he oil to be tested. Place the cork stopper into the lower end of the
air chamber at the bottom of the standard oil tube. The stopper
should be sufficiently inserted to prevent the escape of air, but should
not touch the small outlet tube of the standard oil tube. Heat the
oil to be tested, outside the viscosimeter, to slightly below the tem-
perature at which the viscosity is to be determined and pour it into
the standard oil tube until it ceases to overflow into the overflow cup.

By means of the oil tube thermometer keep the oil in the standard
oil tube well stirred and also stir well the oil in the bath. It is ex-
tremely important that the tem.perature of the oil in the bath be
maintained constant during the entii'e time consumed in making the
test. When the temperature of the oil in the bath and in the stand-
ard oil tube are constant and the oil in the standard oil tube is at
the desired temperature, withdraw the oil tube thermometer; quickly
remove the surplus oil from the overflow cup by means of a pipette
so that the level of the oil in the overflow cup is below the level of
the oil in the tube proper; place the 60-cc. flask in position so that
the oil from the outlet tube will flow into the flask without making
bubbles; snap the cork from its position, and at the same instant
start the stop watch. Stir the liquid in the bath during the run and
carefully maintain it at the previously determined proper temperature.
Stop the watch when the bottom of the meniscus of the oil reaches
the mark on the neck of the receiving flask.

The time in seconds for the delivery of 60-cc. of oil is the Saybolt
viscosity of the oil at the temperature at which the test was made. ^

"Viscosity is commonlv determined at 100°F, 150°F or 210°F.
The bath is 'held constant within .25°F at such a temperature as will
maintain the desired temperature in the standard oil tube. Oil or
water is used as the bath liquid. The oil for the bath should be a
pale engine oil of at least 350°F flash point (open cup). Viscosity
determinations should be made in a room free from draughts and
from rapid changes in temperature. All oil introduced into the stand-
ard oil tube, either for cleaning or for test, shall first be passed

through the strainer. , , . , . i. j u tu^

This is the test for the viscosity of lubricants adopted by the
American Society for Testing Materials. .■ 1 , .f

The Saybolt standard universal viscosimeter is made entirely or
rretal. The standard oil tube is fitted at the toP with an ovcrflovv
cap and the tube is surrounded by a bath. At the bottom of the
standard oil tube is a small outlet tube through which the ml to bo
tested flows into a receiving flask, whose capacity to a ma. k on is
neck is 60 ( + 0.15) cc. The lower end of the outlet tube >« t^n^-'os '»
by a larger tube, which when stoppered by a ^'f ^ ^^^s as a c osed a
chamber and prevents the flow of oil through the cmtlet tube u
the cork is removed and the test started. A 1«."P^:; J ^ '\^, "f, h
to the lower end of the cork as an aid to its rapul removal ^u b'^U
is provided with two stirring paddles and operated by two turn taDie

444

BULLETIN NUMBER SIXTEEN OF

SccHonal View

of

Standard Oil Tube

A

Oil Tube Thermometer.

K Stirring Paddles.

B

Bath Thermometer.

L Bath Vessel.

C

Electric Heater.

M Electric Heater Receptacle.

D

Turntable Cover

N Outlet Cork Stopper.

E

Oyer Flo IV Cup.

P Gas Burner

F

Turntable Handles.

Q Strainer.

G

Steam Inlet or Outlet

R Receiving F/ask.

H

Steam U-Tube.

S Base Block.

J

Standard Oil Tube.

T Tube Cleaning Plunger.

Fig. 100 — Saybolt Universal Viscosimeter.

KANSAS CITY TESTING LABORATORY 445

handles. The temperatures in the standard oil tube and in the bath
are shown by thermometers. The bath may be heated by a gas ring
burner, steam U-tube, or electric heater. The standard oil tube is
cleaned by means of a tube cleaning plunger, and all oil entering
the standard oil tube shall be strained through a 30-mesh brass wire
strainer. A stop watch is used for taking the time of flow of the oil
and a pipette, fitted with a rubber suction bulb, is used for draining
the overflow cup of the standard oil tube.

The standard oil tube should be standardized by the United
States Bureau of Standards, Washington, and conforms to the follow-
ing dimensions:

Minimum, Normal, Maximum,
Dimensions Cm. Cm. Cm.

Inside diameter of outlet tube 0.1750 0.1765 0.1780

Length of outlet tube 1.215 1.225 1.235

Height of overflow rim above bottom of

outlet tube - 12.40 12.50 12.60

Diameter of container of standard oil tube 2.955 2.975 2.995

Outer diameter of outlet tube at lower end 0.28 0.30 0.32

The approximate factors for conversion of readings of the Say-
bolt Universal to other instruments are as follows: (for the usual
range of use) :

To Saybolt Furol 101 *« -113

To MacMichael 50 .65

To Saybolt "A" 0.5 1.0

To Saybolt "C" - 0.46 .72

To Engler 0.027 .035

To Tagliabue OfS .51

. To Penn. R. R. Pipet 0.30 .94

To Scott 0.13 -

To Redwood 0°^ 'T^

To Magruder Plunger 1-^^ f-^

To Ostwald 1-^0 i.JU

These values are not exact as they vary greatly ^ith the actual
viscosity readings. For exact conversion to Engler and Redwood val-
ues, see the following pages.

70°F may be used for light oils, gas oils, "straw" oils, engine oils,
dynamo oils, auto oils, cottonseed oils and the like.

100°F may be used for Engine oils, machine oils and occasionally
cylinder oils.

210°F may be used for cylinder oils, road oils, other heavy oils
—^ and asphaltic fluxes.

■ 338°F may be used for asphalt, fluxes, paraffin wax and residues,

ft Other viscosimeters in use are ,the Engler, Tagliabue. ^Sc-ott. Red-

^■wood, Penn.
^» tens, Stormer,

bey, Cockrell,

chauer, Magruder.

K

I

446

BULLETIN NUMBER SIXTEEN OF

Fig. 101 — Engler
Viscosimeter.

The Engler viscosimeter is used most extensively
in Germany and its dimensions are as follows:

Width of jet 4.5 mm

Inside diameter of the inside vessel for oil.. ..106 mm

Height of vessel below overflow 25 mm

Length of the oil jet 20 mm

Inside diameter of the oil jet upper end 2.9 mm

Inside diameter of the oil jet lower end 2.8 mm

Length of jet projecting from lower part of

outer vessel 3.0 mm

The quotient of the time of outflow of 200 cc. of
oil divided by the time of outflow of 200 cc. of water
is taken as a measure of the viscosity or is the so-
called Engler degree.* ("Specific Viscosity.")

The Redwood viscosity
is used extensively in
England and its value may
be calculated from the
Engler or the Saybolt.

*Tables for the inter-
change of readings on the
Saybolt, Engler and Red-
wood Viscosimeters are on
the following pages.

Fig. 102 — Redwood Viscosimeter.

KANSAS CITY TESTING LABORATORY

447

Bureau of Standards — Viscosimeter Comparisons.

Calculated Time Ratios from Equations:

3.74 for Engler No. 2204 U (See

Kinematic Viscosity = . 00147 t — Tech. Paper No. 112, p. 14, 1919)

t

Kinematic Viscosity=. 00220 t

1.80 for Standard Saybolt Universal

(See Tech. Paper 112, p. 19,1919)

t

Kinematic Viscosity = . 00260 t

1.715 for Redwood (See W. F. Higgins

Collected Researches, National.

t

Physical Lab., Vol. 11, p. 18,
p. 25, 1919.

1914: quoted in Tech. Paper 112,

Time Engler
Second

58

60

62

64

66

68

70

75

80

85

90

95
100
110
120
130
140
150
160
180
200
225
250
275
300
325
350
375
400
500
600

Time Engler
Time,
Saybolt
1.72
1.71
1.70
1.69
1.68
1.68

67
65
63
62
61

,60
59

,58
56

,56
55
54

1.53
1.52
1.52
1.51

51
51
51
51
50
50
50
1.50
1 50*

Time Engler
Time,
Redwood
1.93
1.93
1.92
1.91
1.91
1.90
1.90
1.88
1.87
1.86
1.86
1.85
1.84

83
82
81
81
80
80

1.80
1.79
1.79
1.78
1.78
1.78
1.78
1.78

77
77
77
77*

Multi
Saybolt
bers or

Engler
Degrees.
1.15
1.20
1.25
1.30
35
40
45
50
60
70
80
90

plying factors to reduce
times to Engler num-
Redwood times.

Fe iwood
Saybolt Time. Time.

Engler Degrees. Engler Degrees.

1

1

1

1

1

1

1

1

2.00

2.10

20
30
40
50
60
70
80
90
00

3.50
4.00
4.50
5.00
6.00
7.00
8.00
9.00

29.9
30.1
30.3
30.5
30.7
30.9
31.1
31.3
31.5
31.7
31.9
32.1
32.3
32.5
32.6
32.8
32.9
33.0
33.1
33.2
33.3
33.4
33.5
33.6
33.7
33.9
33.9
34.0
34.1
34 1
34.2,*

26.5
26.7
26.8
26.9
27.0
27.1
27.2
27.3
27.4
27.5
27.6
27.7

27 9
28.0
28.1
28.2
28.2
28.3
28.3
28.4
28.4
28.6
28.5
28.6
28.7
28.8
28.8
28.9

28 9
28.0
2i» . 0*

*This value holds good for all higher viscosities. (Bureau of
Standards.)

448

BULLETIN NUMBER SIXTEEN OF

Viscosimeter Comparisons.

Multiplying factors to reduce
Engler degrees to Saybolt or
Redwood times.

Redwood to Saybolt and
Engler.

Engler

Engler

Redwood

Redwood

Saybolt Time

Degrees.

Saybolt

Degrees.

Times.

Time.

Redwood

Redwood

Time.

Saybolt Time.

Saybolt Time.

Seconds.

Time.

Time.

34

.0335

.890

30

1.12

.0377

36

.0332

.886

32

1.13

.0375

38

.0330

.884

34

1.13

.0372

40

.0328

.882

36

1.14

.0370

42

.0326

.879

38

1.14

.0369

44

.0324

.877

40

1.14

.0368

46

.0322

.875

42

1.15

.0366

4S

.0319

.873

44

1.15

.0365

50

.0317

.871

46

1.15

.0363

55

.0315

.869

48

1.15

.0362

60

.0313

.866

50

1.16

.0361

65

.0312

.864

55

1.16

.0359

70

.0310

.861

60

1.16

.0357

75

.0308

.859

65

1.16

.0355

80

.0307

.858

70

1.17

.0354

85

.0305

.857

75

1.17

.0353

90

.0304

.856

80

1.17

.0352

95

.0303

.855

85

1.17

.0351

100

.0302

.854

90

1.17

.0350

110

.0301

.853

95

1.17

.0350

120

.0300

.852

100

1.17

.0350

130

.0299

.851

110

1.18

.0349

140

.0299

.850

120

1.18

.0348

160

.0298

.849

130

1.18

.0347

180

.0297

.848

140

1.18

.0347

200

.0296

.848

150

1.18

.0347

225

.0295

.848

160

1.18

.0347

250

.0294

.847

180

1.18

.0347

300

.0293

.847

200

1.18

.0347

350

.0293

.847

225

1.18

.0346

400

.0292*

.846*

250

1.18*

.0345*

*This

value hold

s good for a

11 higher

viscosities.

(Bureau of

Standards.)

KANSAS CITY TESTING LABORATORY

449

5-B. VISCOSITY OF FUEL OILS AND ROAD OILS.

Fig-. 103 — Furol Viscosity Tube.
(Cameragraph Co. of Kansas City.)

Viscosity is determined by-
means of the Saybolt Furol
Viscosimeter.

The apparatus and method
of operation is the same as
for the Standard Saybolt
Universal Viscosimeter, all
dimensions being the same
except the diameter of the
outlet tube which shall be as
follows:

Inside diameter of outlet
tube, cm. —

Minimum Normal Maximum
0.313 0.315 0.317

Outside diameter at lower
end, cm. —

Minimum Normal Maximum
0.40 0.43 0.46

Viscosity may be deter-
mined at 104°F (40°C), 122°F
(50°C) or 70°F and is ex-
pressed as — seconds, Saybolt
Furol, being the time in sec-
onds for the delivery of 60
cc. of oil.

Oil showing a time of less than 25 seconds, Saybolt Furol, at
122°F, should be tested on the Saybolt Universal at 122°F. Oil show-
ing a time of less than 32 seconds Saybolt Universal, at 122°F should
be measured in the Saybolt Universal at 100°F (37°8C).

450

BULLETIN NUMBER SIXTEEN OF

5-C. METHOO FOR DETERiMINING THE VISCOSITY OF
KEROSENE AND GASOLINE.

The apparatus used for this test is essentially that
described on pages 55, 56 and 57 of Holde's "Exami-
nation of Hydrocarbon Oils." A diagram of the ap-
paratus is shown in figure 104. The instrument is
known as the Ubbelohde viscosimeter.

The dimensions are as follows:

Normal
Instrument

Fig. 104 — Ubbe-
lohde Viscosi-
meter.

0.125 centimeters
0.125

Inner diameter of outlet tube at top

Inner diam.eter of outlet tube at bottom

Outside diam. of outlet tube at bottom, di 1.0 "

Length of outlet tube, 1 3.0 "

Diameter of container, D 10.5 "

Outside diameter of overflow pipe, d;

Initial head on bottom of outlet tube, hi.... 4.6 "

Average head, h (calculated) 3.992 "

Water rate 200 seconds

Capacity of container 132 cubic centimeters

The apparatus is placed in a horizontal position by means of the
plummet, the outflow tube is examined by looking through from the
top with a sheet of white paper underneath to determine if there
are any obstructions or dirt. If dirty, the outflow tube is cleaned by
drawing a silk thread back and forth through it. Water or cracked
ice, depending upon the temperature desired, is placed in the outer
vessel, the plug is put in place and an excess of kerosene or gasoline
introduced. The excess runs out of the overflow pipe. The plug is
loosened sufficiently to allow just a drop of liquid to pass out to the
jet. When the proper temperature has been maintained for 15 min-
utes the plug is withdrawn and the time required to fill the 100 cc.
flask is determined with the stop watch. The time divided by the
time required for water gives the viscosity. For example, if the time
of outflow of kerosene is 320 seconds and the water is 200 seconds,
the viscosity is 1.6.

KANSAS CITY TESTING LABOR ATORY

451

5-D. VISCOSITY WITH THE MacMICHAEL VISCOSIMETER.

In the MacMichael Viscosimeter a disk is suspended in a cup of
fluid. The force exerted by the rotation of the fluid on the plunger
is measured.

The cup is oil jacketed, being formed of two pieces of heavy spun
brass. Within the oil jacket is immersed an electric heating coil. This
coil draws current from the same line as the motor, only one con-
nection being necessary. The fluid to be tested is heated in place, no
other heating device being required. Stirring is effected by a slight
vertical movement of the plunger. For low temperature work, the
fluid and the adjacent parts are chilled in an ice bath or brine solu-
tion.

The speed control is of the phonograph type. The motor is
adapted for ordinary lighting circuits. Variations in voltage do not
affect the accuracy of the determinations.

In operating, the cup is filled to the mark on the side with the
material to be tested. This requires about 100 cc. The temperature is
raised or lowered by means of the heating coils. The deflection noted
on the dial is the viscosity of the fluid.

The operation is very rapid, so that the drop in temperature on
ordinary work is entirely negligible. For extreme accuracy, the
temperature may be raised slightly above the desired point, and an
allowance made for the drop up to the moment of reading. This will
seldom be found necessary in actual practice. The readings are in
degrees of angular deflection, 300° to the circle, designated as M.
The practical working unit is 1/1000 of the absolute unit. As water
at 20 °C or 68 °F has exactly 1/100 of the absolute unit of viscosity,
water at this temperature reads 10°M. Thus by shifting the decimal
point practical units, absolute units and specific viscosity may be ob-
tained at one reading. Readings are taken directly from the dial, no
intermediate calculations being required.

Fig:. 105 — MacMichael
Viscosimeter.

452

BULLETIN NUMBER SIXTEEN OF

5-E. FLOAT TEST (VISCOSITY) OF PETROLEUM RESIDUES.

The special apparatus for the float test consists of an aluminum
saucer having a diameter of 8.89 centimeters and a depth of 2.54 cm.
and a radius of curvatui'e of 5.16 cm. At the bottom there is an
opening into which a collar may be screwed. This conical collar is
2.22 cm. long, is 0.95 cm. in diameter at the small end, 1.27 cm. in
diameter at the large end and has a wall 0.13 cm. thick. This ap-
paratus and method of operating is shown in Fig. 107.

In making the test the brass conical collar is placed with the
small end down on a brass plate which has been previously amalgam-
ated with mercuric chloride. A small quantity of the material to be
tested is carefully heated until quite fluid. It is then poured into
the collar until slightly moi'e than level with the top. The collar and
plate are placed in ice water until rigid. The excess of material pro-
truding from the collar is cut off with a warm knife. A pan of
water is now heated to the desired temperature. The material should
be kept in the ice water at least 15 minutes at a temperature of 5°C.
The collar with the material is quickly screwed into the aluminum
float which is immediately placed in the warm bath. As the plug of
material becomes warm and fluid it is forced upward and out of the
collar until the water gains entrance to the saucer and causes it to
sink. The time in seconds between placing the apparatus on the
water and when the water breaks through the residue is determined
with the stop watch and is recorded as the measure of the consistency
of the material. Unless otherwise specified, the float test is made
at 50 °C, but it would necessarily be higher with the more viscous
materials.

D

Fig. 107 — Float Test Apparatus.

KANSAS CITY TESTING LABORATORY

453

5-F. ZERO VISCOSITY FOR SEMI-SOLID PETROLEUM

PRODUCTS.

The apparatus used is a cylinder shown in the
sketch and may be constructed from ordinary iron
pipe. The cylinder is 4 cm. in diameter and 13
cm. long with an opening centrally located in the
bottom 1 cm. in diameter and with lips 2 mm.
thick. A tube 150 cm. long is screwed into the
cap on the top.

In making the test the melted asphalt is poured
into the cylinder with the cap off of the top and
the 1 cm. opening on the flat surface. It is cooled
and topped with more asphalt, the cap is put on
with 150 cm. tube and the cylinder is packed in
pulverized ice and supported horizontally so that
the bottom rests on a circular ring at least 1 cm.
high which keeps the ice away from the orifice.
The tube when ice cold is filled with mercury and
after some of the asphalt has protruded from the
orifice it is trimmed off flush with the outer edge.
The apparatus is now supported vertically at the
temperature of 0°C for 5 hours. The weight of
asphalt or bituminous material protruding from
the orifice after this time expressed in decigrams
is the zero viscosity.

- 0 2 CM Thick

Fig. 106 — Zero Viscosi-

meter. ,

rr-

5-G. VISCOSITY OF PETROLATUM.

Obtain a sample that exactly represents batch under inspection.
Melt slowly and heat to a temperature 15° F above its probable melt-
ing point. Chill the thermometer bulb to 40° F, wipe dry, thrust into
melted petrolatum, remove immediately, hold vertically until surface
dulls, and suspend at room temperature for 60 minutes.

Suspend thermometer in the test tube with lowest end of bulb
15 mm. from the bottom. While the glass ring above the bulb is
expected to prevent rubbing of coating of petrolatum, care should
be exercised in inserting thermometer into the test tube.

Surround this assembly with water bath at 60° F. Raise tempera-
ture of bath 2°F per minute to 100° F then 1°F to end of test. Read
thermometer when first drop leaves it and record. An average or
three such tests, if the variation does not exceed 2 F, may be given
as the melting point of the sample under test. If a Pi-eater va. a-
tion, take the average of five determinations, (from page ,5.).), i.»^i
Proc. of A. S. T. M.)

454

BULLETIN NUMBER SIXTEEN OF

6-A. MELTING POINT OF BITUMINOUS MATERIALS.
(SOFTENING POINT.) (Ring and Ball Method.)

The apparatus consists of a brass ring %-inch in diameter, '/4-
inch deep, 3/32-inch wall suspended 1 inch above the bottom of the
beaker; a steel ball %-inch in diameter weighing between 3.45 and
3.50 grams, a standardized thermometer and a 600 cc. glass beaker.

Carefully melt the sample and fill the ring with the material to
be tested, removing any excess. Place the ball in the center of the
ring and suspend in the beaker containing 400 cc. of water at a tem-
perature of 5°C. Set the thermometer bulb within Vz inch of the
sample and at the same level. Apply heat uniformly, preferably
with a 200 watt electric hot plate over the bottom of the beaker suffi-
ciently to raise the temperature of the water 5°C per minute. Record
the temperature at starting the test and every minute thereafter until
the test is completed. The softening point is the temperature at which
the specimen touches the bottom of the beaker. For temperatures
above 99 °C glycerin should be used instead of water. Tests should
check within 3°C,

m -^1 '^:

Fig. 108— Melting Point, Ring and Ball Method.

KANSAS CITY TESTING LABORATORY

455

6-B. MELTING POINT OF BITUMINOUS MATERIALS.

(Cube Method.)

The bituminous matei'ial is carefully melted and poured into the
V^-inch brass cubical mold which has been amalgamated with mercury
and which is set on an amalgamated brass plate. The hot material
should slightly more than fill the mold and when cold the excess may
be cut off with a hot spatula. The cube is removed from the mold
and fastened upon the lower arm of a No. 12 wire B. & S. gauge
bent at right angles and suspended beside a thermometer in a tall
covered beaker of 400 cc. capacity.

This tall form beaker is set in an 800 cc. low form beaker which
is arranged for the application of heat. The wire is passed through
the center of the two opposite faces of the cube which is suspended
with its base one inch above the bottom of the inside beaker. The
inner beaker cover has two openings, one for the wire and one for
the thermometer. The wire is held in place by a cork in the cover.
The bulb of the thermometer is level with the cube and at an equal
distance from the sides of the beaker. Heat is applied to the liquid
in the outer vessel in such manner that the thermometer registers an
increase of 5°C per minute and the temperature at which the bitumen
touches a piece of paper placed in the bottom of the beaker is taken
as the melting point. Determinations should check withm 2°. The
temperature at the beginning of the test should be approximately
room temperature.

4f. ^

6 — - c

<^

a --

Fig. 109— Melting Point, Cube Method.

456

BULLETIN NUMBER SIXTEEN OF

6-C. MELTING POINT OF BITUMINOUS MATERIALS.
(General Electric Method.)

Mold one gram of the bituminous material so that it completely
and uniformly covers the short bulb of a thermometer graduated
to at least 500" F. Fit this thermometer with a cork into a %x6-inch
test tube with a side tubulation or air vent so that the bulb of the
thermometer is %-inch from the bottom of the tube. Support the
thermometer and tube with a clamp and immerse the tube to a depth
of four inches in 400 cc. of commercial concentrated sulphuric acid
in a 600 cc. beaker. The beaker of sulphuric acid is heated by direct
contact with an electric hot plate of 220 watt capacity and 4V^ inches
in diameter.

The melting point is taken from readings of the thermometer
when the bituminous material flows sufficiently that a tear strikes
the bottom of the tube.

THCfiMOMCTCR

SULPtloRiC flCID-

Fig. 110 — Melting Point, General Electric Method.

Comparison of General Electric and Ball and Ring methods for
melting point:

B.&R.

G. E.

246°F

270°F

220

240

185

200

140

150

KANSAS CITY TESTING LABORATORY

457

6-D. WAX MELTING POINT. (SO CALLED "ENGLISH" METHOD.)

The apparatus is shown in figures 111 and 112.

An average sample of the wax to be tested is melted in a suit-
able container in a water bath whose temperature is not more than
35 °F above the approximate melting point of the wax sample. Direct
heat, such as a flame or hot plate, must not be used and the wax
sample must not be held in the melted condition any longer than
necessary.

The test tube is filled with melted wax to a height of 2 in. The
test tube cox'k, carrying the stirrer and the melting point thermo-
meter, with the 3% -in. immersion line at the under surface of the
cork, is inserted into the test tube for a distance of %-in. The lower
end of the thermometer bulb is then %-in. from the bottom of the
test tube.

The air bath being in its proper position in the water bath, the
latter is filled to within Vz in. of the top with water at a tempera-
ture 15 to 20 °F below the approximate melting point of the wax
sample.

Fig-. Ill — :Melting Point of Wax.

The test tube containing the melted wax, with wax stirrer and
thermometer in place is inserted into the air bath ma central ver-
tical position so that the bottom of the test tube is V2 in. fiom the
bottom of the air bath. The temperature of the water bath is ad-
justed by stirring if necessary, so that it is lower than the tempo, a^
ture of the wax sample by not more than 30 F ^n^ not less than
25 °F, when the wax sample has cooled to a temperature 10 F above
its approximate melting point. , . , . („,. > ...ijucf

When these conditions have been obtamed, temporalm ad u. -
ment and stirring of the water bath are discontmued^ the % h'rinff
stirred continuously during the »3"^^>"/l^»; ^ ^he^ test the stn.mg
loop being moved up and down throughout the ^"^ ' ^ f "*f ^ ,^^J if,

and will then again fall gradually.

458

BULLETIN NUMBER SIXTEEN OF

The melting point thermometer reading, estimated to .1°F, is
observed and recorded every 30 seconds, for at least three minutes
after the temperature again begins to fall after remaining almost
constant. The record of temperature readings is then inspected and
the average of the first four readings that lie w^ithin a range of
.2°F is the uncorrected melting point.

The A. S. T. M. wax test thermometer should be used (approx.
37 cm. long 3 in. immersion).

The titer test apparatus shown in Fig. 112 gives practically
the same results as the above and is very simple and inexpensive.

THCfi/^OM€ T€R

V

TCST TUBC

MCLTED wflA-

^^|&^

MCLTING POINT Or PARnmN WAX

Fig. 112 — Melting- Point of Wax (Titer Method).

KANSAS CITY TESTING LABORATORY 459

Mr.LT/f^fG Point CoRver^s

cW PA^FF/H

2345676910
TIME /yV M/NUTE6

Fig. 113 — Freezing Point Curve of Wax.

460

BULLETIN NUMBER SIXTEEN OF

7-A. CLOUD, POUR AND COLD TESTS.

The apparatus is set up as shown in figure
114. The thermometer is per A. S. T. M. spe-
cification, 22.2 cm. long scaled for 4^/4 -in. im-
mersion, —36° to +120°F.

The oil to be tested is brought to a tempera-
ture at least 25 °F above the approximate cloud
point. Moisture, if present, is removed by fil-
tering while warm and thin.

The clear oil is poured into the cold test .I'ar,
a, to a height of not less than 1 nor more than

IM in.

The cold test jar is tightly closed
by the cork, c, carrying the cold
test thermometer, b, in a vertical
position in the center of the jar
with the thermometer bulb resting
on the bottom of the jar.

The disk, e, is placed in the bot-
tom of the jacket, d, and the cold
test jar with the ring gasket, f,
1 in. above the bottom shall be in-
serted into the jacket. The disk,
jacket and inside of jacket shall be
clean and dry.

The temperature of the cooling
bath, g, shall be adjusted so that
it is below the cloud point of
the oil by not less than 15° nor
more than 30 °F and this temperature is maintained throughout the
test. The jacket, containing the cold test jar, is supported firmly
in a vertical position in the cooling bath so that not more than 1 in.
of the jacket projects out of the cooling medium.

At each cold test thermometer reading which is a multiple of
2°F the cold test jar is removed from the jacket, quickly but without
disturbing the oil, inspected for cloud and replaced in the jacket.
This complete operation must be done in not more than three seconds.

When the bottom of the oil has become opaque, to a height of
not less than % nor more than fs in., the reading of the cold test
thermometer, corrected for error if necessary, shall be recorded as
the cloud point. The required height of cloud is approximately at
the middle of the thermometer bulb. The cold test jar may be marked
to indicate the proper level.

Oils having a viscosity greater than 600 seconds, Saybolt Uni-
versal at 100° F, are allowed to stand in the cold test jar at a tem-
perature of 60° to 85 °F for at least five hours prior to making the
test for pour point. A viscous oil which has been stored in a
warm place is liable to show an abnormally low, fictitious pour point

Fig. 114 — Cloud and Pour
Apparatus.

Test

KANSAS CITY TESTING LABORATORY 461

unless this precaution is observed. Oils having a viscosity not greater
than 600 seconds, Saybolt Universal at 100°F. may be tested without
such preliminary standing.

After preliminary standing, if necessary, the oil to be tested is
brought to a temperature of 90°F, or to a temperature 15°F higher
than its pour point, if this pour point is above 75 °F, and is poured
into the cold test jar, a, to a height of not less than 2 nor more than
2M: in. The jar may be marked to indicate the proper level.

The cold test jar shall be tightly closed by the cork, c, carrying
the cold test thermometer, b, in a vertical position in the center of
the jar with the thermometer bulb immersed so that the beginning
of the capillary shall be Va in. below the surface of the oil.

The disk, e, shall be placed in the bottom of the jacket, d, and
the cold test jar, with the ring gasket, f, 1 in. above the bottom is
inserted into the jacket. The disk, gasket and inside of jacket shall
be clean and dry.

The temperature of the cooling bath, g, shall be adjusted so that
it is below the pour point of the oil by not less than 15 nor more
than 30 °F and this temperature shall be maintained throughout the
test. The jacket, containing the cold test jar, shall be supported
firmly in a vertical position in the cooling bath so that not more than
1 in. of the jacket projects out of the cooling medium.

At each cold test thermometer reading which is a multiple of
5°F, the cold test jar shall be removed from the jacket carefully
and shall be tilted just sufficiently to ascertain whether the oil around
the thermometer remains liquid. As long as the oil around the ther-
mometer flows when the jar is tilted slightly, the cold test jar shall
be replaced in the jacket. The complete operation of removal and
replacement shall require not more than three seconds. As soon as
the oil around the thermometer does not flow when the jar is tilted
slightly, the cold test jar shall be held in a horizontal position for
exactly five seconds, and observed carefully. If the oil around the
thermometer shows any movement under these conditions, the cold
test jar shall be immediatelv replaced in the jacket and the same
procedure shall be repeated at the next temperature reading 5 h
lower. As soon as a temperature is reached at which the oil arou"<'
the thermometer shows no movement when the cold test jar '»"<"'"
in a horizontal position for exactly five seconds, the test shall be
stopped.

The lowest reading of the cold test thermometer, corrected for
error if necessary, at which the oil around the thermometer shows
any movement when the cold test jar is held in a horizontal position
for exactly five seconds, shall be recorded as the pour point.

462

BULLETIN NUMBER SIXTEEN OF

8-A. SEDIMENT AND WATER IN PETROLEUM (CENTIFUGE
•• 3IETH0D).

The apparatus is shown in Figs. 115 and 116.

Exactly 50 cc. of 90 per cent benzol are measured into each of
two centrifuge tubes and exactly 50 cc. of the oil to be tested are
then added to each. The centrifuge tubes are tightly stoppered and
shaken vigorously until the contents are thoroughly mixed. The
temperature of the bath is maintained at 100° F and the centrifuge
tubes are immersed therein to the 100 cc. mark for 10 minutes.

The two centrifuge tubes are then placed in the centrifuge on
opposite sides and are whirled at a rate of 1400 to 1500 r. p. m. or
the equivalent for 10 minutes. The combined volume of water and
sediment at the bottom of each tube is read and recorded, estimating
to 0.1 cc. if necessary. The centrifuge tubes are then replaced in
the centrifuge, again whirled for 10 minutes as before and removed
for reading the volume of water and sediment as before. This opera-
tion is repeated until the combined volume of water and sediment in
each tube remains constant for two consecutive readings.

The preferred form of centrifuge has a diameter of swing (tip
to tip of whirling tubes) of 15 to 17 in. and a speed of at least 1500
r. p. m. or the equivalent. If the available centrifuge has a diam-
eter of swing varying from these limits, it is run at the proper speed
to give the same centrifugal force at the tips of the tubes as that
obtained with the preferred form of centrifuge. The proper speed
may be calculated from the following formula in which d represents
diameter of swing (tip to tip of whirling tubes) of the centrifuge
used:

R. p. m. = 1500

V-

I-'ig. 115 — Certtrifuge for B. S.

Fig. 116 — Sedi-
mentation
Tubes.

KANSAS CITY TESTING LABORATORY

463

8-B. WATER IN PETROLEUM PRODUCTS (DiSTILLATION

METHOD).

100 cc. of the oil to be tested ave measured in an accurate 100-cc.
graduated cylinder at room temperature and poured into the distilla-
tion flask. The oil adhering to the walls of the 100-cc. graduated
cylinder is transferred to the distillation flask by rinsing with two
successive 25 cc. portions of gasoline, the cylinder being allowed to
drain each time. The sample is taken with great care to see that
the water and the oil are uniformly mixed, insuring a representative
sample. The apparatus used is that by Dean and Stark (J. of I. and
E. Chem. 12-486) a figui'e of which is shown hei'ewith. The oil and
gasoline in the distillation flask is thoroughly mixed by swirling the
flask with proper care to avoid any loss of material. A boiling stone,
such as a piece of unglazed porcelain, may be introduced for the
purpose of preventing bumping during the subsequent distillation.

SOOc< ^/a3k

Fis

117 — Water Determination .Apparatus.

The flask should be of pyrex glass.

Heat is best applied without danger of bumping or foaming by
immersing the flask in a bath of glycerin. It may be applied with
care using an electric heater or a gas flame. The graduated receiv-
ing tube should be kept cool. Distill until no further increase in the
volume of the recovered water is observed.

464

BULLETIN NUMBER SIXTEEN OF

9-A. END POINT DISTILLATION TESTS OF GASOLINE,

NAPHTHA, BENZINE, PRESSURE DISTILLATE,

TURPENTINE SUBSTITUTES AND KEROSENE.

The apparatus is shown in Figs. 118 and 119.

The condenser bath is filled with cracked ice or other convenient
cooling medium and enough water is added to cover the condenser
tube.

The temperature is maintained between 32°F and 40°F.

The condenser tube is swabbed out to remove any liquid remain-
ing from a previous test.

A piece of unstarched absorbent cloth attached to a cord or cop-
per wire may be used for this purpose.

The bulb of the distillation thermometer is covered uniformly
with long fiber absorbent cotton weighing between 3 and 5 milligrams.

Fresh cotton is used for each distillation.

One hundred (100) cc. of the naphtha are measured into the
100 cc. graduated cylinder, the naphtha and cylinder being both
cooled to a temperature between 55 °F and 65 °F and is transferred
direct to the Engler flask using a long stemmed funnel with a small
flare so that no liquid is permitted to flow into the vapor tube.

The Engler flask has previously been rinsed with the naphtha
under test and has been allowed to drain vertically inverted for at
least five minutes.

f-Adiomrttr* miter

I '' i'

' I' ' n

11 founsen
yi burner
H

*'}! -

II
II

1 12 DiomtUr

/5'-

Ice Water Baih

^ Oufside Diamehr

»o

- ^~"~ — — _ A'o. ?0 Oagt Seamless
'~^~.^~~^ Brass Tubhg

-it:

^—- r£r_6

■.BMIing
Paper

'5f

^

Fig. 118 — End Point Distillation Apparatus.

KANSAS CITY TESTING LABORATORY

465

The thermometer provided with a cork is fitted tightly into the
flask so that it will be in the middle of the neck and so that the lower
end of the capillary tube is on a level with the inside of the bottom
of the vapor outlet at its junction with the neck of the flask.

The charged flask is placed over the 1%-inch opening in the
6x6-inch asbestos board with the vapor outlet tube inserted into the
condenser tube.

A tight connection is made by means of a cork.
The position of the flask shall be so adjusted that the vapor
tube extends into the condenser tube not less than one inch nor more
than two inches.

The graduated cylinder which has previously been used in mea-
suring the charge, is placed without further draining at the outlet
of the condenser tube in such a position that the condenser tube
shall extend into the graduate at least one inch but not below the
100 cc. mark.

If the room temperature is above
65 °F, the cylindrical graduate shall
be immersed up to the 100 cc. mark
in a glass water bath maintained
at a temperature between 55 °F and
65°F.

The top of the graduate is closely
covered with a piece of fiber blot-
ting paper or similar material so
that it fits the condenser tube
tightly.

Heat is applied at a uniform rate
so that the first drop falls from the
condenser in not less than five nor
more than ten minutes.

When the first drop falls from
the end of the condenser, the read-
ing of the distillation thermometer
is recorded as the Initial Boiling
Point.

The receiving cylinder is then
moved so that the end of the con-
denser tube shall touch the side of
the cylinder.

Heat is then regulated so that distillation proceeds at a uni-
form rate of not less than four or more than five cubic centimeters
per minute. ,

The reading of the distillation thermometer is recorded when the
bottom of the meniscus of the distillate in the receiving graduate is
at each 10 cc. mark or if desired, also at each o cc. mark.

After the 90 per cent point has been recorded, the heat may be
increased sufficiently to bring over the heavy ends.

There should be no further increase after this adjustmont and
it is not necessary to maintain the rate as this cannot convenitntly
be done.

-tlMMUid lAO e. c. En^r Duk tor luo In tukiDg dlsUIlfttlon Uut of imoUd*.

Fig. 119 — End Point Flask.

466 BULLETIN NUMBER SIXTEEN OF

However, the time required between 90 per cent and the end point
should not be more than 5 minutes.

The heating shall be continued until the mercury reaches a max-
imum and then starts to fall consistently.

The highest temperature observed shall be recorded as the end
point or maximum temperature.

This point will be reached when the bottom of the flask has be-
come dry.

The total volume of distillate collected in the receiving flask is
recorded as the total recovery.

The cooled residue in the Engler flask is poured into a cylindrical
graduate and the volume is recorded as residue.

The difference between the 100 cc. taken and the sum of the re-
covery and the residue is calculated and recorded as distillation loss.

Description of Apparatus.

The Flask— The Standard 100 cc. Engler flask is shown in fig-
ure 119, the dimensions and allowable tolerance being as follows:

Centimeters Inches Tolerances

Cm.

Diameter of bulb, outside 6.5 2. .56 0.2

Diameter of neck, inside 1.6 0.63 0.1

Length of neck 15.0 5.91 0.4

Length of vapor tube 10.0 3.94 0.3

Diameter of vapor tube, outside.... 0.6 0.24 0.05

Diameter of vapor tube, inside 0.4 0.16 0.05

Thickness of vapor tube wall 0.1 0.04 0.05

The position of the vapor tube shall be 9 cm. (3.55 in.) (+3 mm.)
above the surface of the liquid when the flask contains its charge of
100 cc. The tube is approximately in the middle of the neck and set
at an angle of 75° (tolerance + 3 deg.) with the vertical.

The Condenser. — The condenser (Fig. 118) consists of a ts inch
(14.29 mm) OD No. 20 Stubbs Gage seamless brass tube, 22 in. (55.88
cm) long. It is set at an angle of 75° from the perpendicular and is
surrounded with a cooling bath 15 inches long (38.1 cm.) approxi-
mately 4 in. (10.16 cm.) wide by 6 in. (15.24 cm.) high. The lower
end of the condenser tube is cut off at an acute angle and curved
downward for a length of 3 in. (7.62 cm.) and slightly backward so as
to insure contact with the wall of the graduate at a point 1 to 1%
in. (2.54-3.175 cm.) below the top of the graduate when it is in posi-
tion to receive the distillate.

The Shield. — The shield (Fig. 118) is made of approximately
22 gage sheet metal and is 19 in. (48.26 cm.) high, 11 in. (27.94
cm.) long and 8 in. (20.32 cm.) wide, with a door on one narrow
side, with two openings 1 in. (2.54 cm.) in diameter, equally spaced
in each of two narrow sides, and with a slot cut in one side for the
vapor tube. The centers of these four openings are 8% in (21.59 cm.)
below the top of the shield. There are also three ^2 in. (1.27 cm.)
holes in each of the four sides with their centers 1 in. (2.54 cm.)
above the base of the shield.

KANSAS CITY TESTING LABORATORY 46?

Ring Support and Hard Asbestos Boards.— The ring support
IS the ordinary laboratory type, 4 in. (10.16 cm.) in diameter and
IS supported on a stand mside the shield. There are two hard as-
bestos boards: One 6x6x14 inch (15.24 cm.xl5.24.x6.35 mm) with
a hole 1% in. (3.175 cm.) in diameter (IVs in. if end point is over
470° F) in its center, the sides of which shall be perpendicular to
the surface; the other, an asbestos board to fit tightly inside the
shield with an opening 4 in. (10.16 cm.) in diameter concentric with
the ring support. These are arranged as follows: The second as-
bestos board is placed on the ring and the first or smaller asbestos
board on top so that it may be moved in accordance with the direc-
tions for placing the distilling flask. Direct heat is applied to the
flask only through the IM in. (3.175 cm.) opening in the first asbestos
board.

Gas Burner. — The burner is so constructed that sufficient heat
can be obtained to distill the product at the uniform rate specified
below. The flame should never be so large that it spreads over a
circle of diameter greater than 31/2 in. (8.89 cm.) on the under sur-
face of the asbestos board. A sensitive regulating valve is a neces-
sary adjunct as it gives complete control of heating.

Electric Heater. — The electric heater which may be used in place
of the gas flame, shall be capable of bringing over the first drop with-
in the time specified below when started cold, and of continuing the
distillation at the uniform rate. The electric heater shall be fitted
with an asbestos board top Va to % inch (3.175 to 6.35 mm) thick,
having a hole 1% in. (3.175 cm.) in diameter in the center. When
an electric heater is employed, the portion of the shield above the
asbestos board shall be the same as with the gas burner.

Thermometer — Low distillation thermometer is a mercury, nitro-
gen filled total immersion glass engraved thermometer, length about
381 mm. diameter, 6 to 7 mm. made of pyrex glass with bulb length
of 10 to 15 mm. bulb diameter 5 to 6 mm. range 30 °F to 580 F.
30 °F mark 100 to 110 mm. from bottom of bulb. The 580' F mark
35 to 45 mm. from top of stem. Graduated in 2°F. The allowable
error not over 1°F at any point.

High distillation thermometer is a mercury, nitrogen filled total
immersion glass engraved thermometer, length about 381 mm. diame-
ter, 6 to 7 mm. made of pj/rex glass with bulb length of 10 to 15
mm. bulb diameter 5 to 6 mm. range 30°F to 76°F 30 I mark 25
to 35 mm. above bottom of bulb. 760°F mark 30 to 45 mm below
top of tube. The scale is graduated in 2°F. Accuracy within one
small scale division.

Graduate.-The graduate shall be a cylindrical type of umform
diameter with a pressed or molded base and lipped top. It '^ >?'»J?"-
ated for 100 cc. so that the 10 cc. markings are clearly set out. iml
graduations must be corrected within Vz cc. at any point.

468

BULLETIN NUMBER SIXTEEN OF

9-B. FRACTIONAL GRAVITY DISTILLATION ANALYSIS OF
CRUDE PETROLEUM AND PETROLEUM DISTILLATES.

The apparatus to be used is that shown in Fig. 120. This
apparatus consists of a 1,000 cc. Claisen distilling flask of heavy
p>rex glass having the dimensions shown in the figure. The dis-
tilling flask, the condenser and the condenser tube must be of pyrex
glass or equally resistant glass. The tubulus and the condenser are
set at an angle of 75° to the vertical.

The oil to be tested should be as nearly as possible free from
water. Exactly 800 cubic centimeters at 60 °F are poured into the
distillation flask. The thermometer used in the vapor neck of the
flask is scaled for 3-inch immersion and should read to 760° F. It
is inserted so that the top of the mercury bulb is even with the bot-
tom of the tubulus and is in the center of the neck of the flask. The
other neck of the flask is fitted with a glass tube which goes to the
bottom of the flask and also with a total immersion thermometer
I'eading to 760° F and inserted into the oil.

0Pf7f>T£ /e

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/^/SfiCy/orvi^C C/?f)\^/Ty C?/S7-/i-i.'^r/o/^ ^^ft^eflTc/S

Fig-. 120— Fractional Gravity Distillation .\pparatus.

The distillation is begun using a slightly luminous flame of a Tir-
rell burner. The flame must be protected from drafts. The flask
may be blanketed with asbestos paper. The flame is controlled by a
screw pinch cock on the rubber tubing or by a needle valve in the
base of the burner.

KANSAS CITY TESTING LABORATORY 469

The condenser water should be at or below 60 °F. If the running
water is not sufficiently cold, ice water should be used for circulation
at the beginning of the distillation. The temperature at which the
first drop falls from the lower end of the condenser tube is recorded
as the initial boiling point. The rate of distillation after the first 5%
is taken is 8 cubic centimeters or 1% per minute. Temperature read-
ings are taken every 2 1/2 9c or 20 cubic centimeters. Five per cent
fractions are collected in a 100 cc. gi-aduated cylinder. For smooth
operation of the distillation, two 100 cc. cylinders and one 50 cc.
cylinder should be available. The 40 cc; of distillate are poured into
a 50 cc. graduate to allow the distillate to mix thoroughly. The
specific gravity is taken preferably with special 4-inch hydrometers,
each hydrometer having a range in specific gravity of 0.050. If the
special small hydrometers are not available a Westphal balance should
be used. The receiving cylinder should be kept cold during the begin-
ning of the distillation.

The record of the distillation is conveniently made on a special
form. The specific gravities with the temperatures of observation are
recorded and later corrected to the basis of 60° F. All observations
should be in terms of specific gi'avity and converted to Baume gravity.

The straight fire distillation is continued until a temperature of
572°F is reached. An even cut in the distillation should be made on
the 5% fraction whose end point is first above 572°F. Bejond this
temperature inert gas such as natural gas, coal gas or carbon dio.x-
ide is introduced in sufficient quantity to carry the rate of distillation
without the temperature at any time exceeding 650° F in the oil. Gas
is introduced at the rate of about 10 cu. ft. per hour when cracking
hegins to take place or at a temperature of 600° F in vapor. After
« temperature of 572 °F has been reached, the condenser water is
turned off so that the condenser may be warmed up sufficiently to
prevent any wax that may be present from occluding the condenser
tube. *With ordinarv light crude oil, 90% should be distilled with-
*»ut cracking. In asphaltic base oils, 70 9r should always be distilled
without cracking. The residue in the flask while warm is poured out
*nd weighed in a seamless tin box and its consistency determined
either by use of the penetrometer if the petroleum is asphalt base or
"hy the Saybolt viscosimeter at 210°F if paraffin base. If the residue
Is fluid, it may be suitable for cylinder stock.

In the case of distillates such as pressure distillate, gas oil,
kerosene, gasoline, naphtha, turpentine substitutes, etc., it is not nec-
essary to use the gas tube or the thermometer in the oil un ess spe-
cially desired. In this case, a dry point can be reached "«"»''>' ^^'th-
out appreciable cracking. From the gravity of the 5V f'-a^tions th
gravity of the total distillate at any per cent or temperatu. e ma> lu
calculated as well as the gravity of the stream This tyP^ 0/ «"« y^\^
is indispensable in calculation of the gravity of the P^-"''"^-^ J'"'" Jjj
receiving house gravities in the refinery. (See page 241 for record
form.)

•The rate of distillation cannot ordinarily bo maintain.d for ll.o
heavy fractions.

470 BULLETIN NUMBER SIXTEEN OF

9-C. PROXIMATE DISTILLATION OF PETROLEUM.

400 cc. of the petroleum are poured into a 1,000 cc. flask which
is connected to a condenser (as shown in Fig. 120). The ther-
mometer is inserted so that the top of the bulb is just below the out-
let of the flask. The flame is gradually applied to the oil so that
any foaming will tend to make itself evident. If there is foaming
it will be necessary to heat the upper portion of the flask. Before
the application of the flame to prevent foaming, it is necessary to
get the temperature at which the first drop falls into the receiver.
This is the initial boiling point. The distillate is collected until a
temperature of 410° F is reached when distillation is proceeding at
the rate of 5 cc. per minute. The fraction collected up to this tem-
perature is the gasoline or naphtha, the gravity of which is deter-
mined. If the gravity is less than 57, it is classified as naphtha, if
above this, it is classified as gasoline. Or if initial b. p. is over
160 °F the distillate is classed as naphtha. The distillation is con-
tinued at the same rate until a temperature of 572 °F is reached.
This fraction is kerosene and its gravity is determined. The resi-
due in the flask is fuel oil and is used for the determination of wax
or asphalt, gas oil or lubricants. The information given by this
distillation is:

Water %

Gasoline ( 410°F) (Gr.= = Be°) %

Kerosene ( 410— 572°F) (Gr.= = Be°) %

Fuel Oil— Residuum (Gr.= Be°) %

100.0%

9-D. SAMPLE PREPARATION DISTILLATION OF CRUDE OIL.

The apparatus consists of a 5-gallon steel still, condenser, gas
burner, water supply under pressure, steam producers, superheater
gauges and connections.

Ten thousand cubic centimeters is a convenient charge, giving a
59c fraction of 500 cc, which is sufficient for special tests. The
still is covered with chicken wire and asbestos cement for insulation.
Direct firing is used until a temperature of slightly above 500 °F is
indicated in the vapor or a gravity of 40° Be' (0.825 specific gravity)
is shown in the distillate fraction. At this temperature superheated
steam or gas is introduced.

KANSAS CITY TESTING LABORATORY 471

lOA. FLASH POINT OF KEROSENE AND OTHER VOLATILE

INFLAMMABLE LIQUIDS.

(With Standard "TAG" Closed Tester.)

This is essentially in accordance with the method of the American
Society for Testing Materials, Book of Standards, 1921, page 669.

The test must be performed in a dim light so as to see the flash
plainly.

Surround the tester on three sides with an inclosure to keep
away drafts. A shield about 18 inches square and 2 feet high, open
in front, is satisfactory. See that tester sets firmly and level.

For accuracy, the flash point thermometers which are especially
designed for the instrument should be used as the position of the bulb
of the thermometer in the oil cup is essential.

Put the water-bath thermometer in place. Place a receptacle
under the overflow spout to catch the overflow. Fill the water bath
with water at such a temperature that when testing is started, the
temperature of the water bath will be at least 10°C below the prob-
able flash point of the oil to be tested.

Put the oil cup in place in the water bath. Measure 50 cc. of
the oil to be tested in a pipet or a graduate and place in oil cup.
The temperature of the oil must be at least 10°C below its probable
flash point when testing is started. Destroy any bubbles on the sur-
face of the oil. Put on cover with flash point thermometers in place
and gas tube attached. Light pilot light on cover and adjust flame to
size of the small white bead on cover.

Light and place the heating lamp, filled with alcohol in base of
tester and see that it is centrally located. Adjust flame of alcohol
lamp so that temperature of oil in cup rises at the rate of about 1°C
(1.8°F) per minute or not faster than 1°C (1.8 °F) nor slower than
0.9°C (1.6°F) per minute.

Record the "time of applying the heating lamp," record the "tem-
perature of the water bath at start," record the "temperature of
the oil sample at start." ror- i i i.u

When the temperature of the oil reaches about 5 L below the
probable flash point of the oil, turn the knob on the cover so as to
introduce the test flame into the cup and turn it promptly back again
Do not let it snap back. The time consumed m turning the knoft
down and back should be about one full second, or the time required
to pronounce distinctly the words "one thousand and one.

Record the "time of making the first introduction of the test
flame" and record the "temperature of the oil sample at time ot tnst

^^^^' Repeat the application of the test flame '^^t every p5»C rise in
temperature of the oil until there is a flash of '"; "'^ ^'^^ .",,^,'^^
cup Do not be misled by an enlargement of th<: ,^7, ,|. '. ,,°' / Vho
around it when entered into the cup or by slight ^I'^l^ '' ^"»; "; . ,*^
flame; the true flash consumes the gas in the top of the cup .uul

^^'^SecVdThl^'^tfi^e'"// which the flash point is reached." and the

"'^' K S!:^ rise in temperature of the oil f-- the ^'^ of^^^Z
the first introduction of the test fl^^^^'V^ t^«^/Xwef tlTn S.g'c
flash point is reached" was faster than 1.1 C or slower tnan v.j

472

BULLETIN NUMBER SIXTEEN OF

Thermometer, indicating the temperature of the oil.

Thermometer, indicating the temperature of the water
bath.

A miniature oil well to supply the lest flame when ^fi»
is not available, mounted on the axis about which
the test-flame burner is rotated, which axis is
hollow and provided with connection on one end
for gas hose, and provided also with needle valve
for controlling gas supply, when gas is available,
the gas passing through the empty oil well.

Gas or oil tip for test flame

Cover for oil cup, provided with three openings, which
are in turn covered by a movable slide operated by
a knurled hand knob, which also operates the teat
flame burner in unison with the movable slide, so
that by turning this knob, the test flame is lowered
into the middle opening in the cover, at the same
time that this opening is uncovered by the move-
ment of the slide.

Oil cup (which cannot be seen in the illustration), of
standardized size, weight and shape, fitting into
the top of the wateV bath.

Overflow spout.

Water bath, of copper, fitting into the top of the body,
and provideci with an overflow spoUt and open-
ings in its top, to receive the oil cup and water
bath thermometer.

Body of metal, attached to substantial cast metal baM
provided with three feet

Alcohol lamp for beating the water bath

Gas hotel.

Fig-. 122 — A. S. T. M. Flash Tester.

per minute, the test should be questioned and the alcohol heating lamp
adjusted so as to correct the rate of heating. It will be found that
the wick of this lamp can be so accurately adjusted as to give a
uniform rate of rise in temperature of 1°C per minute and remain so.

Repeat Tests. — It is not necessary to turn off the test flame
with the small regulating valve on the cover, but leave it adjusted to
give the proper size of flame.

Having completed the preliminary test, remove the heating lamp,
lift up the oil cup cover and wipe off the thermometer bulb. Lift
out the oil cup and empty and carefully wipe it. Throw away all
oil samples after once using in making test.

Pour cold water into the water bath, allowing it to overflow
into the receptacle until the temperature of the water in the bath
is lowered to 8°C below the flash point of the oil as shown by the
previous test. With cold water of nearly constant temperature it
will be found that a uniform amount will be required to reduce the
temperature of the water bath to the required point.

Place the oil cup back in the bath and measure into it a 50 cc.
charge of fresh oil. Destroy any bubbles on the surface of the oil,

KANSAS CITY TESTING LABORATORY

473

put on the cover with its thermometer, put in the heating lamp,
record time and temperature of oil and water and proceed to repeat
test as described above. Introduce test flame for first time at a
temperature 5°C below the flash point obtained on the previous test.

Precautions. — Be sure to record barometric pressure either from
laboratory barometer or from nearest Weather Bureau station. Re-
cord temperature of room.

Note and record any flickering of the test flame or slight pre-
liminary flashes when the test flame is introduced into the cup be-
fore the proper flash occurs. Record tin\e and temperature of such
flickers or slight flashes if they occur.

lOB. FLASH AND BURNING POINTS OF ALL TYPES OF

PETROLEUM OILS AND ASPHALTS.

(With New York or Elliott Closed Tester.)

The bath surrounding the oil cup is filled with very high flash
fluid oil or is left unfilled if the oil to be tested has a very high flash
point. The oil cup is filled with the material to be tested to within
3 millimeters of the flange joining the cup and the vapor chamber
above. The glass cover is then placed on the oil cup and the ther-
mometer adjusted so that its bulb is just covered by the oil or bitu-
men. The flame is applied to the bath in such manner that the
temperature is raised at the rate of about 5°C per minute. Every
half minute the testing flame is inserted in the openmg m the cover
and about halfway between the surface of the material and the
cover. The first appearance of a faint bluish flame on the entire
surface of the bitumen or oil shows that the flash point has been
reached, and this temperature is recorded. . , ^

The burning point of the material is now obtamed by removing
the o-las'' cover and replacing the thermometer in the frame. The
temT^erature is raised at the same rate and material tested as before.
The' temperature at which the oil or bitumen ignites and burns is
recorded as the burning point. The flame should be extinguished
with the metal cover very promptly after the burning point is reached.

Fig-. 123 — Elliott Flash Tester.

FlR. 124 — Foster Flash Ttsl.r.

474

BULLETIN NUMBER SIXTEEN OF

IOC. FLASH AND FIRE TESTS (CLEVELAND OPEN TESTER).

Fig-. 12
Flash

5— ClcY
Tester.

The apparatus is shown in Figs. 125 and 126.

The thermometer is suspended or held in a ver-
tical position by any suitable device. The bot-
tom of the bulb is placed V^ in. (0.635 cm.) from
the bottom of the cup, and above a point half way
between the center and back of the cup.

The, cup is filled with oil to be tested in such a
manner that the top of the meniscus is exactly at
the filling line at room temperature. The sur-
face of the oil shall be free from bubbles. There
shall be no oil above the filling line or on the
outside of the apparatus.

The test flame shall be approximately ^2 in.
(0.397 cm.) in diameter.

The test flame is applied as the temperature
read on the thermometer reaches each successive
S'F mark. The flame is passed in a straight
line across the center of the cup. The test flame
shall be while passing across the surface of the
oil, in the plane of the upper edge of the cup.
^^The time for the passage of the test flame across
*" ^"'"the cup shall be approximately one second.

The rate of heating of the oil shall be such that the temperature
read in the thermometer increases not less than 9 nor more than
11 °F per miuute.

The flash point is taken as the temperature read on the ther-
mometer when a flash appears at any point on the surface of the
oil. The true flash must not be confused
with a bluish halo that sometimes surrounds
the test flame.

After determining the flash point the
heating is continued at the specified rate,
and application of the test flame is made at
the specified intervals until the oil ignites
and continues to burn for a period of at
least five seconds. The temperature read
when this occurs shall be taken as the fire
point.

The flash point and fire point tests must
be made in a room or compai'tment fi-ee
from air drafts. It is desirable that the
room or compartment be darkened suf-
ficientb' so that the flash may be readily
discernible.

This method is suitable for lubricants,
heavy fuel oils, road oils and asphalts Th*^
A. S. T. M. flash point thermometer should

be used. It is 38 cm. long and «r«iP.I fo. ^.^ 1 26— Cleveland

1 inch immersion. Flash Cup,

KANSAS CITY TESTING LABORATORY

475

lOD. FLASH POINT OF FUEL OIL (PENSKY-MARTENS).

The apparatus is the Pensky-Martens tester as described in
tentative methods of A. S. T. M. for 1921, page 258. (See Fig. 127).

All parts of the cup and its accessories must be thoroughly clean
and dry before starting the test. Particular care must be taken to
avoid the presence of any gasoline or naphtha used to clean the ap-
paratus after a previous test.

The cup is filled with the oil to be tested up to the level in-
dicated by the filling mark.

The lid is placed on the cup and the latter set in the stove. Care
shall be taken to have the locating devices properly engaged. The
thermometer is inserted. If it is known that the oil will flash above
220° F the high temperature thermometer may be selected; other-
wise, it is preferable to start with the low temperature thermometer
and change in case a temperature of 220 to 230 °F is reached.

The test flame is lighted and adjusted so
that it is of the size of a head is in. (3.97
mm.) in diameter.

Heat is supplied at such a rate that the tem-
perature read on the thermometer increases
not less than 9 nor more than 11 °F per min-
ute. The stirrer is turned at a rate of from
1 to 2 revolutions per second.

Application of the test flame is made at each
temperature reading which is a multiple of
2°F up to 220 °F. For the temperature range
above 220 °F, application shall be made at each
temperature reading which is a multiple of
5°F. Application of the test flame is made by
operating the device controlling the shutter
and test flame burner so that the flame is
lowered in one-half second, left in its lowered
position for one second, and quickly raised to
its high position. Stirring is discontinued dur-
ing the application of the test flame.

The flash point is taken as the temperature read on the ther-
mometer at the time of the flame application that causes a distinct
flash in the interior of the cup. The true flash must not be ^'O' ;
fused with the bluish halo that sometimes surrounds the test t anu
for the applications preceding the one that causes the actual tlasli.

The barometric pressure is observed and recorded No /^o'";;;;^-
tions need be made except in case of dispute when the flash point
figures may be corrected according to the following rule:

For each inch (25 mm.) below 29.92 in. (7G0 mm.) barometric
reading add 1.6°F to the flash point.

For each inch (25 mm.) above 29.92 in. (7(>0 mm.) barometric
reading subtract 1.6°F from the flash point.

Fig. 127 — Pensky-
Martens Flash Test-
er for Fuel Oil.

476

BULLETIN NUMBER SIXTEEN OF

CORRECTIONS OF FLASH
POINT FOR NORMAL BARO-
METRIC PRESSURES.

To correct readings made at
other pressures to the standard
barometric pressure of 760 mm.

Barometer

Correction

Millimeters

Degrees C.

700

—2.1

705

—1.9

710

—1.7

715

—1.6

720

—1.4

725

—1.2

730

—1.0

735

— .9

740

— .7

745

— .5

750

— .3

755

.2

760

0

TYPICAL COMPARISON OF
FLASH POINTS.

A. S.T. M. Closed (Tag) 100° F
Elliott or N. Y. Closed. 100-105° F

Abel 102-106° F

Abel-Pensky 102-105° F

Pensky-Martens 102-106° F

Tag Open Cup 108-112° F

Cleveland Open Cup.. . .110-115° F

765

+ .2

Fig. 128 — Pressure Cracking Apparatus.

KANSAS CITY TESTING LABORATORY 477

llA. CRACKING TEST FOR HEAVY PETROLEUM HYDRO-
CARBONS.

The apparatus is set up as shown in figure 128. (a) is a cylin-
drical tube tested out to a pressure of 3,000 pounds such as is ordi-
narily used for dispensing oxygen gas. (b) is a thermometer well
or plug with a tapered thread and of sufficient length that it pro-
trudes well into the interior of the vessel (a). This plug has an
opening from the outside into which the thermometer (c) is inserted.
This mercury thermometer is graduated preferably in single degrees
Centigrade and is of borosilicate glass, nitrogen filled and reading
up to a temperature of 550°C. (d) is an extra heavy ammonia pipe
fitting connected to a valve (e) and a pressure gauge (f). Pressure
gauge (f) should read to at least 200 atmospheres or 200 kilograms
per square centimeter. Heat is applied by gas burners (g) such as
are used in combustion furnaces and the whole apparatus is supported
on a stand with the end carrying the pressure gauge slightly elevated.

The capacity of the bomb is 1,500 to 1,600 cubic centimeters
and 500 cc. of oil to be tested are poured into it at a temperature of
approximately 20°C. The plug (b) is inserted and screwed in very
tightly, using Stilson wrenches. An iron gasket should be used if
necessary to give" shoulder contact. The threads on the plug may be
dressed with a mixture of equal parts of glycerin, litharge and cop-
per oxide. The flame is applied so that it does not excessively heat
the portion of the container not in contact with the oil. The total
time consumed for the test after the beginning of the application of
the heat should be between 55 minutes and 70 minutes. The heating
is carried on until a pressure of 55 atmospheres is attained, based on
a temperature of 400 °C. It is desirable to keep the container covered
with a sheet of asbestos during the operation. The temperature should
not ordinarily exceed 425^C. The apparatus is cooled to about 20 L
before opening.

The constants in this test are the dimensions of the apparatus,
the amount of oil used, the rate of application of heat and maximum
pressure at 400°C.

The variables are the percentage by volume of oil ''ecovered
after cracking, the amount of carbon fo?-"^^^, the amount of gas
formed, the specific gravity of the gasoline and the total yield of
gasoline. (See pages 235 and 237.)

Variations are due to the character of the oil treated the spe-
cific gravity of the gasoline being higher, the recovery highci. the
carbon"nd%as' form! tion less and the total amount of oil n.ovoi-od
greater with paraffin base and with low specific gravity oils than
with naphthene base and high specific gravity oils.

From one such equilibrium test it is Possible t. approx.nmte y
estimate the amount of total gasoline which ,t would be V^^
obtain from an oil. This may be calculated f^;,"^^;"*. j,";^"; , ' H.
test by taking into consideration the f»^"f ^^%rnor «fter c>^<^^ine
increase in specific gravity of the residue above 210 C after ciack.ng:.

478 BULLETIN NUMBER SIXTEEN OF

IIB. VAPOR PRESSURE.

The vapor pressure of light petroleum hydrocarbons is deter-
mined with the same apparatus used for making the cracking test.
The pressure readings with the corresponding temperature readings
should be taken every 30 pounds and a curve plotted for intermediate
points. The temperature should not be carried above 350°C as crack-
ing will take place. (See curves on page 234.)

lie, HEAT-PRESSURE TEST FOR THE STABILITY
OF MOTOR LUiiRICANTS.

The apparatus used for this test is that shown in figure 128,
being the same as that used for cracking test of heavy petroleum
hydrocarbons.

Exactly 400 cubic centimeters of lubricating oil at a temperature
of approximately 70 °F is placed in the 1,600 cubic centimeter cylin-
der. The cylinder is tightly closed with the plug, using a soft iron
gasket to prevent any leakage. The apparatus is set up oh a suit-
able stand and with a row of Bunsen burners is brought up to a
temperature of 425 °C. It is maintained at exactly this temperature
for 15 minutes. At the end of this time the pressure is recorded.
The cylinder is now quickly cooled with water and the oil is emptied.
The f oITowing notations are made :

The total amount of oil recovered by distilling 100 cubic centi-
meters according to method 9-A, the gravity of the fraction at a
vapor temperature of 410 °F. The amount of kerosene and its grav-
ity. This is the fraction collected between vapor temperatures of
410°F and 572°F. The residue is collected and its gravity is taken.
The amount of pitch in the recovered oil is obtained by evaporating
the oil in an oven in accordance with method 26. The residue is
heated at a temperature of 500°F until it ceases to lose weight. The
residual pitch is calculated to the basis of the residual oil. The re-
covered oil is tested for acidity in accordance with method 20-A.

This test is of great value in determining the stability of motor
oils in use. An oil having poor stability will have an increase in
Baume' gravity of 7° or more and will have a acidity of 10 points or
more expressed in terms of percentage tenth normal acid. Vegetable
or animal oils by this test give an acid value approximately 200 times
as great as mineral oils. This test serves as a very delicate means
of detecting small qvantities of animal or vegetable oil in mineral oils.
The higher the pressure developed the more susceptible the oil is to
decomposition by heat. (See pages 277 and 278.)

IID. VAPOR PRESSURE TESTS FOR LIGHT GASOLINE MADE

FROM GAS.
(Westcott, Handbook of Casinghead Gasoline.)

Apparatus shown on page 466 consists of iron or steel pipe of
2 inch size, with caps screwed on ends. Upper cap has 0.25 inch
nipple screwed in and is connected by a coupling to a 3 inch 30 lb.
pressure gauge. Gauge is known as Inspector's Gas Gauge. All
joints must be perfectly tight. Joints between large pipe and caps
are best sealed with solder. Approximate external dimensions are
indicated in Fig. 129. In addition to apparatus indicated, there is

KANSAS CITY TESTING LABORATORY

479

also required a tin cylinder for filling test tube, 12 by 3 inches, that
can be slipped over outside of tube for convenience in carrying when
not in use. The tin cylinder is provided with a lip for pouring. A
small tin cover 0.75 inch deep, fitting over the bottom of the tin
cylinder may be removed and used for measuring off one-tenth ca-
pacity of test tube. A small tin funnel 2.5 inches in diameter with
stem 3 inches long and three-sixteenths inch in diameter should be
used.

Remove the gauge from the tube and fill tube to 90 per cent
of its capacity. Fill tube preferably by lowering it into the storage
tank in upright position by means of a cord or wire. Leave the tube
entirely immersed for several minute?, withdraw it and pour off
sufficient liquid so that the tube will contain 90% of its capacity. A
small measure having capacity of 10% of the test tube should be used
for that purpose.

In case it is impracticable to lower the tube into the

/\ storage tank, draw the liquid off into the vessel of
I capacity about equal to the test tube. Pour liquid into
y the test tube until about half filled. Shake tube and
contents gently in order to bring both to the same
temperature. After standing for several minutes, pour
out all the liquid from the tube. Draw another sample
from the storage tank into the cylinder and pour
through funnel into the tube until the latter is entirely
full. Withdraw one-tenth as before. Screw gauge
tightly into position, using a little liquid shellac or
pyroxylin cement on joint to insure a tight fit.

Immerse the tube in water at a temperature of 70°F
and allow it to remain for five minutes. Then remove
it from the water and unscrew the gauge sufficiently
to relieve the pressure indicated by the gauge for a
period of 20 seconds and screw the gauge tightly into
the tube again. Then place the tube in water at a tem-
perature of 100° F (90°F from Nov. 1st to March 1st).
The level of the water must be just below the lower
edge of the pressure gauge. Stir the water continually
and maintain the temperature exactly constant for ten
minutes, then tap the gauge lightly with the finger and
read the pressure.

A correction of pressure figures should be made ac-
cording to the initial temperature of the gasoline. This
correction should be as follows:

For tests on samples taken at a temperature of 50 to

59 °F, inc., deduct 1 lb. .

For tests on samples taken at a temperature of 40 to 49 "F, inc.,

deduct 2 lbs. ot^ i i f

For tests on samples taken at a temperature below 40 F, deduct

3 lbs. . , , J •

The gravity of the liquid, the temperature of liquid Pf f P «^^^ '"
tube, the pressure at 70°F before venting tube the ^^^''^f^^^ ^> ^V ""k
at 100° F (90°F from Nov. 1st to March 1st) after venting at 70 t
should all be recorded.

Pig-. l:i9
Vapor
Pressure
Apparatus.

480

BULLETIN NUMBER SIXTEEN OF

12A. CARBON RESIDUE IN LUBRICANTS AND DISTILLATES.

(Conradson Method.)

The apparatus consists of:

(a) Porcelain crucible, wide form, glazed throughout, 25 to 26cc
capacity, 46 mm. in diameter.

(b) Skidmore iron crucible, 45cc (1%-oz.) capacity, 65 mm. in
diameter, 37 to 39 mm. high with cover, without delivery tubes and
one opening closed.

(c) Wrought iron crucible with cover, about 180cc capacity, 80
mm. diameter, 58 to 60 mm. high. At the bottom of this crucible a
layer of sand is placed about 10 mm. deep, or enough to bring the
Skidmore crucible with cover on nearly to the top of the wrought iron
crucible.

(d) Triangle, pipe stem covered, projection on side so as to allow
flame to reach the crucible on all sides.

(e) Sheet iron or asbestos hood provided with a chimney about
2 to 2^2 inches high, 2Vs to 2^/4 inches in diameter to distribute the
heat uniformly during the process.

(f) Asbestos or hollow sheet iron block, 6 to 7 inches square,
1% to iVz inches high, provided with opening in center 3^/4 inches in
diameter at the bottom and 3% inches in diameter at the top. The
test shall be conducted as follows:

Ten grams of the oil to be tested are weighed in the porcelain
crucible, which is placed in the Skidmore crucible and these two cruci-
bles set in the larger iron crucible, being careful to have the Skidmore
crucible set in the center of the iron crucible, covers being applied
to the Skidmore and iron crucibles. Place on triangle and suitable
stand with asbestos block and cover with sheet iron or asbestos hood
in order to distribute the heat uniformly during the process.

Heat from a Bunsen burner or other burner is applied with a
high flame surrounding the large crucible, as shown in Fig — , until
vapors from the oil start to ignite over the crucible, when the heat

is slowed down so that the vapor (flame)
will come off at a uniform rate. The
flame from the ignited vapors should not
extend over two inches above the sheet
iron hood. After the vapor ceases to
come off, the heat is increased as at the
start and kept so for five minutes, mak-
ing the lower part of large crucible red
hot, after which the apparatus is allowed
to cool somewhat before uncovering the
crucible. The porcelain crucible is re-
moved, cooled in a dessicator and
weighed.

The entire process should require about
one-half hour to complete when heat is
properly regulated. The time will de-
pend somewhat upon the kind of oil
tested, as a very thin, rather low flash-
point oil will not take as long as a heavy,
Fig. 130 — Conradson Car- thick, high flash-point oil. (See A. S.
bon Apparatus. T. M. 1918 Standards, page 620.)

KANSAS CITY TESTING LABORATORY

481

12B. FIXED CARBON AND ASH IN OIL AND BITUMINOUS

MATERIALS.

The apparatus used is that shown below, or the furnace shown on
page — , such as is used for burning out mineral aggregates, is quite
satisfactory.

Between .4500 and .5500 gram of the material is placed in a 20-
gram platinum crucible having a tightly fitting cover. It is heated
for seven minutes with the full flame of a Bunsen burner, as shown,
or at 950 °C in the electric furnace. With the open flame the crucible
should be supported with its bottom 6 or 8 cm. above the top of the
burner and the flame should be at least 20 cm. high when burning
freely. A shield is used to protect from drafts. The crucible while
remaining covered is placed in a dessicator, cooled and weighed, then
ignited with lid removed until nothing but the ash remains. The loss
is the fixed carbon and the residue is the ash.

Fig. 131— Bunsen Burner for Fixed Carbon.

482

BULLETIN NUMBER SIXTEEN OF

13. EMULSIFYING PROPERTIES OF LUBRICATING OILS.

The oil and water to be emulsified are contained in an ordinary
commercial lOOcc graduated cylinder, 1 1/16 to 1 2/16 inches inside
diameter. An oil or water bath is provided for maintaining the
contents of the cylinder at a temperature of 130°F, except when a
different temperature is specified, both during the stirring and sub-
sequent settling out of the oil from the emulsion. The paddle used
in stirring is a copper plate 4% inches long, between three-fourths
and seven-eighths inch wide and one-sixteenth inch thick. Means are
provided for revolving this paddle about a verticle axis parallel to
and midway between its two longer edges and for keeping the speed
fairly constant at 1,500 r.p.m. A stop should be provided so that when
the paddle is lowered into the cylinder (or bath raised) the distance
from the bottom of the paddle to the bottom of the cylinder will be
about one-fourth inch. To save time otherwise lost in waiting for the
filled cylinders to come to the temperature of the bath it is desirable
that the bath should be large enough to contain several cylinders.

Pour 27cc of the oil to be tested and 53cc of distilled water into a
cylinder, place cylinder in bath and heat to ISCF. Submerge the
paddle and run it for five minutes at a speed of 1,500 r.p.m. Stop the
paddle, withdraw it from the cylinder, and use the finger to wipe off
the emulsion clinging to the paddle and to return it to the cylinder.
Wipe off the paddle with paper so that it will not contaminate the
next sample. Keep the temperature of the cylinder constant at 130 °F
and take readings every minute of the position of the line of demarca-
tion between the topmost layer of oil and the adjoining emulsion.
The first reading is taken one minute after stopping the paddle. With
oils which act normally the rate of settling out of the oil increases up
to a maximum and then decreases and the maximum value in cc per
hour is called the "demulsibility" and is recorded as the numerical
result of the test. Each rate of settling is the average rate cal-
culated from the time of stopping the paddle to the time of reading,
as shown in the following condensed table:

TIME

Time Since

Stopping

Paddle,

Minutes

Reading at
Interface Be-
tween Oil and
Emulsion

Oil

Settled
Out,
c. c.

Rate of

Settling,

c. c. per

Hour

9.50

0

5

12

15

20

80
77
67
63
61

0

3

13

17

19

0

9.55

36

10.02

65

10.05

68

10.10

57

The demulsibility in this case would be 68, the highest value in
the last column. In cases where the maximum rate of settling has
not been reached at the end of one hour, the test is discontinued and
the demulsibility taken as the number of cc that settled out in the
hour. (See page 34, Bulletin 5 of Bureau of Mines on Report of Com-
mittee for Standard of Petroleum Specifications.)

KANSAS CITY TESTING LABORATORY

483

14. A HEAT OF COMBUSTION OR CALORIFIC VALUE.

The apparatus used for the heating value, calorific value or
British thermal units of petroleum products is shown in figures
132, 133 and 134.

Any type of oxygen bomb calorimeter is satisfactory. Among
these are the Atwater, Mahler, Parr and Kroeker bombs. The de-
scription of the operation of one bomb calorimeter is typical of all.

The lower half of the bomb is placed
in the cast iron holder. About one
gram of the oil is weighed to the near-
est 0.0001 gram into the fuel pan and
is placed in the bomb on the fuel pan
holder. If the oil is volatile it is not
advisable to pour the fuel directly into
the fuel pan. For this purpose, small
gelatine capsules weighing .1 gm. are
used and may be filled with ignited
asbestos and into this the light oil is
discharged from a weighing pipet.
The capsule is immediately closed
leaving a minimum amount of air
space. A similar capsule has been
previously weighed and its calorific
value determined. A stock of stand-
ardized capsules should be kept on
hand in an air tight receptacle. The
platinum fuse wire is cut equal in
length to the taper pin wrench which
is connected to the terminal, being
careful that it does not touch the pan.
The wire is bent down so that it is
covered by the oil or by the lips of the
capsule. The upper half of the bomb
is carefully fitted on the lead gasket to the lower half.
The nut is screwed down over the upper half bemg
careful not to cross the threads. The bomb nut is now
tightened by the use of a long wrench, being careful to
cause no sudden jerking or vibrating which wi 1 throw
the oil from the pan. The bomb is now carefully litted
out and placed on the swivel table and connected with
the oxygen piping. The valve in the top of the bomb
is opened about one turn and the valve in the oxygen
cylinder is carefully and slowly opened so that the pres-
sure in the bomb as shown by the indicator rises to 6m
pounds. The bomb valve is now closed and the oxygen
cylinder is closed. Exactly 1900. grams of water at a
temperature of about 4° below room temperatuie s
weighed into the calorimeter water bucket, ihis s
placed in the calorimeter container. The bomb is con-
nected with the electric wire and is introduced into tne
water, being careful to place it in the center of the
bucket. Two 100 watt lamps placed in P^^f l'''. .j^ .^^ '"

th the fuse wire when a ^0/01*/ .H,s
^'ir.ir.o. TViP snrinff motor is placed in .^eiits

Fig. 132-

-Emerson Bomb Ca-
lorimeter.

f

1

^=-\ /— '1

I — <J — 1

— ' 1

1 ■•

' *

series wit
used for firing.

We 1 K li 1 II »
Holtlo for
L 1 q u I <1
Fuels, Ktc.

484

BULLETIN NUMBER SIXTEEN OF

with a 60 watt lamp on a 110 volt circuit. The cover is put on, the
connections to the bomb wire are made and the stirrer is introduced
as far down as it will go. It should not touch the bomb. The ther-
mometer is introduced and stirring is continued for about five min-
utes. The temperature is read and the stirring continued for exactly
five minutes and the temperature is again read and the charge is
fired by quickly throwing in the switch and withdrawing it. The
stirring is continued for five minutes, the temperature being read at
minute intervals or at the end of five minutes unless extreme ac-
curacy is required. The stirrer is then run for an additional five
minutes and the temperature is again read. The thermometer is
corrected in accordance with the corrections furnished by the Bureau
of Standards. The radiation corrections may be applied to each one
minute interval but for ordinary purposes one-fifth of the radiation
for the five minute period before firing is applied on the 5 minute pe-
riod immediately after firing and four-fifths of the radiation in the
third five minute period is applied on the five minute period imme-
diately after firing. The calorimeter constant (usually about 2400)
is determined by a blank test using exactly 1 gram of benzoic acid.
This constant always remains the same with the same calorimeter

but must be determined each time
a change is made in the calori-
meter. In the case of oil in which
it has been necessary to use the
capsule the correction made must
be applied for the calorific value
of the capsule. This is most con-
veniently applied to the corrected
net rise in temperature of the
thermometer. To convert British
thermal units per pound to calories
per gram, multiply by five-ninths.
To obtain the water evaporative
power, multiply the B. T. U. per
pound by 1.035
„,^„;,^^ and divide by

1000. To obtain
the B. T. U. per
gallon, multiply
the B. T. U. per
pound by the
Oi/jen weight per gallon.

Fig. 134 — Calorimeter Oxygen Connections.

14B. HEAT OF COMBUSTION FROM GRAVITY OF FUEL OILS.

An approximation of the heating value of fuel oil can be obtained
by the following formula:

B. T. U. per lb. = 18700 + 40 (°Be'— 10).

KANSAS CITY TESTING LABORATORY 485

15A. TOTAL SULPHUR IN PETROLEUM PRODUCTS.

The apparatus is shown in Fig. 132 and may be any standard
oxygen bomb calormieter.

The determination may be made at the same time as a determina-
tion of calorific value.

Place 20cc of distilled water in the bottom of the bomb. Use 0 5
to 1.0 g. of oil, weighed into the sample cup of the bomb, when the
material is not volatile. For volatile materials use either a small
gelatine capsule or a very small glass bulb of the type used in the
ultimate organic analysis of such liquids. If the latter is used, place a
few drops of sulphur-free alcohol in the sample cup to start combus-
tion. Arrange the ignition mechanism and close the bomb tightly.
Admit oxygen until a pressure of 35 to 40 atmospheres is reached.
The higher pressure is preferable. Ignite. Place the bomb in cold
water for 20 minutes. Shake vigorously for 25 seconds and allow
to drain for five minutes. Release the pressure rather slowly and
open the bomb. Using distilled water in a wash bottle with a very
fine jet, wash the wires and cover thoroughly, allowing the washings
to collect in the bomb. In the same way wash the sample cup held by
small tongs. Transfer the solution from the bomb to a 500cc beaker
and wash the inside of the bomb thoroughly. The total volume of
solution thus obtained need not exceed 350cc. Avoid any loss of
material by spattering or otherwise in the various washings.

Filter the solution through a washed filter paper into another
beaker, of smaller size if possible. Wash the filter thoroughly. Add
2cc of HC 1 (sp. gr. 1.20) and lOcc of saturated bromine water. To
the hot solution add lOcc of a 107c barium chloride solution, as
hot as possible, in a very fine stream or dropwise so that 30 to 45
seconds are required. Stir vigorously with a glass rod during this
addition and for four minutes afterward. Allow the precipitate to
settle for one hour on a steam bath. Cool and let stand for at least
one hour at room temperature. Filter carefully through a suitable
ashless filter paper and wash the precipitate with hot water, first
by decantation and then on the filter till free from chloride. Trans-
fer the wet filter paper and precipitate to a weighed platinum crucible.
Dry carefully over a low flame. Allow the filter paper to burn away
and then ignite until the precipitate is just burned white. Cool in a
desiccator and weigh. From the increase in weight which is barium
sulphate, calculate the percentage of sulphur as follows:

grams of Ba SO, X 13.734

Percentage of Sulphur = — ;; — - '

grams of oil used

486

BULLETIN NUMBER SIXTEEN OF

15B. SULPHUR BY THE CHEMICAL BOMB.

To the perfectly clean and dry bomb as shown in Fig. 135 add ten
grams of pure sodium peroxide.

Fig. 135 — Parr Sulphur Bomb.

Then add one gram of finely pulverized potassium chlorate.

Thoroughly mix them by shaking.

Add from a weighing pipe approximately one-half gram of oil,
which would be about twenty drops.

Mix thoroughly by shaking.

Fit the cover on tightly and screw down the cover with a wrench.

Ignite by holding the bottom of the fusion cup in the small
pointed flame of the Bunsen burner for a moment (or electrically).

Remove from the flame as soon as the reaction has commenced
which is indicated by the lower portion of the cup becoming a dull red.

After the charge has ignited, the bomb may be cooled in cold
water (or maintained in cold water during ignition).

It is now rinsed off with distilled water and placed in a beaker.

The cover is rinsed off with hot distilled water and hot distilled
water is squirted into the fusion cup until solution is complete.

The fusion cup is now rinsed off thoroughly with hot distilled
water.

The contents of the beaker are boiled to complete solution and
filtered.

Hydrochloric acid is added to the filtrate until the reaction is
distinctly acid.

Ten cubic centimeter of 5 to 10% barium chloride are now added
and barium sulphate is precipitated and filtered in the usual manner.

The barium sulphate is weighed.

This value X 27.47 gives the percentage of sulphur.

Correction should be made for sulphur present as impurities in
the chemicals used.

KANSAS CITY TESTING LABORATORY 487

15C. SULPHUR BY THE ESCHKA METHOD.

This method is not good for oils, in most instances giving a low
result, but may be used where accuracy is not necessary. Weigh out
approximately 1 gram of the oil and mix it with 2.5 grams of sodium
carbonate and 5 grams of calcined magnesia in a platinum dish or
crucible. Heat gradually increasing the temperature until the mass
has a low red color and the mixture on cooling has a grayish tint.
Cool and wash into a 500cc beaker with distilled water and add about
Ice of bromine. Mix until the bromine is thoroughly dissolved and
allow some time for the bromine to react. Now add hydrochloric acid
until the reaction is decidedly acid, the beaker being covered in the
meantime to prevent any mechanical loss. Filter off and wash any
undissolved residue. Precipitate in the usual manner with barium
chloride and weigh as barium sulphate.

Weight of Barium Sulphate x 13.73 = % Sulphur.

15F. SULPHUR IN CORROSIVE FORM.

A clean strip of pure sheet copper about one-half inch wide and
three inches long is heated to redness in a Bunsen flame, and while
red hot dropped into alcohol. The strip is then allowed to dry as
quickly as possible in the air and dropped into a sample of the oil
contained in a clean test tube about half the length of the copper
strip being submerged. The test tube is then closed with a stopper
and left to stand over night at a temperature of 150 °F.

At the end of this time the copper strip is removed and washed
free from oil with gasoline. It is then compared with a similar strip
of copper freshly cleaned by heating to redness in a Bunsen flame
and dropping into alcohol while hot.

If sulphur or corrosive sulphur compounds are present in the oil
the copper test strip will appear discolored when compared with the
freshly cleaned copper, since elementary sulphur attacks copper.

488

BULLETIN NUMBER SIXTEEN OF

15D. SULPHUR IN NAPHTHAS AND ILLUMINATING OILS.

The apparatus is shown in Fig. 136.

Pass two strands of new cotton wicking about 4.5 in. long
through the Vs-in. diameter wick tube so that they are not twisted,
but parallel in the wick tube. Trim the wick with very sharp scissors.
Pour into the clean dry lamp about 20cc of the oil to be tested, insert
the wick and cork and weigh the assembly with an accuracy of
0.001 g. It is advisable to make a blank determination at the same
time and under the same conditions by burning sulphur-free alcohol
in a similar lamp.

Fig. 136 — Sulphur Apparatus for Illuminating Oils.

Rinse out the absorber containing the glass beads thoroughly
with distilled water and add exactly lO.Occ of the standard sodium
carbonate solution from an accurately calibrated burette, allowing
the burette to drain for three minutes before taking the reading.
Rinse the chimney and the spray trap with distilled water, dry the
chimney and connect both to the absorber as shown in Fig. 136. Set up
the apparatus for the blank determination in exactly the same manner
and using exactly lO.Occ of the sodium carbonate solution. Apply
gentle suction to both absorbers, light both the weighed oil lamp
and alcohol lamp and then place in position under the chimneys so
that the tops of the wick tubes extend into the chimneys not more
than one-sixteenth inch. Adjust the wick height and the suction so
that the flame is steady, free from smoke and approximately one-quar-
ter inch high. This requires that the wick be flush with the top of the
wick tube for naphthas, and a little higher for illuminating oils. • The
room must be free from drafts. The suction on the blank should be

KANSAS CITY TESTING LABORATORY 489

so adjusted that air is drawn through both determinations at the
same rate. Continue burning for about two hours, or less if the
sulphur content of the oil is high. During this time the oil should be
consumed at the rate of about 1 gm. per hour.

Extinguish the flames and stop the suction on both absorbers.
Weigh the oil lamp immediately and calculate by difference the
weight of oil consumed. Working with the blank first, disconnect the
spray trap and chimney and wash them thoroughly with methyl orange
solution, using a wash bottle with a very fine jet and collecting the
washings in the absorber. The amount of solution required for wash-
ing should not exceed 35cc. Carefully titrate the very faintly yellow-
ish solution in the absorber with standard HCl, added to the suction
side of the absorber from an accurately calibrated burette. During
this titration, the contents of the absorber should be agitated care-
fully, either by blowing through a rubber tube held between the
operator's lips and connected at the other end with the chimney side
of the absorber or else by the use of a suitable rubber syringe bulb.
As the end point is approached, draw the liquid back into the chimney
side between each addition of acid and then blow it into the suction
side, agitating as before. As soon as the first permanent pink color
appears, the end point has been reached. Read and record the volume
of HCl solution used.

Rinse the chimney and spray trap used in the actual determina-
tion into the absorber to which they were connected, exactly as pre-
scribed for the blank. If the methyl orange solution in the absorber
has a pink color, too much oil has been burned and the determination
must be repeated, burning for a shorter time. Titrate just as in the
blank, making sure that the absorber is cold. Read and record the
volume of HCl solution required.

Calculate the sulphur content of the oil by substituting the proper
values in the following formula:

Percentage of Sulphur =

(HCl for blank, cc — HCl for sample, cc) X 0.1

grams of oil burned

If a blank is not run, the formula is:

(Na=C03,cc — HCl.cc) X 0.1

Percentage of Sulphur = ., , '

grams of oil burned

These formulae are correct only for the standard solutions speci-
fied. Ice of each being equivalent to 0.001 g. of sulphur. The use of
solutions of any other strength, such as N/10, is satisfactory and the
percentage of sulphur may be calculated.

APPARATUS.

Absorber of chemically resistant glass, about l^Occ .^city
containing glass beads or short pieces of elass rod in the suction side
as shown.

490

BULLETIN NUMBER SIXTEEN OF

Fig. 137 — Sulphur Photometer.

Chimney of chemically resistant glass connected with the ab-
sorber by a rubber stopper.

Spray trap of chemically resistant glass connected with the ab-
sorber by a rubber stopper.

Small lamp of about 25cc capacity. This lamp may conveniently
consist of a 25 to 35cc Erlenmeyer flask and a cork carrying a short
section of glass tubing about one-eighth inch in inside diameter.
The cork must be grooved along the sides so that air may enter the
flask while the oil is being consumed.

Ordinary cotton wicking.

Filter pump or other means for continuous suction and rubber
tubing to connect with spray trap.

SOLUTIONS REQUIRED.

Hydrochloric acid — Solution containing 2 275 g. HCl per liter and
carefully checked for accuracy.

Sodium Carbonate — Solution containing 3.306 g. Na-COi per liter.
Exactly 10 Occ should be required to neutralize lO.Occ of the hydro-
chloric acid solution.

Methyl Orange — Solution in distilled water, containing 0.004 g.
methyl orange per liter.

KANSAS CITY TESTING LABORATORY

491

15E. SULPHUR TESTS FOR TURPENTINE SUBSTITUTES.

Place 25 grams of dry white lead in a small porcela'n dish and
mix thoroughly with 50cc of the turpentine substitute to bs tested.
Cover with a watch glass, place en a steam bath for two hours,
remove, and observe the color after eighteen hours. There shall be
no appreciable darkening of the white lead. This test must be per-
formed in an atmosphere free from hydrogen sulphide.

Place five drops of the oil on clean white filter paper and allow
the liquid to evaporate at room temperature, away from direct sun-
light. There should be no oily spot left after thirty minutes.

16A. CAREON AND HYDROGEN IN PETROLEUM PRODUCTS.

The most convenient method is to burn the oil in a special calori-
meter bcmb of the type of the Kroeker. (Fig. 138.)

The bomb must be perfectly dried on the inside by drawing dry
air through the apparatus.

Approximately one gram of oil is now burned exactly as in the
determination of heat of combustion.

The bomb is taken from the calorimeter and is connected on the
tube side with Drechsel bottles containing moist soda lime in the
first bottle and calcium chloride in the second bottle. The outlet of

the bomb is now connected in series with a
U tube containing granulated zinc to de-
compose any acid formed in the combustion,
with a glass stoppered U tube filled with
calcium chloride of about 10 mesh size, with
a glass stoppered U tube filled in the first
arm with soda lime containing 10% water
and the upper part of the second arm with
calcium chloride connected then with an
aspirator bottle.

The outlet of the bomb is gradually
opened so that at lea?t ten minutes is re-
quired to release all of the pressure.

The bomb is now heated and the aspirator
is run at such a rate that about five gallons
of air are drawn through the bomb during a
period of between one and two hours. The
carbon is calculated from the increase in
weight of the soda limo U tube and the
hvdrogen is calculated from the increase in
weio'ht of the calcium chloride U tube.

CO.. X 27 273

f^', carbon

weight of sample

HO X 11.190

— = % hydrogen

weight of sample

Fig

Kroeker Bomb.

492 BULLETIN NUMBER SIXTEEN OF

16B. DETERMINATION OF NITROGEN IN PETROLEUM OR
ASPHALT, BY THE KJELDAHL METHOD.

Five grams of the sample are weighed into a pyrex Kjeldahl digest-
ing flask. Fifty cc of the digestion mixture composed of concentrated
sulphuric acid containing 20'/c of phosphorous pentoxide is added to
the flask. About one-third gram of mercuric oxide is added and the
contents of the flask are heated with a strong flame until the solution
has become pale yellow or colorless. The digested material is now
cooled, diluted with about 150cc of water and neutralized with strong
caustic soda solution. Zinc shavings and some Potassium Sulphide
are added. The flask is quickly connected with the condenser tube
and the ammonia is distilled off into a 25cc of N/10 sulphuric acid.
The excess of acid is titrated with N./IO alkali. Each cubic centimeter
of sulphuric acid consumed is equivalent to .001404 gram of nitrogen.

17. DOCTOR TEST FOR GASOLINE.
Reagent.

Sodium plumbite or "doctor" solution — Dissolve 125 grams of
sodium hydroxide (NaOH) in a liter of distilled water. Add 70 grams
of litharge (PbO) and shake vigorously for 15 or 30 minutes or let
stand with occasional shaking for at least a day. Allow to settle and
decant off the clear liquid. Filtration through a mat of asbestos may
be employed if the solution does not settle clear. The solution should
be kept in a bottle tightly stoppered.

Test.

Shake vigorously for about 15 seconds two volumes of gasoline
and one volume of the "doctor" solution. Note color. A small pinch
of flowers of sulphur should be added and the tube again shaken for
15 seconds and allowed to settle. The quantity of sulphur used should
be such that practically all of the sulphur floats on the sui'face,
separating the gasoline from the "doctor" solution.
Interpretation.

If the gasoline is discolored or if the sulphur film is so dark that
its yellow color is noticeably masked, the test shall be reported as
positive, and the gasoline condemned as "sour." If the liquid remains
unchanged in color and if the sulphur film is bright yellow, or only
slightly discolored with gray or flecked with black, the test shall be
reported negative and the gasoline considered "sweet."

KANSAS CITY TESTING LABORATORY

493

18A. OLEFINS OR UNSATURATED HYDROCARBONS AND

REFINING LOSS IN PETROLEUM PRODUCTS—

WITH BABCOCK BOTTLE.

Use apparatus and equipment as shown in Figs. 139-140.

Weigh up a clean and dry 30'7f Babcock cream bottle, add to it
exactly 5cc of the oil to be tested. Weigh again, giving the amount
of oil used. Cool in ice water and add lOcc of concentrated commer-
cial sulphuric acid, letting the acid run down the sides of the bottle.
Shalie while cooling in the ice water. Keep stoppered with a rubber
stopper. Let stand for one-half hour with occasional shaking and
constant cooling. Add sufficient concentrated sulphuric acid (com-
mercial) to bring the reading about to the top of the scale on the
neck of the bottle. Centrifuge for five minutes in the No. 1 centrifuge
with the resistance at the first notch from the left. This gives a
speed of 1,000 r.p.m. Keep the rubber stopper in while centrifuging
so that there will be no evaporation. The stopper shall be large
enough so that it is not foi'ced into the bottle.

The reading on the neck of the bottle divided by five is the net
amount of saturated hydrocarbons contained. This multiplied by
twenty and taken from 100 gives the per cent of unsaturated hydro-
carbons. For great accuracy the oil may be corrected for specific
gravity and temperature and for the amount adhering to the sides
of the pipet in which case the weighings are used. The waste acid
from the Babcock bottle is poured into a bottle from which the sul-
phuric acid may be recovered by separating the oil and oxidising the
organic material in the acid.

Fig. 139 — Hand Centrifuge.

Fi,?. I'JO — Olefin Tubts.

494

BULLETIN NUMBER SIXTEEN OF

LlO ccio

18B. METHOD USING A lOCC GLASS STOPPERED CYLINDER.

Use apparatus and equipment as shown in Fig. 140.

Add exactly 5cc of the oil to be tested to the cylinder and 2cc of
sulphvric acid of gravity 1.84. Shake thoroughly for about five
minutes and place in centrifuge and centrifuge at the rate of 1,000
r.p m. for five minutes. The shrinkage of the oil in cubic centimeters
X 20 is the percentage of olefins.

ISC. REFINING LOSS OF PETROLEUM PRODUCTS.

Use the color tube as shown in Fig. 98.

To a 50cc color tube that is graduated in .Ice and glass stoppered,
add 45.0cc of the oil. Add exactly Ice of 66° Baume' sulphuric acid.
Shake thoroughly for about five minutes. Set vertically in a rack
for at least one hour and preferably over night. The increase in
volume of the acid in the bottom of the tube X 2-2/9 is the refining
loss.

19A. METHOD FOR DETERMINING AROMATIC AND PARAF-
FIN HYDROCARBONS IN PETROLEUM PRODUCTS.

The apparatus is shown in Fig. 141. The flask
containing 30cc of fuming nitric acid (specific grav-
ity 1.52) is cooled to — 10°C by a salt ice freezing
mixture. The separatory funnel is filled to the lOcc
mark with the oil under test. The oil is run drop
by drop with continuous shaking into the cooled
acid during a period of not less than 45 minutes.
With uncracked petroleum products 15 minutes is
sufficient. The mixture is allowed to stand 15 min-
utes after completion of the reaction and then
enough nitric acid (ordinary concentrated) at — 10°
temperature is added to the contents of the flask
until the- oil under the surface is brought into the
graduated neck. The volume is read when the neck
is at room temperature, the body of the flask being
in the freezing mixture. This volume repi'esents
the paraffin hydrocarbons.

The mixture is transferred to a separatory fun-
nel, the lower layer run off into a 500cc measuring
flask containing 150cc of water. The neck should
be graduated for a lOcc portion into 1/lOcc. The
temperature will rise in proportion to the amount
of olefins and aromatics present and more or less
oil will separate according to the amount of paraffin
hydrocarbons present.

The unattacked oily layer in the separatory funnel

is washed with water and then examined for specific

gravity and boiling point. The aqueous layer of

nitric acid is warmed for 15 minutes to dissolve as

completely as possible the resinous substances

formed. The cooled liquid is shaken with lOOcc of

ether, the aqueous layer separated and the ether

layer again washed free from acid with water, then

^f^' ^A^ ^^^.^ with a solution of caustic potash containing 50

DetermTna^ grams of KOH in 500cc of water with 50cc of

tion. alcohol.

KANSAS CITY TESTING LABORATORY 495

The caustic potash is drawn off and again the ether layer is
washed with water. It is now dried with calcium chloride, filtered,
the ether evaporated and the residue weighed. The residue consists
of reddish brown oil, aromatic nitro-derivatives. The weight divided
by .115 gives the percentage of aromatic hydrocarbons.

The difference between the aromatic and cyclic hydrocarbons and
the paraffin hydrocarbons and 100% is the amount of olefins. This
may be checked by direct determination as shown under olefins.

19B. SHORT METHOD FOR AROMATIC AND CYCLIC HYDRO-
CARBONS.

Distillation of 800cc of the hydrocai'bons under examination may
be made in a one liter distilling flask in accordance with the appar-
atus set forth in Fig. 120. Cuts may be made at 9b° , 120° and 150 °C
and the percentage of aromatic compounds calculated from the spe-
cific gravity using the following specific gravities as the basis:

Specific Gravity Specific Gravity of
of Aromatic Non-x4.romatic

Temperature of Cut Hydrocarbon Hydi'ocarbon

95°C 0.880 0.720

120°C 0.871 0.730

150°C 0.869 0.760

This is in accordance with the Bulletin No. 114 of the Bureau of
Mines, page 95.

20A. FREE FATTY ACIDS.

Accurately weigh 10 g. of the oil into an Erlenmeyer flask, add
50cc of 95 9p alcohol which has been neutralized with weak caustic
soda, and heat to the boiling point. Agitate the flask thorouglily in
order to dissolve the free fatty acids as completely as possible.
Titrate while hot with aqueous tenth-normal alkali, free from car-
bonate, using phenolphthalein, alkali blue or turmeric as an indicator,
agitating thoroughly after each addition of alkali.

To express results as percentage of oleic acid, use the following
equation:

One cc of tenth-normal alkali = .0282 gram of oleic acid. Alkali.
Ice of which is equivalent to 0.5% of oleic acid, may be used.
(A. S. T. M. Method, 1918 Standards, page 620.)

496 BULLETIN NUMBER SIXTEEN OF

20B. COMBINED FATTY ACIDS OR FATTY OILS.

Weigh 10 grams of oil into a 350cc Erlenmeyer flask. Add from
a pipet 50cc of the alcoholic potassium hydroxide solution followed
by 25cc of the purified benzene (C.H.:). Connect with a reversed con-
denser. Boil on steam bath or electric hot plate for 90 minutes, shak-
ing occasionally. Remove and add 25cc of neutral gasoline, and titrate
with the half-normal hydrochloric acid solution after adding two or
three drops of the phenolphthalein indicator solution until the pink
color is destroyed. The absence of the pink color may be determined
after the titration has begun, by allowing the solution to stand at
rest, approximately a minute, and noting the color of the lower zone.
Run two blanks with the same mixture of alcoholic potassium hydrox-
ide solution and purified benzene. From the difference between the
number of cubic centimeters of half-normal acid required for the
blanks and for the determination, the percentage of fatty oil may be
calculated as follows:

No. of cc N/2 acid used x .02805 x 100

= per cent of fatty oil

.195 X weight of oil taken

Solutions:

(a) Approximately half -normal alcoholic potassium hydroxide.
Dissolve 30 grams of potassium hydroxide sticks (or an equivalent
amount of sodium hydroxide sticks) in lOOOcc of purified 92-95%
ethyl alcohol. Allow to settle and filter.

(b) Purified benzene. This may be prepared as follows: To
lOOOcc of "90Sr benzol" add a stick of sodium hydroxide, boil for an
hour, using a condenser loop inside the neck of the flask. Transfer to
a large separatory funnel and add sufficient water to cause the liquid
to separate into two zones. Draw off the lower zone and discard.
Wash the benzene with water once. Transfer the washed benzene to
an Engler distillation flask and distill up to 82 °C, discarding the
residue.

(c) Standard solution of half-normal hydrochloric acid.

(d) Phenolphthalein Indicator. Dissolve one gram of phenolph-
thalein in lOOcc of 95 9f ethyl alcohol.

(e) Neutral gasoline.
(See also method IIC.)

21. FLOC TEST.

Take a hemispherical iron dish and place a small layer of sand
in the bottom. Take a 500cc Florence or Erlenmeyer flask and into
it put 300cc of the oil (after filtering if it contains suspended mat-
ter). Suspend a thermometer in the oil by means of a cork slotted on
the side. Place flask containing the oil in the sand bath and heat
bath so that the oil has reached a temperature of 240 °F at the end of
one hour. Hold oil at temperature of not less than 240 °F nor more
than 250 "F for six hours. The oil may become discolored but there
should be no suspended matter formed in the oil. The flask should
be given a slight rotary motion and if there is a trace of floe, it can
be seen to rise from the center of the bottom.

KANSAS CITY TESTING LABORATORY

497

22. CORROSION AND GUMMING TEST OF GASOLINE AND

NAPHTHA.

The gasoline when subjected to the corrosion test shall show no
black corrosion and no weighable amount of gum.
Directions for making test:

The apparatus used in this test consists of a freshly polished
hemispherical dish of spun copper, approximately 3V2 inches in diam-
eter.

Fill this dish within three-eighths inch of the top with the gaso-
line to be examined and place the dish upon a steam bath. Leave the
dish on the steam bath until all volatile portions have disappeared.

If the gasoline contains any dissolved elementary sulphur the
bottom of the dish will be blackened.

If the gasoline contains undesirable gum-forming constituents
there will be a weighable amount of gum deposited on the dish. Acid
residues will show as gum in this test.

23. PENETRATION OF PETROLEUM ASPHALTS AND OTHER

BITUMINOUS MATERIALS.

The apparatus used for this test is that shown in
Figs. 142, 143 or 144.

The penetration is the consistency of a bituminous
material expressed as the distance that a standard
needle vertically penetrates a sample of the ma-
terial under known conditions of loading, time and
temperature. When the conditions of test are not
snecifically mentioned the load, time and tempera-

ture are understood to be 100 grams, 5 seconds,
25 °C (77°F) respectively and the units of penetra-
tion indicate hundredths of a centimeter. The con-
tainer for holding the material to be tested should
be a flat bottomed cylindrical dish 2,1, inches in
diameter and IVs inches deep or the American Can Co.
Gill style ointment box, deep pattern, three ounce
capacity.

The needle is a cylindrical steel rod two inches
long and wfth a diameter of 0.04 inch and turned
on ?ne end to a sharp point having a taper of one-
Quarter inch. The bath for the sample and the
^ene limeter should hold at least ten 'ters of waten
The sample should be melted at the lowest po.ssible
temperZre and stirred until it is homogenoous a d
fre- from air bubbles. It is then poured "i to the
sample container to a depth of about three-quarters

temperature of penetration for one hour.

In making the test, the sample is j"-™;',/ J„tk\. "cltlct
needle loaded with the specified weight is adjusted

Fig. 142— N.Y.T. L
Penetrometer.

498

BULLETIN NUMBER SIXTEEN OF

with the sui'face of the sample. This may be accomplished by making
contact of the actual needle point with its image reflected by the
surface of the sample or contact may be meted by slightly turning
the container so that a faint scratch on the surface of the bitumen is
observed. The needle is then released for the specified time and the
distance measured by the means provided with the machine. At least
three tests shall be made at different points on the surface of the
sample and after each test the needle shall be wiped clean of all
bituminous matter. The reported penetration is the average of at
least three tests whose values do not differ more than four points
between the maximum and minimum. Other conditions for penetra-
tions particularly for oil asphalt filler and roofing material shall be
the following:

At 0°C (32°F) 200 grams weight 60 seconds.
At 46.1°C (115°F) 50 gram weight 5 seconds.

a

6'--^

C- —

j^

-V

^^;f--v^.

Fig. 143 — Dow Penetrometer.

Fig. 144 — Humboldt
Penetrometer.

KANSAS CITY TESTING LABORATORY

499

24. DUCTILITY OF BITUMINOUS MATERIALS.

The ductility of an asphalt cement or semi-solid bitumen is the
distance which it will elongate before breaking when a briquet of
the material is pulled at a specified rate of speed and at a specified
temperature. The temperature is to be 77 °F and the rate of pulling
is five centimeters per minute unless otherwise required.

The bituminous material is melted preferably in an oven at 325 °F
until it is uniformly and thoi'oughly fluid. The mold herein de-
scribed is assembled on a plate so as to prevent the material from
sticking to it. the surface of the plate and the inside surfaces of the
mold being thoroughly amalgamated.

In filling, the bitumen is poured in a thin stream back and forth
from end to end of the mold until it is more than level full. It is
left to cool for at least 30 minutes when the excess of bitumen is cut
off with a hot spatula so that the mold is just level full.

The briquet with the mold and plate is now placed in the water
bath and kept at a temperature of 77 °F for at least m> hours, when
the briquet is removed from the plate and the side pieces detached.
The briquet is now fastened in the ductility machine by means of
the pins and ring and pulled at the uniform rate of five centimeters
per minute. The water shall completely cover the briquet. The tem-
perature shall be within .2° F of 77° F at
all times. The average of three tests
shall be taken. The ductility machine
shall provide for three briquets being
pulled at one time. The variation from
five centimeters per minute in speed
Fig. 145— Ductility Mold shall not be more than 57r.

The dimensions of the mold are as follows:

Total length (internal) 7.45-7.55 cm.

Distance between clips 2.97-3.06 cm.

Width of clips at mouth 1.98-2.02 cm.

Width of briquet at minimum cross-section

(halfway between clips) 0.99-LOl cm.

Thickness of briquet throughout 0.99-1.01 cm.

'i '''U'^B.O'-P"'" .^^'-: ''-'^ ill!

H

Fig. 146— Ductility .Apparatus.

500

BULLETIN NUMliER SIXTEEN OF

25. LOSS ON HEATING OF OIL AND ASPHALTIC COMPOUNDS.

The loss in weight by oil and asphaltic compounds when they are
heated in an oven at a temperature of 163°C (325°F) is determined
on 50 grams of the water free substance contained in a flat bottomed
dish, the inside dimensions of which are approximately 2^% inches
in diameter and 1% inches deep (this is the 3 ounce Gill style oint-
ment box, deep pattern).

The oven in which the substance is to be heated is brought to
temperature before the sample is introduced and the temperature of
the sample under test shall be regarded as that of a similar quantity
of the same material immediately adjoining it. in the oven in which
the bulb of a standardized thermometer is immersed. The oven may
be any well constructed type either circular or rectangular and the
source of heat may be either gas or electricity. The samples under
test rest in the same relative position in a single row upon a per-
forated shelf 9.75 inches in diameter as shown in Fig. 147. A good
type of oven is also shown in Fig. 148. The shelf is suspended by
a vertical shaft midway in the oven which is revolved by mechanical
means at the rate of from 5 to 6 R. P. M.

This method of test is well adapted for the determination of the
carbonization value of internal combustion engine lubricating oils
25 grams of the oil are heated as above at 500 °F to constant weight.
The carbonization value is the percentage of carbonized residue.

(See page 277, line 13.)

SECTION A-B

ft Bo1e« ftnd l^tbs^
Spac«d EquaU/

TOP VIEW

Fig-. 147— Heat Loss Shelf.

KANSAS CITY TESTING LABORATORY

501

26. ASPHALT IN OIL AND ASPHALTIC COMPOUNDS.

Fifty grams of the crude oil, fuel oil, lubricating oil, road oil or
other material are weighed into a three ounce Gill style ointment
box, deep pattern, and placed in an oven heated either by electricity
or gas and with good circulation to a temperature of approximately
500°F. Heat is maintained until the consistency of the residue is
such that at a temperature of 77 °F it has a penetration of 100. The
amount of asphalt is reported in terms of the 100° penetration ma-
terial.

At least two tests should be made on each sample both as checks
and to facilitate obtaining results on the basis of 100° penetration.
When one sample is softer and one harder than 100° penetration the
percentage of asphalt may be obtained by interpolation.

Fig. 148— Oven for Asphalt Determination.

502

BULLETIN NUMBER SIXTEEN OF

27A. SOLUBILITY IN PETROLEUM ETHER— PRECIPITATION
NUMBER OF LUBRICATING OILS. (A. S. T. M.)

This method is commonly used for steam cylinder stocks and
black oils and may be used for other lubricating oils.

Exactly lO.Occ. of the oil to be tested is measured in each of two
clean and dry centrifuge tubes at room temperature. Each tube
shall be filled to the lOOcc. mark with U. S. P. petroleum benzine
and closed tightly with a softened cork (not a rubber stopper). Each
tube is then inverted at least 20 times, allowing the liquid to drain
thoroughly from the tapei'ed tip of the tube each time. The tubes
are then placed in a v/ater bath at 90° to 95 °F for five minutes. The
corks are momentarily removed to relieve any pressure and each
tube shall again be inverted at least 20 times exactly as before. The
success of this method depends to a large degree upon having a
thoroughly homogeneous mixture which will drain quickly and com-
pletely from the tapered tip when the tube is inverted.

The two centrifuge tubes are
then placed in the centrifuge on
opposite sides and are whirled at a
rate of 1,400 to 1,500 r.p.m. or
equivalent for 10 minutes. The
volume of sediment at the bottom
of each tube is read and recorded,
estimating to 0.05cc, if possible.
The tubes are then replaced in the
centrifuge, again whirled for 10
minutes as before, and removed for
reading the volume of the sedi-
ment as before. This operation is
repeated until the volume of sedi-
ment in each tube remains constant
for three consecutive readings.
In general, not more than four
whirlings are required.

The volume of the solid sediment
at the bottom of each centrifuge
tube is read, estimated to O.lcc. or
closer if possible. If the two read-
ings differ by not more than O.lcc,
the mean of the two shall be re-
ported as the "Precipitation Num-

!.>;„ 1 iQ c. 1 v.1-^ , . ber." If the two readings differ

f- ig. 149 — Solubility Apparatus. u _ ii. n i ^ j

by more than O.lcc, two more de-
terminations shall be made and the average of the four determinations
shall be reported. See figures — and — for apparatus.

The centrifuge should be capable of whirling at least two lOOcc.
centrifuge tubes filled with water at the required speed.

Preferred forms of centrifuge shall have a diameter of swing
(tip to tip of whirling; tubes) of 15 to 17 in. and a speed of at least
1,500 r. p. m. or equivalent. The proper speed may be calculated
from the following formula in which D represents the diameter of
swing (tip to tip of whirling tubes) of the centrifuge used:
16 r. p. m. = 1,500

L/ s fo e TA.e

^ut^^et. ■- — \

1

4

^ "'"'""' ""

\

sec TiOA/A.

: £4.ev^-r*0^

KANSAS CITY TESTING LABORATORY 503

27A-2. SOLUBILITY IN PETROLEUM ETHER AND TAR IN
CYLINDER STOCK, FLUX AND ASPHALTS.

The apparatus is shown in figure 149.

Weigh out ten grams of the cylinder stock into a 200cc. Erlen-
meyer flask (use 1 gram of asphalt).

Add lOOcc. of U. S. P. Petroleum Benzin (84-86°Be' Petroleum
Ether).

Stopper and shake until the oil is completely dissolved.

Allow the flask to stand at least one hour, tightly corked.

Prepare a filter cone obtainable from any laboratory supply
house, as alundum filter cone R A 232 Porous.

Boil in distilled water, wash thoroughly, dry, and ignite. Cool
and weigh.

Attach the apparatus shown to the filter pump and pour the
solution of cylinder stock into the porous alundum filter cone.

Press the cone down if necessary so that the rubber band around
the top of the cone perfectly seals it.

Drain the Erlenmeyer i'lask as thoroughly as possible and wash
it out using altogether 50cc. additional of the U. S. P. Petroleum Ben-
zin pouring about lOcc. through the filter each time.

Care must be taken to wash thoroughly the top part of the alun-
dum cone and to so distribute the washing that the petroleum benzin
comes through perfectly colorless at the last.

Draw air through the residue in the cone until apparently dry,
then place in the drying oven at 105°C for one-half hour or until
it ceases to lose weight.

Cool in a desiccator and weigh.

The increase in weight is the total insoluble matter.

The cone is now placed back in the funnel and chloroform is
poured over it until the chloroform passes through into the filter bot-
tle colorless.

The cone is again dried at lOS^C for fifteen minutes.

This loss in weight is tar.

The residue in the cone is ignited in an oxidizing flame or prefer-
ably in a muffle for fifteen minutes.

The loss is non-tarry organic matter.

Instead of using the alundum cone a gooch crucible may be used.

27B. SOLUBILITY IN CARBON BISULPHIDE.
(TOTAL BITUMEN.)

This test is performed in the same way for asphalteiu-s or solu-
bility in petroleum naphtha except that a 5-gram sample is preferablj
used. The same apparatus is u.sed.

27C. SOLUBILITY IN CARBON TETRACHLORIDE.

This test is performed in the same way as /"J f^^'J^^^^^
except that the flask containing the carbon t^trachloru^ n u^t bo
kept in a dark place. The difference between , fo so^ub.My m
carbon bisulphide and carbon tetrachloride represents the carbonos.

504

BULLETIN NUMBER SIXTEEN OF

28. RESISTANCE OF ASPHALTIC CEMENT TO OXIDATION.

After being subjected to the following tests the film of asphalt
should be brilliant and lustrous, should not be scaly and fragile,
should adhere firmly to the metal and should not be dull and cheesy
in texture.

A strip of thin sheet iron 2 inches wide and 6 inches long is
covered on its lower 4 inches with the melted asphaltic cement. This
strip is placed in an oven at 275 °F for 15 minutes and allowed to
thoroughly drain.

It is removed from the oven and allowed to cool, then placed in
an electrically heated oven at a temperature of 450 °F for one hour.
At the end of the hour, the door of the oven is opened and the heat is
turned off, the specimen being allowed to remain in the oven.

The oven shall be one having an outside diameter of 12x12x12
inches with an opening in the top 1 cm. in diameter, the heating ele-
ments being in the bottom of the oven. The resistance shall be so
distributed that the heat is uniform throughout the oven. The lower
end of the strip shall be suspended so that it is at least 3 cm. from
the bottom of the oven.

The resistance is preferably so arranged that three different
heats can be maintained with a snap switch such that the lowest heat
is 325 'F, the medium heat is 400 °F and the highest heat is 450°F.

at=a D=fit::a

Fig-. 150 — Paraffin Scale Apparatus for Distillation.

KANSAS CITY TESTING LABORATORY

505

29. PARAFFIN WAX OR SCALE IN PETROLEUM AND BITU-
MINOUS PRODUCTS.

The apparatus used is shown in Figs. 150 and 151.

Instead of the metal retort, a glass distilling flask with a glass
air condenser may be used if desired. One hundred grams of the
oil, bitumen or material under examination are weighed into the re-
tort and distilled as rapidly as possible to dry coke. The distillate is
caught in a 150cc. Erlenmeyer flask, the weight of which has been
previously ascertained. During the early stages of distillation a cold,
damp towel wrapped around the stem of the retort will serve to con-
dense the distillate. After high temperatures have been reached, this
towel may be removed. When the distillation is completed, the dis-
tillate is allowed to cool to room temperature and is then weighed in
the flask. This weight minus that of the flask gives the weight of the
total distillate.

Five grams of the well mixed distillate is then weighed into a
lOOcc. Erlenmeyer flask and mixed with 25cc. of Squibb's ether. Twen-
ty-five cc. of Squibb's absolute alcohol is then added, after which the
flask is packed closely in a freezing mixture of finely crushed ice and
salt maintained at — 18°C in a quart tin cup. After remaining 30
minutes in this mixture, the solution is quickly filtered through a No.
575 C S & S. 9 cm. hardened filter paper placed in a glass funnel
which is packed in a freezing mixture as shown in figure. Vacuum
should be employed to hasten filtration. The freezing-mixture reser-
voir sho\\m in the figure may be made by cutting in half a round glass
bottle measuring approximately 120 millimeters in diameter and us-
ing the upper half in an inverted
position. Any precipitate remaining

on the paper should be washed until

2 I "^W^ " free from oil with about 50cc. of a

O I W 1 to 1 mixture of Squibb's ether and

absolute alcohol cooled to — 18°C.

After the paper has been sucked
dry, it should be removed from the
funnel and the adhering paraffin
scale should be scraped off into a
weighed crystallizing dish and dried
on a steam bath. The dish and con-
tents should then be cooled in a
desiccator and weighed.

The weight of the paraffin scale so
obtained, divided by the weight of the
distillate taken and multiphed by the
percentage of the total distillate ob-
tained from the original sanyi'^'.
equals the percentage of the paraffin
scale.
Fig. 151 — Paraffin Scale
Filter.

506

BULLETIN NUMBER SIXTEEN OF

30A. BITUMEN AND GRADING OF ASPHALT SURFACE

MIXTURE.

V^

v^3>

The asphaltic surface is
soflened by warming and is
tho roughly mixed. 100.0
grf ms are weighed into a
thill porcelain dish. This is
placed in a gas or electric
muffle, as shown in fig. 152,
and heated with a good aera-
tion at a temperature not ex-
ceeding 700 °C, preferably
about 500 °C, or at a barely
perceptible red heat.

It is well to use a pyrome-
ter in the muffle. Usually
about two hours is required
for the complete combustion
of the carbonaceous material.
The dish and contents are
now removed from the muf-
fle, allowed to cool and

The

Fig. 152 — Surface Mixture Muffle
Furnace,
weighed. The loss in weight is the percentage of bitumen,
mineral matter is now screened through a nest of screens containing
the 1, 2, 4, 10, 20, 40, 80, 200 meshes to the lineal inch. The amount
passing each screen and retained on the next is recorded. The exact
description of the sizes is as follows:

Opening in

Opening in

Diameter of

Mesh

Inches

Millimeters

Wire, Inch

1

1.050

26.67

0.149

2

0.525

13.33

0.105

4

0.1850

4.699

0.065

10

0.0650

1.651

0.035

20

0.0340

0.864

0.016

40

0.0150

0.381

0.010

80

0.0068

0.173

0.00575

200

0.0029

0.074

0.0021

KANSAS CITY TESTING LABORATORY

507

SOB. BITUMEN AND GRADING OF ASPHALTIC SURFACE
MIXTURE BY EXTRACTION.

Wfiree

Beeiss

CONOCNS

The apparatus used for
this analysis is that shown
in Fig. 155. It consists of a
large metallic soxhlet extrac-
tor of about 500 cubic centi-
meter capacity, a 1,000 cubic
centimeter pyrex extraction
flask, a braes ball reflux con-
denser and a very coarse and
porous alundum extraction
thimble, capable of holding at
least 250 grams of the sur-
face mixture, and a means of
heating, preferably a 200
watt electric hot plate,
although an alcohol lamp or
Bunsen burner are suitable.

At least 1,000 grams of the
Asphaltic Surface Mixture
are placed on a large pie pan
under a hot plate, in an oven
or over a radiator so that the
mixture completely softens.
The mixture is now thor-
oughly stirred and exactly
250 grams are weighed out
to the nearest 0.1 gram and
arg packed into the alundum extraction thimble. The extraction
thimble has previously been heated for at l^ast one horn a Oo C
The thimble and the mixture are now weighed and placed in tnc
soxhle? tube of the extractor. Five hundred cubic cent.met..s of
benzol or carbon tetrachloride are added to the f ^^^ f -X,; '*,Jn'
through the condenser or directly. The apparatus i. tightly con
riPfted the stonners being of cork treating with a solution ol
^yioxylene in acSe. Thellask containing the solvent is now heated

7M/r7BI-£

/,OOC>cc ^yeax

(^LCO/-IOL. Lfir7P

Fig. 155 — K. C. T. L. Surface :Mixture
Extraction Apparatus.

508

BULLETIN NUMBER SIXTEEN OF

for three hours so that
the solvent refluxes at
least ten times. If a
general supply of cold
water is not available,
ice w^ater may be used for
cooling as shown in the
figure. At the end of
three hours and immedi-
ately after the solvent has
refluxed the thimble con-
taining the extraction mix-
ture is taken out of the
soxhlet tube and dried for
one hour at a temperature
of 105 °C. The loss in
weight multiplied by 0.4
IS the percentage of bitu-
men.

The exi^racted mineral
aggregate is examined for
the presence of carbona-
ceous matter, which would
be evidence of the over-
heating of the surface
mixture in its manufacture. The mineral is now graded through
screens in accordance with the method set forth in paragraph 30-A.

Fig. 154-— Serf ens and IMr^chine for
Sieving Surface Mixtures.

31. TENSILE STRENGTH OF BITUMINOUS SURFACE MIXTURE.

The surface mixture to be tested is
heated to over 240 °F to soften it and
is thoroughly compressed into a standard
cement testing briquet mold. The mold
is then packed in ice for at least two
hours. It is now quickly put in the
tensile strength machine used for testing
Portland cement and pulled until it fails.
Good bituminous surface mixture will Fig. 153 — Mineral Aggre-
give a tensile strength of as high as 600 sate Grading Balance,

lbs. per sq. in. Poorly cemented material will give a tensile strength
usually lower than 200 lbs. per sq. in.

KANSAS CITY TESTING LABORATORY

509

32. SPECIFIC GRAVITY OF GASES BY VISCOSITY OR EFFU-
SION METHOD.

The apparatus is shown in Fig. 156.

The apparatus is first filled with distilled water through the
reservoir, while the reservoir is in position on its support, and
while the three-way cock is set to connect the gas chamber with the
surrounding atmosphere. Enough water should be introduced to fill
the apparatus to the mark on the glass tube a few centimeters below
the stop cock. The water jacket should be filled with water and the
whole apparatus allowed to come to room temperature before starting

a test. Care should be taken that the ap-
paratus is kept at a constant temperature
during any test and no water should be lost
from, or added to the reservoir during a
test. For each test the temperature of the
water in the jacket surrounding the gas
chamber should be observed in order to per-
mit correction of the observed specific
gravity to the specific gravity of dry gas.

The orifice tube should be screwed in
position on the three-way cock and tight-
ened with a small wrench. It is very im-
portant that the orifice tube fit gas tight,
since if there is a small leak at the base the
results will be incorrect. When not in use
the orifice tube should be protected from
dust and moisture by attaching its cover.
It should never be left on the apparatus
unless the cock is turned to shut off con-
nection with the gas chamber. This is to
prevent the condensation of water vapor in
the orifice. The orifice tube should be kept on the screw plug, in the
base of the apparatus, which is intended to serve as a holder.

To make a test the gas chamber is filled with a samp e of an
drawn m through the side connection of the three-way cocj^ by lowe. -
ing the reservoir. The cock is then closed, the ff *^»-^'«>^ .P^X . to
its support and the air allowed to stand within the gas ^ham e. to
become saturated with water vapor and to ensure that is a the
temperature of the apparatus. Sufficient air .«h«" i^''^.;J ,^;;' ,'"tJe
that when the sample is compi^essed by ^'^'t "^Tn onsm-e thai the
water level will remain below the lower mark. To ^"s^J t^^J* \^l

water will drain from the inner s^^'^'-^^^ ^^/^^'^f Ju^^ "t^a Howe 1
same extent in each test, the same period of time ^houl Ik al ons

after each filling before beginning the t^^^' .^^h^^/^.^lh fhe orifice
riod, the cock is turned to connect the f^^^^]^^"^^''^^^^^ ^^ a'stop
and the time of effusion of the ^^\^^!'Xl\.^^l Jtw-t-n the pns^
watch. The time to be observed '« that fps np f^t v.u^ h,

sage of the water meniscus from the "^JJ^„f ,"^r ^^ken to have the
above the gas chamber. In timing ^^'"^ .^J'^^^^Jf^, f.'h^ould be made

Fig-. 156-
Specific
Gases
Method.

-Apparatus for

Gravity of

by Effusion

510 BULLETIN NUMBER SIXTEEN OF

in timing makes a difference of about one per cent in the apparent
specific gravity.

After the air time has been determined, the apparatus should
be filled with the gas, whose specific gravity is to be determined^
The gas chamber is filled by lowering the reservoir as was done with
the air and then allowing the gas to flow out through the orifice.
This rinsing of the gas chamber should be done three times to en-
sure a sample uncontaminated with air. The time for the effusion
of the gas is then determined in exactly the same manner as with
air.

If the time of effusion with either gas or air is irregular from
test to test, this may be the result of moisture condensing in the
orifice. This moisture can be removed by blowing dry air through
the orifice. Care must be taken at all times to keep the orifice free
from dust or water. Especial care should be taken to keep water from
getting into the stop cock because it may be blown into the orifice
and cause sei'ious trouble. To prevent this, never raise the reservoir
from its holder while the cock is open from the gas chamber to the
inlet or outlet.

The specific gravity of a gas may be defined as the ratio of the
weight of a given volume of gas to the weight of an equal volume of
air measured at the same temperature and pressure. The specific
gravity of a dry gas referred to dry air is, for all practical purposes,
the same for any temperature. But the specific gravity of dry gas
compared with dry air is always different from the specific gravity
of saturated gas referred to saturated air. Moreover the latter value
is different at different temperatures and pressures.

The specific gravity of the gas under the conditions of the test
is the ratio of the square of the time for gas effusion to the square of
the time for air effusion, i. e.,

I Tg *
Ss = ^ — \
[ Ta I

The following equations show the relation between the specific
gravities of saturated gas compared with saturated air and the spe-
cific gravity of dry gas referred to dry air.

(S + k)

Ss =

(1 + k)
S = Ss (1 + k) — k

S = Specific gravity of dry gas referred to dry air.

Ss = Specific gravity of saturated gas referred to saturated air.

The values of k for gas at 760 mm. pressiire and at various tem-
peratures are as follows:

KANSAS CITY TESTING LABORATORY

511

Temperature

Degrees C.

k

0

0.004

5

.005

10

.008

15

.011

20

.015

25

.020

30

.027

The following is an example of the use of these formulas. The
specific gravity (S) of pure dry hydrogen is 0.0695. The specific
gravity of saturated hydrogen (Ss) at 20°C is

0.0695 + 0.015

Ss = = 0.0833

1 + 0.015

This is the value which the effusion apparatus would give at 20''C
v/ith pure hydrogen.

Where a large number of tests are being run on gases having a
limited range of specific gravities it is convenient to prepare a table
giving the specific" gravity of saturated gas at different temperatures
and the corresponding values of the specific gravity of the dry gas,
for the range of specific gravity and temperature which will be met
with. The derivation of these formulas is discussed in Technologic
Paper No. 94, of Bureau of Standards, where further information re-
garding them may be obtained.

512 BULLETIN NUMBER SIXTEEN OF

33A. ABSORPTION METHOD FOR TESTING NATURAL AND

CASINGHEAD GAS.

Fill the two-armed pipet commonly known as the Hofman ap-
paratus with distilled water. The glass stop cock at the top of the
closed graduated arm is a two-way cock, so that the tube above the
stop cock can be completely cleared of air. The end of the stop cock
through which the outside discharge takes place is closed with a
rubber tube and pinch cock. A funnel is set on top of the tube,
water is introduced and the tube is washed out with distilled water.
The pinch cock is closed, the funnel is removed and the gas is intro-
duced in the usual manner by displacement with water until about
50cc are in the graduated arm. The level of the water is made the
same in the two arms and the reading of the quantity of gas is made
after it has adjusted itself to the room temperature.

Twenty-five cc of Claroline oil or straw oil are introduced into the
open arm. The open arm is now stoppered or held with the thumb so
that no air can gain access and the oil is shaken over into the other
arm so that it overlies the water. The water is now withdrawn
through the stop cock at the lower end of the U. The arm is now
filled and kept filled with Claroline or straw oil shaking until the gas
ceases to be absorbed. The absorption is calculated in percentage.

The amount of gasoline that may be obtained by absorption from
the gas may be approximately calculated from the following table:

. Casinghead Gas Yield.

Yield of Gasoline
Absorption Gallons per 1000

Percentage Cu. Ft. of Gas

25 50

30 : 75

35 1.50

40 2.00

50 2.50

60 - 3.50

80 - 5.00

One gallon of gasoline obtained from 1000 cu. ft. of gas reduces
the volume about 25 to 30 cu. ft. and reduces the heating value about
75 to 100 B. T. U. per cu. ft. or IV2 to 10%. One gallon of gasoline at
20c a gallon would then extract .6c from the value of gas at 20c per
1000 cu. ft. About one-half of the natural gas of the United States
contains gasoline in commercially obtainable quantity. Soine casing-
head gas such as at Sisterville, West Va., gives 13 gallons of gasoline
per 1000 cu. ft. and has a heating value of 2500 B. T. U. per cu. ft.
Shellac is the best thread dressing material for gasoline and oil joints
since it is not soluble in gasoline nor water.

KANSAS CITY TESTING LABORATORY

513

33B. FREEZING METHOD FOR TESTING NATURAL GAS FOR

GASOLINE CONTENT.

This method is from Technical Paper 104, Bureau
of Mines, page 26. The sample of natural gas or
casinghead gas is introduced in the usual manner
into the apparatus shown.

In this apparatus (a) is a three-way stop cock,
(c) is a tube filled with glass wool and phosphorus
pentoxide for the purpose of drying, (b) is a portion
of tube which is introduced into liquid air, (d) is a
, manometer tube containing mercury and is closed at
the further end.

In filling the manometer, the apparatus must be
completely exhausted of its air. Sufficient mercury
is introduced so that its level rests at the zero point
of the scale when under a vacuum. The three-way
stop cock at (a) connects to the vacuum pump and
to the gas sample container. The sample of gas is
drawn in at ordinary atmospheric pressure and the
stop cock (a) is closed and the bulb (b) is intro-
duced into the cooling medium. The temperature
below 100°C is taken. At this temperature all of the
gasoline constituents are completely liquefied.
While maintained at this low temperature, the vapor
above the liquefied gasoline is exhausted with the
^^^ vacuum pump thus removing the non-condensible
gas. The bulb is now taken out of the refrig-
erant and allowed to warm up to the temperature
at the beginning of the test. The mercury level
in the manometer is read, the pressure indicated
being the partial pressure of the gasoline in the
sample before the dry gas had been removed.

,. . 100 a,

The percentage by volume of gasolme vapor is — ^

a being the partial pressure of the gasoline vapor after the test,
b being the original atmospheric pressure of the sample. Ihe per-
centage of gasoline vapor gives the number of pints of gasoline that
may be expected in the manufacture of gasoline from the gas under
test by the absorption process.

Fig. 15 7 —
Freezing
Apparatus
for Natural
Gas. >

514 BULLETIN NUMBER SIXTEEN OF

34. COMPLETE ANALYSIS OF GAS.

This apparatus is that described in the Journal of Industrial &
Engineering Chemistry by G. A. Burrell and G. G. Oberfell, Vol. 8,
page 229.

It is designed for the analysis of a gas mixture containing carbon
dioxide, unsaturated hydrocarbons, principally ethylene, oxygen, car-
bon monoxide, methane, ethane, hydrogen and nitrogen.

In the analysis the capillary train and U tube are swept free of
gases by drawing a sample of air into the buret and passing it into
the alkaline pyrogallate pipet G to remove oxygen. The residual
nitrogen is then passed into all the pipets and through the CuO tube
to sweep out other gases that may have been contained therein. The
electric current is now turned on the electric heating oven, the tem-
perature having been established by previous experiments. About a
100 watt furnace is required. The temperature desired is between
275 and 300 ^C. Some of the gas mixture is now drawn into the buret,
measured and passed into the pipets E, F and G for the removal
respectively of carbon dioxide, illuminants, and oxygen. After these
constituents have been remo\ed the stop cocks H, I and J are turned
so that communication is made between the buret and the pipet cor-
responding to J and through the CuO tube. The gas mixture is
passed back and forth through the tube fux'nace until no further
diminution in volume is noted by reading the gas volume in the buret.
Fifteen minutes is usually required, the carbon monoxide being con-
verted to carbon dioxide and the hydrogen to H^O. The CO burns
more rapidly if any hydrogen is present. When the gas is cooled and
no further contractiontakes place the remaining volume is read in the
buret. The carbon dioxide is now removed by placing the gas mixture
into the KOH pipet E. After the hydrogen and carbon monoxide
have been determined the residual gas is placed in the KOH pipet for
storage and the stop cock is closed. Enough oxygen to burn the
paraffin hydrocarbons is then drawn into the buret, measured and
passed into the slov/ combustion pipet J and the platinum spiral is
heated to almost white heat. The residual gas is now withdrawn from
the pipet E into the buret and from there slowly passed at the rate
of not more than lOcc per minute into the pipet J. While operating
it is well to cover the slow combustion pipet with gauze as occasion-
ally if the gas is passed in too rapidly an explosion takes place. After
combustion is complete, the contraction and the carbon dioxide are
measured and the gas again passed into the slow combustion pipet
and burned again. A small amount of further contraction may take
place but may be ignored unless excessive.

For calculation of results the following example and formulae are
useful :

KANSAS CITY TESTING LABORATORY

515

A-Somple intake

B'S-ifo^ stopcock as in Stttndttrd
Orsat apparatus

C-2-nay stop cock as in Burrell and ^

Oberfell apparatus for opening the |

nvasurinq burette, either to the _^ . . j T'"
absorption pipettes or ffje rBrass"

compensator Cjlinder^

'T)urmem«t«f

I xTransU

I .--Niehronw Wif«

AlunJum Cement PAcKina
Fuicd Silica Tube
Copper Oxide Packing

i^^Transit

1

Leads 10
Lamp Ban*

Fig. 158— Orsat-Burrell Apparatus for Analysis of Gus.

516 BULLETIN NUMBER SIXTEEN OF

Analysis of Gas From Pressure Stills.

a. Volume of sample taken

b. Volume after KOH absorption

c. Carbon Dioxide — CO2

d. Volume after Br^ or Oleum absorption

e. Olefins or illuminants

f. Volirme after alkaline pyrogallate absorp-

tion

g. Oxygen, O.

h. Volume after burning in CuO
i. Hydrogen, Hj

j. Volume after absorption in KOH
k. Carbon Monoxide CO
1. Volume taken for slow combustion
m. Oxygen added
n. Total volume
0. Volume after burning
p. Contraction from burning
q. Volume after KOH absorption
r. Contraction from CO2
s. Methane in sample
t. Ethane in sample
u. Nitrogen in sample

To calculate amount of methane in the sample from the contrac-
tion from burning, "p," and the absorption with KOH, "r," use the
following formulae:

4p — 5r

44.1cc

44.0CC

O.lcc =

0.22%

39.4CC

4.6cc —

10.43%

39.3cc

O.lcc —

0.22%

35.2cc

4. Ice =

9.30%

35.0CC

0.2cc =

0.45%

17.5CC

75.6CC

93.1CC

61.5CC

32.6CC

45.0CC

16.5CC

16.0CC =

72.56%

0.3cc =

1.36%

1.2cc =

5.46%

^uctiiaiic \aj

3

Ethane (t)

4r — 2p

3

or to obtain %

in original gas

% Methane

100 js

al

% Ethane

100 jt

al

% Nitrogen

100 ju

al

KANSAS CITY TESTING LABORATORY 517

35A. HEATING VALUE OF NATURAL GAS BY COMBUSTION.

The usual method of determining the heating value of natural
gas by combustion is by the continuous method.

The gas is burned and the water is collected when a certain defi-
nite amount of gas has been burned, for example, one-tenth of a
foot. With each one-tenth of a foot, the water is collected in a
separate receptacle and weighed.

The temperature of the incoming water is recorded and the tem-
perature of the outgoing water, the gases of combustion having
been brought to the temperature of the outgoing water. The water
condensed from the combustion of the hydrogen in the gas is also
collected. From this information, the heating value in B. T. U. is
calculated as follows:

ti = temperature of incoming water
U = temperature of outgoing water
w = pounds of water passed through

c =pounds of water condensed (average for each 0.1 cu. ft.).
From which B. T. U. per cubic foot = 10 (w + c + 0.02) (t.-t,) —
9704c

Example:
ti = 63.0°F.
t. =111.0°F.
w = 1.7531 lbs.
c = 0.0091 lbs.

10 (1.7531 + 0.0091 + 0.02) (111.0-63.0)— (9704) (.0091 ) =855.3—
88.3 = 767 B. T. U. per cubic foot.

This type of instrument is represented by the Junker and the
Sargent calorimeters. Correction of course must be niadc for the
temperature and pressure on the gas in the meter. This type ol
calorimeter is shown in Fig. 159.

A very clever tvpe of combustion calorimeter for gas is the Union
calorimeter offered 'for sale only in Europe at this tmie. It depends
upon the combustion of a very small Quantity of gas resulting in the
rise of temperature and expansion of the fl"\^ J.^^^.f ; . J^",]l''^ "v
combustion is proportional to the expansion as indicated b.v a capillary

column.

518

BULLETIN NUMBER SIXTEEN OF

Fig. 159 — Gas Calorimeter.

35B. HEATING VALUE OF NATURAL GAS FROM OXYGEN

CONSUMED IN BURNING.

The natural gas is burned with an excess of oxygen in a regular
combustion pipe J as shown in the apparatus in Fig. 158.

Vo
B. T. U. per cu. ft. is equal to 504 where Vo = volume of

\7ti

oxygen consumed in burning Vn volumes of natural gas.

35C. B. T. U. OF GAS BY CALCULATION FROM ANALYSIS.

The heating value of natural gas or any other gas may be cal-
culated as follows:

Percentage of illuminants X 20.00 =
Percentage of CO X 3.41 =

Percentage of CH4 X 10.65 =

Percentage of H2 X 3.45 =

The sum of these is the B. T. U. per cubic foot.

KANSAS CITY TESTING LABORATORY 519

REAGENTS USED IN GAS ANALYSIS.

(1) Potassium Hydroxide.

(a) For carbon dioxide determination.

500 grams of commercial potassium hydroxide are dissolved in 1
liter of distilled water. Ice. of this solution absorbs 40cc. of CO-.

(b) For the preparation of potassium pyrogallate for oxygen
testing.

120 grams of potassium hydrate are dissolved in lOOcc. of water.
Five grams of crystalline pyrogallic acid are used with lOOcc. of this
solution.

(2) Potassium Pyrogallate.

This solution is prepared when used except for charging absorp-
tion pipet. Five grams mixed with lOOcc. of potassium hydrate (b)
gives a solution in which Ice. absorbs 2cc. of oxygen.

(3) Sodium Hydroxide.

One hundred grams are dissolved in 300 grams of water and
may be used instead of potassium hydrate where given above.

(4) Cuprous Chloride.

Method of pi'eparation is to place a layer of copper oxide about
% inch deep in the bottom of a two-liter acid bottle. Add an excess
of long pieces of heavy copper wire reaching from the top to the
bottom of the bottle and fill the bottle with hydrochloric acid of
about 1.10 specific gravity. The absorption capacity of this reagent
is 4cc. of carbon monoxide CO for each Ice. of reagent. Metallic
copper must always be maintained v/ith the reagent to keep it in
good condition.

(5) Ammoniacal Cuprous Chloride.

The acid cuprous chloride as prepared above is treated with am-
monia until a faint odor of ammonia is perceptible. Likewise an
excess of copper wire is maintained. The absorption capacity is
Ice. of CO to Ice. of reagent.

(6) Sodium Hypobromite.

This is made of two solutions, one containing 100 grams of
caustic soda with 250cc. of distilled water, making 284cc. of solu-
tion. The other, 25 grams of liquid bromine, 25 grains of po-
tassium bromine and 200cc. of water. The two solutions are not
mixed until ready to use when equal parts are mixed. This reagent
is very good for the determination of illuminants.

(7) Fuming Sulphuric Acid. . , , i

Ordinary concentrated sulphuric acid is mi.xed with an equal
weight of sulphuric anhydride. One cc. of this reagent absorbs See.
of olefins or illuminants.

(8) Palladium Chloride. ,. , , • , .♦;„„ «f
Five 2-rams of palladium wire are dissolved in a solution ot

30cc. of hvdrochloric acid and 2cc. of nitric acid. . ,u f^ . ^r

The solution is evaporated to dryness on a water bath, 5cc. ot
hydrochloric acid are added and 25cc. of water and completo so u-
tion is made. The solution is diluted to ^^Ooc It contains one ur
cent palladous chloride and Ice. absorbs two-thirds of Ice. of h>
drogen.

520

BULLETIN NUMBER SIXTEEN OF

Comparison of Temperatures by the Fahrenheit and

Centigrade Scales.

CJent. Fahr.

Cent.

Fahr.

Cent.

Fahr.

Cent.

Fahr.

— 2ff3* —459.4

,

Absolut© Zero

—200° —328.0

- 5.6

+22.0

15.6

60.0

36.1

97.0

Temperature of

— 5.0

+23.0

16.0

60.8

36.7

98.0

Liquid Air

— 4.4

+24.0

16.1

61.0

37.0

96.6

-130° —202.0

— 4.0

+24.8

16.7

62.0

37.2

99.0

Pure Grain Alcohol

— 3.9

+25.0

17.0

62.6

37.8

100.0

Freezes

— 3.3

+26.0

17.2

63.0

38.0

100.4

—70° —94.0

— 3.0

+26.6

17.8

64.0

38.3

101.0

Ammonia Freezes

— 2.8

+2Y.0

18.0

64.4

38.9

102.0

— (75°0)

— 2.2

+28.0

18.3

65.0

39.0

102.2

-40° —40.

— 2.0

+28.4

18.9

66.0

39.4

103.0

Mercury Freezes

— 1.7

+29.0

19.0

66.2

40.0

104.0

(— 39.5C)

— 1.1

+30.0

19.4

67.0

40.6

105.0

—30' —22

— 1.0

+30.2

20.0

68.0

41.0

105.8

Ammonia Liquefies

— 0.6

+31.0

20.6

69.0

41.1

106.9

at — S3.7°0

0.

+32.0

21.0

69.8

41.7

107.0

—28 —18.4

+ 0.6

+33.0

21.1

70.0

42.0

107.6

—26 —14.8

1.0

33.8

21.7

71.0

42.2

108.0

—24 —11.2

1.1

34.0

22.0

71.6

42.8

109.0

—22 — 7.6

1.7

35.0

9-7 2

72.0

43.0

10G.4

—20 — 4.0

2.0

35.6

22.8

73.0

43.3

110.0

—19 — 2.2

2.2

36.0

23.0

73.4

43.9

111.0

— 18 — 0.4

2.8

37.0

23.3

74.0

44.0

111.2

_17.g _ 0.0

3.0

37.4

23.9

75.0

44.4

112.0

—17.2 + 1.0

3.3

38.0

24.0

75.2

45.0

113.0

—17.0 + 1.4

3.9

39.0

24.4

76.0

45.6

114.0

—16.7 + 2.0

4.0

39.2

25.0

77.0

46.0

114.8

—16.1 + 3.0

4.4

40.0

25.6

78.0

46.1

115.0

—16.0 + 3.2

5.0

41.0

26.0

78.8

46.7

116.0

—15.6 + 4.0

5.6

42.0

26.1

79.0

47.0

116.6

—15.0 + 5.0

6.0

42.8

26.7

80.0

47.2

117.0

—14.4 + 6.0

6.1

43.0

27.0

8U.6

47.8

118.0

—14.0 +6.8

6.7

44.0

27.2

81.0

48.0

118.4

—13.9 + V.O

7.0

44.6

27.8

82.0

48.3

119.0

—13.3 4- 8.0

7.2

46.0

28.0

82.4

48.9

120.0

—13.0 + 8.6

7.8

46.0

28.3

83.0

49.0

120.2

—12.8 4- 9.0

8.0

46.4

28.9

84.0

49.4

121.0

—12.2 +10.0

8.3

47.0

29.0

84.2

50.0

122.0

—12.0 +10.4

8.9

48.0

29.4

86.0

50.6

12«.0

—11.7 +11.0

9.0

48.2

30.0

86.0

51.0

123.8

—11.1 +12.0

9.4

49.0

30.6

87.0

51.1

134.0

—11.0 +12.2

10.0

50.0

31.0

87.8

51.7

125.0

—10.6 +13.0

10.6

51.0

31.1

88.0

52.0

125.6

—10.0 +14.0

11.0

51.8

31.7

89.0

52.2

126.0

— 9.4 +15.0

11.1

52.0

32.0

89.6

52.8

127.0

— 8.0 +15.8

11.7

53.0

32.2

90.0

53.0

127.4

— 8.9 +16.0

12.0

53.6

2S..8

91.0

53.3

128.0

— 8.3 +17.0

12.2

54.0

33.0

91.4

53.9

129.0

— 8.0 +17.6

12.8

55.0

33.3

92.0

54.0

129.2

— 7.8 +18.0

13.0

55.4

33.9

93.0

54.4

130.0

— 7.2 +19.0

13.3

56.0

34.0

93.2

K.O

131.0

— 7.0 +19.4

13.9

57.0

34.4

94.0

55.6

132.0

— 6.7 +20.0

14.0

57.2

ffi.O

95.0

56.0

132.8

— 6.1 +21.0

14.4

58.0

35.6

96.0

56.1

133.0

— a.O +21.2

15.0

59.0

36.0

96.8

56.7

134.0

KANSAS CITY TESTING LABORATORY

521

Temperature Conversion Tables.

Cent.

Pahr.

57.0

134.6

57.2

135.0

57.8

136.0

58.0

136.4

58.3

137.0

58.9

138.0

59.0

138.2

59.4

139.Q

eo.o

140.0

eo.6

141.0

m.o

141.8

61.1

142.0

61.7

143.0

62.0

143.6

62.2

144.0

62.8

145.0

63.0

145.4

63.0

146.0

63.9

147.0

64.0

147.2

64.4

148.0

^.0

149.0

65.6

150.0

66.0

150.8

66.1

151.0

66.7

152.0

6f7.0

152.6

67.2

1.53.0

67.8

1.54.0

68.0

154.4

68.3

155.0

68.9

15<>.0

69.0

1,W.2

69.4

157.0

70.0

158.0

70.6

1.59.0

71.0

159.8

71.1

160.0

71.7

161.0

72.0

161.6

72.2

162.0

72.8

163.0

7.3.0

163.4

73.3

164.0

73.9

lf.5.0

74.0

1^5.2

74.4

166.0

75.0

167.0

75.6

168.0

76.0

108.8

76.1

169.0

7(5.7

170.0

77.0

170.G

77.2

in.6

Cent. Pahr.

77.8

78.0

78.3

78.9

79.0

79.4

80.0

80.6

81.0

81.1

81.7

82.0

82.2

82.8

83.0

83.3

83.9

84.0

81.4

85.0

85.6

86.0

86.1

86.7

S7.0

87.2

87.8

88.0

88.3

88.9

89.0

89.4

90.0

90.6

91.0

91.1

91.7

92.0

92.2

92.8

93.0

93.3

93.9 ■

94.0

94.4

95.0

95.6

96.0

96.1

96.7

97.0

97.2

97.8

9S.0

172.0

172.4

173.0

174.0

174.2

175.0

176.0

177.0

177.8

178.0

179.0

179.6

180.0

181.0

181.4

182.0

l&S.O

183.2

184.0

185.0

186.0

186.8

187.0

188.0

188.6

189.0

190.0

190.4

191.0

192.0

192.2

193.0

194.0

196.0

195.8

196.0

197.0

197.6

198.0

199.0

199.4

200.0

201.0

201.2

202.0

203.0

204.0

204.8

205.0

206.0

206.6

207.0

208.0

208.4

Cent. Fahr.

98.3

209.0

98.9

210.0

99.0

210.2

99.4

211.0

100.0

212.0

100.6

213.0

101.0

213.8

101.1

214.0

101.7

215.0

102.0

215.6

102.2

216.0

102.8

217.0

103.0

217.1

103.3

218.0

103.9

219..)

104.0

219.2

104.4

220.9

105.0

•i2l.9

105.6

222.0

ir^.O

222.8

106.1

22S.0

106.7

M4.0

107.0

22t.C'

107.2

::25.0

107.8

22fi.O

108.0

226.4

108.3

227.0

108.9

228.0

109.0

228.2

109.4

229.0

110.0

230.0

110.6

231.0

111.0

2.31.8

111.1

232.0

111.7

2.33.0

112.0

2.!3.6

112.2

231.0

112.8

2r^ 'J

113.0

2.!5.4

113.3

23'i.O

113.9

237.0

114.0

237.2

114.4

23S.0

115.0

239.0

115.6

240.0

110.0

240.8

116.1

24 : 0

116.7

242.0

117.0

242.0

117.2

2J.1.0

117.8

244.0

118.0

244.4

118.3

24.'i.O

118.9

2l«i't

Cent.

Fahr.

119.0

246.2

119.4

247.0

120.0

248.0

120.6

24:'.0

121.0

249.8

121.1

250.0

121.7

251.0

122.0

251.6

122.2

252.0

122.8

2.53.0

123.0

253.4

123.3

2.54.0

123.9

266.0

124.0

255.2

124.4

256.0

125.0

257.0

125.6

258.0

126.0

258.8

126.1

259.0

126.7

2<.0.0

127.0

260.6

127.2

2(n.O

127.8

262.0

128.0

2(e.4

128.3

2(«.0

128.9

2r>4.0

]2il.O

2t4.2

12!>.4

2(k">.0

i:».o

2116.0

130.6

2ti7.0

131.0

2<>7.8

131.1

2«».0

131.7

269.0

i;«.o

2li9.«

i:h.2

270.0

i:r2.8

271.0

1:51.0

2f7l.4

133.3

272.0

i:«.o

273.0

l.St.O

273.2

i:a.4

271.0

1X5.0

27.-..0

i.y.o

276 t»

i:»i.o

27<i.8

136.1

277.0

1.*.7

2780

137.0

2:h.«i

137.2

279.0

i:{7.8

2S0.O

i:«.o

2S0.4

i:«3

2S1 0

i;«.9

'Sf'.O

i:ft»o

■xi

1.'«).4

2s:{0

522

BULLETIN NUMBER SIXTEEN OF

TE3IPERATURE CONVERSION TABLES— Continued.

Cent.

Fahr.

140.0

284.0

140.6

285.0

141.0

285.8

141.1

286.0

141.7

2»7.0

142.0

287.6

142.2

28S.0

142.8

289.0

143.0

289.4

14.3.3

290.0

143.9

291.0

144.0

291.2

144.4

292.0

145.0

263.0

145.6

294.0

146.0

294.8

146.1

295.0

146.7

296.0

147.0

296.6

147.2

297.0

147.8

298.0

148.0

2984

148.3

299.0

148.9

300.0

149.0

31)0.2

149.4

301.0

150.0

302 .0

152.0

.305.6

154.0

309.2

156.0

312.8

153.0

316.4

leoo

3:00

162.0

323.6

164.0

327.2

166.0

330.8

168.0

3.'14.4

170.0

338.0

172.0

341.6

174.0

345.2

176.0

348.8

178.0

352.4

ISO.O

3560

182.0

359.6

184.0

&53.2

186.0

3^6.8

18&0

370.4

IfiO.O

374 0

192.0

377.6

1940

381.2

196.0

3S4.8

198.0

3S8.4

200.0

382.0

2<K.0

401.0

210.0

410.0

Cent.

Fahr.

Cent.

Fahr.

215.0

419.0

590.0

1094.0

220.0

428.0

600.0

1112.0

225.0

437.0

610.0

1130.0

230.0

446.0

620.0

1148.0

235.0

455.0

630.0

1166.0

240.0

464.0

640.0

11S4.0

245.0

473.0

650.0

1202.0

250.0

482.0

660.0

1220.0

254.0

489.2

670.0

12.38.0

^55.0

491.0

680.0

1256.0

260.0

500.0

690.0

1274.0

285.0

509.0

700.0

1292.0

270.0

518.0

no.o

13100

275.0

527.0

720.0

1^8.0

230.0

536.0

730.0

1346.0

283.0

541.4

740.0

1.3G4.0

285.0

545.0

750.0

13S2.0

2880

550.4

760.0

1400.0

290.0

554.0

770.0

1418.0

2^5.0

563.0

780.0

1430.0

300.0

572.0

790.0

1454.0

305.0

5S1.0

800.0

1472.0

310.0

590.0

810 0

1490.0

315.0

500.0

8200

1508.0

.320.0

608.0

8^).0

1526.0

325.0

617.0

840.0

1.544.0

330.0

626.0

850.0

1562.0

335.0

6350

8.-30.0

1580 0

310.0

644.0

870.0

1598.0

345.0

653.0

&S0.0

1616.0

350.0

6^.2.0

890.0

lf34.0

360.0

680.0

900.0

1662.0

S70 0

698.0

920.0

1688.0

380.0

716.0

940.0

1724.0

390.0

734.0

960.0

1760.0

40C'.0

752.0

9S0.0

1796.0

410.0

770.0

ICOO.O

1832.0

4200

788.0

1020 0

1868.0

430.0

806.0

1040.0

19O4.0

440.0

824.0

1060.0

1940.0

450.0

842.0

1080.0

1976.0

460.0

86O.0

1100.0

2012.0

470.0

878.0

1120 0

2O48.0

480.O

896.0

1140.0

2084.0

490.0

914.0

11'%.0

21«^.0

500.0

932.0

1180.0

2156.0

510.0

950.0

1200.0

2192 J3

520.0

9680

1220.0

2228.0

530.0

&S6.0

1240.0

226* .0

540.0

1004.0

1260.0

2300.0

550.0

1022.0

1580.0

2336.0

560.0

10400

1300.0

2.372.0

570.0

1058.0

1320.0

2408.0

5800

1076.0

1.^0.0

2444.0

Cent.

Fahr.

1360.0
1380.0
1400.0
1420.0
1440.0
1460.0
1480.0
1500.0
1520.0
1540.0
1560.0
1580.0
1600.0
1620.0
1640.0
1660.0
1680.0
1700.0
1720.0
1740.0
1760.0
1780.0
190O.0
1=25.0
1S.5C.0
1S75.0
1900.0
1925 0
IKiO.O
1975.0
2000.0
2400.0
2500.0
3000.0
3SO0.0
4000.0
5000.0

eooo.o

2480.0
2516.0
2552.0
2588.0
2624.0
2660.0
2896.0
2732.0
2768.0
2804.0
2840.0
28rr6.0
2912.0
2918.0
2984.0
3020.0
3056.0
3092.0
3128.0
3164.0
3200.0
3236.0
3272.0
3317.0
3362.0
3407.0
34^2.0
3407.0
3542.0
3587.0
30.32. 0
3812.0
45.33.0
5432.0
6332.0
7232.0
9032.0
10632.0

TEMPER.\1T'RE READING CONVERSION FACTORS.
Temp. Centirrade = 5/9 (F.-32') = 5/4 R.
Temp. Fahrenheit = 9/5 C. + 32 = 9/4 R. + 32.
Temp. Rea-.jmur = 4/5 O. = 4/9 fF.— 32).

KANSAS CITY TESTING LABORATORY

523

BAUME', SPECIFIC GRAVITY AND POUNDS PER GALLON.
(U. S. BUREAU OF STANDARDS.)

10

10000

.9993

8.328

8.322

11

.9929

.99-22

8.269

8.263

12

.9859

.9352

8 211

8.205

13

.9790

.9783

8.153

8.148

14

.9722

.9715

8.096

8.091

15

.9G55

.9549

8.041

8.035

16

.9589

.9583

7.966

7.980

17

.95^4

.9517

7.931

7.926

IS

9459

.9453

7.8T7

7.S72

19

.9393

.9390

7.825

7.820

20

.93a3

.9327

7.772

7.767

21

.9272

.9265

7.721

7.716

22

.9211

.9204

7 670

7.665

23

.9150

.9144

7.320

7.615

24

.9091

.90S5

7.570

7.565

25

.9032

.9026

7.522

7.517

26

.8974

.89:9

7.473

7.469

27

.8917

.8912

7 425

7.421

28

.8861

.8855

7.378

7.374

29

.8805

.8799

7.a'?2

7.328

30

.8750

.8745

, 7.286

7.282

31

.8696

.8690

7 2a

7.236

32:

.8642

.8637

7.196

7.192

33

.8589

.8.584

7.152

7.147

Si

.^37

.a^iSl

7.108

7.104

85

.8485

.8480

7.065

7.061

36

.8434

.8429

7.022

7.018

37

.8383

.sns

6.980

i 6.976

38

.8333

.8.328

6.939

1 6.9.35

.9986
8.317
.9915
8.258
.9S4o
8.194
.9777
8.] 42

.9709
8.086

.9642
8.030

.9582
7.975

.9511
7.921

.9447
7.867

.9383
7.814

.9321
7.762

.9259
7.711

.9198
7.660

.9138
7.610

.S0T9
7.561

.9021
7.512

.8963
7.464 -

.8906
7.416

.8850
7.369

.8794
7.323

.8739
7.277

.86®
7.232

.86.31
7.187

.8578
7.143

.8i26
7.100

.&S75
7.057

.8424
7.014

.8373
6.972

.&323
6.930

.9979

.9972

8 311

8.305

.9ro8

.9i:01

8.252

8.2!6

.9838

.9831

8.194

8.188

.9770

.9763

8.137

8.131

.9702

.9695

8080

8.074

.9635

.9629

8.024

8.019

.9569 j

.9563

7.»39

7.Q64

.9504

.9498

7.915

7.910

W-IC

9434

7.861

7.853

.9377

.93n

7.S09

7.S04

.9315

.9309

7.757

7.752

.9253

.^247

7.706

7.701

.9192. '

.9186

7.655 1

7.650

.9132

.9126

7.005

7.600

.9073

.9067

7.5.56

7.551

.CO! 5

.9009

7507

7.502

.8957

.8951

7.459

7.454

.8900

.8895

7.411

7.407

.8S44

.88.38

7.3:^

I.SfM

.8788

.8783

7.318

7.314

.8734

.8728

7.273

7.268

.8-379

.86'4

7.2-J7

7.2"3

.86:6

.8621

7.183

7.178

.8573

.8568

7139

7.1.34

.8521

.S516

7.095

7.091

.8109

.8464

7.052

7.048

.8419

.8113

7.010

7.006

.8368

.8.363

6968

6.9.-4

.8318

.8314

fi (y*^

f. W"

.9964
S.299

.9G94
8.240

93-25
S.182

.9756
8.125

.9688
8 069

.96:2
8.013

.£556
7.9.19

.!:4>2
7.904

.9428
7.S51

.9X3
7.7^
9302
7.747

.9241
7.696

.9180
7645

.9121
7.595
9061

;..54'i
.roo3

7.497

.8946
7.449

8899
7.402

SS33
7 355

.8777
7.309

.8723
7.''64

8669
"218

8-15
7.173

.8563
7.130

.8511
7.0^7

8459
7.044

(4408
7 001

6.PW

.8.309
fi91S

6

7

.9957

.9950

, 8.293

8.287

! .9887

.9S80

! 8.234

8.228

.9818

.9611

8.176

8.171

.9749

.9743

8.119

8.114

.9 82

.9675

8.033

8.058

.9'315

.9609

8.007

8.002

.9550

.C543

7.653

7.948

' .9485

.9479

7.899

7.894

.9421

.9415

7.816

7.841

.9358

.9352

7.793

7.788

.9293

.9290

7.742

7.736

.9235

.9220

7.690

7.6ffi

.9174
7.640

.9115
7.590

.9053
7.541

.8997
7.493

.8940
7.445

.8883
7397

8827
7.351

.8772
7.305

.8717
7.259

.8363
7 214

8610
7.169

.8557
7.125

.R5()5
7 082

.8454
7.0:!9

.H4I>3
6.997

.8.^53
6.955

.91(38
7.635

.9109
7.5S5

.f060
7.536

.8992
7.488

.&)M
7.440

.8878
7.393

.8822
7.»t6

.8706
7.300
8712
7.254

.8(K>8
7.210

.8605
7.165

.8.5.52
7.121

8500
7.0V8

.8149
7.035
8W
6.P03

0.051

6.010

.994S
8.281
.9873
8.223
.fSW
S.1S6
.973e
8.108
.9369
8.052

.9102
7.997
.9537
7.942
.9472
7.888
.9409
7.835
.9346
7.783
.9-28t
7.731
.9223
7.680
.9162
7.630
.9103
' 7.580
.9044
7.531

.8983
7.483
' .8!>29
7.436
.8872
7.3S8
.8816
7.341
.8761
7.295
8706
7.249
.8663
7.205
.8600
7.161
, .8W7
7.117
' 8406
7 074
.844 »
7.031

.8.<«>3
6.080
.8!M3
8.M7
8294
ftOnrt

.9936
8.275

.9666
8.217

.9797
8.159

.9729
8.102

ri«2
8.017

.9606
7.991

.9530
7937

.9466
7.883

.0402
7.830

.9340
7.778

.9278
7.726

.9217
7.675

.9156
7.625

.9097
7.575

.9038
7.526

.S9S0
7478

.8923
7.4,30

.8S61

7.383

.8811

7.3 .7

.8755
7.291
8701

7 245

.»A^

7.201

.8694
7.1.16

.8542
7. lis

.S4'»
706P
SIW
7.0-7

RTW
«««

.ft.T'W

A.e4.Y

«2»
rtOOJ

J

524

BULLETIN NUMBER SIXTEEN OF

BAUME, SPECIFIC GRAVITY AND POUNDS PER GALLON— Con.
U. S. BUREAU OF STANDARDS— Con.

0

1

2

3

4

5

6

'

8

9

30

.82&4

.8279

.8274

.8269

.8264

.8260

.8256

.8250

. .8245

.8240

6.898

6.894

6.889

6.885

6.881

6.877

6.873

6.8S9

6.865

6.861

40

.8235

.8230

.8226

.8221

.8216

.8211

.8206

.8202

.8197

.8192

6.857

6.853

6.849

6.845

6.841

6837

6.833

6.829

6.825

6.821

41

.8187

.8182

.8178

.8173

.8168

.8163

.8159

.8154

.8149

.8144

6.817

6.813

6.809

6.805

6.801

6.797

6.793

6.789

6.785

6.781

42

.8140

.8135

.8130

.8125

.8121

.8116

.8111

.8107

.8102

.8097

6.777

6.773

6.769

6.7f>5

6.761

6.758

6.754

6.750

6.746

6.742

43

.8092

.8088

.8083

.8078

.8074

.80.-0

.80'-:5

.8030

.8065

.8051

6.7.38

6.734

6.730

6.726

6.722

6.718

6.715

6.711

6.707

6.703

44

.8046

.8041

.80.37

.8032'

.8028

.8023

.8018

.8014

.8009

.8005

6.6G9

6.695

6.091

6.688

6.684

6680 -

6.676

6.672

6.668

6.665

ir.

.8000

.7995

.7991

.7936

.7982

.7977

.7973

.7908

.7964

.7959

6.6<>1

6.657

6.653

6.649

6.646

6.642

6.688

6.634

6.630

6.627

46

.7955

.7960

.7946

.7941

.7937

.7932

.7928

.7923

.7919

.7914

6.623

6.619

6.616

6.612

6.608

6.604

e.eoo

6.567

6.593

6.589

47

.7910

.7905

.7901

.7896

.7892

.7887

.7883

.7878

.7874

.7870

6586

6.582

6.578

6.574

6.571

6.567

6.563

6.560

6.556

6.552

48

.7865

.7861

7856

.7a52

.7848

.7843

.7839

.7834

.7830

.7826

6.548

6.545

6.541

6.537

6.534

6 530

6.5-26

6.523

6.519

6.515

49

.7831

.7817

.7812

.7808

.7804

.7799

.7795

.7791

.7786

.7782

6.511

6..508

6.504

6.501

6.497

3.494

6.490

6.486

6.483

6.479

50

.7778

.7773

.7769

.7765

.7761

.7755

.7752

.7748

.7743

.7739

6.476

e.472

6.468

6.465

6.461

6.453

6.454

6.450

6.447

6.443

51

.77.35

.7731

.7726

.7722

.7717

.7713

.7709

.7705

.7701

.7697

6.140

6.436

6.432

6-.429

6.425

6.421

6.418

6.415

6.411

6.408

52

.7692

.76S8

.7684

.7680

.7675

.7671

.7667

.7663

.7^0

.7654

6.404

6.401

6.397

6.394

6.380

6387

6.383

6.380

6.376

6.373

53

.76.=i0

.7546

.7612

.7638

.7634

.7629

.7625

.7621

.7617

.7613

6,369

6.336

6.362

6.359

6.355

3.3.51

6.348

6.345

6.341

6.338

54

.7r09

.7605

.7600

.7596

.7592

.7588

.7584

.7580

.7576

.7572

6.334

6.331

6.327

6.324

6.321

6.317

6.314

6.311

6.307

6.304

55

.7568

.7563

.7559

.7555

.7551

.7547

.7543

.7539

.75.35

.7531

6300

6.296

6.293

6.290

6.287

6.28.31

6.280

6.276

6.273

6.270

56

.7527

.7523

.7519

.7515

.7511

.7507

.7503

.7490

.7495

.7491

6.26fl

6.263

6.250

6.256

6.253

3.249

6.246

6.243

6.240

6.236

57

.7487

.7483

.7479

.7475

.7471

.7437

.7463

.7459

.7455

.7451

6.233

6.229

6.226

6.223

6.219

6.216

6.213

6.209

6.206

6.203

58

.7447

.7443

.7439

.7435

.7431

.7427

.7423

.7419

.7415

.7411

6.199

6.193

6.193

6.190

6.186

5.183

6.180

6.176

6.173

6.170

59

.7407

.7403

.7400

.7396

.7392

.73S8

.7384

.7390

.7376

.7372

6.166

6.133

6.160

0.157

6.1.54

6.1.50

6.147

6.144

6.141

6.137

60

.7368

.7335

.7361

.7.3.57

.7353

.7.349

.7.345

.7341

.7338

.7334

6.1.34

6.131

6.128

6.124

6.121

6118

6.115

6.112

6.108

6.105

Rl

.7330

.7.326

.7322

.7318

.7.315

.7311

.7307

.7303

.7299

.7295

6.102

6.099

6096

6.093

6 090

5.083

6.983

6.080

6.077

6.073

52

.7292

.7288

.7284

.7280

.7277

.7273

.79!CQ

.7265

.7261

.7258

6.070

6.067

6.064

6.060

6.057

6.054

6.051

6.948

6.045

6.042

63

.72.54

.7250

.7246

.7243

.7239

.7235

.7231

.7228

.7224

.7220

6.038

6.oa5

6.032

6.029

6.026

6.023

6.020

6.017

6014

6.010

«

.7216

.7213

.7209

.7205

.7202

.7198

.7194

.7191

.7187

.7183

60O7

6.004

6.0O1

5.998

5.995

5992

5.989

5.986

5.983

5.990

65

.n79

.7176

.7172

.7168

.7165

.7161

.7157

.7154

.7150

.7147

5.976

5.973

5.970

5.967

5.964

5.931

5.G58

5.955

5.952

5.949

66

.7143

.7139

.71.36

.7132

.7128

.7125

.n21

.7117

.7114

.7110

5.946

5.943

5.940

5.937

5.934

5.931

5.928

5.925

5.928

5.919

67

.7107

.7103

.7099

.7096

.7092

.70^9

.7085

.7081

.7078

.7074

5 916

.■>91.3

5910

5.907

5 904

f; oni

5«ns

5«35

589?

5.8R9

525

KANSAS CITY TESTING LABORATORY

BAUME , SPECIFIC GRAVITY AND POUNDS PER GALLON— Con.

U. S. BUREAU OF STANDARDS— Con.

0

1

68

.7071

.70(57

5.886

5.883

69

.7035

.7032

5.866

5.853

70

.7000

.6997

5.827

5.824

71

.6935

.6962

5.798

5.795

72

.6031

.6927

5.769

5.766

73

.6897

.6893

5.741

5.738

74

.eS63

.6859

5.712

5.710

.75

.68^

.6826

5.685

5.682

76

.6796

.6793

5.667

5.^4

77

.6763

.6760

5.629

5.627

78

.6731

.6728

5.eo2

5.600

79

.6699

.6695

5.576

5.573

80

.(x.e7

.6663

5.549

5.546

81

.6635

.6632

5.522

5.520

82

.6004

.6601

5.497

5.494

83

.^73

.6570

5.471

5.468

84

.6542

.^39

5.4i5

5.443

85

.6512

.6509

5.420

5.417

86

.6482

.6479

5.305

5.3K

87

.6452

.6449

5.370

5.367

88

.6422

.6419

5.345

5.343

89

.6393

.6390

5.320

5.318

90

.6364

.6361

5.296

5.294

91

.6335

.6332

5.272

5.270

92

.6.306

.6303

5.248

5.^6

93

.6278

.6275

5.225

5.222

94

.6250

.6247

5.201

5.199

95

.6222

.6219

5.178

5.176

96

.6195

.6192

5.155

5.153

97

.6167

.6165

5.132

5.130

36

.6140

.6138

5.110

5.108

99

.6114

.6111

5.088

5.085

.00

.6087
5.066

::::::::i

.7064
5.8S0

.7028
5.850

.6993
5.821

.6958
5.792
24
5.763

.6890
5.735

.6856
5.707

.6823
5.679

.6790
5.652

.6757
5.624

.6724
5.597

.6692
5.570

.6660
5.543

.6629
5.517

.6698
5.481

.6.567
5.4^

.6536
5.440

.6506
5.415

.6476
5.390

.6146
5.365

.6416
5.340

.6387
5.316

.6^8
5.291

.6329
5.267

.6301
5.214

.6272
5.220

.6214
5.196

.6217
5.174

.6189
5.150

.6162
5.128

.6135
5.106

.6108
5.083

.7060
5.877

.7025
5.848

.6990
5.818

.6955
5.789

.6920
5.76U

5.732

.6853
5.704

.6819
5.676

.6786
5.649

.6753
5.621

.6721
5.594

.6689
5.568

.6657
5.541

.6626
5.515

.6594
5.489

.^64
5.463

.6533
5.437

.6503
5.412

.6473
5.387

.6443
5.362

.6413
5.338

.63S4
5.313

.6355
5.289

.6326
5.265

.6298
5.241

.6270
5.218

.6242
5.194

.6214
5.171

.6186
5.148

.61.59
5.126

.6132
5.103

.6106
5.081

.7056
5.874

.7021
5.845

.6986
5.815

.6951
5.786

.6917
5.758

.6883
5.7-29

.6849
5.701

.6816
5.673

.6783
5.643

.6750
5.618

.6718
5.592

.6686
5.566

.6^4
5.538

.6623
5.512

.6.591
5.486

.6560
5.4'jO

.6530
5.435

.6.500
' 5.410

.6470
5.385

.6440
5.300

.(410
5.335

.6391
5.311

.6352
5.286

.6323
5.263

.6295
5.239

.6267
5.216

.6239
5.192

.6211
5.169

.ms4

5.140
.6157

5.124
.6130

5.101
.6103

5.079

.7053
5.871

.7018
5.842

.6963
5.812

.69^8
5.784

.6914
5.755

.6880
5.727

.6846
5.6ce

.6813
5.671

.6780
5.643

.6747
5.616

.6715
5.589

.6C83
5.562

6551
5.536

.6619
5.510

.6588
5.4S4

.6557
5.458

65-27
.5.432

.6497
5.407

.6467
5.382

.6437
5,3.57
M07
5.333

.6.378
5.308

.6349
5.284

.6.321
5.261

.6292
5.230

.6-'64
5.213

.6256
5.190

ervs

5.166

61 SI
5.144

.61.54
5.121

.6127
5.099

61 OO
5.076

.7049

5.868

.7014
5.839

.6979
5.810

.6944
5.781

.6910
5.752

.t876
5.724

.6843
5.696

.6809
5.668

.6776
5.640

.6744
5.613

.6711
5.586

.6679
5.560

.6t48
5.533

.6616
5.507

.6585
5.4S1

.6554
5.455

.6524
5.430

.6494
5.405

.6464
5.380

.6434
5.3.56

.6404
5.330

.6375
5.306

.6346
5.281

.6318
5.258

.6289
5.234

.6261
5.210

.62.33
5.187

5.164

.6178
5.142

.6151
5.119

.6124
5.096

.6098
6.074

.7046
5.865

.70U
5.836

.8976
5.807

.6941
5.77S

.6907
5.749

.6873
5.721

.6839
5.693

.68u6
5.665

.6773
5.638

.6740
5.610

.6708
5.584

.6676
5.557

.6645
5.531

.6613
5.504

.(582
5.478

.6551
5.453

.6521
5.427

.6490
5.402

.64'>1
5. .377

.6431
5.352

.6401
5.328

.6.372
5.304

.6343
5.279

.a315
5.256

.6286
5.232

.62.58
5.'20e

.6-231
5.185

.6-203
5.162

.6176
5.140

.6148
5.116

.6122
5.094

.6(106
6.073

.7042
5.862

.7007
5.833

.6972
5.804

.6938
5.T75

.6903
5.746

.6889
5.718

.6836
5.690

.6803
5.662

.6770
5.635

.6737
5.608

.6705
5.561

.66rr3
5.554

.6641
5.528

.»no

5.502

.6579
5.476

.6548
5.450

.6618
5.425

.6487
5.400

.6656
5.375

.6428
5.350

.6399
5.325

.6309
5.301

.6.^1
5.277

mn

5.253
.e2S4

5.230
.6256

5.206
.fitSS

5.183

flaw

.5.160

.(1173
5.1.37

.61.46
i 5.114

.6119
6.092

.6002
6.070

.7039
6.859

.7004
5.830

.6669
5.801

.6934
5.772

.6900
5.744

5.715

.6833
5.687

.6799
5.660

.6787
5.632

.6734
5.605

.6702
5.578

.(■^70
5.552

.6638
5.525

.6607
5.490

.6576
5.473

.6545
5.448

.6515
5.422

.(48*
5.397

.6456
5.3T2

.6425
5.347

.6396
5.323

.«m

5.2W

.63*
5.275

.6;«i9
5251

.(K81
6.227

.6263
5.304

.6225
.5.190

.(VlW
5.167

.8170

5.i;«>
(n4.«

5112
.611(1

5.0OO
.91011

6.0(H

526

BULLETIN NUMBER SIXTEEN OF

BAUME' GRAVITY BY PETROLEUM ASSOCIATION FORMULA

EQUIVALENTS OF SPECIFIC GRAVITY AND WEIGHT IN

POUNDS PER U. S. GALLON FOR OILS OR FLUIDS

LIGHTER THAN WATER. (With Extension of Table

for Oils Heavier Than Water.)

(MODULUS 141.5 TAGLIABUE.)

Baume'

.0

.1

.2

.3

.4

.5

.6

.7

.8

.9

4

1.044

1.043

1.042

1.041

1.041

1.040

1.039

1.039

1.038

1.037

8.70

8.69

8.68

8.67

8.67

8.66

8.66

8.65

8.65

8.64 Pds

5

1.037

1.036

1.035

1.034

1.034

1.033

1.032

1.032

1.031

1.030

8.64

8.63

8.62

8.61

8.61

8.61

8.60

8.60

8.59

8.58 Pds

6

1.029

1.028

1.027

1.026

1.026

1.025

1.024

1.024

1.023

1.022

8.57

8.56

8.56

8.55

8.55

8.54

8.53

8.53

8.52

8.51 Pds

7

1.022

1.021

1.020

1.019

1.019

1.018

1.017

1.017

1.016

1.015

8.51

8.51

8.50

8.49

8.49

8.48

8.47

8.47

8.46

8.46 Pds

8

1.014

1.013

1.012

1.011

1.011

1.010

1.009

1.009

1.008

1.007

8.45

8.49

8.43

8.42

8.42

8.41

8.41

8.41

8.40

8.39 Pds

9

1.007

1.006

1.005

1.004

1.004

1.003

1.002

1.002

1.001

1.000

8.39

8.38

8.37

8.36

8.36

8.36

8.35

8.35

8.34

8.33 Pds

10

1.000

.9993

.9986

.9979

.9972

.9965

.9958

.9951

.9944

.9937

8.331

8.325

8.319.

8.314

8.308

8.302

8.296

8.290

8.284

8.279

11

.9930

.9923

.9916

.9909

.9902

.9895

.9888

.9881

.9874

.9868

8.273

8.267

8.261

8.255

8.249

8.244

8.238

8.232

8.226

8.221

12

.9861

.9854

.9847

.9840

.9833

.9826

.9820

.9813

.9806

.9799

8.215

8.209

8.204

8.198

8.192

8.186

8.181

8.175

8.169

8.164

13

.9792

.9786

.9779

.9772

.9765

.9759

.9752

.9745

.9738

.9732

8.158

8.153

8.147

8.141

8.135

8.130

8.124

8.119

8.113

8.108

14

.9725

.9718

.9712

.9705

.9698

.9692

.9685

.9679

.9672

.9665

8.102

8.096

8.091

8.085

8.079

8.074

8.069

8.064

8.058

8.052

15

.9659

.9652

.9646

.9639

.9632

.9626

.9619

.9613

.9606

.9600

8.047

8.041

8.036

8.030

8.024

8.019

8.014

8.009

8.003

7.998

16

.9593

.9587

.9580

.9574

.9567

.9561

.9554

.9548

.9542

.9535

.7992

7.987

7.981

7.976

7.970

7.965

7.959

7.954

7.949

7.944

17

.9529

.9522

.9516

.9509

.9503

.9497

.9490

.9484

.9478

.9471

7.939

7.933

7.928

7.922

7.917

7.912

7.906

7.901

7.896

7.890

18

.9465

.9459

.9452

.9446

.9440

.9433

.9427

.9421

.9415

.9408

7.885

7.880

7.874

7.869

7.864

7.859

7.854

7.849

7.844

7.838

19

.9402

.9396

.9390

.9383

.9377

.9371

.9365

.9359

.9352

.9346

7.833

7.828

7.823

7.817

7.812

7.807

7.802

7.797

7.791

7.786

20

.9340

.9334

.9328

.9322

.9315

.9309

.9303

.9297

.9291

.9285

7.781

7.776

7.771

7.766

7.760

7.755

7.750

7.745

7.740

7.735

21

.9279

.9273

.9267

.9260

.9254

.9248

.9242

.9236

.9230

.9224

7.730

7.725

7.720

7.715

7.710

7.705

7.700

7.695

7.690

7.685

22

.9218

.9212

.9206

.9200

.9194

.9188

.9182

.9176

.9170

.9165

7.680

7.675

7.670

7.665

7.660

7.655

7.650

7.645

7.640

7.635

23

.9159

.9153

.9147

.9141

.9135

.9129

.9123

.9117

.9111

.9106

7.630

7.G25

7.620

7.615

7.610

7.605

7.600

7.595

7.590

7.586

24

.9100

.9094

.9088

.9982

.9076

.9071

.9065

.9059

.9053

.9047

7.581

7.576

7.571

7.566

7.561

7.557

7.552

7.547

7.542

7.537

25

.9042

.9036

.9030

.9024

.9018

.9013

.9007

.9001

.8996

.8990

7.533

7.528

7.523

7.518

7.513

7.509

7.504

7.499

7.495

7.490

26

.8984

.8978

.8973

.8967

.8961

.8956

.8950

.8944

.8939

.8933

7.485

7.480

7.475

7.471

7.465

7.461

7.456

7.451

7.447

7.442

27

.8927

.8922

.8916

.8911

.8905

.8899

.8894

.8888

.8883

.8877

1A?.1

7.433

7.428

7.424

7.419

7.414

7.410

7.405

7.400

7.395

28

.8871

.8866

.8860

.8855

.8849

.8844

.8838

.8833

.8827

.8822

7.390

7.386

7.381

7.377

7.372

7.378

7.363

7.359

7.354

7.350

29

.8816

.8811

.8805

.8800

.8794

.8789

.8783

.8778

.8772

.8767

7.345

7.340

7.335

7.331

7.326

7.322 .

7.318

7.313

7.308

7.304

30

.8762

.8756

.8751

.8745

.8740

.8735

.8729

.8721

.8718

.8713

7.300

7.295

7.290

7.285

7.281

7.277

7.272

7.268

7.263

7.259

31

.8708

.8702

.8697

.8692

.8686

.8681

.8676

.8670

.8665

.8660

7.255

7.250

7.245

7.241

7.236

7.2.32

7.228

7.223

7.219

7.215

32

.8654

8649

.8644

.8639

.8633

.8628

.8623

.8618

.8612

.8607

7.210

7.205

7.201

7.197

7.192

7.188

7.184

7.180

7.175

7.170

33

.8602

.8597

.8591

.8586

.8581

.8576

.8571

.8565

.8560

.8555

7.166

7.162

7.157

7.153

7.149

7.145

7.141

7.136

7.131

7.127

34

.8550

.8545

.8540

.8534

.8529

.8524

.8519

.8514

.8509

.8504

7.123

7.119

7.115

7.110

7.106

7.101

7.097

7.093

7.089

7.085

KANSAS CITY TESTING LABORATORY

527

BAUME', SPECIFIC GRAVITY AND POUNDS PER GALLON— Con.

(MODULUS 141.5.)

Baume '

35

36

37

38

39

40

41

42

43

44

45

46

47

48

49

50

51

52

53

54

55

56

57

58

59

60

61

62

63

64

65

66

67

.0

.8498
7.080

.8448
7.038

.8398
6.996

.8348
6.955

.8299
6.914

.8251
6.874 !
.8203
6.834

.8156
6.795

.8109
6.756

.8063
6.717

.8017
6.679

.7972
6.641

.7927
6.604

.7883
6.567

.7839
6.531

.7796
6.495

.7753
6.459

.7711
6.424

.7669
6.389

.7628
6.355

.7587
6.321

.7547
6.287

.7507
6.254

.7467
6.221

.7428
6.188

.7389
6.156
.7351
6.124

.7313
6.092

.7275
6.061

.7238
6.030

.7201
5.999

.7165
5.969

.7128
5.938

.8493
7.076

.8443
7.034

.8393
6.992

.8343
6.951

.8294
6.910

.8246
6.870

.8198
6.830

.8151
6.791

.8104
6.751

.8058
6.713

.8012
6.675

.7967
6.637

.7923
6.601

.7879
6.564

.7835
6.527

.7792
8.492

.7749
6.456

.7707
6.421

.7665
6.386

.7624
6.352

.7583
6.317

.7543
6.284

.7503
6.251

.7463
6.217

.7424
6.185

.7385
6.152

.7347
6.121

.7390
6.089

.7271
6.057

.7234
6.027

.7197
5.996

.7161
5.966

.7125
5.936

.3

.8488
7.071

.8438
7.030

.8388
6.988

.8338
6.946

.8289
6.906

.8241
6.866

.8193
6.826

.8146
6.786

.8100
6.748

.8053
6.709

.8008
6.671

.7963
6.634

.7918
6.596

.7874
6.560
.7831
6.524

.7788
6.488

.7745
6.452

.7703
6.417
.7661
6.382

.7620
6.348

.7579
6.314

.7539
6.281

.7499
6.247

.7459
6.214

.7420
6.182

.7381
6.149

.7343
6.117

.7305
6.086

.7268
6.055

.7230
6.023

.7194
5.993

.7157
5.962

.7121
5.933

.4

.8483
7.067

.8433
7.026

.8383
6.984

.8333
6.942

.8285
6.902

.8236
6.861
.8189
6.822
.8142
6.783

.8095
6.744

.8049
6.706

.8003
6.667
.7958
6.630

.7914
6.593

.7870
6.556

.7826
6.520

.7783
6.484

.7741
6.449

.7699
6.414

.7657
6.379

.7616
6.345

.7575
6.311

.7535
6.277

.7495
6.244

.7455
6.211

.7416
6.178

.7377
6.146

.7339
6.114

.7301
6.082

.7264
6.0.52

.7227
6^021

.7190
5.990

.7154
5.960

.7118
5.930

.5

.8478
7.063

.8428
7.021

.8378
6.980

.8328
6.938

.8280
6.898

.8232
6.858
.8184
6.818
-8137
6.779

.8090
6.740

.8044
6.701

.7999
6.664

.7954
6.626
.7909
6.589

.7865
6.552

.7822
6.517

.7779
6.481

.7736
6.445

.7694
6.410

.7653
6.376

.7612
6.342
.7.571
6.307

.7531
6.274
.7491
6.241
.7451
6.207

.7412
6.175

.7374
6.143

.7335
6.111

.7298
6.080

.7260
6.048

.7223
6.017

.7186
5.087

.7150
5.957

.7114
5.927

■ 8473
7.059

.8423
7.017

.8373
6.976

.8324
6.935

.8275
6.894
.8227
6.854
.8179
6.814

.8132
6.775

.8086
6.736

.8040
6.698

.7994
6.660
.7949
6.623
.7905
6.586
.7861
6.549

.7818
G.513

.7775
6.477

.7732
6.442

.7690
6.407

.7649
6.372

.7608
6.338

.7567
6.304

.7.527
6.271

.7487
6.237

.7447
6.204

.7408
6.172

.7370
6.140

.7332
6.108
.7294
6.077

.7256
6.045

.7219
6.014

.7183
5.984

.7146
5.953
.7111
5.924

.8468
7.055

.8418
7.013

.8368
6.971

.8319
6.931

.8270
6.890

.8222
6.850

.8174
6.810

.8128
6.771

.8081
6.732

.8035
6.694

.7990
6.656

.7945
6.619
.7901
6.582
.7857
6.546

.7813
6.. 500

.7770
6.473

.7728
6.438

.7686
6.403

.7645
6.369

.7603
6.334

.7563
6.301

.7.523
6.267

.7483
6.234

.7443
6.201

.7405
6.169

.7366
6.137

.7328
6.105

.7290
6.073

.7253
6.042

.7216
6.012

.7179

6.981

1 .7143

5.951

.7107

I 5.921

.8

.8463
7.051

.8413
7.009
( .8363
6.967

.8314
6.926

.8265
6.886
.8217
6.846

.8170
6.806

.8123
6.767

.8076
6.728
.8031
6.691

.7985
6.652
.7941
6.616

.7896
6.578
.7852
6.542

.7809
6.506

.7766
6.470

.7724
6.435

.7682
6.400

.7640
6.365

.7599
G.331

.7559
6.297

.7519
6.264

.7479
6.231

.7440
6.198
.7401
6.166

.7362
6.133
.7324
6.102

.7286
6.070

.7249
6.039

.7212
6.008

.7175
5.977

.7139
B.948

.7103
5.918

.9

.8458
7.046

.8408
7.005

.8358
6.963
.8309
6.922

.8260
6.881

.8212
6.841

.8165
6.802

.8118
6.763

.8072
6.725

.8026
6.868
.7981
6.649

.7936
6.611

.7892
6.575

.7848
6.538

.7805
6.502

.7762
6.467
.7720
6.432

.7678
6.397

.7636
6.362

.7595
6.327

.7555
6.294

.7515
6.261

.7475
6.227

.7436
6.195

.7397
6.162

.7358
6.130

.7320
6.09S

.7283
6.067

.7245
6.036

.7208
6.005

.7172
5.975

.7136
5.945

.7100
6.916

.8453
7.042

.8403
7.001

.8353
6.959

.8304
6.918

.8256
6.878

.8208
6.838

.8160
6.798

.8114
6.760
.8067
6.721

.8022
6.683

.7976
6.645

.7932
6.608

.7887
6.571

.7844
6.535

.7800
6.498

.7758
6.463

.7715
6.427

.7074
6.393

.7632
6.358
.7591
6.324
.7551
6.291

.7511
6.257
.7471
6.224

.7432
6.191

.7393
6.159
.7354
6.127

.7316
6.095

.7279
6.064

.7242
6.033

.7205
6.002

.7168
5.972
.7132
5.942

.709fl
6.912

528

BULLETIN NUMBER SIXTEEN OF

BAUMK, SPECIFIC GRAVITY AND POUNDS PER GALLON— Con.

(MODULUS 141.5.)

0

1

a

3

4

5

6

7

a

0

68

.7093

.7089

.7086

.T«£J

.7079

.7075

1

.7071

.7068

.7064

.7061

6.909

5.906

6.903

5.&00

5.898

5.894

5.891

5.888

6.885

6.883

09

.7057

.7054

.7050

.7047

.7043

.7040

.7036

.7033

.7029

.7028

5.879

5.877

5.873

5.871

5.868

5.865

5.862

5.859

5.856

6.853

70

.7022

.7019

.7015

.7012

.7008

.7005

.7001

.6998

.6095

.6991

6.850

5.848

6.844

5.842

5.838

5.S36

5.833

5.830

6.828

6.824

71

.e&S8

.6984

.6981

.6977

.6074

.6970

.6967

.6964

.6960

.6997

6.822

5.818

5.816

5.813

5.810

5.807

5.S04

5.802

5.798

5.T96

72

.6953

.6950

.6946

.6^3

.6940

.6986

.6933

.6929

.69218

.8988

5.793

6.790

6.787

5.784

5.782

5.778

5.776

6.773

5.770

6.768

73

.esifl

.6916

.6012

.6909

.6906

.6902

.6899

.6806

.6892

.rtW»

6.76*

5.762

5.758

5.756

5.753

5.750

5.748

5.745

5.742

6.739

74

.fiSSfi

.m>p.

.Stf!9

.6876

.6872

.6660

' .6866

.6862

.6859

.6858

5.737

5.733

5.731

6.728

5.725

5.723

5.720

5.717

6.714

6.712

75

.6652

.6^9

.6846

.6842

.6839

.6836

.6832

.6829

.6826

.6»a

6.708

5.706

5.703

5.700

5.698

5.665

5.692

5.689

5.687

6.684

7fl

.6819

.6816

6813

.6809

.6806

.6803

.6800

.6796

.6793

.6790

5.6S1

5.678

5.676

5.673

5.670

5.668

5.665

5.662

5.659

S.6o7

77

.6787

.6783

.6789

.6777

.6774

.6770

.6767

.6764

.6761

.ffiST

5.654

5.651

5.M8

5.646

5.643

5.640

5.638

5.635

5.633

5.629

78

.6754

.6751

.6748

.6745

.6741

.6738

.6735

.6732

.6728

.6725

6.627

5.624

5.622

5.619

5.616

5.613

5.611

5.608

5.606

6.608

79

.6722

.6719

.6716

.6713

.6709

.6706

.6703

.6700

.6697

.6693

6.600

5.507

5.595

5.593

5.589

5.587

5.584

5.582

5.579

6.576

80

.6690

.6687

.6684

.6681

.6678

.6675

.6671

.eecs

.ouuo

.6668

5.573

5.571

5.568

5.566

: 5.563

5.561

5.558

6.555

5.553

5.550

81

.6659

.6656

.6653

.6649

.6646

.0643

.er40

.6637

.6634

.6631

5.548

5.545

5.543 .

5.540

5.537

5.534

5.532

5.529

5.527

5.524

82

.6628

.6625

.6621

.6618

.6615

.6612

.6609

.6606

.6603

.6-300

5.522

5.519

5.516

5.513

5.511

5.508

5.506

5.503

5.501

5.496

83

.6507

.6564

.6591

.6588

.65^

.6581

.6578

.6575

.6572

.6599

5.496

5.493

5.491

5.488

5.4®

5.483

5.480

5.473

5.475

6.473

84

.6566

.6563

.6560

.^57

.6554

.6551

.6548

.6545

.6542

.6639

5.470

5.468

5.465

5.463

5.460

5.458

5.455

5.453

5.450

6.448

85

.6536

.6533

.6530

.^27

.6524

.6521

.6518

.6515

.6512

.6509

a445

5.443

6.440

5.438

5.435

5.433

5.430

5.428

5.425

6.^3

86

.ffi06

.6503

.6500

.6497

.6494

.6491

.6438

.6485

.6482

.6479

5.420

5.418

5.415

5.419

5.410

5.408

5.405

5.403

5.400

5.898

87

.6476

.6473

.6470

.6*57

.6464

.6461

.6458

.6455

.6452

.6440

5.395

5.393

5.390

5.388

5.385

5.383

5.380

6.378

5.375

5.373

88

.6446

.6444

.6441

.6438

.64S

.6432

.6429

.6426

.6423

.6420

5.370

5.368

5.366

5.363

5.361

5.358

5.356

5.353

5.351

5.^9

89

.6417

.6414

.6411

.6409

.6406

.6403

.6400

.6397

.6394

.6391

5.346

5.344

5.341

6.3^

5.237

5.334

5.332

5.329

5.327

6.824

90

.6388

.6385

.6382

.6380

.6377

.6374

.6371

.6368

.6365

.6362

5.322

5.319

5.317

5.315

5.313

5.310

5.308

5.305

5.303

6.300

91

.6360

.6357

.6354

.6351

.6348

.6345

.6^2

.6340

.6337

.6334

6.299

5.296

5.294

5.291

5.289

5.286

5.284

5.282

5.27»

5.277

92

.6.331

.6328

.6325

.6323

.fift)

.6317

.6314

.63U

.sm

.6306

5.274

6.272

5.269

5.268

5.2«

5.263

5.260

5.2S8

5.256

6.254

93

.6303

.6300

.6297

.6294

.62«2

.6289

.6286

.6283

.6281

.6278

6.251

6.249

5.246

5.241

5.242

5.239

5.237

6.234

6.233

5.230

94

.&!75

.6272

.6260

.6267

.6264

.6-261

.6258

.6258

.6253

.6290

6.228

6.22S

5.223

5.221

5.219

5.216

6.214

5.212

5.20e

6.207

96

.6247

.6244

.6242

.e-.iao

.6236

.6233

.6231

.6228

.6225

.8223

5.204

5.202

5.200

5.198

5.196

5.193

6.191

6.189

5.186

6.184

96

.6220

.6217

.6214

.6212

.6209

.6206

.6203

.6201

.6196

.61£6

5.182

6.179

5.177

5.175

5.173

5.170

5.168

5.166

5.164

6.161

97

.6193

.6190

.6187

.6184

.6182

.6179

.6176

.6174

.6171

.ei«

6.150

5.157

6.154

5.152

5.150

5.14?

1 5.145

6.144

6.141

S.U9

98

.6166

.6163

.6160

.6158

i .6155

.6152

i .6150

.6147

.6144

.8141

6.137

6. 134

5.132

6.130

' 5.128

5.125

' 5.124

5.121

6.119

B.IVS

99

.6130

.6136

.6134

.6131

.6128

.6126

.6123

.6120

.6113

.8116

5.114

5.112

6.110

6.108

5.105

5.104

snoi

5.099

6.097

G.004

KANSAS CITY TESTING LABORATORY

529

REDUCTION OF BAUME' GRAVITY READINGS TO 60 F.

(This table shows the degrees Baume' at 60° F of oils having, at the desig-
nated temperatures, the observed degrees Baume' indicated. For example, If the
observed degrees Baume' is 20.0 at 7S° F, the true degrees Baume' at 60° F
will be 19.0. Intermediate values not given in the table may be conveniently
interpolated. For example, if the observed degrees Baume' is 20.4 at 78° F, the
true degrees Baume' at 60° F will be 19.4. The headings "Observed Degrees
Baume'" and "Observed Temperature" signify the true indication of the hy-
drometer and the true temperature of the oil — that is, the observed readings
corrected, if necessary, for instrumental errors.)

Observed Degrees Baume'

Observed

Temperature in

-F.

8.0

9.0

10.0

11.0

12.0

13.0

14.0

15.0

16.0

Corresponding Degrees Baume at 60° F.

60

8.0
7.9
7.8
7.7
7.6

7.5
7.4
7.3
7.2
7.1

7.1
6.9
6.8
6.7
6.7

6.6
6.5
6.4
6.3
6.3

6.2
6.1
6.0
5.9

5.8

5.7
5.6
5.5
5.4
5.4

5.3

5.2
5.1
5.0
4.9

4.8
4.7
4.6
4.5
4.4

4.3
4.2
4.1
4.0
3.9
3.8

9.0
8.9
8.0
8.7
8.6

8.5
8.4
8.3
8.2
8.1

8.1
7.9
7.8
7.7
7.6

7.6
7.5
7.4
8.3
7.3

7.2
7.1
7.0
6.9
6.8

6.7
6.6
6.5
6.4
6.4

6.3
6.2
6,1
6.0
5.9

5.8
5.7
5.6
5.5
5.4

5.4
5.3
52.
5.1
5.0
4.9

10.0
9.9
9.8
9.7
9.6

9.5
9.4
9.3
9.2
9.1

9.1
9.0
8.9
8.8
8.8

8.7
8.6
8.5
8.4
8.3

8.3
8.2
8.1
8.0
8.0

7.9
7.8
7.7
7.6
7.5

7.4
7.3
7.2
7.1
7.0

6.9
6.8
6.7
6.6
6.5

6.5
6.4
6.3
6.2
6 1
6.0

11.0
10.9
10.8
10.7
10.6

10.5
10.5
10.4
10.3
10.2

10.1

10.1

10.0

9.9

9.8

9.8
9.7
9.6
9.5
9.4

9.4
9.3
9.2
9.1
9.0

9.0
8.9
8.8
8.7
8.6

8.5
8.4
8.3
8.2
8.1

8.0
7.9
7.8
7.7
7.6

7.6
7.5
7.4
7.3
7.2
7.1

12.0
11.9
11.8
11.7
11.6

11.5
11.5
11.4
11.3
11.2

11.1
11.1
11.0
10.9
10.8

10.8
10.7
10.6
10.5
••10.5

10.4
10.3
10.2
10.1
10.0

9.9
9.9
9.8
9.7
9.6

9.6
9.4
9.3
9 2
9.1

9.1
9.0
8.9
8 8
8.8

8.7
8.6
8.5
8.4
8 3
8.2

13.0
12.9
12.8
12.7
12.6

12.5
12.5
12.4
12.3
12.2

12.2
12.1
12.0
11.9
11.8

11.8
11.7
11.6
11.5
11.4

11.4
11.3
11.2
11.1
11.0

10.9
10.9
10.8
10.7
10.6

10.5
10.5
10.4
10.3
10.2

10 2

11.1

10.0

9 9

9.8

9.8
9.7
9.6
9.5
9.4
9.3

14.0
13.9
13.8
13.7
13.6

13.6
12.5
13.4
13.3
13.3

13.2
13.1
13.0
13.9
12.9

12.8
12.7
12 7
12.6
12.5

12.4
12.3
12.3
12 2
12.1

12.0
12.0
11.9
11.8
11.7

11.7
11.6
11.5
11 4
11.3

11.3
11 2
11 1
11 0
10.9

10 9
10 8
10 7
10 6
10 5
10 4

15.0
14.9
14.8
14.7
14.7

14.6
14.5
14.5
14.4
14.3

14.3

14.2
14.1
14.1
14 0

13.9
13.8
13.7
13.7
13 6

13.5
13.5
13.4
13.3
13.2

13 2
13 1
13 0
12.9
12.8

12 8
12.7
12.6
12 B
12 1

12 4
12 3
12 2
12 1
12 0

11 9
11 9
11 8
117
11 6
11 5

16.0

62

15.9

64

15.8

66

15.7

68

15.7

70

72

15.6
15.5

74

15.5

76

15.4

78

15.3

80

15.3

82

15.2

84

15.1

86

15 0

88

15.0

90

14 9

92

14.8

94

14 .7

96

14.7

98

14 .6

100

14. B
14.4
14.4
14 3
14 2

102

104

106

108

110

111
14 1
MO
13 9
13 9

112

114

116

118

120

13 8
13 8
13 7
13 6
13 5

122

124

126

128

130

13 5
13 4

13 3

134

13 2

13 1

138

140

13 0
13 0

142

r^ 9

144

12 «

12 7

148

12.6

530

BULLETIN NUMBER SIXTEEN OF

REDUCTION OF BAUME GRAVITY READINGS TO 60 F— Con.

Observed Degrees Baume'

Observed
Temperature in

op

17.0

18.0

19.0

20.0

21.0

22.0

23.0

24.0

25.0

26.0

Corresponding Degrees Baume' at 60° F.

30

18.6
18.6
18.5
18.3
18.2

18.1
18.0
17.9
17.8
17.6

17.5
17.4
17.3
17.2
17.1

17.0
16.9
16.8
16.7
16.6

16.5
16.4
16.3
16.2
16.1

16.0
15.9
15.8
15.7
15.5

15.4
15.3
15.2
15.1
15.0

14.9
14.8
14.7
14.5
14.4
1
T14.3
tU 2
14.1
14.0
13.9

13.8

19.7
19.6
19.5
19.4
19.3

19.1
19.0
18.9
18.8
18.7

18.6
18.5
18.3
18.2
18.1

18.0
17.9
17.8
17.7
17.6

17.5
17.4
17.3
17.2
17.1

17.0
16.9
16.8
17.6
16.5

16.4
16.3
16.2
16.1
16.0

15.9
15.8
15.7
15.5
15.4

15.3
15.2
15.1
15.0
14.9

14.8

20.7
20.6
20.5
20.4
20.3

20.1
20.0
19.9
19.8
19.7

19.6
19.5
19.3
19.2
19.1

19.0
18.9
18.8
18.7
18.6

18.5
18.4
18.2
18.1
18.0

17.9
17.8
17.7
17.6
17.5

17.3
17.2
17.1
17.0
16.9

16.8
16.7
16.6
16.4
16.3

16.2
16.1
16.0
15.9
15.8

15.7

21.7
21.6
21.5
21.4
21.3

21.2
21.1
20.9
20.8
20.7

20.6
20.5
20.3
20.2
20.1

20.0
19.9
19.8
19.7
19.5

19.4
19.3
19.2
19.1
19.0

18.9
18.8
18.7
18.6
18.4

18.3
18.2
18.1
18.0
17.9

17.8
17.7
17.6
17.5
17.3

17.2
17.1
17.0
16.9
16.8

16.7

22.7
22.6
22.5
22.4
22.3

22 2
22.1
21.9
21.8
21.7

21.6
21.5
21.3
21.2
21.1

21.0
20.9
20.8
20.7
20.5

20.4
20.3
20.2
20.1
19.9

19.8
19.7
19.6
19.5
19.4

19.3
19.2
19.1
19.0
18.8

18.7
18.6
18.5
18.4
18.2

18.1

18.0

'17.9

m.s

17.7
17.6

23.7
23.6
23.5
23.4
23.3

23.2
23.1
22.9

22.8
22.7

22.6
22.5
22.3
22.2
22.1

22.0
21.9
21.8
21.7
21.5

21.4
21.3
21.2
21.1
20.9

20.8
20.7
20.6
20.5
20.4

20.3
20.2
20.1
20.0
19.8

19.7
19.6
19.5
19.4
19.2

19.1
19.0
18.9
18.8
18.7

18.6

24.8
24.7
24.6
24.5
24.4

24.2
24.1
23.9
23.8
23.7

23.6
23.5
23.3
23.2
23.1

23.0
22.9
22.8
22.7
22.5

22.4
22.3
22.2
22.1
21.9

21.8
21.7
21.6
21.5
21.3

21.2
21.1
21.0
20.9
20.8

'20.7
'20.5
:20 . 4
20.3
'20.2

20.1
20.0
19.9
19.8
19.6

19.5

25.8
25.7
25.6
25.5
25.4

25.2
25.1
24.9
24.8

24.7

24.6
24.5
24.3
24.2
24.1

24.0
23.9
23.8
23.7
23.5

23.4
23.3
23.2
23.1
22.9

22.8
22.7
22.6
22.5
22.3

22.2
22.1
22.0
21.9
21.8

21.7
21.5
21.4
21.3
21.2

21.1
21.0
20.9
20.8
20.6

20.5

26.9
26.8
26.7
26.5
26.4

26.2
26.1
26.0
25.9
25.8

25.6
25.5
25.4
25.3
25.1

25.0
24.9
24.7
24.6
24.5

24.4
24.3
24.1
24.0
23.9

23.8
23.7
23.5
23.4
23.3

23.2
23.1
23.0
22.8
22.7

22.6
22.5
22.4
22.3
22.2

22.0
21.9
21.8
21.7
21.5

21.4

27.9

32

27.8

34

27.7

36

27.5

38

27.4

40

27.2

42

27.1

44

27.0

46

26.9

48

26.8

50

26.6

52

26.5

54

26.4

56

26.3

58 ...

26.1

60

26.0

62

25.9

64

25.7

66

68

70

25.6
25.5

25.4

72 . .'

25.3

74

76

25.1
25.0

78

80

82

84

24.9

24.8
24.7
24.5

86

24.4

88

90

24.3

24.2

92

24.1

94

24.0

96

23.8

98

23.7

100

102

23.6
23.5

104

23.4

106

23.3

108

23.1

110

23.0

112

22.9

114

22.8

116

118...

120

22.7
22.5

22.4

KANSAS CITY TESTING LABORATORY

531

REDUCTION OF BAUME GRAVITY READINGS TO 60 F— Con.

Observed Degrees Baume'

Observed

Temperature in

op

27.0

28.0

29.0

30.0

31.0

32.0

33.0

34.0

25.0

36.0

Corresponding Degrees Baume' at 60° F

30

29.0
28.8
28.7
28.5
28.4

28.3
28.2
28.1
27.9
27.8

27.6
27.5
27.4
27.3
27.1

27.0
26.9
26.7
26.6
26.5

26.4
26.3
26.1
26.0
25.8

25.7
25.6
25.5
25.4
25.2

25.1
25.0
24.9
24.7
24.6

24.5
24.4
24.3
24.2
24.0

23.9
23.8
23.7
23.6
23.4

23.3

30.0
29.8
29.7
29.5
29.4

29.3
29.2
29.1
28.9
28.8

38.6
28.5
28.4
28.3
28.1

28.0
27.9
27.7
27.6
27.5

27.4
27.3
27.1
27.0
26.8

26.7
26.6
26.5
26.4
26.2

26,1
26,0
25,9
25,7
25,6

25,5
25,4
25.3
25.2
25.0

24.9
24,8
24,7
24,6
24,4

24.3

31.0
30.9
30.8
30.6
30.5

30.4
30.2
30.1
29.9
29.8

29.7
29.6
29,4
29,3
29,1

29.0
28.9
28.7
28.6

28.4

28.3
28.2
28.1
27.9
27.8

27.7
27,6
27,5
27 3

27,2

27,0
26.9
26.8
26,7
26,6

26,4
26,3
26 2
26.1
25.9

25.8
25.7
25,6
25,5
25,3

25,2

32.0
31.9
31.8
31.6
31.5

31.4
31.2
31.1
30.9
30.8

30.7
30.6
30.4
30.3
30.1

30.0
29.9
29.7
29.6
29.4

29.3
29.2
29.1
28.9
28.8

28,7
28.6
28.5
28.3
28.2

28.0
27.9
27.8
27.7
27.6

27.4
27 3
27.1
27,0
26.9

26,8
26,7
26,6
26,4
26.3

26 2

33.1
33.0
32.8
32.7
32.5

32.4
32.2
32.1
31.9
31.8

31.7
31.6
31.4
31.3
31.1

31.0
30.9
30.7
30.6
30.4

30.3
30.2
30.1
29.9
29.8

29.7
29.5
29.4
29.2
29.1

29.0
28,9
28,8
28.6
28,5

28.3
28 .-2
28.1
28.0
27.8

27.7
27,6
27,5
27,3
27,2

27 1

34.1
34.0
33.8
33.7
33.5

33.4
33.2
33.1
32,9
32,8

32,7
32.6
32.4
32.3
32.1

32.0
31.9
31.7
31.6
31.4

31.3
31.2
31.1
20.9
30.8

30.7
30.5
30,4
30.2
30.1

30.0
29.9
29.8
29 6
29.5

29.3
29 2
29 1
29 0
28.8

28.7
28 6
28,4
28,3
28.2

28 1

35.2
35.0
34.8
34.7
34.5

34.4
34.3
34,2
34,0
33.9

33.7
33.6
33.4
33.3
33.1

33.0
32.9
32.7
32.6
32,4

32,2
32,1
32,0
31,8
31.7

31.6
31 5
31 3
31 2
31,0

30,9
30,8
30,7
30 5
30,4

30 3
30,2
30,0
29 9
29.7

29 6
29,6
29.3
29 2
29 1

29.0

36.2
36.0
35.8
35.7
35.5

35.4
35.3
35.2
35.0
34.9

34.7
34.6
34.4
34.3
34.1

34.0
33.9
33.7
33.6
33.4

33 2
33.1
33.0
32 8
32.7

32.6
32 5
32,3
32 2
32,0

31,9
31 8
31 6
31,5
31.4

31.3
31.2
31 0
30 9
30.7

30.6
30.4
30.3
30 2
30,1

30,0

37.3
37.1
36.9
36.8
36.6

36.5
36.3
36.2
36.1
35.9

35.7
35.6
35,4
35,3
35,1

35.0
34 9
34.7
34 6
34.4

34.2
34.1
33,9
33,8
33,6

33 5
33 1
33 2
83 1
33 0

32 9

32 7
32 6
32 5
32 3

32 2
32 1
31 9
31 8
31 6

31 5
31 3
31 2
311
31.0

30 9

38.3

32

38.1

34

38.0

36

37.8

38

37.7

40

37.5

42

37.3

44

37.2

46

37.1

48

36 9

50

36.7

52

36 6

54

36.4

56

58

36 3
36.1

60

36 0
35 9
35,7

35 6
35,4

36 2
36 1
34 9
34 8
34 6

62

64

66

68

•70

72

74

76

78

80

34 6
34 4
34 2
34 I
34 0

82

84

86

88

90

33 9
33 7

92

33 6

94

33 6

96

33 3

98

100

33 2
33 0

102

32 9

104

32 7

106

32 6

108

110

32 5
32 3

112

32 2

114

32 I

32 0

118

120

SI 9

532

BULLETIN NUMBER SIXTEEN OF

REDUCTION OF BAUME GRAVITY READINGS TO 60 F— Con.

Observed Degrees Baume'

Observed
Temperature in

37.0

38.0

39.0

40.0

41.0

42.0

43.0

44.0

45.0

46.0

Corr

esponding Degrees Baume' at 60° F

30

32

39.3
39.2
39.0
38.9
38.7

38.5
38.4
38.2
38.1
37.9

37.8
37.6
37.4
37.3
37.1

37.0
36.9
36.7
36.6
36.4

36.2
36.1
35.9
35.8
35.6

35.5
35.3
35 2
35.1
34.9

34.8
34.6
34.5
34.4
34.2

34.1
33.9
33.8
33.6
33.5

33.4
33.2
33.1
33.0
32.9

32.8

40.3
40.2
40.0
39.9
39.7

39.5
39.4
39.2
39.1
38.9

38.8
38.6
38.4
38.3
38.1

38.0
37:9
37.7
37.6
37.4

37.2
37.1
36.9
36.8
36.6

36.5
36.3
36.2
36.1
35.9

35.8
35.6
35.5
35.4
35.2

35 1
34.9
34.8
34 6
34.5

34.4
34.2
34.1
34.0
33.9

33.7

41.4
41.3
41.1
41.0
40.8

40.6
40.5
40.3
40.1
39.9

39.8
39.6
39.5
39.3
39.1

39.0
38.9
38.7
38.6
38.4

38.2
38.1
37.9
37.8
37.6

37.5

37.3
37.2
37.0
36.9

36.7
36.6
36.4
36.3
36.1

36.0
35 8
35.7
35.5
35.4

35.3
35.1
35.0
34.9
34.8

34.6

42.4
42.3
42.1
42.0
41.8

41.6
41.5
41.3
41.1
40.9

40.8
40.7
40.5
40.3
40.1

40.0
39.9
39.7
39.5
39.4

39.2
39 1
38.9
38.7
38.6

38.5
38.3
38.2
38.0
37.9

37.7
37.6
37.4
37.3
37.1

37.0
36.8
36.7
36.5
36.4

36.3
36.1
36.0
35.9
35.7

35.6

43.5
43.4
43.2
43.1
42.9

42.7
42.5
42.4
42.2
42.0

41.8
41.7
41.5
41.3
41.1

41.0
40.9
40.7
40.5
40.4

40.2
40.0
39.8
39.7
39.5

39.4
39.2
39.1
38.9
38.8

38.6
38.5
38.3
38 2
38.0

37.9
37.7
37.6
37.4
37.3

37.2
37.0
36.9
36.8
36.6

36.5

44.5
44.3
44.2
44.0
43.9

43.7
43.5
43.4
43.2
43.0

42.8
42 6
42.5
42.2
42.1

42.0
41.9
41.7
41.5
41.4

41.2
41.0
40.8
40.7
40.5

40.4
40.2
40.1
39.9
39.8

39.6
39.5
39.3
39.2
39.0

38.9
38.7
38.6
38 4
38.3

38.1
38.0
37.8
37.7
37.5

37.4

45.6
45.4
45.3
45.1
45.0

44.8
44.6
44.4
44.2
44.1

43.9
43.7
43.5
43.3
43.1

43.0
42.9
42.7
42.5
42.4

42.2
42.0
41.8
41.7
41 5

41.3

41.2
41.0
40.9
40.7

40.5
40.4
40.2
40.1
39.9

39.8
39.6
39.5
39.3
39.2

39.0
38 9

38.7
38 6
38.4

38.3

46.6
46.4
46.3
46.1
46.0

45.8
45.6
45.4
45.2
45.1

44.9
44.7
44.5
44.3
44.1

44.0
43.9
43.7
43.5
43.3

43.1
43.0
42.8
42.7
42.5

42.3
42.2
42.0
41.9
41.7

41.5
41.4
41.2
41.1
40.9

40.7
40.6
40.4
40.3
40.1

40.0
39.8
39.7
39.5
39.4

39 2

47.7
47.5
47.3
47.2
47.0

46.8
46.6
45.4
46.2
46.1

45.9
45.7
45.5
45.3
45.2

45.0
44.9
44.7
44.5
44 3

44.1
44.0
43.8
43.6
43.4

43.2
43.1
42.9
42.8
42.6

42.5
42.3
42.2
42.0
41.8

41.6
41.5
41.3
41.2
41.0

40.9
40.7
40.6
40.4
40.3

40.1

48.7
48.5

34

48.3

36

48.2

38

48.0

40

47.8

42

44

47.6
47.4

46

47.2

48

47.1

50

46.9

52

46.7

54

46.5

56

46.3

58

46.2

60

46.0

62

45.9

64

45.7

66

45.5

68

45.3

70

45.1

72

45.0

74

44.8

76

44.6

78

44.4

80

44.2

82

44.1

84

43.9

86

43.8

88

43.6

90

43.5

92

43.3

94

43.2

96

43.0

98

42.8

100

42.6

102

42.5

104

42.3

106

42.2

108

42.0

110

41.8

112

41.6

114

41.5

116

118

120

41.4
41.2

41.0

KANSAS CITY TESTING LABORATORY

533

REDUCTION OF BAUME GRAVITY READINGS TO 60 F— Con.

Observed

Temperature in

°F.

Observed Degrees Baume'

47.0 48.0 49.0 50.0 51.0 52.0 53.0 54.0 55.0 56.0

Corresponding Degrees Baume' at 60° F.

30..
32..
34..
36..
38..

40. .
42..
44. .
46..
48..

50..

52.

54.

56.

58.

60.
62.
64.
66.
68.

70.
72.
74.

76.
78.

80.

a.

ii.
66.
88.

90.
92.
94.
96.
98.

100.
102.
104.
106.
108.

110.
112.
114.
116.
118.

120.

49.8
49.6
49.4
49.3
49.1

48.9
48.7
48.5
48.3
48.1

47.9
47.7
47.6
47.4
47.2

47.0
46.9
46.7
46.5
46.3

46.1
46.0
45.8
45.6
45.4

45.2
45.1
44.9
44.7
44.5

44.
44.
44.
43.
43.

43,
43
43
43
42

42
42
42
42
42

41

50.8
50.6
50.4
50.3
50.1

49.9
49.7
49.5
49.3
49.1

48.9
48.7
48.6
48.4
48.2

48.0
47.9
47.7
47.5
47.3

47.1
47.0
46.8
46.6
46 4

46.2
46.1
45.9
45.7
45.5

51.9
51.7
51.5
51.4
51.2

51.0
50.8
50.6
50.4
50.2

50.0
49.8
49.6
49.4
49.2

49.0
48.8
48.6
48.4
48.3

48.1
47.9
47.7
47.5
47.3

47.2
47.0
46.8
46.6
46.4

4

45.4

46.3

2

45.2

46.1

1

45.1

46.0

9

44.9

45.8

7

44.7

45.6

5

44.5

45.4

4

44.3

45.2

2

44.1

45.0

1

44.0

44.9

9

43.9

44.8

7

43.7

44.6

5

43.5

44.4

4

43.4

44.3

3

43.3

44.2

.1

43.1

44.0

.9

42.9

43.8

53.0
52.8
52.6
52.4
52.2

52.0
51.8
51.6
51.4
51.2

51.0
50.8
50.6
40.4
50.2

50.0
49.8
49.6
49.4
49.3

49.1
48.9
48.7
48.5
48.3

48.2
48.0
47.8
47.6
47.4

47.3
47.1
46.9
46.7
46.6

46.4
46.2
46.0
45.8
45.7

45.6
45.4
45 3
46.1
44.9

54.1
53.9
53.7
53.5
53.3

53.0
52.8
52.6
52.4
52.2

52.0
51.8
51.6
51.4
51.2

51.0
50.8
50.6
50.4
50.3

SO.l
49.9
49.7
49.5
49.3

49.1
48.9
48.7
48.5
48.3

48.2
48.0
47.8
47.6
47.5

44.7

46.6
46.3
46.2
46.0
45.8

46.6

55.1
54.9
54.7
54.5
54.3

54.1
53.8

53
53
53

53.0
52.8
52.6
52.4
52.2

52 0
51.8
51.6
51.4
51.3

51.1
50.9
50.7
50.5
50.3

50.1
49.9
49.7
49.5
49.3

49.2
49.0

48 8
48 6
48.4

48.3
48 1
47.9

47.7
47.6

47
47
47
46
46

56

2

56

0

55

8

55

6

55

4

55

2

54

9

54

7

54

5

54

2

54

0

53

8

53

6

53

.4

53
53

.2

0

46.5

52.8
52.6
52.4
52.2

52.0
51.8
51.6
51.4
51.2

51.0
50.8
50.6
50.4
60.2

60.1
49.9
49.7
49.6
49.3

49.2
49.0
48 8
48.6
48.4

48 3
48.1
48 0
47.8
47.6

57.3
57.1
56.8
56.6
56.4

56.2
56.0
55.7
55.5
55.2

55.0
54 8
54.6
54.4
54.2

54 0
53.8
53.6
53.4
53.2

53 0
52.8
52.6
62 4
52 2

52 0

51 8

51 6

51 4

51 2

51 0
60 9
60.7
60.5
60.3

49 2
49 0
48 H
48 6
48 4

68
68
57
57
57

57.2
57.0
66.8
66.5
56.3

56.
65.
56.
66
65

55 0
54.8
54.6
54 4
54.2

54.0
52.8
63.5
53 3
53.1

52 9
62.7
62 6
62.3
62.1

51 9
51.8
61 6
61 4
61 2

46.4 48 2

61.0
50 8
60.6
60 4
60.S

50.1
49 9
49 7
49 6
49 3

49 1

69.4
69.2
58.9
58.7
68.6

68.2
58.0
57.8
67 6
57.3

57.1
56 9
56 6
56 4
56.2

66

0

66

8

66

6

66

4

56

2

65

0

64

8

64

5

54

3

64

1

53

9

53

7

63

6

63

3

63

1

52

9

52

7

52

6

62

3

52

1

61

9

61

7

61

f>

61

3

51

2

61

0

60

.•.0

H

'I'

1

r.o 0

534

BULLETIN NUMBER SIXTEEN OF

REDUCTION OF BAUME GRAVITY READINGS TO 60 F— Con.

Observed

temperature In

'f

32..^
34....
36....
38....

40....
42....
44....
46....
48....

50....
52....
54....
56....
58....

60....
62....
64....
66...,
68..,.

70....
72....
74....
76....
78....

80....
82....
84....
86....
88....

90....
92....
94....
96. . . .
98....

100....
102....
104....
106....
108....

110....
112,...
114....
116....
118....

120....

Obserred degrees Baumfi

57.0

60.5
60.3
60.0
59.8
59.5

59.3
59.1
58.9
58.6
58.4

58.1
57.9
57.7
57.5
57.3

57.0
56.8
56.6
56.4
56.1

55.9
55.7
55.5
55.3
55.0

54.8
54.6
54.4
54.2
54.0

53.8
53.6
53.4
53.2
53.0

52.8
52.6
52.4
52.2
52.1

51.9
51.7
51.5
51.3
51.1

50.9

58.0

59.0 60.0 61.0 62.0

63.0

64.0

Corresponding degrees Baumi at 60° F

65.0

61.6

62.7

63.7

64.8

65.8

66.9

67.9

69.0

61.3

62.4

63.4

64.5

65.5

66.6

67.7

68.8

61.0

62.1

63.1

64.2

65.2

66.3

67.4

68.5

60.8

61.9

62.9

64.0

65.0

66.1

67.1

68.2

60.5

61.6

62.6

63.7

64.7

65.8

66.8

67.9

60.3

61.4

62.4

63.5

64.5

65.5

66.5

67.6

60.1

61.2

62.2

63.3

64.3

65.3

66.3

67.4

59.9

61.0

62.0

63.0

64.0

65.0

66.0

67.1

59.6

60.7

61.7

62.7

63.7

64.8

65.8

66.8

59.4

60.4

61.4

62.5

6S.5

64.5

65.5

66.5

59.1

60.2

61.2

62.2

63.2

64.2

65.2

66.2

58.9

60.0

61.0

62.0

63.0

64.0

65.0

66.0

58.7

59.8

60.8

61.8

62.8

63.8

64.8

65.8

58.5

59.5

60.5

61.5

62.5

63.6

64.6

65.6

58.3

59.3

60.3

61.3

62.3

63.3

64.3

65.3

58.0

59.0

60.0

61.0

62.0

63.0

64.0

65.0

57.8

58.8

59.8

60.8

61.8

62.7

63.7

64.7

57.6

58.6

59.6

60.5

61.5

62.5

63.5

64.5

57.4

58.3

59.3

60.3

61.3

62.3

63.3

64.2

57.1

58.1

59.1

60.1

61.1

62.1

63.1

64.0

56.9

57.9

58.9

59.8

60.8

61.8

62.8

63.8

56.7

57.7

58.7

59.6

60.6

61.6

62.6

63.5

56.5

57.4

58.4

59.3

60.3

61.3

62.3

63.2

56.3

57.2

58.2

59.1

60.1

61.0

62.0

63.0

56.0

57.0

58.0

58.9

59.9

64.8

61.8

62.8

55.8

56.8

57.8

58.7

59.7

60.6

61.6

62.6

55.6

56.5

57.5

58.4

59.4

60.4

61.4

62.3

55.4

56.3

57.3

58.2

59.2

60.1

61.1

62.0

55.2

56.1

57.1

58.0

59.0

59.9

60.9

61.8

55.0

55.9

56.9

57.8

58.8

59.7

60.6

61.5

54.8

55.7

56.7

57.6

58.6

59.5

60.4

61.3

54.6

55.5

56.5

57.4

58.4

59.3

60.2

61.1

54.3

55.2

56.2

57.1

58.1

59.0

59.9

60.8

54.1

55.0

56.0

56.9

57.9

58.8

59.7

60.6

53.9

54.8

55.8

56.7

57.6

58.5

59.5

60.4

53.7

54.6

55.6

56.5

57.4

58.3

59.3

60.2

53.5

54.4

55.4

56.3

57.2

58.1

59.0

59.9

53.3

54.2

55.2

56.1

57.0

57.9

58.8

59.7

53.1

54.0

55.0

55.9

56.8

57.7

58.6

59.5

53.0

53.9

54.8

55.7

56.6

57.5

58.4

59.3

52.8

53.7

54.6

55.5

56.4

57.3

58.2

59.1

52.6

53.5

54.4

55.2

56.2

57.1

58.0

58.9

52.4

53.3

54.2

55.1

56.0

56.9

57.8

58.7

52.2

53.1

54.0

54.9

55.8

56.7

57.6

58.4

52.0

52.9

53.8

54.7

55.6

56.5

57.4

58.2

SI. 8

52.7

53.6

54.5

55.4

56.3

57.2

58.0

KANSAS CITY TESTING LABORATORY

535

REDUCTION OF BAUME GRAVITY READINGS TO 60 F— Con.

Observed Degrees Baume'.

Observed
Temperature in

°F.

67.0

68.0

69.0

70.0

71.0

72.0

73.0

74.0

75.0

76.0

Corresponding Degrees Baume' at 60° F.

30

71.1
70.9
70.6
70.3
70.0

69.7
69.4
69.1
68.8
68.6

68.3
68.0
67.8
67.6
67.3

67.0
66.7
66.4
66.2
66.0

65.7
65.4
65.2
64.9
64.7

64.5
64.2
63.9
63.7
63.4

63.2
63.0
62.7
62.5
62.2

62.0
61.8
61.6
61.3
61.1

60.9
60.7
60 5
60.2
60.0

59.8

72.1
71.9
71.6
71.3
71.0

70.7
70.4
70.1
69.8
69.6

69.3
69.0
68.8
68.6
68.3

68.0
67.7
67.4
67,2
67.0

66.7
66.4
66.2
65.9
65.6

65.4
65.2
64.9
64.7
64.4

64.2
64.0
63.7
63.5
63.2

63.0
62.8
62.5
62.3
62.0

61.8
61.6
61.4
61.1
60.9

60.7

73.2
73.0

72.7
72.4
72.1

71.8
71.5
71.2
70.9
70.6

70.4
70.1
69.9
69.6
69.3

69 0
68.7
68.4
68.2
67.9

67.6
67.4
67.2
66.9
66.6

66.4
66.1
65.9
65.8
65.3

65.1
64.9
64,6
64.4
64.1

63.9
63 7
63.4
63 2
62.9

62.7
62.5
62.3
62.0
61.8

61.6

74.3
74.0
73.7
73.4
73.1

72.8
72.5
72.2
71.9
71.6

71.4
71.1
70.9
70.6
70.3

70.0
69.7
69.4
69.2
68.9

68.6
68.4
68.2
67.9
67.6

67.4
67.1
66.8
66.6
66.3

66.1
65.8
65.6
65.4
65.1

64.9
64.6
64.3
64.1
63.8

63.6
63.3
63.1
62.9
62.7

62.5

75.4
75.1
74.8
74.5
74.2

73.9
73.6
73.3
73.0

72.7

72.5
72.2
71.9
71.6
71.3

71.0
70.7
70.4
70,1
69.8

69.5
69.3
69.1
68.8
68.5

68.3
68.0
67.7
67.5
67.2

67.0
66.7
66.5
66.3
66.0

65 8
65,5
65.2
65.0
64.8

64.5
64.2
64.0
63.8
63.6

63.3

76.4
76 1
75.8
75.5
75.2

74.9
74.6
74.3
74.0
73.7

73.5
73.2
72.9
72.6
72.3

72.0
71.7
71.4
71.1
70.8

70.5
70.3
70.1
69.8
69.5

69.3
69.0
68.7
68.4
68.2

68.0
67.7
67.4
67.2
66.9

66.7
66.4
66.1
66.9
65.7

65.4
66 2
64.9
64.7
64.5

64.2

77.5
77.2
76.9
76.6
76 3

76.0
75.7
75.4
75.1
74.8

74.5
74.2
73.9
73.6
73.3

73.0
72.7
72.4
72.1
71.8

71.5
71.2
71.0
70.8
70.5

70.2
69.9
69.6
69.3
69.1

68.9
68.6
68 3
68.1
67.8

67 6
67.3
67.0
66.8
66.6

66.3
66 1
65.8
65 6
65.4

66.1

78.5
78.2
77.9
77.6
77.3

77.0
76.7
76.4
76.1
75.8

75.5
75.2
74.9
74.6
74.3

74.0
73.7
73.4
73.1
.72.8

72.5
72 2
72.0
71.8
71.5

71.2
70.9
70.6
70 3
70.1

69 9
69.6
69 3
69 0
68.8

68,6
68 2
67 9
67.7
67 5

67 2
67.0
66 7
66 6
66 3

66.0

79.6
79.3
79.0
78.7
78.4

78.1
77.8
77.5
77.1
76.8

76.5
76.2
75.9
75,6
75,3

75.0
74.7
74.4
74,1
73.8

73.5
73.2
72 9
72.7
72.4

72.1
71.8
71 6
71.3
71.0

60 8
70 6
70 2
69 9
69 . 7

69.4
69 1
68 8
68 6
68 4

68 1
67 8
67 6
67 4
67.1

66.8

80.7

32

80.4

34

80.1

36

79.7

38

79.4

40

79.1

42

78.8

44

78.5

46

78.1

48

77.8

50

77.5
77.2
76 9
76.6
76.3

52

54

56

58

60

76.0
75.7
76.4
75.1
74.8

62

64

66

68

70

74,5
74 2
73 •)

72

74

73.7
73.4

76

80

73.1
72 8

82

72 5

84

72 3

86

72 9

88

71 7
71 4

92

71 1

94

70 8

96

70.6

98

100

70 4
70 1

102

69 8

69 6

106

69.3

108

110

09 0

68 7

112

6K 6

114

68 3

116

68 0

120

67.7

536

BULLETIN NUMBER SIXTEEN OF

REDUCTION OF BAUME GRAVITY READINGS TO 60 F— Con.

Observed

Mmperature In

Observed degrees Baumfi

77.0

78.0

79.0 80.0 81.0 82.0

83.0

84.0

Conesponding degrees Bsumi at 60* F

8S.0

30.
32.
34.
36.
38.

40.
42.
44.
46.
48.

SO.

S2,
54.
56.
58.

60.
62.
64.
66.
68.

70.
72.
74.
76.
78.

80.
82.
84,
86.
88.

90.
52.
94.

96.
98.

100.
102.
104.
106.
108.

110.
112
114
116.
118.

8t8
81.5
81.2
80.-e
80.5

sai

79.8
79.5
79.2
78.9

78.6
78.2
77.9
77.6
77.3

77.0
76.7
76.4
76.1
75.8

75.5
75.2
74.9
74.6
74.3

74.0
73.7
73.4
73.2
72.9

72.6
72.3
72.0
71.7
71.5

71.2
71.0
70.7
70.4
70.1

69.8
69.6
69. 4
69.1
68.8

68.5

82.9

84.0

85.0

86.1

87.1

88.2

89.3

90.4

82.6

83.7

84.7

85.8

86.8

87.9

89.0

90.1

82.2

83.3

84.3

85.4

86.4

87 5

88.6

89.7

81.9

83.0

84.0

85.1

86.1

87 2

88.2

89.3

81.5

82.6

83.6

84.7

85.7

86.8

87.8

88.9

81.1

82.2

83.2

84.3

85 3

86.4

87 4

88.5

80.8

81.9

82.9

84.0

85.0

86.1

87.1

88.2

60.5

81.6

82.6

83.7

84.7

85.8

86.8

87.8

8a2

81.3

82.3

83.4

84.4

85.4

86.5

87.5

79.9

81.0

82.0

83.0

84.0

85.1

86.1

87.1

79.6

80.6

81.6

82.6

83.6

84.7

85.7

86.7

79.2

80.3

81.3

82.3

83.3

84.3

85.3

86.3

78-9

79.9

81.0

82.0

83.0

84.0

85.0

86.0

78.6

79.6

80.6

81.6

82-6

83.7

84.7

85 7

78.3

79.3

80.3

81.3

82.3

83.3

84.3

85.3

78.0

79.0

80.0

81.0

82.0

83.0

84.0

85.0

77.7

78.7

79.7

80.7

81.7

82.7

83.7

84.7

77.4

78.4

79.4

80.4

81.4

82.3

83.4

84.3

77.1

78.1

79.1

80.0

81.0

82.0

83.0

84.0

76.8

77.7

78.7

79.7

80.7

81.7

82.7

83.7

76.5

77.4

78.4

79.4

80.4

81.4

82.4

83.3

76.2

77.1

78.1

79.1

80.1

81.1

82.1

83.0

75.9

76.8

77.8

78.8

79.8

80.7

81.7

82.7

75.6

76.5

77.5

78.4

79.4

80.4

81.4

82.4

75.3

76.2

77.2

78.1

79.1

8a 1

81.1

82.0

75.0

75.9

76.9

77.8

78.8

79.8

80.8

81.7

74.7

75.6

76.6

77.5

7&5

79.4

80.4

81.3

74.5

75.3

76.3

77 2

78.2

79.1

80.1

81.0

74.1

75.0

76.0

76.9

77 9

78.8

79.8

80.7

73.9

74.8

75.8

76.7

77.6

7&5

79.5

80.4

73.6

74.5

75.5

76.4

77.3

78.2

79.2

80.1

73.3

74.2

75.2

76.1

77.0

77.9

78.9

79.8

73.0

73.9

74.9

75.8

76.7

77.6

78.6

79.5

72.7

73.6

74.6

75 5

76.4

77.3

78.3

79.2

72.4

73.3

74.3

75 2

76.1

77.0

78.0

7a 9

72.1

73.0

74.0

74.9

75 8

76.7

77.6

78.5

71.9

72.8

73.7

74.6

75 5

76.4

77.3

78.2

71.6

72.5

73.4

74.3

75.2

76.1

77.0

77.9

71.3

72.2

73.1

74.0

74.9

75.8

76.7

77 6

71.0

71.9

72.8

73.7

74.6

75.5

76.4

77.3

70.7

71.6

72.5

73.4

74.3

75 2

7&1

77.0

70.5

71.4

72.3

73.2

74.1

74.9

75.8

76.7

70.3

71.2

72.1

72.9

73.8

74.6

75 5

76.4

70.0

70.9

71.8

72 6

73.5

74.3

75 2

76.1

69.7

70.6

71.5

72.3

73.2

74.0

74.9

75.8

69.4

70.3

71.2

72.0

72.9

73.7

74.6

75.5

KANSAS CITY TESTING LABORATORY

537

BAUME', SPECIFIC GRAVITY AND POUNDS PER GALLON— Con.

Observed degrees Baam6

ObseiT«d
temperatoie in

87.0

88.0

89.0

9ao

91.0

92.0

93.0

94.0

9S.0

96.0

Correspondlac deeiees Baumi at 60°

F

SO

92.6
92.2
91.8
91.4
91.0

90.6
90.3
89.9
89 6
89 2

88.8
88.4
88.0
87.7
87.3

87.0
86.7
86.3
86.0
85.6

85.3
85.0
84.6
84.3
84.0

83.6
83.2
82.9
82.6
82.3

82.0
81.7
81.3
81.0
80.7

80.4
80.1
79.7
79.4
79.1

78.8
78.5
78.2
77.9
77.5

77.2

93.6
93.2
92.9
92.5
92.1

91.7
91.3
90.9
90.6
90.2

89.8
89.4
89.0
88.7
88.3

88.0
87.7
87.3
87.0
86.6

86.3
86.0
85.6
85.3
85.0

84.6
84.2
83.8
83.5
83.2

82.9
82.6
82.2
81.9
81.6

81.3
81.0
80 6
80.3
80.0

79.7
79.4
79 1
78.8
78.4

78.1

94.7
94.3
93.9
93.6
93.2

92.8
92.4
92.0
91.7
91.3

90 9
90 5
90 1
89.7
89.4

89.0
88.6
88.3
88.0
87.6

87.3
86.9
86.5
86.2
85.9

85.5
85.1
84.7
84.4
84.1

83.8
83.5
83.1
82.8
82.5

82.2
81.9
81.5
81.2
80 9

80.6
80.3
60.0
79.7
79.3

79.0

95. 7
95.3

94.9
94.6
94.2

93.8
93.4
93.0
92.7
92.3

91.9
91.5
91.1
90.7
90.4

90.0
89.6
89 3
89 0

8a 6

88.3
87.9
87.5
87.2
86.9

86.5
86.1
85.7
85.4
85.1

84.8
84.4
84.1
83.7
83.4

83.1
82.8
82.5
82.1
81.8

81.5
81.2
80.9
80.6
80.2

79 9

95.9
95.6
95.2

94.9
94.5
94.1
93.7
93.3

92.9
92.5
92.1
91.7
91.4

91.0
90 6
90.3
89.9
89.5

89 2
88.8
88.4
88.1
87.8

87.4
87.0
86.6
85.3
86.0

85.7
85.3
85.0
84.6
84.3

84.0
83.7
83.4
83.0
82.7

82.4
82,1
81.7
81.4
81.1

80.8

95.9
95.5
95.1
94.7
94.3

93.9
93.5
93.1
92.7
92.4

92.0
91.6
91.3
90.9
90.5

90.1
89.8
89 4
891
88.7

88.4
88.0
87.6
87.3
87.0

86.6
86.2
85.9
85.6
85.2

84.9
84.6
84.3
83.9
83.6

83.3
83.0
82 6
82.3
82.0

81.7

96 i
95.7
95.3

94.9
94 5
94.1
93.7
93.4

93.0
92.6
92.2
91.8
91.4

91.0
90.7
90 3
90 0
89 6

89.3
88.9
88.5
88.2
87.9

87.5
87.1
86.8
86.5
861

85.8
85.5
85.2
84.8
84 5

84.2
83.8
83.5
83.2
82.8

82. S

95.9
95.5
95.1
94 7
94.4

94.0
93.6
93.2
92.8
92.4

92.0
91.7
91.3
91.0
90.6

90.2
89.8
89 4
89.1
88.8

88.4
8&1
87.7
87.4
87.0

86.7
86.4
86 1
85.7
85.4

85.1
84.7
84.4
84.1
83.7

83.4

95.7
95.4

95.0
94.6
94.2
93.8
93.4

93.0
92.7
92.3
92.0
91.6

91.2
90 8
904
90.0
89.7

89 3
89.0
88.6
88 3
88 0

87.6
87.3
87.0
86.6
86 5

86.0
85.6
85.3
85 0
64 6

84.3

32

34

36

38

40

42

44

46

48

50

52

54

56

58

£0

96.0
95.6
95.2
94.8
94.4

62

(4

66

68

70

94.0
93. T
913

72

93.0

76 ■

92. «

92.2
91 8

82

91.4

91.0

86

9a7

90

92

90.3
900
89.6

89. S

96

e«.o

(8.6
88 S

102

87.9

S7<

106

»7.1

108

110

K.9

866

112

861

114

M.9

116

SV«

118

•S.I

538

BULLETIN NUMBER SIXTEEN OF

Reduction of Specific Gravity Readings to 60 °F.

This tabic shows Ihe specific si-avitit-s at 60"/60"F of oils ha\ing, at the
designated lemperaturi s, the observed specific gravities indicated. For example,
if the observed specific gravity is 0.614 at SCP, the true specific gravity at
60V60°P is 0.621 (under 0.610) plus 0.001 or 0.625. The headings "Observed spe-
cific gravity" and "Observed temperature" signify the true indication of the
hydrometer and the true temperature of the oil; that is, the observed readings
corrected, if necessary, for instrumental errors.

Observed Specific Gravity.

Observed
Tempera-
ture, ° F.

0.600

0.610

0.620

0.630

*

0.640

0.650

0.660

0.670

0.584

0.594

0.604

0.614

0.624

0.634

0.644

0.654

.585

.595

.606

.616

.025

.635

.645

.655

.586

.596

.607

.617

.626

.636

.646

.656

.587

.597

.608

.618

.027

.637

.647

.657

.588

.598

.609

.619

.628

.638

.648

.659

.589

.599

.610

.620

.6295

.6395

.6495

.660

.590

.600

.611

.620

.6305

.6405

.6505

.661

.591

.601

.612

.621

.6315

.6415

.6515

.662

.592

.602

.613

.622

.6325

.6425

.6525

.663

.593

.603

.614

.623

.6335

.6435

.6535

.664

.595

.005

.615

.6245

.6345

.645

.654

.665

.596

.606

.616

.626

.636

.646

.656

.666

.597

.607

.617

.627

.637

.647

.657

.667

.598

.608

.618

.628

.638

.648

.658

.668

.599

.609

.619

.629

.639

.649

.659

.669

.600

.610

•.620

.630

.640

.650

.660

.670

.601

.611

.621

.631

.641

.651

.661

.671

.602

.612

.622

.632

.642

.652

.662

.672

.603

.613

.623

.633

.643

.653

.663

.673

.604

.614

.6245

.6345

.644

.654

.664

.674

.605

.615

.6255

.6355

.645

.655

.665

.675

.606

.616

.6265

.6365

.646

.656

.666

.676

.607

.617

.6275

.6375

.647

.657

.667

.677

.608

.618

.6285

.6385

,648

.658

.668

.678

.609

.620

.6295

.6395

.649

.659

.669

.679

.611

.621

.630

.640

.650

.660

.670

.680

.612

.622

.632

.641

.651

.661

.671

.671

.613

.623

.633

.642

.652

.662

.672

.682

.614

.624

.634

.643

.653

.663

,673

.683

.615

.625

.635

.644

.654

.664

.674

.683

.616

.626

.636

.645

.655

.665

.675

.684

.617

.627

.637

.646

.656

.666

.676

.685

.618

.628

.638

.647

.657

.667

.677

.686

.619

.629

.639

.648

.658

.668

.678

.687

.620

.630

.640

.649

.659

.669

.679

.688

.621

.631

.641

.650

660

.670

.680

.689

.622

.632

.642

.651

.661

.671

.680

.690

.623

.633

.643

.652

.662

.672

.681

.691

.624

.634

.644

.653

,663

.673

.682

.692

.625

.635

.645

.654

.664

.674

.683

.693

.626

.636

.646

.655

.665

.675

.684

.694

.627

.637

.647

.656

.606

.676

.685

.695

.629

.638

.648

.657

.667

.677

.686

.696

.630

.639

.049

.658

.668

.678

.687

.697

.631

.640

650

.659

.669

.679

.688

.698

.632

.641

.651

.660

.670

.680

.689

.699

0.665
.666
.667
.668
.669

.670
.671
.672
.673
.674

.675
.676
.677
.678
.679

.680
.681
.682
.683
.684

.685

.686

.687

.6875

.6885

.689
.690
.691
.692
.693

.694
.695
.696
.697
.698

.699
.700
.701
.702
.703

.704
.704
.705
.706
.707

.708

KANSAS CITY TESTING LABORATORY

539

REDUCTION OF SPECIFIC GRAVITY TO 60 °F— Continued.
Observed Specific Gravity.

Observed

Tempera-

0 700

0.710

0.720

0.730

0.740

0.750

0.760

0.770

0.780

0.790

ture, ° F.

30

0.685

0.695

0.705

0.716

0.723

0.736

0.746

0.757

0.767

0.777

32

.686

.696

.706

.717

.727

.737

.747

.758

.768

.778

34

.687

.697

.707

.718

.728

.738

.748

.759

.769

.779

36

.688

.698

.708

.719

.729

.739

.749

.760

.770

.780

38

.689

.699

.709

.720

.730

.740

.750

.761

.771

.781

40

.6905

.7005

.7105

.7205

.7310

.7140

.7515

.7615

.7715

.7820

42

.6915

.7015

.7115

.7215

.7315

.7420

.7520

.7625

.7725

7825

44

.6925

.7025

.7125

.7225

.7325

.7430

.7530

.7630

.7735

.7835

46

.0935

.7035

.7135

.7235

.7335

.7440

.7540

.7640

.7740

7845

48

.6940

.7045

.7145

.7245

.7345

.7445

.7550

.7650

.7750

.7850

50

.6950

.7055

.7155

.7255

.7355

.7455

.7555

.7660

.7760

.7860

52

.6960

.7065

.7165

.7265

.7365

.7465

.7565

.7665

.7765

.7870

54

.6970

.7070

.7170

.7270

.7370

.7475

.7575

.7675

.7775

.7875

56

.6980

.7080

.7180

.7280

.7380

.7480

.7580

.7685

.7785

.7885

58

.6990

.7090

.7190

.7290

.7390

.7490

.7590

.7090

.7790

.7890

60 ... .

.7000

.7100

.7200

.7300

.7400

.7500

.7600

.7700

.7800

.7900

62. ....

.7010

.7110

.7210

.7310

.7410

.7510

.7610

.7710

.7810

.7905

64

.7020

.7120

.7220

.7320

.7415

.7515

.7615

.7715

.7815

.7915

66

.7030

.7130

.7225

.7325

.7425

.7525

.7625

.7725

.7825

7925

68

.7040

.7135

.7235

.7335

.7435

.7535

.7630

.7730

.7830

.7930

70

.7050

.7145

.7245

.7345

.7445

.7545

.7640

.7740

7840

.7940
.7945
.7955

72

7055

.7155

.7255

.7355

.7450

.7550

.7650

.7750

i85|).

74

7065

.7165

.7265

.7365

.7460

.7560

.765?

.7755

.7855

76

.7075

.7175

.7275

.7370

.7470

.7570

.7665

.7765

.7865

7965
.7970

78

.7085

.7185

.7285

.7380

.7480

.7580

.7675

.7775

.7875

80

.709

.719

.729

.739

.748

.758

.768'

.778

.788

.798
.798
799
800
801

82

.710

.720

.730

.740

.749

.759

.769

.779

.(89

84

86

88

.711
.712
.713

.721
.722
.723

.731
.732
.733

.741
.741
.742

.750
.751
.752

.760
.761
.762

.770
.771
.771

.780
.780
.781

.789
.790
.791

90

92

94

96

98

.714
.715
.716
.716
.717

.724
.724
.725
.726
.727

.733
.734
.735
.736
.737

.743
.744
.745

•.746
.747

.753
.754
.755
.755
.756

.763
.763
.764
.765
.766

.772
.773
.774
.775
.775

.782
.783
.784
.784
.785

.792
.793
.793
.794
.795

802
802
803
.804
80S

100

102

104

106

108

.718
.719
.720
.721

.722

.728
.729
.7.30
.731
.732

.738
.739
.740
.741
.741

.747
.748
.749
.750
.751

.757
.758
.759
.760
.760

.767
.768
.768
.769
.770

.776
.777
.778
.779
.779

.786
.787
.788
.788
.789

796
796

.797
798

.799

805
806
807
808
808

110

112

114

116

118

.723
.724
.725
.726
.726

.733
.734
.734
.735
.736

.742
.743
.744
.745
.746

.751
.753
.753
.754
.755

.761
.762
.703
.704
.765

.771
.772
.772
.773
.774

.780
.781
.782
.783
.784

.790
791
.791
.792
.793

.799
800
801
.802
.803

809
RtO
811
811
8U

120

.727

.737

.746

.756

.765

.775

.784

794

.803

813

540

BULLETIN NUMBER SIXTEEN OF

REDUCTION OF SPECIFIC GRAVITY TO 60 °F— Continued.
Observed Specific Gravity.

Observed
Tempera-
ture, ° F.

0.800

0.788
.788
.789
.790
.791

.7920
.7930
.7935
.7945
.7950

.7960
.7970
.7975
.7985
.7995

.8000
.8005
.8015
.8025
.8030

.8040
.8045
.8055
.8065
.8070

.808
.808
.809
.810
.811

.812
.812
.813
.814
.815

.815
.816
.817
.817
.818

.819
.820
.820
.821
.822

.823

0.810

0,798
.799
.799
.800
.801

.8020
.8030
.8035
.8045
.8050

.8060
.8070
.8075
.8085
.8095

.8100
.8105
.8115
.8125
.8130

.8140
.8145
.8155
.8160
.8170

.817
.818
.819
.820
.820

.821
.822
.823
.823
.824

.825
.826
.826
.827
.828

.829
.829
.830
.831
.832

.832

0.820

0.808
.809
.810
.811
.812

.8125
.8130
.8140
.8145
.8155

.8160
.8170
.8175
.8185
.8195

.8200
.8205
.8215
.8220
.8230

.'8240
.8245
.8255
.8260
.8270

.827
.828
.829
.830
.830

.831
.832
.832
.833
.834

.835
.835
.836
.837
.838

.838
.839
.840
.840
.841

.842

0 830

0.818
.819
.820
.821
.822

.8225
.8230
.8240
.8245
.8255

.8260
.8270
.8280
.8285
.8295

.8300
.8305
.8315
.8320
.8330

.8340
.8345
.8355
.8360
.8370

.837
.838
.839
.839
.840

.841
.842
.842
.843
.844

.844
.845
.846
.847
.847

.848
.849
.850
.850
.851

.852

0.840

0.828
.829
.830
.831
.832

.8325
.8335
.8340
.8345
.8355

.8365
.8370
.8380
.8385
.8395

.8400
.8405
.8415
.8420
.8430

.8440
.8445
.8455
.8460
.8470

.847
.848
.849
.849
.850

.851
.852
.852
.853
.854

.854
.855
.856
.857
.857

.858
.859
.859
.860
.861

.862

0,850

0.839
.839
.840
.841
.842

.8425
.8435
.8440
.8450
.8455

.8465
.8470
.8480
.8485
.8495

.8500
.8505
.8515
.8520
.8530

.8540
.8545
.8550
.8560
.8565

.857
.858
.859
,859
.860

.861
.861
.862
.863
.864

.864
.865
.866
.866
.867

.868
.869
.869
.870
.871

.872

0.860

0,849
.849
.850
.851
.852

.8525
.8535
.8540
.8550
.8555

.8565
.8570
.8580
.8585
.8595

.8600
.8605
.8615
.8620
.8630

.8635
.8645
.8650
.8660
.8665

.867

.869
.870

.871
.871
.872
.873
.873

.874
.875
.876
.876
.877

.878
.878
.879
.880
.881

.881

0.870

0.859
.860
.860
.861
.862

.8625
.8635
.8640
.8650
.8655

.8665
.8670
.8680
.8685
.8695

.8700
.8705
.8715
.8720
.8730

.8735
.8745
.8750
,8760
.8765

.877
.878
.878
.879
.880

.881
.881 ■
.882
.883
.883

.884
.885
.886
,886
,887

,889
,890
.890

.891

0 880

0.869
.870
.870
.871
.872

.8730
.8735
.8740
.8750
.8755

.8765
.8770
.8780
.8785

.8795

.8800
.8805
.8815
.8820
.8830

.8835
.8845
.8850
.8860
.8865

.887

.890

.891
.891
.892
.893
.893

.894
.895
.895
.896
.897

.898
.899
.900
.900

.901

KANSAS CITY TESTING LABORATORY

541

REDUCTION OF SPECIFIC GRAVITY TO 60 °F— Continued.
Observed Specific Gravity.

Observed
Temperature

0.900

0.910

0.920

0.930

0.940

0.950

0.960

0.970

0.980

0.990

1.000

60

0.900
.901
.901
.902
.903

.904
.904
.905
.906
.906

.907 .

.907

.908

.909

.910

.910
.911
.912
.913
.913

.914
.915
.915
.916
.917

.917
.918
.919
.919
.920

.921
.922
.923
.924
.925

.926
.927
.927
.928
.929

.930
.930
.931
.932
.933

.933

0.910
.911
.911
,912
.913

.914
.914
.915
.916
.916

.917
.917
.918
.919
.920

.920
.921
.922
.922
.923

.924
.925
.925
.926
.927

.927
.928
.929
.929
.930

.931
.932
.933
.934
.935

.936
.937
.937
.938
.939

.940
.940
.941
.942
.943

.943

0.920
.921
.921
.922
.923

.924
.924
.925
.926
.926

.927
.927
.928
.929
.930

.930
.931
.932
.932
.933

.934
.935
.935
.936
.937

.937
.938
.939
.939
.940

.941
.942
.943
.944
.945

.946
.947
.947
.948
.949

.950
.950
.951
.952
.953

.953

0.930
.931
.931
.932
.933

.934
.934
.935
.936
.936

.937
.937
.938
.939
.940

.940
.941
.942
.942
.943

.944
.944
.945
.946
.947

.947
.948
.949
.949
.950

.951
.952
.953
.954
.955

.956
.957
.957
.958
.959

.960
.960
.901
.962
.963

963

0.940
.941
.941
.942
.943

.944
.944
.945
.946
.946

.947
.947
.948
.949
.950

.951
.952
.952
.953
.954

.955
.955
.956
.957
.958

.958
.959
.960
.960
.961

.962
.963
.963
.964
.965

.966
.966
.967
.968
.968

.969
.970
.971
.971
.972

.973

0.950
.951
.951
.952
.953

.954
.954
.955
.956
.957

.957
.958
.959
.959
.900

.961
.962
.962
.903
.964

.965
.965
.960
.967
.968

.968
.969
.970
.970
.971

.972
.973
.973
.974
.975

.976
.976
.977
.978
.978

. .979
.980
.981
.981
.982

.983

0.960
.961
.961
.962
.963

.964

.964
.965
.966
.967

.967
.968
.969
.969
.970

.971
.972
.972
.973
.974

.975
"975
.976
.977
.978

.978
.979
.980
.980
.981

.982
.983
.983
.984
.985

.986
.986
.987
.988
.988

.989
.990
.991
.991
.992

.993

0.970
.971
.971
.972
.973

.974
.974
.975
.976
.976

.977
.978
.979
.979
.980

.981
.982
.982
.983
.984

.984
.985
.986
.987
.987

.988
.989
.989
.990
.991

992
.992
.993
.994

994

.995
.996
.997
.997
.998.

.999"
1 000*
1 000^
1.001,
1.002.

1 002'

0.980
.981
.981
.982
.983

.984

.984
.985
.986
.986

.987
.988
.989
.989
.990

.991
.991
.992
.993
.993

.994
.995
.996
.996
.997

.998

.998

.999

1.000

1.001

1.001
1 002
1 003
1 003
1 004

1.005
l.(M)6
l.OOH
1 (M)7
1 (H)8

1 OOS
1 0(KI
1 010
1 Oil
1 Oil

1 012

0.990
.991
.991
.992
.993

.994
.994
.995
.996
.996

.997
.998
.998
.999
1.000

1.001
1.001
1.002
1.003
1.003

1.004
1.005
l.(H)5
1.006
1.007

1.008
1.008
1 009
1.010
1.010

1.011
1 012
1 012
1.013
1.011

1 015
1 015
1 016
I 017
1 017

1 (IIS
I 019
I 019
1 020
1 021

1 U22

1 000

62

1.001

64

1 001

66

1.002

68

70

1.003
1.004

72

1.004

74

1.005

76

1.006

78

1.006

80

1.007
1.008
1.008
1.009
1 010

82

84

86

88

90

1 Oil
1 Oil
1 012
1.013
1.013

92

94

96

98

100

1.014
1 015
1 015
1 016
I 017

102

104

106

108

110

1 018
1 018

112

1 019

114

1 020

116

t 020

118

120

1 021
1 022

122

1 022

124

1 023

126

1 024

128

130

I 023
1 025

132

1 026

134

1 027

136

1 027

138

140

1 (t2H
1 (»2«

142

1 029

144

1 030

146

1 031

148

150

t 032

542

BULLETIN NUMBER SIXTEEN OF

REDUCTION OF SPECIFIC GRAVITY TO 60 °F— Continued.
OBSERVED SPECIFIC GRAVITY.

Observed

Tempera-

1.010

1 020

1.030

1.040

1,050

1.060

1.070

1.080

1.090

1.100

t ire, ° F.

60

1.010

1.020

1.030

1.040

1.050

1 060

1 070

1.080

1.090

1.100

62

1.011

1 021

1.031

1.041

1.051

1.061

1 071

1.081

1.091

1.101

64

1.011

1 021

1 031

1.041

1.051

1 061

1 071

1 081

1 091

1.101

66

1.012

1.022

1 032

1.042

1.052

1 062

1 072

1.082

.1092

1.102

68

1.013

1.023

1.033

1.043

1 053

1 063

1.073

1.083

1.093

1 103

70

1.013

1.023

1.033

1.043

1.053

1 063

1 073

1.083

1.093

1.103

72

1.014

1 024

1 034

1 044

1.054

1.064

1.074

1.084

1.094

1.104

74

1.015

1.025

1.035

1.045

1.055

1.065

1 075

1 085

1.095

1.105

76

1.016

1.026

1.035

1.045

1.055

1.065

1.075

1.085

1.095

1.105

78

1.016

1.026

1 036

1 046

1.056

1.066

1.076

1.086

1.096

1.106

80

1 017

1.027

1 037

1.047

1.057

1.067

1.077

1.087

1.097

1.107

82

1.018

1.028

1 037

1 047

1.057

1.067

1,077

1.087

1.097

1.107

84

1 018

1 028

1.038

1.048

1.058

1 068

1 078

1.088

1.098

1.108

86

1.019

1.029

1.039

1.049

1.059

1.069

1 079

1.089

1.099

1.108

88

1.O20

1.030

1.040

1.050

1.059

1.069

1.079

1.089

1.099

1 109

90

1 020

1 030

1 040

1.050

1.060

1.070

1.080

1.090

1.100

1.110

92

1 021

1.031

1 041

1.051

1.061

10 71

1.081

1.091

1.101

1.110

94

1.022

1.032

. 1,042

1.052

1.061

1.071

1.081

1.091

1.101

1.111

96

1.022

1.032

1,042

1.052

1 062

1.072

1.082

1.092

1.102

1.112

98

1.023

1.033

1.043

1.053

1.063

1.073

1.083

1.093

1.103

1.112

100

1.024

1.034

1.044

1.054

1.063

1.073

1.083

1.093

1.103

1.113

102

1.024

1.034

1 044

1.054

1.064

1.074

1.084

1.094

1.104

1.114

104

1.025

1.035

1 045

1.055

1 065

1.075

1.085

1.095

1.105

1.114

106

1 026

1.036

1 046

1 056

1 065

1.075

1 085

1.095

1.105

1.115

108

1.027

1.037

1.046

1.056

1.066

1.076

1.086

1.096

1.106

1.116

110

1.027

1.037

1.047

1,057

1.067

1.077

1.087

1.097

1.107

1 116

112

1.028

1.038

1.048

1,058

1.067

1.077

1.087

1.097

1.107

1.117

114

1.029

1 039

1 048

1,058

1.068

1,078

1 088

1.098

1.108

1.118

116

1,029

1 039

1.049

1.059

1.069

1,079

1.088

1.098

1.108

1 118

118

1.030

1.040

1.05,3

1.060

1.069

1 079

1.089

1.099

1.109

1.119

120

1 031

1.041

1 050

1.060

1 070

1,080

1,090

1 100

1 110

1.120

122

1 031

1.041

1.051

1.061

1.071

1,081

1 090

1,100

1.110

1.120

124

1 032

1.042

1.052

1.062

1.071

1,081

1.091

1,101

1.111

1.121

126

1.033

1,043

1.052

1.062

1.072

1,082

1.092

1.102

1.112

1.121

128

1.033

1.043

1.053

1.063

1.073

1.083

1.092

1.102

1.112

1.122

130

1.034

1.044

1.054

1.064

1.073

1.083

1.093

1.103

1.113

1.123

132

1.035

1.045

1.054

1.064

1.074

1.084

1.094

1.104

1.114

1.123

134

1.036

1.046

1.055

1.065

1.075

1.085

1.094

1.104

1.114

1.124

136

1.036

1.046

1 056

1.066

1.075

1.085

1.095

1.105

1.115

1.125

138

1.037

1.047

1 057

1.067

1.076

1.086

1.096

1.106

1.116

1.125

110

1.038

1 048

1.057

1.067

1.077

1.087

1 096

1 106

1.116

1.126

112

1.038

1.048

1,058

1.068

1,077

1.087

1 097

1,107

1 117

1.127

114

1.039

1.049

1.059

1.1G9

1,078

1 088

1.098

1.108

1.118

1.127

146

1 040

1.050

1 059

1.069

1 079

1.089

1.098

1.108

1 118

1.129

148

1.040

1.050

1.060

1.070

1,079

1.089

1.099

1.109

1.119

1.128

150

1.041

1.051

1.061

1.071

1,080

1.090

1 100

1.110

1.120

1 129

KANSAS CITY TESTING LABORATORY

543

Specific Gravity Tables.

Equivalent of Degrees Baume' (American Standard) and Specific

Gravity at 60 "F.

^^^ FOR LIQUIDS HEAVIER THAN

X^/^^i. ct

O J_fClL4.11iC

-L**U -

Sp. Gr.

WATER.

Degrees

Specific

Degrees

Specific

Degrees

Specific

Degrees

Specific

Baume'

Gravity

Baume'

Gravity

Baume'

Gravity

Baume'

Gravity

0.0

1.0000

.7

1.0262

.4

l.(»38

.1

1.0829

.1

1.0007

.8

1.0269

.5

1.0545

.2

1.0837

.2

1.0014

.9

1.0276

.6

1.0553

.3

1.0845

.3

1.0021

4.0

1.02S4

.7

1.0561

.4

1.0853

.4

1.0028

.1

1.0291

.8

1.(^69

.5

1.0861

.5

1.00^

.2

1.0298

.9

1.0576

.6

1.0871)

.6

1.0042

.3

1.0306

8.0

1.0584

.7

1.0678

.7

1.0049

.4

1.0313

.1

1.0692

.8

1.0886

.8

1.0(»5

.5

1.0320

.2

1.0599

.9

1.0894

.9

i.(xm

.6

1.0328

.3

1.0607

12.0

1.09O2

1.0

1.0069

.7

1.0335

.4

1.0615

■1

1.0910

.1

1.0076

.8

1.0342

.5

1.0623

2

1.0919

.2

1.0063

.9

1.0350

.6

1.0630

.3

10927

.3

1.0090

5.0

1.0-^7

.7

1.0638

.4

1.0936

.4

1.0097

.1

1.0366

.8

1.064^

.5

1.0943

.5

1.0105

.2

1.0372

.9

1.06.54

.6

1.0052

.6

1.0112

.3

1.0379

9.0

1.0662

.7

1.0900

.7

1.0119

.4

1.0387

.1

1.0670

.8

1.0068

.8

1.0126

.5

1.0394

.2 "

1.0677

.9

1.0G77

.9

1.0133

.6

1.0402

.3

1.0685

13.0

1.0985

■2.0

1.0140

.7

1.0409

.4

1.0693

.1

1.0903

.1

1.0147

.8

1.0417

.5

1.0701

.2

1.1008

.2

1.0154

.9

1.0424

.6

1.0709

.3

1.1010

.3

1.0161

6.0

l.(H32

.7

1.0717

.4

1.1018

.4

1.0168

.1

1.0431

.8

1.0725

.5

1.1027

.5

1.0175

.2

1.0447

.9

1.0733

.6

1.1036

.6

1.0183

.3

1.W54

10.0

1.0741

.7

I.IOIS

.7

1.0190

.4

Lot's

.1

1.0749

.8

1.106Z

.8

1.0197

.5

1.0469

.2

1.0757

.9

i.ioeo

9

1.0^04

.6

1.0477

.3

1.0765

14.0

l.lOfV

3.0
.1
.2
.3
.4
.5
.6

1.0211
1.0218
1.0236
1.0233
1.0240
1.0247
1.0255

.7
.8
.9
7.0
.1
.2
.3

1.0481
1.0492
1.0600
l.(K07
1.051.T
1.0522
1.0530

.4
.5
.6

.7

.8

.9

11.0

1.0773
1.0781
1.0789
1.0797
1.0905
1.0813
1.0821

.1
.2
.3
.4

.5
.«

.7

1.1077
1.10»
1.1094
l.UOS
1.1111
1.1120
1.U28

544

BULLETIN NUMBER SIXTEEN OF

EQUIVALENT BAUME' DEGREES— Con.

Degrees

Specific

Degrees

Specific

Degrees

Specific

Degrees

Spedfio

Baume'

Gravity

Baume/

Gravity

Baume'

Gravity

Baume'

Gravity

.8

1.1137

.2

1.1526

.6

1.1944

28.0

1.2.393

.9

1.1145

.3

1.1535

.7

1.19.54

.1

1.2404

15.0

1.1154

.4

1.1545

.8

1.1964

.2

1.2414

.1

1.1162

.5

1.1554

.9

1.1974

.3

1.2425

.2

1.1171

.6

1.1563

24.0

1.1983

.4

1.2436

.3

l.llSO

.7

1.1.572

.1

1.1993

.5

1.2446

.4

1.1138

.8

1.1.581

.2

1.2003

.6

1.2457

.5

1.1197

.9

1.1591

.3

1.2013

.7

1.2468

.6

1.1206

20.0

l.lfiOO

4

1.2028

.8

1.2478

.7

1.1214

.1

1.1609

.5

1.2033

.9

1.2489

.8

1.1223

.2

1.1619

.6

1.2043

29.0

1.2500

.9

1.1232

.3

1.1628

.7

1.2053

.1

1.2511

16.0

1.1240

.4

1.1637

.8

1.2063

.2

1.2522

.1

1.1249

.5

1.1647

.9

1.2073

.3

1.2532

.2

1.1258

.6

1.1656

25.0

1.2083

.4

1.2543

.3

1.12^7

7

1.1665

.1

1.2093

.5

1.2554

.4

1.1275

.8

1.1675

.2

1.2104

.6

1.2565

.5

1.12S4

.9

1.1684

.3

1.2114

.7

1.2576

.6

1.1293

21.0

1.1694

.4

1.2124

.8

1.2587

.7

1.1302

.1

1.1703

.5

1.2134

.9

1.2598

.8

1.1310

.2

1.1712

.6

1.2144

30.0

1.2609

.9

1.1319

.3

1.1722

.7

1.2154

.1

1.2620

17.0

1.1328

.4

1.1731

.8

1.2164

.2

1.2631

.1

1.1337

.5

1.1741

.9

1.2175

.3

1.2642

.2

1.1346

.6

1.1750

26.0

1.2185

.4

1.2653

.3

1.1. ')55

. .7

1.1760

.1

1.2195

.5

1.2664

.4 •

1.1364

.8

1.1769

.2

1 .2205

.6

1.2675

.5

1.1373

.9

1.1779

.3

1.2216

.7

1.2886

.6

1.1381

22.0

1.1789

.4

1.2226

.8

1.2697

.7

1.1390

.1

1.1798

.5

1.22.%

.9

1.2708

.8

1.1399

2

1.1808

.6

1.2247

31.0

1.2719

.9

1.1408

.3

1.1817

.7

1.2-257

.1

1.2730

18.0

1.1417

.4

1.1827

.8

1.2267

.2

1.2742

.1

1.1426

.5

1.1S37

.9

1.2278

.3

1.2753

.2

1.1435

.6

1.1846

27.0

1.2288

.4

1.2764

.3

1.1444

.7

1.18.56

.1

1.2299

.5

1.2775

.4

1.1453

.8

1.1866

.2

1.2309

.6

1.2787

.5

1.1462

.9

1.1876

.3

1.2319

.7

1.2798

.6

1.1472

23.0

1.1885

.4

1.2330

.8

1.2800

.7

1.1481

.1

1.1895

.5

1.2340

.9

1.2821

.8

1.1490

.2

1.19(»

.6

1.23.M

32.0

1.2832

.9

1.1499

.3

1.1915

.7

1.2361

.1

1.2843

19.0

1.1508

.4

1.1924

.8

1.2372

.2

1,2^5

.1

1.1517

.5

1.1934

.9

1.2383

.3

1.2866

KANSAS CITY TESTING LABORATORY

545

EQUIVALENT BAUME' DEGREES— Con.

Degrees

Specific

Degrees

Specific

Degrees

Specific

Degrees

Specific

Baume' ■

i

Gravity

Baume' i

Gravity

Baume'

Gravity

Baume'

Gravity

.4

1.2877

.8

1.3401

•2

1.3969

.6

1.458S

.6

1.2889

.9

1.3414

.3

1.3983

.7

1.4602

.6

1.2900

37.0

1.3426

■•* 1

1.3996

.8

1.4617

.T

1.2912

.1

1.3438

.5 1

1.4010

.9

1.4632

S

1.2923

.2

1.3451

.6 i

1.4023

46.0

1.4646

.9

1.2935

.3

1.3463

.7

1.4037

.1

1.4661

S3.0

1.2946

.4

1.3476

.8

1.4050

.2

1.4676

.1

1.2958

.5

1.3488

.9

1.4064

.3

1.4691

.2

1.2970

.6

1.3501

42.0

1.4078

.4

1.4706

.3

1.2981

.7

1.3514

.1

1.4091

.5

1.4721

.4

1.2993

.8

1.3526

.2

1.4105

.6

1.4736

.5

1.3004

.9

1.^39

.3

1.4119

.7

1.4751

.6

1.3016

38.0

1.3551

.4

1.4133

.8

1.476G

.7

1.3028

.1

1.3.T64

.5

1.4146

.9

1.4781

.8

1.3040

.2

1.3577

.6

1.4160

47.0

1.4796

.9

1.3051

.8

1.3653

.7

1.4174

.1

1.4811

34.0

1.3063

.4

1.3602

.8

1.4188

.2

1.4838

.1

1.3075

.5

1.3615

.9

1.4202

.3

1.4841

.2

1.3087

.6

1.3628

43.0

1,4216

.4

1.4857

.3

1.3098

.7

1.3641

.1

1.4230

.5

1.4372

,4

1.3110

.8

1.3653

.2

1.4244

.6

1.4887

.5

1.3122

.9

1.3666

.3

1.4258

.7

1.4902

.6

1.3134

39.0

1.3679

.4

1.4272

.8

1.4918

.7

1.3146

.1

1.3692

.5

1.4286

.9

1.4933

.8

1.3158

.2

1.3705

.6

1.4300

48.0

1.4948

9

1.3170

.3

1.3n8

.7

1.4314

.1

1.4964

35.0

1.3182

.4

1.3r31

.8

1.4328

.2

1.4979

.1

1.3194

.5

1.3744

.9

1.4342

.3

1.4995

.2
.3

1.3206

.6

1.3757

44.0

1,4356

.4

1.5010

1.3218

.7

1.3770

.1

1.4371

.6

1.5026

. .4

1.3230

.8

1.3783

.2 -

1.4385

.«

l.RHl

.5

1.3242

.9

1.3796

.3

1.4399

.7

1.5057

.G
.7
.8
.9
36.0
.1
.2
.3
.4
.5
.6
.7

1.3254
1.3266
1.3278
1.3291
1.3303
1.3315
1.3327
1.3329
1.3352
1.3364
1.3376
i 1.3389

40.0
.1

.2
.3
.4

.5
.6
.7
.8
.9
41.0
.1

1.3810
1.3823
1.3836
1.3849
1.3862
1,3876
1.3889
1.3902
1.3916
1.3928
1.3942
1.3956

.4
.5
.6
.7
.8
.9
45.0
.1
.2
.3
.4
.5

1.4414
1.4428
1.4442
1.4457
1.4471
1.4486
1.4500
1.4515
1.4529
1.4544
1.4558
1.4573

.8
.9
49.0
.1
.2
.3
.4
.5
.6
.7
.8
.0

1.5073
1 1.5088
' 1.5104
1.5120
1.5136
1.B152
1.51fltr
1,5183
1.5199
1.5216
1 SOT
1.6247

546

BULLETIN NUMBER SIXTEEN OF

EQUIVALENT BAUME' DEGREES— Con.

Degrees

Specific

Degrees

Specific

Degrees

Specific

Degrees

Specific

Baume'

Gravity

Baume'

Gravity

Baume'

Gravity

Baume'

Gravity

50.0

1.5263

.1

1.6129

.1

1.7079

.1

1.8148

.1

1.5279

.2

1.6147

.2

1.7099

.2

1.8170

.2

1.5i295

.3

1.6165

.3

1.7119

.3

1.8193

.3

1.5312

.4

1.6183

.4

1.71.^9

.4

1.8Z16

.4

1.5328

.5

1.6201

.5

1.7160

.5

1.8239

.5

1.5344

.6

1.^9

.6

1.7180

.6

1.8262

.6

1.5360

.7

l.&£fr

.7

1.7200

.7

1.8286

.7

1.5376

.8

1.6256

.8

1.7221

.8

1.83U8

.8

1.5393

.9

1.6459

.9

1.72141

.9

1.83S1

.9

1.5409

56.0

1.6292

61.0

1.7262

66.0

1.8354

51.0

1.5436

.1

1.6310

.1

1.7282

.1

1.8378

.1

1.5442

.2

1.6329

.2

1.7303

.2

1.8401

.2

1.5458

.3

1.6347

.3

1.7324

.3

1.W24

.3

1.5475

.4

1.6366

.4

1.7344

.4

1.9*48

.4

1.5491

.5

1.6384

.5

1.73R5

.5

1.8471

.5

1.5508

.6

1.6403

.6

1.7386

.6

1.84^

.6

1.. 5.525

.7

1.6421

.7

1.7407

.7

1.8519

.7

1.5641

.8

1.6440

.8

1.7428

.8

1.8542

.8

1.5558

.9

1.6459

.9

1.7449

9

1.8566

.9

1.5575

37.0

1.6477

62.0

1.7470

67.0

1.8690

52.0

1.5591

.1

1.6496

.1

1.7491

.1

1.8614

.1

1.5608

.2

1.6515

.2

1.7512

.2

1.8638

.2

1.5625

.3

1.6534

.3

1.7533

.3

1.8662

.3

1.5642

-4

1.6553

.4

1.7K4

.4

1.8fiRB

.4

1.5659

.5

1.^71

.5

1.7576

.5

i.gno

5

1.5676

.6

1.6590

.8

1.7507

.6

1.8734

.6

1.5693

.7

1.6909

.7

1.7618

.7

1.8758

.7

1.5710

.8

1.6628

.8

1.7640

.8

1.8782

.8

1.5727

.9

1.W59

.9

1.7661

.9

1.8807

.9

1.5744

58.0

1.6067

63.0

1.7683

68.0

1.8831

53.0

1.5761

.1

1.6686

.1

1.7705

.1

1.8856

.1

1.5r8

.2

1.6705

.2

1.7726

JZ

1.8880

.2

1.5796

.3

1.6724

.3

1.7748

.3

1,8905

.3

1.5812

.4

1.6744

.4

1.7770

.4

1.8990

.4

1.5830

.5

1.6763

.5

1.7791

.6

1.8954

.5

1.5847

.6

1.6782

.6

1.7813

.6

1.8979

.6

1.5864

.7

1.6802

.7

1.7835

.7

1.9004

.7

1.5882

.8

l.effil

.8

1.7857

.8

1.9029

.8

1.5899

.9

1.6841

.9

1.7879

.9

1.9064

.9

1.5917

59.0

1.6860

64.0

1.7901

69.0

1.9079

54.0

1.5934

.1

1.6880

.1

1.7923

.1

1.9104

.1

1.5952

.2

1.6900

.2

1.7946

.2

1.9129

.2

1.5969

.3

1.6919

.3

1.7968

.3

1.9155

.3

i.59gfr

.4

1,6939

.4

1.7990

.4

1.9180

.4

1.6004

.5

1.6959

.5

1.8912

.5

1.9206

.5

1.6022

.6

1.6979

.6

1.8035

.«

1.9231

.6

1.0040

.7

1.6999

.7

1.8057

.7

1.92S6

.7

1.6058

.8

1.7019

.8

1.8080

.8

1.9282

.8

1.6075

.9

1.7039

.9

1.8102

.9

1.9308

.9

1.6093

60.0

1.7039

65.0

1.8125

70.0

1.9333

.W.O

1.6111

KANSAS CITY TESTING LABORATORY

547

SPECIFIC GRAVITY AND CONTENT OF SULPHURIC ACID.

Specific

Gravity

15°

in vacuo

100 parts by

weight
correspond to

%
SO.

%
HjSO*

l.OOO
1.006
1.010
1.015

1.020
1.025
1.030
1.03S
1.040
1.045
1.050
1.055

i.oeo

1.065
1.070

1.075
1.080
1.085

i.oeo

1.095
1.100
1.105
1.110
1.115
1.120
1.125
1.130
1.135
1.140
1.145
1.150
1.155
1.100
1.16S
1.170
1.175
1.180
1.185

0.07

0.68

1.28

1.88

2.47

3.07

3.67

4.27

4.87

5.45

6.02

6.59

7.16

7.73

8.32

8.90

9.47

10.04

10.60

11.16

11.71

12.27

12.82

13.36

13.89

14.42

14.95

15.48

16.01

16.54

17.07

17.59

18.11

18.64

19.16

19.60

20.21

20.73

O.OO
0.83

i.m

21.30

3.03

3.76

4.40

5.23

5.96

6.67

7.37

8.07

8.77

9.47

10.19

10.90

11.60

12.30

12.99

13.67

14.35

15.03

15.71

16.38

17.01

17.66

18.31

18.96

19.61

20.26

20.91

21.55

22.19

22.83

23.47

24.12

24.76

25.40

1 liter

contains

grams

SO.

1

7

13

19

26

32

38

44

51

57

63

70

76

82

89

96

103

109

116

122

129

136

143

149

156

162

169

176

183

189

196

203

210

217

224

231

238

246

H2SO*

1

8

16

23

31

39

46

54

62

71

77

85

93

102

109

117

125

133

142

150

158

166

175

183

191

199

207

215

223

231

239

248

257

266

275

283

292

301

Specific 100 parts by
Gravity weight

15° correspond to

4° % %

in vacuo SO. H^SO,

1 liter

contains

grams

1.190
1.195
1.200
1.205
1.210
1.215
1.220
1.225
1.230
1.235
1.240
1.245
1.250
1.255
1.260
1.265
1.270
1.2'/5
1.280
1.285
1.290
1.295
1.300
1.305
1.310
1.315
1.320
1.325
1.330
1.335
1.340
1.345
1.350
1.355
1.360
1.365
1.370
1.375

21.26
21.78
22.30
32.82
23.33
23.84
24.36
24.88
25.39
25.88
26.35
26.83
27.29
27.76
28.22
28.69
29.15
29.62
30.10
30.57
31.04
31.52

32.4(j
32.94
33.41
33.88
34.35
34.80
35.27
35.71
36.14
38.58
57.02
37.45
37.89
38.32
38.75

26.04

26.68

27.30

27.95

28.58

29.21

29.84

30.48

31.11

31.70

32.28

32.86

33.43

34.00

34.57

35.14

35.71

36.29

36.87

37.45

38.03

38.61

39.19

39.77

40.35

40.5.:

41.50

42.08

42.66

43.20

43.74

44.28

44.82

45.35

45.88

46.41

46.94

47.47

SO,

263
260
268
275
282
290
297
305
312
320
327
334
341
348
356
363
370
377
385
393
400
408
416
424
432
439
447
455
462
471
479
4S6
494
502
509
517
525
533

H,SO«

310
319
328
337
346
355
384
373
382
391
400
409
418
426
435
444
454
462
472
481
490
500
510
519
529
538

557

571

590
605
614
624
633
643
653

548

BULLETIN NUMBER SIXTEEN OF

SPECIFIC GRAVITY AND CONTENT OF SULPHURIC ACID—

Continued.

Specific

100 parts by

1 liter

Specific

100 parts by

1 liter

Gravity

weight

contains

Gravity

weight

contain*

15*

correspond to

grams

15°
4°

correepond to

grams

4*

%

%

%

%

In vacuo

SO,

HjSO.

SO,

H,S04

in vacuo

SO,

H,S0.

SO,

HjSO.

1
1.380

39.18

48.00

641

682

1.675 1

61.20

74.97

1025

1256

1.385

39.62

48.53

549

672

1.680

61.57

75.42

1034

1267

1.390

40.05

49.06

557

682

1.685

61.93

75,86

1043

1278

1.395

40.48

49.50

564

^92

1.690

62.29

76.30

1053

1289

1.400

40.91

50.11

573

702

1.695

62.64

76.73

1062

1301

1.406

41.33

50.63

581

711

1.700

63.00

77.17

1071

1312

1.410

41.76

51.15

589

721

1.705

63.35

77.60

lOSO

1323

1.415

42.17

51.66

597

730

1.710

63.70

78.04

1089

1334

1.420

42.57

52.15

604

740

1.715

64.07

78.48

1099

1346

1.425

42.9(3

52.63

612

750

1.720

W.43

78.92

1108

1^7

1.430

43.36

53.11

620

759

1.725

64.78

79.36

1118

1369

1.435

43.75

53.59

628

769

1.730

65.14

79.80

1127

1381

1.440

44.14

54.07

636

779

1.735

65.50

80.24

1136

1392

1.445

44.53

54.55

643

789

1.740

65.86

80.68

1146

1404

1.450

44.92

65.03

651

798

1.745

66.22

81.12

1156

1416

1.455

45.31

55.50

659

808

1.750

66.58

81.56

1165

1427

1.460

45.69

55.97

667

817

1.755

66.94

82.00

1175

1439

1.465

46.07

56.43

675

827

1.760

67.30

82.44

1185

1451

1.470

46.45

56.90

683

837

1.7^

97.65

82,88

1194

1463

1.475

46.83

57.37

691

846

1.770

68.02

83 32

1204

1475

1.480

47.21

57.83

699

856

1.775

68.49

83.90

1216

1489

1.485

47.57

58.28

707

865

1.780

68.98

84.50

1228

1504

1.490

47.95

58.74

715

876

1.785

69.47

85.10

1240

1519

1.4&5

48.34

59.22

723

885

1.790

69.96

85.70

1252

1534

1.500

48.73

59.70

731

896

1.795

70.46

86.30

1265

1549

1.505

49.12

60.18

739

906

1.800

70.94

86.90

1277

1564

1.510

49.51

60.65

748

916

1.805

71.50

87.60

1291

1581

1.515

49.89

61.12

756

926

1.810

72.08

88.30

1305

1598

1.520

50.28

61.59

764

- 936

1.815

72.69

89.05

1319

1621

1.525

50.66

62.06

773

946

1.820

73.51

90.05

1338

1639

1.530

51.04

62.53

781

957

1.821

73.63

90.20

1341

1643

1.5S5

51.43

63.00

789

967

1.822

73.80

90.40

1345

1647

1.540

51.78

63.43

797

977

1.823

73.96

90.60

1348

1651

1.545

52.12

63.85

805

987

1.824

74.12

90.80

1352

1656

1.550

52.46

64.26

813

99S

1.825

74.29

91.00

1356

1961

1.555

52.79

64.67

821

1006

1.826

74.49

91.25

1390

1666

1.560

53.12

65.08

829

1015

1.827

74.69

91.50

1364

leri

1.565

53.46

65.49

837

1025

1.828

74.86

91.70

1368

i6rr6

1.570

53.80

65.90

845

1035

1.829

75.03

91.90

1372

1681

1.575

54.13

66.30

853

1044

1.830

75.19

92.10

1376

1685

1.580

54.46

66.71

861

1054

1.831

75.35

92.30

1380

1090

1.585

54.80

67.13

869

lO&t

1.832

75,53

92.52

]384

1695

1.590

55.18

67.59

877

1075

1.833

75.72

92.75

1388

170O

1.595

55.55

68.05

886

1085

1.834

75.96

93.05

1393

1706

i.eoo

55.93

68.51

897

1096

1.835

76.27

93.43

1400

1713

1.605

56.30

68.97

904

nor;

1.836

76.57

93.80

1405

1722

1.610

56.68

69.43

913

1118

1.837

76.90

94.20

1412

1730

1.615

57.05

69.89

921

U28

1.838

77.23

94.60

1419

1739

1.620

57.40

70.32

930

1139

1.839

77.55

95.00

1426

1748

1.625

57.75

70.74

938

1150

1.840

78.04

95.60

1436

1759

1.630

58.09

71.19

947

1160

1.8405

78.33

95.95

1441

1765

1.635

58.43

71.57

955

1170

1.8410

79.19

97.00

1458

1786

1.640

58.77

71.99

964

1181

1,8415

79.76

97.70

1469

1799

1.645

59.10

72.40

972

; 1192

1.8410

80.16

98.20

1476

18D8

1.650

69.45

72.82

981

1202

1.8405

80.57

98.70

1483

1816

1.655

59.78

73.23

989

1212

1.8400

80.98

99.20

1490

1825 •

1.660

60.11

73.64

998

1222

1.8395

81.18

99.45

1494

1330

1.665

60.46

74.07

1007

12S3

1.8390

81.39

90.70

1497

1834

1.670

60.82

74.51

1016

, 1244

1.8385

81.59

99.95

1500

1838

KANSAS CITY TESTING LABORATORY

549

Percentage of Sulphur Trioxide and Sulphuric Acid in
Fuming Sulphuric Acid.

The acid

The acid

1

The add

Total SO,

contains %

Total SO3

contains %

Total

contains %

as found
by titration

as found
by titration

as found
by titration ,

I-I2SO. SO,

HiSO, SO,

\

H2SO.

SO,

81.8326

100 ; 0

87.8775

66 34

93.9389

33 67

81.8163

99 1

8S.0612

65 35

94.1224

32 68

82.0000

98 , 2

88. -2448

64 36

94.3061

31 69

82.1836

97 ' 3

88.4285

63 37

94.4897

30 70

82.3674

96 ' 4

8S.6122

62 38

94.6734

29 71

82.5510

95 5

88.7959

61 39

94.S571

28 72

82.7346

94 6

88.9795

60 40

95.0408

27 73

82.9183

93 7

89.1632

59 41

95.2244

26 74

8a 1020

92 8

89.3469

58 42

95.4061

25 75

83.2857

91 9

89.5306

57 43

95.5918

24 76

83.4693

90 1 10

89.7142

56 44

95.7755

23

77

83.6530

89 11

89.8979

55 45

95.9591

22

78

83.8367

88 ! 12

90.0816

54 46

96.1428

21

79

81.0204

srr 13

90.2653

53 47

96.3265

20

80

84.2040
84.3877

86
85

14
15

90.4489
90.6326

52 48
51 1 49

96.5102
96.6938

19
18

81
82

84 5714

84

16

90.8163

50 : 50

96.8775

17

83

84.7551

83

17

91.0000

49 51

97.0612

16

84
85
86

87

84.9387

85.1224

82
81

18

19

91.1836
91.3673

48 52
47 53

97.2448
97.42^

15
14

85.3061

80

20

91.5510

46 54

97.6122

13

85.4897
85.67^
85.8571
86.0408
86.2244
86.4081
86.5918
86.7755
86.9591
87.1428
87.3265
87.5102
87.6938

79
78
77
76
75
74
73
72
71
70
1 69
68
67

21
22
23
24
25
26
27
28
29
30
31
32
33

91.7346
91.9183
93.1020
92.2857
92.4693
92.6530
92.8367
93.0204
93.2040
93.3677
93.5n4
93.7551

45
44
43
42
41
40
39
38
37
36
35
34

55
56
'57
68
59
60
61
62
63
64
65
66

97.7959
97.9795
9S.1633
983469
98.5306
98.7142
98.8979
99.0816
99.2753
99.4489
99.6326
99.8163

12
11
10
9
8
7
6
5
4
3

1

88
89
90

n

92
99

1 **
95

96

fl»r

96

99

550

BULLETIN NUMBER SIXTEEN OF

Sodium Hydroxide Solution at 15°C (Caustic Soda)

LUNGE.

1 Liter Contains

Specific

Degrees

Degrees

Per Cent

Per Cent

Grams

Gravity

Baume'

Twaddell

Na,0.

NaOH.

NajO. NaOH.

1.007

1.0

1.4

0.47

0.61

4

6

1.014

2.8

2.9

0.03

1.20

9

12

1.022

3.1

4.4

1.55

2.0O

16

21

1.029

4.1

5.8

2.10

2.70

22

28

1.036

5.1

7.2

2.60

3.35

27

35

1.015

6.2

9.0

3.10

4.00

32

42

1.052

7.2

10.4

3.60

4.64

38

48

1.060

8.2

12.0

4.10

5.29

43

56

1.067

9.1

13.4

4.55

5.87

49

63

1.075

10.1

15.0

5.08

6.55

55

70

1.083

11.1

16.6

5.67

7.31

61

7»

1.091

12.1

18.2

6.20

8.00

68

87

1.100

13.2

20.0

6.73

8.68

74

95

1.108

14.1

21.6

7.30

9.42

81

104

1.116

15.1

23.2

7.80

10.06

87

112

1.125

le.i

25.0

8.50

10.97

96

123

1.134

17.1

26.8

9.18

11.84

104

134

1.142

18.0

28.4

9.80

12.6i

112

144

1.152

19.1

30.4

10.50

13.55

121

156

1.162

20.2

32.4 ■

11.14

14.37

129

167

1.171

21.2

34.2

11.73

15.13

137

177

1.180

22.1

36.0

12.33

15.91

146

188

1.190

23.1

38.0

13.00

16.77

155

200

1.200

24.2

40.0

13.70

17.67

164

212

1.210

26.2

42.0

14.40

18.58

174

225

1.220

26.1

44.0

15.18

19.58

185

239

1.231

27.2

46.2

15.96

20.59

196

253

1.241

28.2

48.2

16.76

21.42

208

266

1.252

29.2

50.4

17.55

22.64

220

283

1.263

30.2

52.6

18.35

23.67

232

299

1.274

31.2

54.8

19.23

24.81

245

316

1.285

32.2

57.0

20.00

25.80

257

332

1.297

33.2

59.4

20.80

26.83

270

348

1.308

34.1

61.6

21.55

27.80

282

364

1.320

35.2

64.0

22.35

28.83

295

381

1.332

35.1

66.4

23.20

29.93

309

399

1.345

37.2

69.0

24.20

31.22

326

420

1.357

38.1

71.4

25.17

32.47

342

441

1.370

39.2

74.0

26.12

33.69

359

462

1.383

40.2

76.6

27.10

34.96

375

483

1.397

41.2

79.4

28.10

36.25

392

506

1.410

42.2

sa.o

29.05

37.47

410

528

1.424

43.2

84.8

30.08

38.80

428

553

1.438

44.2

87.6

31.00

39.99

446

575

1.453

45.2

90.6

32.10

41.41

466

602

1.468

46.2

93.6

33.20

42.83

487

629

1.483

47.2

96.6

34.40

44.38

510

658

1.498

48.2

99.6

35.70

46.15

5ffi

691

1.514

49.2

102.8

36.90

47.60

559

721

1.530

50.2

106.0

38.00

49.02

581

750

KANSAS CITY TESTING LABORATORY

551

Table of Chloride of Calcium Solution.

!

Ammonia Gauge

Specific

Degree

Degree Sal-

Freezing

Pressure

>ravity at 64

Beauuie at 64

ometer at 64

Per Cent

Point in

Pounds per

Hegrees F.

Degrrees F. i

Degrees F.

of CaCl.:

Degrees F.

Square Inch

1.007

1

4

0.943

+31.20

46

1.014

2

8

1.886

+30.40

45

1.021

3

12

2.829

+29.60

44

1.028

4

16

3.772

+28.80

43

1.035

5

20

4.715

+28.00

42

1.043

6

24

5.658

+28.89

41

1.060

7

28

6.601

+25.78

40

1.06S

8

32

7.544

+24.67

38

1.085

9

36

8.487

+23.56

37

1.073

10

40

9.430

+22.09

S5.5

l.OSl

11

44

10.373

+20.62

34

1.069

12

48

11.316

+19.14

32.5

1.097

13

52

12.259

+17.67

90.5

I.IOS

14

56

13.202

+15.75

29

1.114

15

60

14.145

+13.82

27

1.122

16

64

15.088

+11.80

25

1.131

17

68

16.031

+ 9.96

23.5

1.140

18

72

16.974

+ 7.68

21.5

1.149

19

76

17.917

+ 5.40

20

1.158

30

80

18.860

+ 3.12

18

1.167

2a

84

19.803

-0.84

16

1.176

22

88

20.746

— 4.44

12.6

1.186

23

92

21.689

— 8.03

10.5

1.196

24

96

22.632

'—11.63

8

1.205

25

100

23.575

-15.23

6

1 215

26

104

24.518

-*19.56

4

1 '>^^

27

108

25.461

—24.43

1.5

1 236

28

112

26.404

—29.29

1" vacuum

1 9Afi

29

116

27.^7

-^.30

5" vacuum

1.257
1.2fi8
1.279
1.290
1.302
1.313

30

120

28.290

—41.32

8.5" vacuum

31
32
33
34

1 35

29.233

—47.66

12" vacuum

30.176
31.119

—54.00
—44.32

1,5" vacuum
10' vacuum

33.062
.3.?.

1 —34.66
—25.00

4" vacuum
1.5poun>t8

Table of Brine Solution.

(CHLORIDE OF SODIUM— COMMON SALT.)

o ^ tii

£ S « iH T, > 3? b o -

B

■Orh

W-

:i

1.

1.

1.007

0.992

1.037

0.96

1.073

0.892

1.115

0.855

1.150

0.829

1.191

0.783

8.35

8.4

8.65

895

9.3

9.6

9.94

00

■c fl a

O es 53

3 IS «

0.

0.084

0.432

0.8^

1.395

1.92

2.486

8.35

8..S16

8.218

8 0.i5

7.906

7.68

7.455

05

:5S8

s~

Cap

■.a^ 3 a «)

3 a «) P

12.4

0.

62.4

R2.8

0.629

62 172

64.7

3.2.37

rt1.4«>

ei>.!>5

fl.i<)5

n0 2S3

09.57

10.43.%

SO.l.-M

71.76

U.'W!

57.408

74.26

18.5<5

65.«»fi

h

«

h

u "

° 1

III

aa.

SI .8

264

186

12.?

AW

100

552

BULLETIN NUMBER SIXTEEN OF

The Metric System, Fundamental Equivalents.

The fundamental unit of the metric system is the Meter — the
unit of length. From this the units of capacity (Liter) and of weight
(Gram) were derived. All other units are the decimal subdivisions
or multiples of these. These three units are simply related, e. g.,
for all practical purposes one Cubic Decimeter equals one Liter and
one Liter of water weighs one Kilogram. The metric tables are
formed by combining the words "Meter," "Gram," and "Liter" with
the six numerical prefixes, as in the following tables:

Prefixes. Meaning.

milli- = one thousandth . .1/1000 0.001

centi- = one hundredth ..1/100 0.01

deci- = one tenth 1/10 0.1

Unit = one 1.

deka- = ten 10/1 10.

hecto- = one hundred 100/1 100.

kilo- = one thousand ...1000/1 1000.

Units.

"meter" for length
"gram" for weightormass
"liter" for capacity

All lengths, areas, and cubic measures in the following tables are
derived from the international meter, the legal equivalent being 1
Meter rrr 39.37 Inches (law of July 28, 1866). In 1893 the United
States Office of Standard Weights and Measures was authorized _ to
derive the yard from the meter, using for the purpose the relation
legalized in 1866, 1 Yard = 3600/3937 Meter.

The customary weights derived from the international kilogram
are based on the value of 1 avoirdupois pound = 453.5924277 grams.
This value is carried out farther than that given in the law, but is in
accord with the latter as far as it is there given. The value of the
troy pound is based upon the relation just mentioned and also the
equivalent 5760/7000 avoirdupois pounds equal 1 troy pound.

In the following tables the metric unit has been selected as the
common unit so that conversions may be made through the metric
unit.

KANSAS CITY TESTING LABORATORY

553

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554

BULLETIN NUMBER SIXTEEN OF

(D

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cr

cr

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CO

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Absolute Cent. Fahr. Reaumur.

Degrees Absolute 1.0 1.0 Vj Vj

Degrees Centigrade 1.0 1.0 'A Vg

Degrees Fahrenheit Vj Vg 1.0 */»

Degrees Reaumur % '/< Vi 1.0

COMPARATIVE TEMPERATURE POINTS.

Absolute zero= — 273° Centigrade= —459.4° Fahr.= —218.4° Reaum.
Freezing water- 0° C.= 273° A.= 32° F. = 0° R.
Boiling waters 100° C.= 373° A. = 212° F. = 80° R.

HEAT QUANTITY CONVERSION FACTORS.

One British Thermal Unit = 251.995 X calories (gm.) = 0.251995 X

Cal. Large.
One gram caloric = 0.00396832 British Thermal Units.
One B. T. U. per pound = '.. calorie per gram.
One calorie per gram = 1.8 B. T. U. per pound.

TIME CONVERSION FACTORS.

One year = 365 days, 5 hours, 48 minutes, 48 seconds = 12 calendar
months.
= 52.1693 + weeks = 8765.8133 + hrs. = 525948.8 minutes
= 31556928 seconds.
One week 7 days = 168 hrs. = 10080 minutes = 604800 seconds.
One day = 24 hours = 1440 minutes = 86400 seconds.
One hour = 60 minutes = 3600 seconds.
One minute = 60 seconds.

VELOCITY CONVERSION FACTORS.

Mi 'hr Ft. /sec. Km. /In. Xl/sec. ,MI./il;i. Km. /Ja.

' 1 2 :!. 4. ".. 6.

1 Miles per hour 1.0000 1.4667 1.6093 0.44704 24.00 38.62

2* Feet per second 0.6819 1.0000 1.0973 0.30480 16.37 26.33

3. Kilometers/hour .0.6214 0.9114 1.0000 0.2778 14.913 24.00

4 Meters per second.2.237 3.281 3.600 1.0000 53.69 S6.40

5 MUes pel day 0.04167 0.06112 0.06706 0.01863 1.0000 1.609
6.' Kilometers/day "::::0.02589 0.03797 0.04167 0.01157 0.6214 1.0000

CONVERSION FACTORS FOR MONEY.

* T.OOb Dollar (ufs.) j-OJO '

100.000 Cent (U. S.) . "^1"

0.196 Guinea (English) ^ 21 sh. uigs 6.10972

0.2055 Pound Sterling = 20 shillings 4.8<j6o

(Sovereign) niiru

4.11 Shilling (s) - ;2 PO'ice 0.2-^. 1

40.93 Penny (d) = 4 farthings 0.0 0«

163.72 Farthing ZfSl, 'f£

0.822 Crown — ?«„ i *^ • n "via

4.200 Mark (Germany) = 100 pfennigs O-^H^^

F^anclFrance) ^ 100 centimes O.^.T ^^

518.2 Centime

562 BULLETIN NUMBER SIXTEEN OF

CLASSIFICATION OF U. S. PATENTS ON PETROLEUM REFIN-
ING.

A. Water separation, dehydration, de-emulsification, heating and

physical purification of oil and bottom settlings.

B. Cracking, conversion, and decomposition processes.

C. Paraffin and wax.

D. Chemical treatment of petroleum.

1. Acid or alkali.

2. Other than acid or alkali.

E. Asphalt.

1. Compositions.

2. Production.

3. Refining.

F. Simple distillation.

1. Fire.

2. Steam.

3. Gas.

4. Air.

5. Vacuum.

I. Batch.
II. Continuous.

G. Coal oil. Kerosene and Illuminating oils.

H. Oil-fire prevention, extinction and storage.
I. Recovery of acid-sludge and alkali-sludge.
J. Gasoline production and treatment.
K. Gas.

1. Production.

2. Treatment.

3. Production of carbon black.
L. Chemical products.

M. Patented blends and compounds.

N. Testing apparatus.

0. Lubricating oils.

P. Electrical processes.

Q. Transporting oil.

R. Methods of removing carbon and coke.

S. Mechanical appliances in oil refining, and processes.

(Not covering any particular operation.)
T. Plastics.

U. Conden,sers and condensing.
V. Desulphurizing and deodorizing.
W. Oil shales, oil sands and coals.

KANSAS CITY TESTING LABORATORY

563

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922).

NAME Number

Aab, Geo. and S. K. Campbell 369,902

Abbott, L. S 1,332,018

Adair, Jas 35,497

Adair, Jas., and Twaddle, H. W. C 56,343

Adair, Thos. D 1,106,352

Adams, Chas 52,509

Adams, J. H 1,320,354

Adams, J. H 1,320,726-7

Adams, J. H 976,975

Adams, Jos. H 1,327,263

Adams, Henry W 12,614

Adamson, Wm 45,007

Adiassewich, Alexander 629,536

Alberger, J. L 37,798

Alexander, Clive M 1,230,975

Alexander, Clive M 1,387,677

Alexander, C. M., and Taber, G. H., Jr. . . 1,381,098

Alexander, Jas. H 229,287

Alexander, Jas. H. and Eberhard 156,265

Alexander, Robt 435,198

Alkemade, J. von R 1,076,000

Allan, Hugh Logie 1,390,742

Allan, D. M., Jr 1,187,797

Allen, Geo 182,625

Allen, W. H 1,167,966

Allison, Wm 1,395,694

Alter, David, and Hill, S. A 20,026

Alvord, Clark 213,157

Ambruson, H. J 1,252,642

Amend, Otto 480,311

Amend, Otto 480,312

Amend, Otto 747,348

Amend, Otto 551,941

Amend, Otto 601,331

Amend, Otto 747,347

Andrews & Averill 1,319,828

Andrews, B., and Averill, W. C, Jr 1,329,739

Andrews, B., and Averill, W. C, Jr 1,312,467

Andrews, Samuel 58,197

Andrews, Samuel 69,745

Angus, H. R 407,274

Anthony, C. E 620,082

Archbold, Geo ^"^•°??

Archer, Wm J'^aPI

Ard, L: B 1,373,698-9

Artmann, Carl ^'2^1-227

Arvine, Freeling W ^?^'2xf

Arvine, Freeling W tll'll^

Ash, Horace W llt'Wo

Ash, Horace W 779,198

Ash, Horace W 757.387

Ashworth, A. A \imiil

Ashworth, A. A ^'^SS'fc?

Atwood, Luther iVLnk

Atwood, Luther 21,80b

Atwood, Luther 22,40b

Atwood, Luther o^nnc

Atwood, Luther oq qq7

Atwood, Luther oaoAR

Atwood, Luther ob T!ia

Atwood, Luther ii'^tl

Atwood, Luther qi qrs

Atwood, Luther il'tnc.

Atwood, L. and W ]Ant

Atwood, L. and W oofi 161

Atwood, W C'7o'aB9

Aukerman, Cal M , ^li'^^i

Averill, W. C, Jr 1,375,246

Date

Sep. 13, 1887
Feb. 24, 1920
June 10, 1862
July 17, 1866
Aug. 4, 1914
Feb. 13, 1866
Oct. 28, 1919
Nov. 4, 1919
Nov. 29, 1910
Jan. 6, 1920
Apr. 3, 1855
Nov. 15, 1864
July 25, 1899
March 3, 1863
June 26, 1917
Aug. 16, 1920
June 14,1321
June 29, 1880
Oct. 27, 1874
Aug. 26, 1890
Oct. 14, 1913
Sept. 13, 1921
June 20, 1916
Sept. 26, 1876
Jan. 11, 1916
Nov. 1, 1921,
April 27, 1858
Mar. 11, 1879
Jan. 8, 1918
Aug. 9, 1892
Aug. 9, 1892
Dec. 22, 1903
Dec. 24, 1895
Mar. 29, 1898
Dec. 22, 1903
Oct. 28, 1919
Feb. 3, 1920
Aug. 5, 1919
Sept. 25, 1866
Oct. 15, 1867
July 16, 1889
Feb. 21, 1899
Aug. 8, 1893
Sept. 6, 1864
April 5, 1921
July 2, 1912
July 18, 1899
Julv 8, 1890
Jan. 8, 1905
Jan. 8, 1905
April 12, 1901
April 15. 1919
April 15, 1919
April 10, 1860
Oct. 19. IS.-iS
Dec. 28, 1858
Dec. 28, 1858
Feb. 22, 1859
Mar. 29, 1H.'S9
May 29. I860
Mav29. 1860
April 10. IKtiii
Mar, 26. 1861
Aug. 12, 1858
Auk- 12. 1856
April 16. 1880
April 30, 1901
April 19, 1921

Class

C

B, D

U

F

A

C

B

B

B

B

O

D 1

F

B, G

B

B

B

F

F

E3

C

F

D 1

A, O

J

F

R

Kl

B

B

D 1, V

V, D 1

V, D 1

V, D 1

B

B

S

Fl, 1

S

F

B-T

E 1

F

W

K 1

A

G N

K 2. F

E2. F

F 1

S

s

K2

n

B

H

M

G

G B

F

II

H. I) 1

W . F

G

A

B

F

564

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Bacon, Brooks & Clark 1,131,309

Bacon, Brooks & Clark 1,334,731

Bacon & Clark 1,101,482

Backhaus, Arthur A 1,271,114

Backhaiis, Arthur A 1,271,115

Backhaus, A. A 1,296,902

Baillard, Chas. L 340,411

Baker, Leslie A 299,61 1

Ballard, A. M 1,327,691

Barber, Guy M 1,251,'952

Barbet, E. A 1,319,319

Barnes, \Vm. T 24,920

Barnes, Wm. T 24,921

Barrett, Michael 59,531

Barron, Thos. J 46,987

Barniekel, W. S 1,093,092

Barnickel, W. S 1,223,659

Barniekel, W. S 1,223,660

Bartels, E 1.115,887

Barstow, Frank Q 181,814

Barthel, Peter 135,879

Baskerville, Chas 1,231,985

Bassett, R. D 1,120,669'

Bassett, R. D 1,120,670

Bates, H. F 1,046,541

Baum, E. P 1,109.103

Baj-nes, R., and Fearenside, J 299,324

Beckley. R. E 1,127,722

Bell, A. F. L 1,231,695

Bell, A. F. L 581,451

Bell. A. F. L 617,712

Brll. A. F. L 580,592

Bell, A. F. L 655,430

Boll. A. F. L 505,416

Bellingrath, Leonard, Jr 20,465

Bending, Wm. P 998,670

Benham, E. B 1,262,576

Benham, E. B 1,040,124

Benton, G. L 342,564

Benton, G. L 342.565

Bending, Wm. P 1,144,522

Benhoff, G. F., Jr., and Jensen, J. O 1,181,564

Berend, Ludwig 1,167,373

Berg, Fried) ieh 645,743

Berg, Friedrich 560,463

Berg, F 736,479

Berg, F 736,480

Berg, F 623,066

Berg. H.J 93,952

Bergius, Friedrich 1,344,671

Bergius, Friedrich 1,391.664

Bibby, John, and Lapham, A 48,896

Bicknell, John E 313,979

Bicknell, John E 400,042

Bicknell, John E 400,043

Biddison, P. McD., and Boyd, H. T 1,345,740

Blelouss, Elias 1,384,423

Biggins, Jas. E 1,274,976

Blacher, L., and Sztencel, S 956,276

Black, J. C 968,640

Black, J. C 1,152,478

Black, J. C 1,164,162

Black, John C 1,275,648

Blakeman, Wm. N., Jr 1,385,035-6

Blakeman, Wm. N., Jr 1,385,037

Blowski, Jno. and A 1,186,373

Born, Sidney 1,234,124

Borrman, C. H 1,220,067

Date

Class

Mar. 9, 1915

J B

Mar. 23, 1920

B

June 23, 1914

B

July 2, 1918

M

July 2, 1918

M

Mar. 11, 1919

M

April 20, 1886

D 1

June 3, 1884

A

Jan. 13,1920

K

Jan. 1, 1918

S

Oct. 21, 1919

F

Aug. 2, 1859

U

Aug. 2, 1859

G

Nov. 6, 1866

I

Mar. 28, 1865

M

April 14, 1914

A D 1

April 24, 1917

A D 1

April 24. 1917

A

Nov. 3. 1914

H

Sept. 5, 1876

C

Feb, 18, 1873

E 1, 3

July 3, 1917

I

Dec. 15, 1914

J

Dec. 15, 1914

J

Dec. 10, 1912

K 1

Sept. 1, 1914

A

May 27, 1884

D2

Feb. 9, 1915

B

July 3, 1917

BR

April 27, 1897

E3, 2

Jan. 17, 1899

E2, 3

April 13, 1897

E 3

Aug. 7, 1900

E2, 3

Sept. 19, 1893

E 2, 3

June 1, 1858

Fl, 4

Julv25, 1911

A

April 9, 1918

K 1

Oct. 1, 1912

B

May 25, 1886

B

May 25, 1886

B

June 29, 1915

D 1

May 2, 1916

F2

Jan. 11, 1916

D 1

Mar. 20, 1900

F2, 1

May 19, 1896

D 1

Aug. 18, 1903

V, D 1

Aug. 18, 1903

V

April 11, 1899

D 1

Aug. 24. 1869

F 1

June 29, 1920

B

Sept. 27, 1921

D 3

July 25, 1865

F 1

Mar. 17, 1885

F2

Mar. 26, 1889

C

Mar. 26, 1889

C

.July 6. 1920

B

July 12, 1921

LD

Aug. 6, 1918

B

April 26, 1910

I

Aug. 30, 1910

D 1

Sept. 7, 1915

F3

Dec. 14, 1915

D 2, F 3

Aug. 13, 1918

J

Julv 19, 1921

M

July 19, 1921

D3

June 6, 1916

I

July 24, 1917

F 1, n, s

Mar. 20, 1917

F2, 11

KANSAS CITY TESTING LABORATORY

565

UNITED STATES PETROLEUiM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Bostick, J. W., and Homer, Chas. H 1,380,863

Bowman, F 12,852

Bowman, Levi M 1,347,932

Boyd & Hapgood 1,363,833

Boyle, Alex. M 1,276,866

Brace, H. B., and Swart, W. T 54,495

Brackebusch, Hans 275,565

Bradford, Geo 805,116

Bragg, John 604,515

Braggins, Edw 46,633

Brander, G. A 1,361,005

Bransky, Oscar E 1,396,399

Braun, Otto 243,496

Breinig, Revere 306,897

Brickman, Saml 1,279,506

Brooks, Essex & Smith 1,191,916

Brooks & Smith 1,231,123

Brown, Arthur L 1,234,862

Brown, Ernest 1,225,569

Brown, D. P., and Neeley, J. W 361,671

Brown, E. G., Cammann, O. N., and Wil-
cox, O 510,672

Brown, L. W 994,100

Brown, W. A 1,309,794

Brown, Wm 10,055

Brownlee, R. H., and Uhlinger 1,265,043

Brownlee, R. H 1,325,927

Brownlee, R. H 1,308,161

Brucke, Otto 963,510

Brundred, Wm. J 148,806

Buerger, C. B 1,302,761

BuUard, John 34,195

Burcey, Chas. J. T 122,810

Burch; Eli F 1,396,249

Burch, EU F 1,238,101

Burdon, J. W. M. and M. M 1,112,051

Burghardt, C. A 309,027

Burk, H. R 284,811

Burke, A. M., and Wright, S 65,999

Burke, C. R ^'Ht'nli

Burket, D. M., and Gray, J. C 57,285

Burrell, G. A., Voress, C. L., and Canter,

Y Q 1,38^,091)

Burke,' Chas'. 'r .'.'.'.".".'.'.'.'.' .' J'?n?'??Q

Burgess, Louis ^'qSrUt

Burrows,H.G i n?^?o?

Burton, W. M n'nig'Irt"

Burton. W. M J'?A?'qM

Burton, W.M i'mu3

Burton, W. M I'l 1788 1

Burton, W. M • • ^'iol'^?;

Burwell, A. W., and Sherman, L. O iia-i^t

Bush, Asa A .T-k 'oso

Busse, Heinrich q',7'o88

Byerley, Francis X 34 J 288

Byerey,F. X ,^.,29

Byerley, F.X 4^^.,^

Byerey, F. X 32353

iS^:^:x::::::::::::::::::::::::: i«^.«^2

n u- A n .. 779,398

Ca kms, A. C -JG^fiSi

Calkins, A. O q„j^ g28

Campbell, Andrew 1,384;990

Campbell, Jas.R 563,206

Cantour, David 601,988

Carman, r . J 02 08'J

Carpenter, Calvin, Jr

Date
Jime 7, 1921
May 15, 1855
July 27, 1920
Dec. 28, 1920
Aug. 27, 1918
May 8, 1866
April 10, 1883
Nov. 21, 1905
May 24, 1898
Mar. 7, 1865
Dec. 7, 1920
Nov, 8, 1921
June 28, 1881
Oct. 21, 1884
Sept. 24, 1918
July 18, 1916
June 26, 1917
July 31, 1917
May 8, 1917
April 26, 1887

Dec. 12, 1893
May 30, 1911
July 15, 1919
Sept. 27, 1853
May 7, 191«
Dec. 23,-1919
July 1, 1919
July 5, 1910
Mar. 24, 1874
May 6, 1919
Jan. 21, 1862
Jan. 16, 1872
Nov. 8, 1921
Aug. 28, 1917
Sept. 29. 1914
Dec. 9, 1884
Sept. 11, 1883
June 25. 1867
June 22. 1920
Aug. 21. 1866

June 28. 1921
Sept. 6, 1921
Deo. 20. 1921
July 25. 1911
Mar. 11. 1913
Jan. 7. 1913
Aug. 4. 1914
Sept. 29. 1914
Jan. 11. 1916
S«'pt. 8, 1903
Dec. 19, 1SH2
Jan. 10, 1888
Aug. 10. 1886
Aug. 7. 1894
Oct. 1, 18!'r>
July 19. 18S1
Oct. 22. 1872
June 22. 1876

Jan. 3, 1905
S«.pt. 6, 1904
Aug. 1. 19>1

July IS'. 1"'-1
Jan. II. 1896
July 25. 1893
S«-pt. 16, 1868

Class

A

F 1

SO

O

W

M G

D 1

F 1, 5

V, D 1

F5

W

D

U

I

F

L

L

D2

D2

Fl. 2

Fl, 2
A
A

f W
K 3, B
B
F
A.
F2
S
G
F
F

O T
K 1
U
G
D 1

O

K J

H

H

F2, II

». E 2

H.J

J. H

(• H

H

V. D 1

F 1

T

(• F

K 2. 3. F

F 4.2

('

C

C

B

D 1

("

LP

F

V

O

566

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number Date Class

Carter, G. F 680,639 Aug. 13, 1901 S

Carthesy, J. H 1,316,770 Sept. 23, 1919 F

Cassal, N. C, and Gerrans, B. H 1,330,844 Feb. 17, 1920 B

Catlin, Robt. M 1,272,377 July 16, 1918 W

Cazin, Francis F. M 400,634 April 2, 1889 F

Cazin, F. M. F 400,633 April 2, 1889 V, G

Chamberlain, H. P 1,221,790 April 3, 1917 B

Chemin, Jean C. 0 297,766 April 29, 1884 FD

Cheney, Samuel 230,239 July 20, 1880 F2

Cherry, Cummings 15,642 Sept. 2, 1856 A

Cherry, C 15,643 Sept. 2, 1856 W

Cherry, Louis Bond 1,229,886 June 12, 1917 B. P

Cherry, L. B 1,327,023 Jan. 6, 1920 P

Chesebrough, Robt. A 127,568 June 4, 1872 M

Chesebrough, Robt. A 237,484 Feb. 8, 1881 M

Chesebrough, R. A 49,502 Aug. 22, 1865 G. S

Chesebrough, R. A 48,367 June 27, 1865 S

Chesebrough, R. A 51,557 Dec. 19, 1865 S

Chesebrough, R. A 51,558 Dec. 19, 1865 S

Chesebrough, R. A 524,704 Aug. 21, 1894 F 2, II

Chevrier, Gervais 106,915 Aug. 30, 1870 I

Childs, Samuel Il,0o9 June 13, 1854 F 1, 2, I

Clark, C. E 1,147,608 July 20, 1915 K 1

Clark, Edward M 1,119,496 Dec. 1, 1914 B

Clark, E. M 1,129,034 Feb. 16, 1915 B

Clark, E. M 1,388,514 Aug. 23, 1921 B

Clark, E. M 1,132,163 March 16, 1915 B

Clark, Frank W 547,332 Oct. 1, 1895 F 3, 4

Clark, R. C, and Beecher, W. F 275,589 April 10, 1883 F 1, 4

Clark, R. C, and Warren, M. H 298,825 May 20, 1884 F

Clark, R. C, and Warren, M. H 318,698 May 26, 1885 F

Clark, S. G 34,816 April 1, 1862 G, F 2, II

Clarke, Edw 232,685 Sept. 28, 1880 I

Clifltord, Victor 1,266,407 May 14, 1918 H

Coast, John W., Jr 1,250,798 Dec. 18, 1917 B

Coast, John W., Jr 1,250,800 Dec. 18, 1917 B

Coast, John W., Jr ^ 1,250,801 Dec. 18, 1917 B

Coast, John W. ,Jr 1,207,724 June 24, 1919 S

Coast, John W., Jr 1,252,401 Jan. 8, 1918 B

Coast, John W., Jr 1,253,000 Jan. 8, 1918 B

Coast, John W., Jr 1,258,190 Mar. 5, 1918 B

Coast, John W., Jr 1,252,999 Jan. 8, 1918 B

Coast, John W., Jr 1,291,414 Jan. 14, 1919 B

Coast, John W., Jr 1,250,799 Dec. 18, 1917 B

Coast, John W., Jr 1,258,191 Mar. 5, 1918 B

Coast, John W., Jr 1,388,629 Aug. 23, 1921 B

Coast, John W., Jr 1,400,800 Dec. 20, 1921 B

Coast, John W., Jr 1,370,881 Mar. 8, 1921 B

Coast, John W., Jr 1,372,937 Mar. 29, 1921 B

Coast, John W., Jr 1,374,357 Aug. 12, 1921 B

Coast, John W., Jr 1,379,333 May 24, 1921 BR

Coast, John W., Jr 1,333,964 Mar. 16, 1920 B

Coast, John W., Jr 1,345,132-3-4 June 29, 1920 B

Coast, John W., Jr 1,348,264-5-6 Aug. 3, 1920 B

Coast, John W., Jr 1,348,267-8 Aug. 3, 1920 B

Coast, John W., Jr 1,349,815-6-7 Aug. 17, 1920 B

Coast, John W., Jr 1,355,311-2 Oct. 12, 1920 B

Coast, John W., Jr 1,353,316 Sept. 21, 1920 B

Coast, John W., Jr 1,374,357 April 12, 1921 F

Cobb, J. 0 1,201,558 Oct. 17, 1916 A

Cobb, E. B 1,387,835 Aug. 16, 1921 D

Cobb, E. B 1,315,623 Sept. 9, 1919 I, D

Cobb, E. B 1,322,762 Nov. 25, 1919 B, D

Cobb, Ernest B 1,388,517 Aug. 23, 1921 D

Cobb, Ernest B 1,357,224-5 Nov. 2, 1920 D

Cobb, Ernest B 1,300,816 April 15, 1919 D

Cochran, A : 1,296,367 Mar. 4, 1919 B

Cole, Jas., Jr 182,169 Sept. 12, 1876 F 2. 4 II

KANSAS CITY TESTING LABORATORY

567

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Coleman, John T 191,406

Colin, T. F 607,017

Colin, T. F 723,368

Colin, T. F 744,720

Colin, T. F 685,907

Collins, Jacob 1,028,439

Collins, John F 59,334

Collins, Jos. G 32,557

Connelly, Martin 240,093

Connelly, Martin 240,094

Cook & Price 1,190,633

Cooper, A. S 617,226

Cooper, H. C 1,323,837

Cooper, Isaac N 1,349,048

Corfield, Wm 54,061

Corfield, Wm 54,060

Cornell, Sidney 1,202,969

Cosden, J. S 981,176

Cosden, J. S., and Coast, J. W., Jr 2o8,196

Cosden, J. S., and Coast, J. W., Jr 1,261,215

Cottrell & Wright S^Z'HI

Cottrell & Speed ^^Z'U^

Cottrell & Speed ^?Z',,^

Cottrell, F. G 987 lU

Courtois, F. A ^88,250

Cowan, Wm. P 558,.58

Crane, Frederick D , VlfA^l

Crane, Adolphus G Hl^'lln

Crane, Gerard ?VVn9^

Crawford, Benjamin ika'.ai

Crocker, Samuel H ^29,463

Cronemeyer, A. H lltHl

Cronenberger, W. M 'ic^Aat

Cronin,C.J i U^'ool

Cross. A. B ^'^ll'mt

Cross, Jas. P • , o^L'^ls.

Cross, Roy • • ■ ■ J'^nt'^io

Cross, Walter M vioi'tki

Cross, W. M iitAol

Culmer, Geo., and Geo. C. K tllUn

Culmer, Geo., and Geo. C. K 63.5,430

Culmer, F. W , !;s'nA9

Cunningham, Christopher io»,u4^

Danckxvardt, P ■ |;^73;653

Danckwardt, P 1 317 077

Danckwardt, P , 'qi;q'ki»

Daugherty, Alvin A 213 395

Daul, John 25'8;284

Daul, L.OU1S ■■■■: .^^'-^i i 99q 042

Davidson, J. G., and Ford, R. W 1238644

Davidson, Samuel ^ „gg 'j'g'j.g

Davis, C.S._ ' 6-^1,078

Davis, John 1 j 159,186

Davis, John T ' jj_^ gg4

Davis, Samuel ^ a23!681

Day, D. F . . 826,089

Day, David T 1,221.698

Day, David T 1,004,632

Day, David T 1,280,178

Day, David T j 366,894

Day, David T , 342,741

Day, David T ^ 386,768

Day, David T li280,179

Day, Roland B i '357,276-7-8

Day, Roland B ' j 174,970-1

Dayton, W. C 1,398,687

Dean, Daniel A

Date

May 29, 1877
July 12, 1898
Mar. 24, 1903
Nov. 24, 1903
Nov. 5, 1901
June 4, 1912
Oct. 30, 1866
June 18, 1861
April 12, 1881
April 12, 1881
July 11, 1916
Jan. 3, 1899
Dec. 21, 1919
Aug. 10, 1920
April 17, 1866
April 17, 1866
Oct. 31, 1916
Jan. 10, 1911
Mar. 5, 1918
April 2, 1918
Mar. 21, 1911
Mar. 21, 1911
Mar. 21, 1911
Mar. 21, 1911
April 25, 1905
April 14, 1896
April 17, 1917
Aug. 27, 1918
Aug. 17, 1880
Mar. 28, 1871
July 16, 1872
Jan. 13, 1903
Sept. 7, 1915
May 5, 1874
Jan. 13, 1920
Aug. 14, 1866
Feb. 5, 1918
Oct. 31, 1916
Dec. 30, 1919
Oct. 24, 1899
Oct. 24, 1899
July 29, 1879
Dec. 22, 1874

June 1. 1915
April 5. 1921
Sept. 23. 1919
Sept. 21. 1920
Mar. 18. 1879
May 23, 1882
June 5, 1917
Aug. 28. 1917
Mar. 1. 1921
April 2, 1901
Nov. 2. 1915
June 18. 1867
Dec. 2. 1919
Julv 17. 1906
April 3. 1917
Oct. 3. 1911
Oct. 1. 1918
Jan. 18. 1921
.June 8. 1920
Auk. 9. 1921
Oct. 1. lOlH
Nov. 2. 1920
Mar. 14. 1916
Nov. 29. 1921

Class
F

V, D 1
V, D
V, D
V, D
A

F4, I
S

D 1, V
D 1, V
E3
E2, 3
J
H
M
M
F2
F2, II
B
B
P

PA
P
P
N

r

M D

F

E 1

B

B

A

M

F

J K

M

B

B

H

K

W

G

C

.]. K 1. I

B. n

B, V

B

F2

F2

P

J. K 2

I!

K 1. 11

K 2. 11

S

w

V. 1>

B. n

B

w

1)2

w

B
B
B

K I
F

568

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Dean, Richard 290,866

Dean, Richard 305,056

Dean, Richard 310,497

Dean, Richard 314,368

Dean, Richard 342,500

Dehnst, Julius 1,112,602

DeSmedt, Edw. J 236,995

DeSmedt, Edw. J 237,662

Dewar & Redwood 419,931

Dewar & Redwood 426,173

Dewitt, Henry C 63,299

Dickey, Julius C 166,349

Diehl, H. A 469,777

Dieterichs, E. F 253,990

Ditniar, Peter 246,096

Divine, S. ., and Seely, C. A 55,071

Divine, R. E 1,303,662-3

Dmne, R. E 1,303,779

Doe, Wm 174,789

Dow, Allan W 688,073

Downard, J. S., and Roloson, B. A 722,500

Downer, Wm. P 44,519

Drake, Thos 471,963

Draper, Henry V. P 238^867

Drayton, Thos 11 239

Dubbs, C. P 1,231,'509

Dubbs, C. P 1,392,629

Dubbs, J. A 1,100,717

Dubbs, J. A 1,135,506

Dubbs, J. A 470,911

Dubbs, J. A 646,'639

Dubbs, J. A 1,002,570

Dubbs, J. A 1,057,227

Dubbs, J. A 694,621

Dubbs, J. A 694,622

Dubbs, J. A 407,182

Dubbs, J. A 1,123, 502

Dubbs, Henry 161,672

Dubbs, L. A 1,319^053

Dubler, John B 251.770

Dubler, J. B 283,471

Dubreui!, A 48,265

Duffus, G. H. S *. .46,088-9-90

Duffy, J. T 1,356,196

Duncan, W. M 1,342,947

Dundas, R. C 1,056,980

Dundas, R. C 1,120,039

Dundas, R. C 1,257,199

Dunham, F. H 1,003,040

Dunham, F. H 1,013,283

Dunkle, Allen H 530,300

Dunscomb, Edward 62,739

Dupia.s, A. C. G., and Fell, W. S 749,368

Durant, C. W., and Griinth, J 132,263

Dvorkovitz, Paul 546,697

Dyar, N. A., and Augustus, J. F 25.362

Dyer, E. I 1,207,381

Dyer, E. I 1,220,504

Dyer, E. I., and Heise, A. R 1,242,784

Dyer, Frank L 579,360

Dyer, Walter 1,256,535

Dyer, Walter and W. E 1,256,536

D'Yarmett, E. C 1,376,713

Earle, G. W 1,221,038

Eastlake, Lewis S 1,352,502

Eaton, Richard 110,638

Edeleanu, Lazar 911,553

Date

Class

Dec. 25, 1883

F2, II

Sept. 16, 1884

F 1, 2, II

Jan. 6, 1885

F

Mar. 24, 1885

F 1, 2, 3, II

May 25, 1886

F2, II

Oct. 6, 1914

V, D

Jan. 25, 1881

E 1, 2

Feb. 8, 1881

E 1, 2

Jan. 21, 1890

B

April 22, 1890

B

Mar. 26. 1867

M

Aug. 3, 1875

Fl

Mar. 1, 1892

E2, 3

Feb. 21, 1882

F 1, 2

Aug. 23, 1881

M

Mav 29, 1866

F2

April 22, 1919

K

May 13, 1919

I

Mar. 14, 1876

S

Dec. 3, 1901

E 1, 2, B

Mar. 10, 1903

E 2

Oct. 4, 1864

D 1

Mar. 29, 1892

L

Mar. 15, 1881

G D

July 4, 1854

D

June 26, 1917

B

Oct. 4, 1921

B

June 2, 1914

B

April 13.1915

E2,B

Mar. 15, 1892

V

April 3, 1900

F2, 4

Sept. 5, 1911

A, F

Mar. 25, 1913

E2

Mar. 4, 1902

F4, II

Mar. 4, 1902

F4

July 16, 1889

V, D

Jan. 5, 1915

A

April 6, 1875

D.S

Oct. 21, 1919

B

Jan. 3, 1882

F

Aug. 21, 1883

Fl, II

June 20, 1865

F2

Jan. 31, 1865

F, S

Oct. 19, 1920

J. K

June 8, 1920

F

Mar. 25, 1913

E2, B

Dec. 8, 1914

Fl, II

Feb. 19, 1918

B

Sept. 12, 1911...

E

Jan. 2, 1912

E2

Dec. 4, 1894

U

Mar. 12, 1867

S

Jan. 12, 1904

F, S

Oct. 15, 1872

U

Sept. 24, 1895

F2

Sept. 6, 1859

M

Dec. 5, 1916

A

Mar. 27, 1917

A

Oct. 9, 1917

A

Mar. 23, 1897

F2. 5

Feb. 19, 1918

D

Feb. 19, 1918

D

May 3, 1921

J,B

April 3, 1917

H

Sept. 14, 1920

O

Jan. 3, 1871

O

Feb. 2, 1909

D

KANSAS CITY TESTING LABORATORY

569

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Edgerton, Henry H 159,655

Edwards, E. A 439,745

Edwards, Jos. B 100,874

Edwards, Jos. B 1,277,884

Eggleston, J. E 1,018,040

Ekstrand, Chas 1,388,415

Eldred, B. E., and Mersereau, G 1,234,886

Elliott, W. S 1,242,667

Ellis, Carleton 1,089,359

Ellis, Carleton 1,191,880

Ellis, Carleton 1,216,971

Ellis, Carleton 1,249,278

Ellis, Carleton 1,318,060-1

Ellis, Carleton 1,365,044

Ellis, Carleton 1,365,046

Ellis, Carleton 1,345,589

Ellis, Carleton 1,341,975

Ellis, Carleton 1,396,999

Ellis, C, and Cohen, M.J 1,365,048

Ellis, C, and Cohen, M.J 1,365,050

Ellis, C, and Cohen, M. J 1,365,051-2

Ellis, C, and Wells, Alfred A 1,365,053

Ellis, John, and Kattell, E. C 63,789

Ellis, John, and Kattell, E. C 68,860

Ellithorpe, S. B 52 277

Emerson, Victor Lee ^'^^^'Ina^

Emerson, Victor Lee 1,367,806-7

Emerson, V. L ^'S^^SoI

Emerson, V. L I'^fAl].

Emory, F. F kVMH

Engle, Jacob P \^li?\ol

Erickson, Emil T i'281,320

Erwin, J. B., and O. R J'?!^?S2

Eva, Gray and Christy Hl^'llt

Evans, Edward , hlaAol

Evans, G. P. . . .- ^•^^'Sio nT.

Everest, H.B 212.914

Everest, H. B ^»-426

Ewing, Cha.s. R ^'"fc'o?t

Ewing, M. P 5b,»t)<:

Ewing', M. P.', and Everest, H. B 58,021

Fagan, John G ^'Hl'lol

Fairchild, J. H 53,528

Fales, Levis ^9,740

Fales, Levi S ^j;}.^^

Fales, Levi S m'ltl

Fales, I^vi S ofi'nq?

Farrar, Alonzo «^;^^^

Farrar, A o/ic ana

Farrar, F. F., and Gill, F. P . . . . ^ 206.309

Faucett, H. W., and McGowan, T \ll'At

Faucett & McGowan 1 1 7 sri

Faucett & McGowan li40;5;i2

Faust Samuel D 1 108 351

Fazi, Romolo de 1 070 435

Felizat, Louis i;i79:296

Felton, D. F 1 394.181

Fenton, Jas. 1 1 396 174

Fenton, Jas. T ' 5;j'9(j,|

Fichet, L. V^ 40'8'.472

Field, John K 956.066

Flemmg, J . C ^ 324.766

Flemmg, R j 325.668

Flemmg, R 60,571

Fleury. Huot i ' /-• ^

Flowers, G. W., and Happersett, J. C. and ^^^

D. W

Date
Feb. 9, 1875
Nov. 4, 1890
Mar. 15, 1870
Sept. 3, 1918
Feb. 20, 1912
Aug. 23, 1921
Julv 31, 1917
Oct. 9, 1917
Mar. 3, 1914
July 18. 1916
Feb. 20, 1917
Dec. 4, 1917
Oct. 7, 1919
Jan. 11, 1921
Jan. 11, 1921
July 6, 1920
June 1, 1920
Nov, 15, 1£21
Jan. 11, 1921
Jan. 11. 1921
Jan. 11. 1921
Jan. 11. 1921
April 16, 1867
Sept. 17, 1867
Jan. 30, 1866
July 13, 1920
Feb. 8, 1921 v
Oct. 19, 1920
April 20, 1920
Aug. 3, 1915
Aug. 23, 1892
Oct. 15, 1918
Feb. 3, 1914
June 16, 1914
Feb. 26, 1918
Jan. 25, 1921
Mar. 4. 1879
Sept. 3. 1867
Jan. 13. 1914
Julv 31, 1866
Sept. 11, 1866

Aug. 3, 1916
Mar. 27. 1866
Sept. 5. 1865
Jan. 23. 1866
Sept. 5, 1865
Nov. 23, 1869
Oct. 26, 1869
Mar. 15. 1870
July 23. 1878
Nov. 26. 1872
Nov. 26. 1872
Aug. 8. 1«71
Mnv 18, 1920
Aug. 2r). 1914
Aug. 19. 1913
April 11. 19K"'
Oct. IH. 1921
Nov. 8. 1921
April 17. 1866
Aug. 6. 1889
April 26. 1910
Dec. 9. 1919
Dec. 23. 1919
Or(. 21. 1865

Feb. 24. 1868

II

B

Class

Kl

F 2, 4,

F2

B

F,V

B

B

A, D

O

D, L

B

J.

B

L

L

D3

B

B

L

L

L

L

F2, II

F2, II

U

B

B

F

F

S

A

W

H

O

V

F

F

F 2. 5. U

S

F 2. 5 II

F2, 6 11

H

U

S

F. II

F 4. I

1

1>

1

I

S. F

S. I)

U

F

M

I>

K 1

U

H

»•• 2. 11

n 1

S. A

H

K

K f.. I '

M

570

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Fordred, John 54,267

Forrest, Chas. N 1,163,593

Forward, C. B 1,189,083

Forward, C. B 1,181,301

Forward, C. B 1,202,823

Forward, C. B 998,569

Forward, C. B 1,100,966

Forward, C. B 1,088,693

Forward, C. B 1,088,692

Forward, C. B 1,247,808

Forward, C. B 1,255,149

Forward, C. B 1,274,405

Forward, C. B 1,299,449

Forward, C. B., and Davidson, J. M 611,620

Foster, Arthur B 1,394,486

Foubert, Andre 71,156

Foubert, Andre 118,602

Foubert, Andre 60,166

Fowler, David W 75,147

Frances & Morgan 1,313^629

Franke, A. H 1,142,512

Frasch, Hans A 488,628

Frasch, Hans A 640,292

Frasch, Hans A 525,811

Frasch, Hans A 581,546

Frasch, Hans A 1,212,620

Frasch, H. A 1,318,657

Frasch, Herman 845,735

Frasch, Herman 968,760

Frasch, Herman . . . ; 487,216

Frasch, Herman 564,520

Frasch, Herman 490,144

Frasch, Herman 553,191

Frasch, Herman 561,216

Frasch, Herman 564,921

Frasch, Herman 448,480

Frasch, Herman 378,246

Frasch, Herman 951,729

Frasch, Herman 951,272

Frasch, Herman 622,799

Frasch, Herman 190,483

Frasch, Herman 630,496

Frasch, Herman 500,252

Frasch, Herman 572,676

Frasch, Herman 231,420

Frasch, Herman 205,792

Frasch, Herman 649,047

Frasch, Herman 340,499

Frasch, Herman 487,119

Frasch, Herman 281,045

Frasch, Herman 564,922-2

Frasch, Herman 564,924

Frasch, Herman 649,048

Frasch, Herman 542,849

Frasch, Herman 543,619

Fraser, Wm. M 1,259,223

Fraser, Wm. M 1,258,103

Frederici, C. F 48,672

Freel, John 504,917

French, Edw. H 1,394,488

Gaggin, Richard 118,359

Gallsworthy, Benjamin 1,234,327

Galloupe, J. H 1,283,723

Galloupe, J. H 1,365,822

Gardner, H. A., and Bielouss, E 1,384,447

Gardner, J., and Harris, J. F 442,802

Date

Class

April 24, 1866

W, D 1

Dec. 7, 1915

E 1,3

June 27, 1916

B.J

May 2, 1916

F2, II

Oct. 31, 1916

B

July 18, 1911

E 2, B

June 23, 1914

B

Mar. 3, 1914

B

Mar. 3, 1914

E2, B

Nov. 27, 1917

U

Feb. 5, 1918

B

Aug. 6, 1918

B

April 8, 1919

F

Oct. 4, 1898

E 2, 3, ]

Oct. 18, 1921

B

Nov. 19, 1867

F2

Aug. 29, 1871

F

Dec. 4, 1866

F 1

Mar. 3, 1868

M

Aug. 19, 1919

D

June 8, 1915

A

Dec. 27, 1892

I

Jan. 2, 1900

F2, II

Sept. 11, 1894

D 1

April 27, 1897

E 2, 3

Jan. 16, 1917

B

Oct. 14, 1919

F

Feb. 26, 1907

F2, II

Aug. 30, 1910

F 1

Nov. 29, 1892

V

July 28, 1896

V

Jan. 17, 1893

V

Jan. 14, 1896

S

June 2, 1896

D 1

July 28, 1896

V

March 17, 1891

V

Feb. 21, 1888

V, D

Mar. 8, 1910

G, D

Mar. 8, 1910

G, D

April 11, 1899

V

May 8, 1877

r2, 4

Aug. 8, 1899

V

June 27, 1893

V

Dec. 8, 1896

V, D

Aug. 24, 1880

U

July 9, 1878

F

May 8, 1900

O, V

April 20, 1886

F

Nov. 29, 1892

V

July 10, 1883

F2, 3

July 28, 1996

V

Julv 28, 1896

V, F

May 8, 1900

V, D

July 16, 1895

V, D 1

July 30, 1895

V

Mar. 12, 1918

E 1, 2

Mar. 5. 1918

E 1, 2

July 11, 1865

F

Sept. 12, 1893

S, F

Oct. 18, 1921

D

Aug. 22, 1871

D2,V

July 24, 1917

F2, II

Nov. 5, 1918

W

Jan. 18, 1921

W

July 12, 1921

L, D

Dec. 16, 1890

V, F

D 1

KANSAS CITY TESTING LABORATORY

571

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Herber, Samuel M 1,183,457

Hibbert, Harold 1,270 J59

Hicks, Enoch O 1,378,229

Higbie, M. S., and Dougherty, A 387,358

Higbie, M. S., and Dougherty, A 387,357

Higgins, Chas. S 309,718

Higham, A. D 54,157

Hill, R. L. 1,269,439

Hill, S., and Thumm, C. F 101,364

Hill, S., and Thamm, C. F 101,364

Hill, S., and Thumm, C. F 102,819

Hill, S., and Thumm, C. F 114,293

Hird, Harold Pearson 1,368,149

Hirshberg, Leon 1,042,915

Hirt, Leon E 1,222,402

Hirt, Leon E 1,250,879

Hirt, Leon E 1,264,796

Hodkinson, M 26,326

Hofferberth, John 105,683

Hoffman, Bernhard 641,962

Hoffman, Ross J 405,738

Hoffman, Wm. John 1,367,968

Holmes, F. W., and Blasdell, E 1,055,747

Hoge, Daniel W 1,382,727

Holmes, Fletcher B 1,276,219

Holmes, Jos. E 23,427

Holmes, Jos. E 1,241,979

Holmes, J. E 24,212

Hood, J. J., and Salamon, A. G 962,840

Hopkins, A. S 1,199,463

Hopkins, A. S 1,199,464

Horner, E. N 22,727

Houlehan, Arthur Earl 1,334,033

Houlehan, Arthur Earl 1,337,317

Houlker, Christopher 110,364

Hout, F., and Rogers, John 71,619

Hout, F., and Rogers, John 63,051

Howard, F A 1,284,687

Howarth, John 42,772

Howe, Bphriam 7,667

Howell, 1,294,909

Howell, C. G „^^'^'*);

Howell, H. F 216,518

Hudson, Chas. R ^^I'lli

Hudson, Samuel if^^^I

Huglo, Victor ?55'^.r^

Hubbard, P 1,326,056

Humason.G.A 1.291.89&

Humphreys. R. E Moo'mn

Humphreys, R. E J'Jfo'Snn

Humphreys, R. E }'oifi'I?q

Humphreys, R. E.- I'o.o'c?,

Humphreys & Burton ' co'^In

H untington, John o^r'l^r

Hussey. John S Hllfok

Huston, John B fol-xnc

Huston, John B 486,406

Hyde, Burrows iHl.vyv

Ihart,J.P 5^4,258

ISEdLdw.;:::;::::::::::::::': i.2«5;2oo

Jaeger, W.G.W 24.217

Jaeger, W. G. W 24.561

Jaeger, W. G. W ^*-^^'*

Date

May 16, 1916
June 25. 1918
May 17. 1921
Aug. 7. 1888
Aug. 7, 1888
Dec. 23, 1884
April 24, 1866
June 11, 1918
Mar. 29, 1870
Mar. 29, 1870
Mav 10. 1870
May 2, 1871
Feb. 8, 1921
Oct. 29, 1912
April 10, 1917
Dec. 18, 1917
April 30, 1918
Nov. 29, 1859
July 26, 1870
Jan. 23, 1900
June 25, 1889
Feb. 8. 1921
Mar. 11, 1913
June 28, 1921
Aug. 20, 1918
Mar. 29, 18o9
Oct. 2, 1917
May 31, 1859
June 28, 1910
Sept. 26, 1916
Sept. 26, 1916
Jan. 25, 1859
Mar. 16, 1920
April 20, 1920
Dec. 2a. 1870
Dec. 3. 1867
Mar. 19. 1867
Nov. 12, 1918
May 17, 1864
Sept. 24, 1850
Feb. 18. 1919
July 16. 1867
June 17. 1879
Aug. 20. 1901
Feb. 20. 1872
April 5. 1910
Dec. 23, 1919
Jan. 21. 1919
Dec. 22. 1914
Dec. 22. 1914
Dec. 1, 1914
Nov. 26. 1918
June 15. 1920
Mar. 12, 1867
S<-pt. 3. 191H
April 29. 1H8«
Nov. 16, 1892
July 21. 1883

July 24. 1900
Aug. 23. 1910
Nov. 19, 1918

May 31, 1869
June 28. 1869
May 1. 1866

1, II
1. II
1. II
1,3 II

Class

F, 2, 3 D

B, K2
B

C, E, 1
C, E. 1, 3
N

F

B

F

F

F

F

F

D

B. F

B, P

K, 3

G, W
Fl. I
M
S
M
B

D

G. W
B.J
W

D2

n

H
W. 1)

o

F4

S

F

W. F

M

S

Fl. 2

L

A

G

B

B •

S

B. S

B

B

I

B

F

<•

S

V

T

A

F2. 11
1i

\V

W, S
K I, J

II

572

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number Date Class

James, CM 86,232 Jan. 26, 1869

Jann, John 52,574 Feb. 13, 1866

Jann, John 57,727 Sept. 4, 1866

Jenkins, U. S 1,226,520 May 15, 1917

Jenkins, U. S 1,321,749 Nov. 11, 1919

Jenney, W. P 190,762 May 15, 1877

Jenney, W. P...- 178,061 May 30, 1876

Jenney, W. P 178,154 May 30, 1876

Jennings, Isaiah 1,453 Dec. 31, 1839

Jensen, J. 0 1,388,718 Aug. 23, 1921

Jensen, J. 0 1,268,721 June 4, 1918

Johansen, E. M 1,373,661 April 29, 1921

Johnson, John 54,917 May 22, 1866

Johnson , Walter 1,354,257 Sept. 21, 1920

Johnson & Snodgrass 1,283,202 Oct. 29, 1918

Johnston, Jas. J 117,425 July 25, 1871

Johnston, Jas. J 117,426 July 25, 1871

Johnston, Jas. J - 48,285 June 20, 1865

Johnston, Jas. J 31,982 April 9, 1861

Johnston, Jas. J 50,935 Nov. 14, 1865

Johnston, Jas. J 91,448 June 15, 1869

Jones, Albert R 1,328,522 Jan. 20, 1920

Jones, Frank 1,373,890 April 5, 1921

Jones, Harry Wagenseller 1,336,357 April 6, 1920

Jones, Harry Wagenseller 1,347,543 July 27, 1920

Jones, Harry Wagenseller 1,347,544 July 27, 1920

Jones, Philip 1,255,018 Jan. 28, 1918

Jones, E. C, and Jones, L. B 1,089,926 Mar. 10, 1914

Jones & Jones 1,157,225 . Oct. 19, 1915

Jones, R. G 1,166,375 Dec. 28, 1915

Jones, R. G 1,005,977 Oct. 17, 1911

Jordery, Chas. A 126,552 May 7, 1872

Joseph, Irwin S 1,362,105 Dec. 14, 1920

Just, John A 658,988 Oct. 2, 1900

Kasson, H. R., and Saxton, S. S 998,691 July 25, 1911

Kattell, E. C 222,408 Dec. 9, 1879

Kayser, Adolf 508,479 Nov. 14, 1893

Kayser, A 640,918 Jan. 9, 1900

Keen, Morris L 25,552 Sept. 20, 1859

Kelley, E. G 67,988 Aug. 20, 1867 F

Kelley, E. G., and Tait, A. H 32,568 June 18, 1861 F

Kelley, E. G 84,195 Nov. 17, 1868 F 1, II

Kells, Edw 298,210 May 6, 1884 F

Kells, Edw 374,838 Dec. 13, 1887 F 1, I

Kelsey, S. E 1,029,366 April 7, 1914 B

Kelsey, S.'E 1,302,669 May 6, 1919 S

Kendall, Edw. D 413,187 Oct. 22, 1889 D

Kendall, Edw. D 359,357 Mar. 15, 1887 Dl

Kendall, Edw. D 284,437 Sept. 4, 1883 D, M

Kendall, Edw. D 451,660 May 6, 1891 D 1, 2

Kendall, Edw. D 1,192,529 July 25, 1916 K 2, J

Kendall, Edw. D 1,154,517 Sept. 21, 1915 D 1, S

Kendall, Edw. D 1,154,516 Sept. 21, 1915 D 1

Kennard, Harold J 1,394,771 Oct. 25, 1921 P

Kennedy, C. F 1,356,631 Oct. 26, 1920 O, D

Kennedy, D. McD 370,950 Oct. 4, 1887 V

Kennedy, J. S 1,339,112 May 4, 1920

Xerr, Arthur Neal 1,371,427 Sept. 5, 1918 K2

Kerr, A. N 1,199,903 Oct. 3, 1916 J

Keyt, A.N 1,262,808 April 16, 1918 D

Kipper, H. B 1,253,048 Jan. 8, 1918 Dl

Kirchoffer, G. W 32,373 May 21, 1861 G. W

Kirk, Arthur 78,878 June 16, 1868 F 1, II

Kirk, J. L 215,756 May 27, 1879 F 1, II

Kirk, Solomon W 267,752 Nov. 21, 1882 C

Kirschbraun, L 1,940,750 Aug. 15, 1916 E 1, 2

F 1, 2 II

M

M

J, B

I
I
I. T

M

W

A

I

S

B, P

S

F

A

F4, 5

S

F2

F2, II

W

K2, S
Kl, 2
K 1
F2, II
A
M
A
M

E 1, 2
F2, 4
D 1, V
V, D 1
Fl

1,11

1, 2 II

KANSAS CITY TESTING LABORATORY

573

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)—

Continued.

NAME Number

Garner, J. B., and Clayton, H. D 1,262,769

Garner, J. B 1,299,455

Garner, J. B., and Cooper, H. C 1,332,290

Garrity, W. F., and Jarvais, A 1,190,538

Gar vey, Benjamin 29,218

Gathmann, Louis 768,796

Gathmann, Louis 755,760

Gav, Cassius M 1,179,001

Gearing, CM 212,084

Gellen, A 1,063,025

Gengembre, H. P 52,283

Gengembre, H. P 52,284

Gengembre, H. P 24,454

Gengembre, H. P 25,109

Gengembre, H. P 27,542

Gengembre, H. P 33,699

Gerbeth, F. L. de 81,071

Gesner, Abraham 11,205

Gesner, A 11,203

Gesner, A H'|?o

Gesner, Abraham ' Vi

Gibbons, Samuel f A'ff o

Gibbons, S !!'o, «

Gibbons, S °5,810

Gibbons, S , „S?'?I^

GilehrLst, V. T ^•^IHtl

Gillespie, Jas 23,362

Gillons,G. H ^iti'Tc,

Goldwater, Henry ?oo'Iot

Goldwater, Henry "JnT'nAo

Goodaire, Wm., and Stead, Geo lli'^^,

Gordon, Thos 451,-24

Covers, F.X ^'??I'ln9

Grade, John Ut'lm

Grade, John iit'Ank

Grade, John WAne.

Grade, John al'na^

Grade, John r-c'^?o

Crah^'m'^cV '. '• '^'isP

(_rranam, c r> Ifi a03

Grannis, C. W ono'oQo

Grant, H. F ^'^^^o??

Grant, Jas. B ooo'tA

Grant, J. B., and Mason, A iialVh

Grant & Mason Hi'tit

Grant & Mason iin'^tl

Gray,A,MeD 663 23o

Gray, Daniel T gS^35

^^^y-S-T 1,005.425

Gray, E. B^ .. 1.193.540

^^y-^-^ .. l,193,.>n

Gray, G W gg., .,29

^''^y- i'l" 923.428

^ray. J. L 1.192,889

^""^y- •'■'i' 923.427

Gray, J . L . . . 1 331 909

Gray, John Lathrop , 'iin'sRO

G->-.Tho-T ••■ ;?^«;SJ5

Gray, T. T ,'97, en

Gregory. Ralph and Wmton 46 791

Green, Joel. 1,252.000

Greene. H. J 1110, 924

Greenstreet, Chas. J 1110 923

Greenstreet, Chas. J 1110 025

Greenstreet, C. J l'l66;982

Greenstreet, C J

Date

April 16, 1918
April 8, 1919
Mar. 2, 1920
Julv 11, 1916
July 17, 1860
Aug. 30, 1904
Mar. 29, 1904
April 11, 1916
Feb. 4, 1879
Mav 27, 1913
Jan. 30, 1866
Jan. 30, 1866
June 21, 1859
Aug. 16, 1859
Mar. 20, 1860
Nov. 12, I861
Aug. 18, 1868
June 27, 1854
June 27, 1854
June 27, 1854
Mar. 27, 1855
Mar. 2, 1869
Mar. 9, 1869
Jan. 12, 1869
Sept. 17, 1867
Aug. 2, 1921
Mar. 29, 1859
Jan. 13. 1914
July 19. 1887
July 22. 1890
Mar. 22. 1870
May 5. 1891
Mar. 18. 1919
May 16. 1871
May 16, 1871
July 25, 1871
Julv 25, 1871
Jan. 26, 1870
Mar. 17. 1896
July 7. 1903
Sept. 9, 1862
May 13. 1919
Aug. 21, 1806
April 6. 1^86
April 6, 1886
April 6. 1886
July 10. 1900
Dec. 6. 1881
Oct. 25. 1881
Julv 17. 1883
Oct. 10. 1911
Aug. 8. 1916
Aug. 8. 1916
June 1. 1909
June 1. 1909
Aug. 1. 1916
June 1. 1909
Feb. 24. 1920
May 25. 19'_'0
on. 25, 1915
Julv 2. 1918
Miir. 14. 1865
Jan. 1. 1918
Oct. 26. 1915
Sept. 15. 1914
Sept. 16. 19U
Sept. lb. 1914

1,5

1,11

Class

L

J, K

K, J

O, A

G

F

F

J

F

I

A

A

G

G. B

G, W

G

L, P

G

G

G

G

O

F

F2

F 1

F

G. F

F 1,11

Fl,2,

S

1

1)

\v

F4

F

F

F

F

II
2 11

II

1. 1

i.n

II

F2,
D 1

r. G

O

F

F 1. 2. 6. II

F 2. 6. II

A

C

C

C

C, S

I

n. J

H

I

1

F

I

I)
V
<< 1 2. 7. 1. S I

K i
K 1
It

n

H

574

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Greenstreet, C.J 1,299,1'72

Grieg, A., and Smith, Jas 42,171

Griffin, Jonathan 23,167

Groble, J. C 1,283,502

Grogan, Henry 94,409

Grogan, H., and Lape, G. T 89,988

Grousilliers, Hector de 378,774

Guillaume, Emile 996,081

Guhck, W. R 1,187,061

Gumpoldt, Emil 616,838

Hadley, B. E 1,300,230

Hague, S. L 775,448

Hague, S. L 759,988

Hall, C. H 86,535

Hall, C. H 55,855

Hall, C. H., and Ellis, John 58,813

Hall, T. G 372,672

Hall, Wm. A 1,175,909

Hall, Wm. A 1,105,772

Hall, Wm. A 1,194,289

Hall, Wm. A 1,2.39,099

Hall, Wm. A 1,175,910

Hall, Wm. A 1,247,671

Hall, Wm. A 1,242,795

Hall, Wm. A 1,242,796

Hall, Wm. A 1,239,100

Hall, Wm. A 1,261,930

Hall, Wm. A 1,242,746

Hall, Wm. A 1,242,795

Hall, Wm. A 1,285,136

Hall, Wm. C 266,990

Halvor.son, Halvor 305,182

Halvorson, H 305,180

Hamilton, T. S 1,018,971

Hand, Hacry W 596,874

Handv, Jas. O 1,281,355

Handy, Jas. O 1,281,354

Hansen, JuHas 1,084,738

Hardy, C. A 51,042

Hardy, C. A 40,168

Hardy, C. A 46,899

Harris, Ford W 1,281,952

Harris, John 1,283,508

Harris, MUo 170,730

Harrison, Poole 1,355,554

Hart, Thos. M 1,252,433

Hartshorn, H. M 91,843

Hastings, D., and Brink, A. W 867,505

Hatch, N. B 22,798

Hawes, Benj. N 444,833

Hazlett, R. W., and Hobbs, J. H 24,211

Hebard, Benj. F 31,457

Heckenbleikner & Gilchrist 1,310,078

Hedges, E. E 1,383,205

Helbing, H., and Passmire, F. S 666,010

Hempel, H 621,338

Hempel, H 621,411

Henderson, Geo. A 1,266,261

Henderson, N. M 490,199

Henderson, N. M 340,878

Henderson, H 1,335,438

Hennebutte, H 1,165,878

Hennebutte, H 1,165,877

Hense, Rudolf 1,073,233

Herber, Samuel M 1,111,580

Date

Jan.

Mar.

Mar.

Nov.

Aug.

May

Feb.

June

June

Dec.

I, 1916
29, 1864
8, 1859
5, 1918
31, 1869

II, 1869
28, 1888
27, 1911
13, 1916
27, 1898

April 8, 1919
Nov. 22, 1904
May 17, 1904
Feb. 2, 1869
June 26, 1866
Oct. 16, 1866
Nov. 8, 1887
Mar. 14, 1916
Aug. 4, 1914
Aug. 8, 1916
Sept. 4, 1917
Mar. 14, 1916
Nov. 27, 1917
Oct. 9, 1917
Oct. 9, 1917
Sept. 4, 1917
April 9, 1918
Oct. 9, 1917
Oct. 9, 1917
Nov. 19, 1918
Nov. 7, 1882
Sept. 16, 1884
Sept. 16, 1884
Feb. 27, 1912
Jan. 4, 1898
Oct. 15, 1918
Oct. 15, 1918
Jan. 20, 1914
Nov. 21, 1865
Oct. 6, 1863
Mar. 21, 1865
Oct. 15, 1918
Nov. 5, 1918
Dec. 7, 1875
Oct. 12, 1920
Jan. 8, 1918
June 29, 1869
Oct. 1, 1907
Feb. 1, 1859
Jan. 20, 1891
May 31, 1859
Feb. 19, 1861
July 15, 1919
June 28, 1921
Jan. 15, 1901
Mar. 21, 1899
Mar. 21, 1899
May 14, 1918
Jan. 17, 1893
April 27, 1886
Mar. 30, 1920
Dec. 28, 1915
Dec. 28, 1915
Sept. 16, 1913
Sept. 22, 1914

Class

a

K 1

M

K

F2

F2,

I

B

M

M

II

S

W, S

W, S

F2

F 1, 2 II

F 1, II

V

B

B, Kl

B

B

B, K 1

B

B

B

B

B

B

B

B

F2

S

F

A

U, S

O

0

c

F

F2, 4

F

A, P

K2

U

N

A, E 2, 3

N

K, 2, J

G

V

G, S

M

I

W

D 1

M

M

E 1

C

F

B, F

F

F4, 1

M

F, D 1

KANSAS CITY TESTING LABORATORY

575

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME

Number

Date

Class

Kitchen, J. M. W 1,008,273

Klauber, Laurence M 1,371,378

Klein, John S 306,837

Kline, Geo. H 253,362

Klosterman, Robt 152,650

Knottenbelt, H. W 1,194,033

Knottenbelt, H. W 1,277,605

Koch, G. T., and Stallkamp, A. L 1,380,067

Koehler, Herman 507,441

Koehler, W. C, and Kink, L 1,084,016

Koetchaw, R 1,325,299

Koppers, H 1,098,723

Kormann, Frederick A 1,332,849

Kotschevar, H. J 1,357,998

Kreiser, J. M 384,768

Kresier, J. M 366,487

Kreusler, A „^^'2^°

Kroll, C 1,373,251

Lachman, W ^•^S?'^^?

La[^g.^ohn:;:;:::;::::::.: 471.291

Laing, John t„HoI

Laird Robt. H 507,230

Laird, Robt. H ^. 498.518

Laird, R. E., and Raney, Jos. H , 'Hn'ooc

Laird, W.G HM?

Laird & Raney ^'Wy'ltl

Laird & Raney MH'^^Q

Laird & Raney -^'i aa'im

Lamb, D. M }83,401

Lambe, Frederick , l.-'kin

Lambert, Chas. G J'wq'nqs

Lamplough, F 1 199 909

Landes, Wm Hw^o^

Landsberg, L 179 iqi

Lane, Edw lli'lil

Lang, J. S ^l\f°

Lapham,Allen 266,281

Lapp, C. E 1,075,481

Lasher, L>. t -'„, r coo

Lawrence, W P 1.31|-j'^2

jlrTr . 1,288,934

^ ' w^T 727,391

Leman ^^^. T ^^g 23

pn'^'^rd, F j;59 07,;

J^"r^ rwH.' F ■ 1.261,410

LePley. Clyde E 1,310.164

Leslie, L. H ■ • , o.,n ro-x

Leslie, E. H., and Barbre, C I981 w

133,042
1.251.978

Lessing, Rudolf.

Letchford, R. M.. and Nation, W

Levy, E. D., and Jacobs, H. W ]'tmAM

Lewis, Jos. W • • • I'^iq^V.^.l

Lewis, F. B., and Cooke, T. S 1,.59^,.)»J

Lewis, Sylvester

Lewis, S

Lewis, S „■ ' ' ' ' xir' -o

Linderborg, G., and Scott, W. B 1,256.310

Lindsy , Wm. J 1 '284 .1 1 7

Linn, S. S ■• •

Livesav, Jas., and Kidd, Jas
Livingston, Julius I . . .

Livingston, Max

Livingston, Max

35.527

42.671

43.156

1 220,651

258,778
239,260
237,560
728.257

Nov. 7, 1911

F 1, 2 II

July 25, 1919

N

Oct. 21, 1884

S

Nov. 30, 1886

Fl, II S

June 30, 1874

F

Aug. 8, 1916

W

Sept. 3, 1918

D 1

May 31, 1921

D, L

Oct. 24, 1893

V

Jan. 13, 1914

0

Dec. 16, 1919

B

June 2, 1911

F2, II

Mar. 2, 1920

F

Nov. 9, 1920

B, K

June 19, 1888

S

July 12, 1887

F

Oct. 10, 1856

F

Mar. 29, 1921

F

Dec. 28, 1920

S

Feb. 15, 1916

F2, II

April 23, 1918

L

Mar. 22, 1892

B

Dec. 27, 1892

B

Oct. 24, 1893

F 2, 11

May 30, 1893 '

F

Nov. 3, 1914

A. P

Oct. 4, 1919

F

June 8, 1915

A, P

June 8, 1915

A. P

June 8, 1915

A, P

Oct. 17, 1876

I). 1

April 19, 1870

C

Nov. 6, 1917

B

June 5, 1917

B

Oct. 3, 1916

B

Jan. 9, 1917

I

Jan. 11, 1876

F 1. II

April 12, 1910

B

Oct. 30, 1866

F

May 14, 1918

B

Oct. 11. 1913

I) I

Sept. 9. 1919

K

April 20. 187.T

E 1

Dec. 24, 1918

I)

May 5, 1903

U

Sept. 8, 1891

F2, 11

June 13, 1S93

F2

Oct. 2, 1900

T

April 2, 1918

F

July 15. 1919

S

April 20, 1920

I)

Oct. 15. 191«

K 2

Nov. 12. 1872

("

Jan. 1. 1918

Q

Jan. 4. 1921

H

Oct. 4. 1921

B

June 10, 1862

M

May 10, 1864

V

June 14, 1864

M

Mar. 27, 1917

K 2. B

Feb. 12, 1918

K I

Nov. 5. 191H

M

Mov 30, 1882

F

Mur. 22. 1881

T

Fib. 8. 1881

K

May 19. 1903

K II

576

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Lockhart, Chas., and Grade, J 40,632

Lockhart & Grade 80,294

Loew, Oscar 101,284

Lofhjelm, Karl 546,018

Loftus, Robt. G 113,782

Lof tus, Robt. G 81,654

Loftus, Robt. G 43,157

Long, F. R 1,256,146

Loomis, C. C 1,280,612

Loomis, Wells, Hitchcock & Stryker 66,364

Looney, John J 139,009

Lorch, H. D 1,264,668

Lorraine, David G 1,396,860

Lessen, Clemens 537,121

Low, Frank S 1,192,653

Lowe, L. P., and Ruff, F. C 1,351,859

Lowe, W. P., and Bilfinger, C. W 556,155

Lucas, Owen D 1,168,404

Lucas, Owen D 1,183,091

Lugo, Orazio 51,843

Lugo, Orazio 60,757

Lugo, Orazio 58,113

Lugo, O., and Sehrade, T. O. L 60,396

Lupton, Geo 110,054

Lutz, H. E 240,914

Maag, G. C 1,142,525

McAfee, Aimer M 1,277,092

McAfee, A. M 1,099,096

McAfee, A. M 1,127,465

McAfee, A. M 1,144,304

McAfee, A. M 1,202,081

McAfee, A. M 1,277,329

McAfee, A. M 1,277,328

McAfee, A. M 1,235,523

McAfee, A. M 1,326,072

McAfee, A. M 1,326,073

McArthur, D. R 1,119,974

McAig, D. C 1,255,449

McCabe, J. R 1,376,713

McCarty, F 91,953

McCarty, Wm. F. M 1,274,912

McCarty, W. F. M 1,274,913

McCaskell, J. A 1,317,514

McComb, Wm. F 1,374,858

McComb, Wm. M 1,337,144

McCue, J. and W. B 21,143

McElrov, Karl P 1,259,757

McElroy, Karl P 1,259,758

McGinnis, Walter R . . .' 1.328,680

McGowan, Thompson 492,421

McGowan, T 454,061

McGowan, T 443,328

McGowan, T 658,857

McGowan, T 257,961

McGowan, T 431,386

McGowan, T 166,285

McGowan, T 492,419

McGowan & Van Syckel, S 154,700

McGowan & Van Syckel, S 156,229

McHenry, C. D 1,154,869

McKee, Ralph H 1,244,444

McKibben, Chas. W 1,327,835

McKibben, Chas. W 1,299,589

McKibben, Chas. W 1,299,590

McKissack, R. I 1,113,029

McManus, H 305,097

Date

Class

Nov. 17, 1863

F

July 28, 1868

F

Mar. 29, 1870

D 1

Sept. 10, 1895

F

April 18, 1871

D 1

Sept. 1, 1868

K2

June 14, 1864

I

Feb. 12, 1918

S

Oct. 1, 1918

L

July 2, 1867

M

May 20, 1873

D 1

April 30, 1918

F2, 5

Nov. 15, 1921

B-D-3

April 9, 1895

V

July 25, 1916

J, B

Sept. 7, 1920

B

Mar. 10, 1896

B

Jan. 18, 1916

B

May 16, 1916

B

Jan. 2, 1886

F 3

Jan. 1, 1867

V, D 1

Sept. 18, 1866

F 3, 4, I

Dec. 11, 1866

F 3, 4, I

Dec. 13, 1870

D

May 3, 1881

Fl, II

June 8, 1915

B

Aug. 27, 1918

C

June 2, 1914

B

Feb. 9, 1915

B

June 22, 1915

B

Oct. 24, 1916

B

Aug. 27, 1918

D

Aug. 27, 1818

D

July 31, 1917

B

Dec. 23, 1919

B

Dec. 23, 1919

B

Dec. 8, 1914

B

Feb. 5, 1918

S

May 3, 1921

B, P

June 29, 1869

F2, II

Aug. 6, 1918

B

Aug. 6, 1918

B

Sept. 30, 1919

W

April 12, 1921

B

April 13, 1920

B

Aug. 10, 1858

W

Mar. 19, 1918

K2, B

Mar. 19, 1918

K2

Jan. 20, 1920

K J

Feb. 28, 1893

F

June 16, 1891

F

Dec. 23, 1890

F

Oct. 2, 1900

V

May 16, 1882

F 3, D 1

July 1, 1880

F

Aug. 3, 1875

F2

Feb. 28, 1893

S

Sept. 1, 1874

S

Oct. 27, 1874

F 1

Sept. 28, 1915

B, K 1

Oct. 23, 1917

L

Jan. 13, 1920

A

April 8, 1919

A

April 8, 1919

A

Oct. 6, 1914

K 1

Sept. 16, 1884

I

KANSAS CITY TESTING LABORATORY

577

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME

Number

McMillan, F. M 215,471

McOmber, L. W 1,345,452

McSwinney, Daniel J 1,384,805

MacBeth, A 1,325,448

MacDougall, A J 1,381,319

Macalpine, Thos 655,500

Macalpine, Thos 686,663

Macalpine, Thos 684,813

Macalpine, Thos 741,517

Maitland, H. T 1,188,961

Maitland, H. T 1,272,979

Mann, F. W. . . .- 619,593

Mann, M. D 1,365,045

Mann & Chappcll, M. L 1,163,025

Mann & Chappell 1,183,094

Mann & Chappell 1,214,204

Mann & Chappell 1,249,444

Mann & Chappell 1,257,906

Mann, Matthew D., Jr 1,365,043

Mann, Matthew D, Jr 1,365,043

Mann, Stephen S 204,235

Mann, Stephen S 1^2,855

Mann & Williams ^'^^^'So^

Mansfield, David „°?'°°"

Marrin, Thos 211,762

Marrin, Thos 243,930

Martin, J. N 254,990

Martini, Dan ???'on?

Mason, Allan 444,203

Mason, Allan 444,202

Mason, F.B. ^'o^I'ot?

Mathieu, Jean A fli'^ll

Maybury, Wm ^37,756

Meeds, Wilber R lln'ifn

Meeds, W. R 250,830

Meigher, Jas. D 224,301

Mellen, G. H., and Hazelton, J. C 57,74 J

Mengel, Chas. C ]lt'^?ii

Mengel, C. C 465,703

Mengel.C.C 452,5/8

Meriam, J. B ^^'^46

Meredith, S , nkAt^

Merriam, E. S ^'^Sf'fill

Merrick, Thos. E rjlA^t

Merrill, Francis B wtrX

Merrill, Joshua •^'^•^^^

Merrill, Joshua

Merrill, Joshua

Merrill, Joshua

Merrill, Joshua

Merrill, Joshua

Merrill, Joshua . „,„ 07c

Merrill, Willis C 339 201

Meriz, Josef 1,282;906

Mesereau, G 1 308,802

Mesereau, G ' .^g ^^g

Meucci, Antonio 1,296:832

Midgely, T., Jr. ._. 1 327,247

W -, rto 00

32,951
32,706
32,704
32,705
90,284
43,325

1,178.532
205,407

Mieschke-Smith,
Mijs, Jan. . . .

Miles, George. ; 1,168.534

Miles, George w 77 n7fi

Miller, Jas .

77,070
1,359.614

Miller, Jas. Roys l'312!265

Miller, J. R '" 38'64l

Millochau, Adolph 37'918

Millochau, A

Date

May 20, 1879
July 6, 1920
July 19, 1921
Dec. 16, 1919
June 14, 1921
Aug. 7, 1900
Nov. 12, 1901
Dec. 25, 1900
Oct. 13, 1903
June 27, 1916
July 16, 1918
Feb. 14, 1899
Jan. 11, 1921
Dec. 7, 1915
May 16, 1916
Jan. 30, 1917
Dec. 11, 1917
Feb. 26, 1918
Jan. 11, 1921
Jan. 11, 1921
May 28, 1878
July 7, 1874
Jan. 11, 1921
June 26, 1866
Jan. 28, 1879
July 5, 1881
Mar. 14, 1882
June 30, 1908
Jan. 6, 1891
Jan. 6, 1891
Feb. 11, 1919
Nov. 29, 1887
Sept. 1, 1903
Oct. 31, 1882
Dec. 13, 1881
Feb. 10, 1880
Sept. 4, 1866 .
July 11. 1871
Dec. 22, 1891
May 19, 1892
Feb. 12, 1867
July 31, 1855
May 27, 1919
June 22, 1869
Mav 31, 1904
Dec. 17, 1861
July 30, 1861
July 2. 1861
July 2, 1861
July 2. 1861
May 18, 1869
June 28. 1864
Jan. 1, 1918
April 6. 1886
Oct. 29. 1918
July 8. 1919
Sopt. 9. 1862
Mar. 11. 1919
Jan. 6. 1920
April 11. 1916
Junp2r.. 1878
Jan. 18. 1916
April 21. 1868
Nov. 21, 1920
Aug. 5. 1919
May 19. 1863
Mar. 17, 1863

Class

C

B

M

H

D

D 1. 2

D 1,2

F 2, 5, 1

D

O, D

D 1

B

D

D

L

B

B

B

L

L

N

N

K. L

M

C

F

F

B, P

F 1,2, II

F 1,2,11

M

F 2, 5, II

F 1, 2. II

M

M

F 1

M

F

Fl,:

F3, '

C

W

J-K

O. D

F

S

S

S

D

n

F

1)

F, 3

F2.

<

K

D I

M

F

C

F. S

r

Ff..

o

B

D 1
D I

4. II

I
1

1.2
1

II

11

578

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Millochau, A 53,167

Millochau, A 46,923

Millochau, A 41,085

Millochau, A 49,777

Mills, E. N 1,007,788

Millspaugh, Pethuel 127,259

Mims, John C 713,475

Minshall, F. W 415,876

Mitchell, Willis 1,141,072

Montague, H. E 1,227,551

Moonev, L 1,174,888

Moore,"E. A 786,828

Moore, George H 586,520

Moore, E. S., and Thomas, H. H 1,281,808

Moore, J. B 1,130,318

Morehouse, C. L 55,426

Morehouse, C. L 174,921

Morfit, Clarence 66,243

Morris, W. L 1,137,075

Morris, W. L 1,305,735

Mott, Leander M 54,192

Mowbray, George M 25,575

Mueller, C. L. E 1,297,388

Mumford, Russell Wm 1,377,021

Munson, A. L 440,830

Murray, Thos. E 1,273,523

Murray, T. E., and Ricketts, E. B 1,293,866

Murray, T. E 1,302,200

Myers, Geo. W 147,783

Navin, F 1,312,266

Neahous, Herman 242,554

Neal, Stephens 1,036,306

Neilson, Albert 232,618

Nelson, John 1,391,568

Newton, Daniel L 1,330,490

Newton, D. F., and Anderson, N. H 1,376,631

Newton, D. L ". 1,356,878

Newall, Robert 53,656

Newsome, Thos. J 405,047

Nichols, H. M 1,302,832

Nichols, H. M 1,356,550

Nicholson, John 22,973

Nicolai, J. H. and W. F 224,037

Nicolai, Pierre 225,635

Nikiforoff, A 755,309

Noad, James 985,053

Nomi, Konosuke 1,386,945

Nordenson, Carl O 1,218,575

Norton, J. W., and Rouse, F. H 313,514

Norton & Rouse • 336,941

Noteman, Alonzo 512,894

Noyes, John E 82,151

Ogilvy, David J 1,268,142

O'Hara, Jas 22,573

Olsen, Geo 1,199,491

O'Neall, J. M 754,687

Opl, Karl l',128,494

Origet, Maurice 1,370,476

Paine, Henry M 9,119

Palmer, Chas. S 1,187,380

Palmer, Chas. S 1,268,763

Palmer, Chas. S 1,313,009

Paris, Augu.ste Jean, Jr 1,367,828

Parker, J. H 958,820

Date

Class

Mar. 13, 1866

F 1

Mar. 21, 1865

F 1

Jan. 5, 1864

D 1

Sept, 5, 1865

N

Nov. 7, 1911

Q

May 28, 1872

M

Nov. 11, 1902

D 1, E3

Nov. 26, 1889

F 2, 3, V

May 25, 1915

K 1

May 22, 1917

B

Mar. 7, 1916

R

April 11, 1905

A

July 13, 1897

V, Dl

Oct. 15, 1918

S

Mar. 2, 1915

B

June 5, 1866

D 1, C

Mar. 21, 1876

G

July 2, 1867

U

April 27, 1915

c

June 3, 1919

0

April 24, 1866

0

Sept. 27, 1859

F 1, 4, II

Mar. 18, 1919

M

May 3, 1921

0, P

Nov. 18. 1890

D

July 23, 1918

S

Feb. 11, 1919

F

April 29, 1919

S

Feb. 24, 1874

K2, S

Aug. 5, 1919

W

June 7, 1881

C

Aug. 20, 1912

F2

April 5, 1881

F

Sept. 20, 1921

B

Feb. 10, 1920

K

May 3, 1921

F

Oct. 26, 1920

K, J

April 3, 1866

V, D

June 11, 1889

A

May 6, 1919

S

Oct. 26, 1920

C

Feb. 15, 1859

w

Feb. 3, 1880

G, S

Mar. 16, 1880

F2

Mar. 22, 1904

B

Feb. 21, 1911

B, W

Aug. 9, 1921

F

Mar. 6, 1917

K 1

Mar. 10, 1885

S

Mar. 2, 1886

F2, 4, D 1

Jan. 16, 1894

D

Sept. 15, 1868

G, M

June 4, 1918

W

Jan. 11, 1859

K3

Sept. 26, 1916

J, A

Mar. 15,1904

F 1, 2 II

Feb. 16, 1915

C

Mar. 1, 1921

F

July 13, 1852

M

June 13, 1916

B

June 4, 1918

Kl

Aug. 12, 1919

B

Feb. 8, 1921

B

May 24, 1910

B

KANSAS CITY TESTING LABORATORY

579

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)—

Continued.

NAME Ntunber

Parker, R. B 1,252,481

Parker, W. C 169,189

Parker, W. M 1,226,990

Parsons, Chas. C 88,978

Parsons, C. Chauncey 93,739

Paisons, H. E 214,946

Pease, Fiancis S 226,187

Pemberton, Henry 24,952

Pennissat, Andre 204,244

Perkins, A. H 36,632

Perkins, George H 399,073

Perkins, Geo. H 240,923

Perkins, J., and Burnet, Wm. H 47,125

Perkins, W. D 731,943

Perrier, Odilon 544,516

Perrine, Robt. M 419,347

Peterson, F. P 1,031,664

Petroff, Grigoii 1,087,888

Petroff, G. 1,233,700

Petty, T. K., and Warden, W. G 37,263

Peucben, S. C 531,560

Pfieter, F 1,296,115

Pfiefer, F 1,296,116

PbilUp.A 1.286.091

Phillips, Joseph oofi'aTs

Pictet, Raoul P. ^'?8r'qm

Pielsticker, Carl M IS^Tco

Pielsticker, Carl M , ill'l.A

Pizel, Daniel ^'oo?'{o?

Pinckney, T. DeWitt ^ , ^21,421

Pine, J. A. W., and Ruggles, Wm. B 1'°^!'^^ '

Pinkham, C. W 34,772

Pitt, Wm. H 379,492

Pitt,Wm.H 411.394

Place, Chas. T .^ ^^^■?|?

Poisat, A. M., and Knab, D. C 7,124

Pollak, R. R ^'^li•V^l

Ponton. John IahiH

Poole, WiUard B • i'm7'l87

Forges, P., and Neumann, R I'Yic'^^s

Porter, Alonzo W Mt'lll

Poterie, George a^nlt

Pray. Lyman ■■■ "'"x"

Prentiss, E. F., and Robertson, R. A 48,435

Prentiss & Robertson ^'sloll

Price, C r sia iqi

Price, Walter B. . ■•••■■•••■ , ^TS'ogi

Price. W. B., and Dietz, Ernest - • 1.349.294

PriAardiGeo.I.:::: 1;264;«|

Prichard, G L • ■ ^ 339 973

Primose, John 478.265

Propfe. U . 297 j 53

Prutzman. Paul W 1 'sss'ssi

Prutzman, Paul W. .....•.■ • ^'•^•WTi2

Prutzman, Paul, and Goodwm, G. L J'nf, 094

Puening, Franz l'358'l74

Puening, Franz l'o4o',408

Pyzel, Dame 1 276,690

Puzel. Danie 1,383,024

Pyzel, Darnel

^ • ,_ TT D .. 1,382.234

Quinby, Henry R 31,998

Quinn. Abraham 36!481

Quinn, A

», ^», d .... 1,366,849

Ramage, Alexander b

Date

Jan. 8, 1918
Oct. 26, 1875
May 22, 1917
April 13, 1869
Aug. 17, 1869
April 29, 1879
AprU 6, 1880
Aug. 2, 1859
Mav 28, 1878
Oct. 7, 1862
Mai. 5, 1889
May 3, 1881
April 4, 1865
June 23, 1903
Aug. 13, 1895
Jan. 14, 1890
July 2, 1912
Feb. 17, 1914
July 17, 1917
Dec. 23, 1862
Dec. 25, 1894
Mar. 4. 1919
Mar. 4, 1919
Nov. 26. 1918
Jan. 18, 1870 <
June 5, 1917
Feb. 6. 1877
June 14. 1892
Aug. 19, 1913
Nov. 11, 1879
April 1. 1913
Mar. 25. 1862
Mar. 13, 1888
Sept. 17, 1889
June 21. 1881
Feb. 26. 1850
Jan. 22. 1918
July 13. 1875
May 18. 1920
Feb. 13, 1912
Jan. 27. 1874
June 2. 1891
Jan. 8. 1867
June 27. 1865
Mar. 8. 1864

July 16. li"«
Oct. 22. 1895
Aug. 10. 1920
June 26. 1894
ApiilliO. 1918
Jan. 7. 1919
Sept. 6. 1921
July 5, 1892
Nov. 15, 1921
Aug. 28. 1917
Dec. 13. 1921
Mar. 21, 1916
Nov. 9. 1920
Oct. 8. 1912
Aug. 20. 1918
June 28. 1921

June 21. 1921
April 9, 1861
Sept. 16, 1862

Jan. 18. 1921

II

2. n
II

Class

K2

O

B

F2. 5

C

F, K 2

N

W, I

I

T

F

S

F2,

F 1,

F 1,2

V. D

J. K2

I

D 1

S

P

K

K

Q

G. M

B

D 1

F2. II

C

N

E3

M.G

F.V.

F. V
F

F2.
A
N
B
C
G
W
S, F
l'

f;

F2.

I) 1

H

G. I> 1
F2. II
I

F

F I. II

D

A

F

K

B

C

S

F2

A P

K

F

I> :i

Ll-

II

II
4

2. S

580

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number Date

Rand, Alonzo C 62,362 Feb. 26, 1867

Rave, C has 425,905 April 15, 1890

Reese, Jacob 38,602 May 19, 1863

Reese, Jacob 150,614 May 5, 1874

Reeves, S. H 1,302,090 April 29, 1919

Reeves, W. P 1,283,559 Nov. 5, 1918

Reilly, P. C 1,310,164 July 15, 1919

Rensink, G. C 1,134,419 April 6, 1915

Requa, Chas. W 77,094 April 21, 1868

Restieux, Thos 63,749 April 9, 1867

Reynolds, F. R 1,119,453 Dec. 1, 1914

Rial, Wirt D 1,390,386 Sept. 13, 1921

Rice, L. M., and Adams, S. E 90,392 May 25, 1869

Richardson, Clifford 551,294 Dec. 10, 1895

Richardson, Wm. D 1,257,397 Feb. 26, 1918

Richardson, John E 65,275 May 28, 1867

Richter, Felix 1,098,763 June 2, 1914

Richter, Felix 1,098,764 June 2, 1914

Rites, F. M 1,167,021 Jan. 4, 1916

Rites, F. M 1,144,788 June 29, 1915

Rites, F. M 1,144,789 June 29, 1915

Rittman, Walter F 1,352,916-7 Sept. 14, 1920

Rittman, Walter F 1,330,008 Feb. 3, 1920

Rittman, Walter F 1,365,602 Jan. 11, 1921

Rittman, Walter F., and Dutton, Clarence

B 1,365,603 Jan. 11, 1921

Rittman, Walter F., and Dutton, Clarence

B 1,365,604 Jan. 11, 1921

Roberts, A. E., and Emery, A. L 1,016,958 Feb. 13, 1912

Robertson, J. H 1,238,339 Aug. 28, 1917

Robinson, Clarence 1 1,387,868 Aug. 16, 1921

Robinson, C.I 1,014,520 Jan. 9, 1912

Robinson, C.I 1,018,374 Feb. 20, 1912

Robinson, C. 1 968,692 Aug. 30, 1910

Robinson, C. 1 910,584 Jan. 26, 1909

Robinson, J. C 218,901 Aug. 26, 1879

Rodman, Hugh 1,209,336 Dec. 19, 1916

Rogers, Allen 1,378,424 May 17, 1921

Rogers, Davenport 211,055 Dec. 17, 1878

Rogers, D 284,331 Sept. 4, 1883

Rogers, F. M 1,299,385 April 1, 1919

Rogers, F. M., and Cooke, T. S 1,122,220 Dec. 22, 1914

Rogers, Henry H 120,539 Oct. 31, 1871

Rogers, John 50,276 Oct. 3, 1865

Rogers, Lebbeus H 1,269,747 June 18, 1918

Rogers, M.C 1,148,990 Aug. 3, 1915

Rogers, Wm. B 60,559 Dec. 18, 1866

Roots, James 340,522 April 20, 1886

Rose, H. C 182,775 Oct. 3, 1876

Rose, James R 1,252,033 Jan. 1, 1918

Rosen, Jean 1,165,909 Dec. 28, 1915

Rosen, Jean 1,162,654 Nov. 30, 1915

Rosenbaum, R. R 1,324,983 Dec. 16, 1919

Rosenbaum, R. R 1,332,359 Mar. 2, 1920

Rosenbaum, R. R 1,278,023 Sept. 3, 1918

Ross, S. J., and Schofield, H 1,204,492 Nov. 14, 1916

Roth, P., and Venturino, M. E 1,208,378 Dec. 12, 1916

Roth & Venturino 1,208,214 Dec. 12, 1916

Rcth & Venturino 1,208,378 Dec. 12, 1916

Rowlands, P. 0 1,252,955 Jan. 8, 1918

Rowsell, John 299,167 May 27, 1884

Rowsey, G. L 1,316,511 Sept. 16, 1919

Rudigier, Edw. A 1,386,077 Aug. 2, 1921

Ruff, F. C 1,263,289 April 16, 1918

Ruff, F. C 1,319,420 Oct. 21, 1919

Ruff, F. C 1,325,582 Dee. 23, 1919

Ryan, H. D 1,327,572 Jan. 6, 1920

3, A

Class

S
I. P

s
s

T

S

F, S

A

F 1, 2, I

V. D 1

F2

F

S

E

P

C

D

D

K 1, B

K 1, B

K 1, B

B

B

B

B

B

Q

B, P

D

I

Fl

D 1

V, D

F2, II

B

B

F2,

F

A

J

F

F

W

S

M

M, G

F 1, 2, II

B, K 1

O

B

B

E

C,

B

B

B

B

S

D

F

F

D

B

B

W

4,11

E 2

KANSAS CITY TESTING LABORATORY

581

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number Date Class

Ryder, Henry 142,515 Sept. 2, 18731 " F, S

Ryder, Watson 214,199 April 8, 1879 ..^, ] F 1, II

Ryder, W., and Qualey, J. A 739,757 Sept. 22, 1903 . F .i

Sabatier, P., and Malihe, A 1,124,333 Jan. 12, 1915 B, P

Sabatier, P., and Malihe, A 1,152,765 Sept. 7, 1915 B

Salathe, Frederick 452,764 May 19, 1891 T

Salathe, F 564,341 July 21, 1896 T

Sampson, C. E., and Woods, W 1,177,816 April 4, 1916 B

Sangster, W. H 54,414 May 1, 1866 S, D

Sangster, W. H., and Spencer, T. C 56,276 July 10, 1866 F

Sargent, Thos. D 20,587 June 15, 1858 W

Saunders, H. F., and Sutherland, L. T. . . . 1,362,355 Dec. 14, 1920 L

Savage, Wallace 1,279,918 Sept. 24, 1918 E 1

Sawyer, G. T., Rowland, W., Jr., and

Hatch, T. C 33,905 Dec. 10, 186' S

Saybolt, Geo. M 565,039 Aug. 4, 1896 D 1

Saybolt, G. M 989,927 April 18, 1911 J. K 2

Saybolt, G. M 218,066 July 29, 1879 N

Saybolt, G. M 245,658 Aug. 9, 1881 N

Schalk, Emil 146,405 Jan. 13, 1874 D

Schalk, Emil 133,598 Dec. 3, 1872 D, S

Schesch, H. A 54,218 April 24, 1866 F

Scheuffgen, Robert 1,118,9.52 Dec. 1, 1914 H

Schieffelin, S 1,381,936 June 21, 1921 W

Schildhaus, G., and Condrea, C 956,184 April 26, 1910 ' I

Schill, E 1,100,260 June 16, 1914 F, K 2

Schill, E 1,142,275 June 8, 1915 J, K 2

Schiller, Max 580,652 April 13, 1897 V

Schmidt, A. T 164,694 June 22, 1875 D

Schmidt, W. A., and Wolcott, E. R 1,307,930 June 24, 1919 B

Schubert, Julius 156,600 Nov. 3, 1874 A

Schwartz, Stephen 1,247,883 Nov. 27, 1917 B

Scott, John B 58,180 Sept, 18, 1866 M

Seeger, Robt 1,394,688 Oct. 25, 1921 B

Seeger, Robert 1,259,786 Mar. 19, 1918 B

Seely, E. D 57,390 Aug. 21, 1866 M

Seely C A 87,207 Feb. 23, 1869 F

Seibert, N. M., and Brady, J. D 1,290,369 Jan. 7, 1919 A

Seidenschur, F., and Dehnst, J 1,162,729 Nov. 30, 1915 B

Seigle A 567,751 Sept. 15, 1896 F 1, II

Seille' A 567,752 Sept. 15, 1896 F

Sellers, H. L., and Conyngton. H. R 549,499 Nov. 5, 1895 E3

Setzler, H.B 1,292,966 Jan. 28, 91? B

Sewell, B. F. Brooke 781,045 Jan. 31. 190d J

Sexton, Wm. A 1.248.730 ^ec. 4 1917 A

Seymour, M. J 306.965 Oct. 21, 884 A

ShantPr IS 61,474 Jan. 22, 1867 Fl.i.a

IKeVp t: ::.::;:::::;:::::: 1.352:265 Aug 31. mo r

Sharnlps P T 1,373,773 April 5, 1921 A

ShawFD .•.•:.:.■.. 1098 412 June 2, 1914 Kl

Shtw' G E 61.572 Jan. 29. 1867 N

Shaw GE 56,107 July 3. 1866 N

iheet's. EaH H.. '. ! i ! ! ! ! ! ! ! i ! ! 1.273,191 July 23. 1918 K 2. J

Shprman T. O 968.088 Aug. 23, 1910 H

iheSan; l! o! ! i ! 1 ! ! ! ! ! ! ! ! ! ! . ! 1.260,584 Mar. 26. 1918 B. J

iS-o'V^ ::::: ISill y:Al\\' nt

^^^"•■•■■•■■•••••■••■••■■::: i.Si K^M^ I

Shreves, F. (^ ,,^.p j^ ,S5fi ^

irrnYon^'^'aTt^r H:. " and Mantius. O. . ! ! 1,384:978 July 19 192. I

Sr^m'' A- '"' ''''""''• SS aS23:19!8 .

Slater, Wm. A to am Vah 97 l«K6 O

582

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number Date

Slocum, F. L., and Stutz, C. C 1,304,211 May 20, 1919

Slocum, F. L., and Stutz, C. C 1,304,212 May 20, 1919

Small, H. J., and Stillman, H 595,788 Dec. 21, 1897

Smedley, J. D 37,709 Feb. 17, 1863

Smith, A. D 1,239,423 Sept. 4, 1917

Smith, A. D 1,374,402 Apiil 12, 1921

Smith, A. D 1,324,075 Dec. 9, 1919

Smith, C. A 558,747 April 21, 1896

Smith, H. C 300,811 June 24, 1884

Smith, Hamilton L 60,585 Dec. 18, 1866

Smith, H. L 60,076 Nov. 27, 1866

Smith, H. J., and Jones, W 35,184 May 6, 1852

Smith, Rolin H 306,653 Oct. 14, 1884

Smith, Wm 23,719 April 19, 1859

Smith, Wm. A 596,437 Dec. 28, 1897

Smothers, H. F., and Norquist, E. E 1,261,337 May 14, 1918

Snee, J. A 1,165,458 Dec. 28, 1915

Snelling, Walter O 1,371,268 Mar. 15, 1921

Snelling, Walter O 1,056,845 Mar. 25, 1913

Snelling, Walter 0 1,186,855 June 13, 1916

Snelling, W. 0 1,215,732 Feb. 13, 1917

Snow, Wm. B 1.30,668 Aug. 20, 1872

Snow, Wm. B 137,496 April 1, 1873

Soderlund & Boberg 1,252,962 Jan. 18, 1918

Sommer, Adolph 525,696 Sept. 11, 1894

Sommer, Adolph 523,716 July 31, 1894

Southey. A. W 1,120,857 Dec. 15, 1914

Spangle, George W 58,905 Oct. 16, 1866

Spane, & Masland 695,123 Mar. 11, 1902

Spears, Wm 107,734 Sept. 27, 1870

Spier, Robert, and Mather, J 168,060 Sept. 21, 1875

Speller, F. N 774,341 Nov. 8, 1904

Squires, Frederick . 1,249,232 Dec. 5, 1917

Squire, F. B 197,197 Nov. 13, 1877

Stafford, Jas. B 10,813 April 25, 1854

Stapp, A. A 1,324,212-13 Dec. 9, 1919

Stanley, A. M 1,177,904 April 4, 1916

Starke, Eric A 597,920 Jan. 25, 1898

Starke, E. A 781,240 Jan. 31, 1905

Starke, E. A 913,780 Mar. 2, 1909

Starke, E. A 1,109,187 Sept. 1, 1914

Stearns, H. A 103,385 May 24, 1870

Steenbergh, B. Van 1,124,364 Jan. 12, 1915

Steinschneider, 1,302,988 May 6, 1919

Steinschneider, Leo 981,953 Jan. 17, 1919

Steinschneider, Leo 1,192,581 July 25, 1916

Stelwagon, W. H 503,996 Aug. 29, 1893

Stephens, Sam F 1,375,427 April 19, 1921

Stevens, E. W 1,374,199 April 5, 1921

Stevens, Levi 363,432 May 24, 1887

Stevens, Levi 414,601 Nov. 5, 1889

Stevens, Wm. H 1,165,462 Dec. 28, 1915

Stewart, John 24,587 June 28, 1859

Stewart, J. L 162,965 May 4, 1875

Stewart, J. L., and Logan, J. P 113,811 April 18, 1871

Stewart, J. L., and Dubler, J. B 136.557 Mar. 4. 1873

Stewart, Lyman 1,163,570 Dec. 7, 1915

Still, Carl ' 1,080,177 Dec. 2, 1913

Stombs, D. S., and Brace, J 27,842 April 10, 1860

Stone, C. W 1,070,555 Aug. 19, 1913

Stott, Chas 68,257 Aug. 19, 1867

Strache, H., and Forges, P 1,205,578 Nov. 21, 1916

Straight, Halver R 1,330,014 Feb. 3, 1920

Straight, H. R 1,323,204 Nov. 25, 1919

Strain, E. W 311,543 Feb. 3, 1885

Strather, W. P 1,326,618 Dec. 30, 1919

Street. G.E.J 695,123 Mar. 11, 1902

Class

B

B

D 1, F2

S

J, B

F, B

B

V, D

F, II
S

F2, 4, I

N

C

G, S
V

Q

K2

B

J, K, 2, B

Fl

V

S

S

F2

V

V

K 1

D

M

F, G

U

N

J, K2

N

U

B

Kl

Dl

E 3, B

D, F 2

D 1

F2, II

K 1, B

S

F 5

F5

S

B

B, P

F2

B

M

W

F2, II

F

S

B

S

G

A

F

B

W

W

F 1, 2, II

O

M

1,2

KANSAS CITY TESTING LABORATORY

583

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)—

Continued.

NAME Number

Stringfellow, John H. W 454,777

Stuber, John, Stuber, Jacob, and Mager,

John W 123,741

Stutz, C. C 1,359,931

Suckert, Julius 534,295

Suhr, C. L 1,122,169

Swan, O. C 1,250,526

Swan, O. C 1,284,945

Swaton, J. A 1,260,731

Sylvester, F 68,669

Symmes, H. K 26,000

Symonds, D 65,136

Symonds, D 65,137

Taber, Geo. H., Jr 1,363,487

Tagliabue, Chas. J 265,462

Tagliabue, Chas. J 254,176

Tagliabue, Chas. J 1,263,145

Tagliabue, Giuseppe 36,826

Tagliabue, Giuseppe ^^''*oI

Tagliabue, John 5M^S

Tait, A. H 96,997

Tait E.W 1,069,908

TaitiG.M.S 1-128,549

Tait, A. H., and Avis, J. W H'^^t

Tait & Avis 63,115

Tait & Avis 135,673

Tatro,Jos.A H'lf

Tatro, Jos. A , iS?'?^^

Taveau, Rene de M '^•^iMni

Taylor, H. K., and Graham, D. M ?1'2I?

Taylor & Graham ^.tv oqT

Tempere, Albert J , ,oI ocA

Testellin, A., and Renard, G I'i-o'^Kc

Theisen, Eduard t?o'1^c

Thiesen, Eduard ^fo'ot^

Thiele, Felix Co , olAlr

Thiele, Felix Carl ^'H^'^tn

Thirault, A .I'S^V

Thirault, A ilaLk

Thirault, A i78's8q

Thomas, John J iaoo^Q

Thomas, Joshua oTT'^qn

Thomas, Joshua iiVtlA

Thomas, Richard , oos Kn9

Thompson, N. W I'tnifivn

Thompson,W.P L. '^O'fgO

Thumm, Chas. F avj inn

Thurlow, E. W ' 3'067

Thursby, John. .^ 32V,465

Tiemann, Julius H 3.30 637

Tiemann J. H ■ ■ , o„o ,;,„;

Tienen, W. O. Th. van 201 91'!

Tilton, Ole l.lOS.'lW?

Timmons, J. K . .^q .^.nj

Timmons, and Swain, O 1*279 (ill

Timmons, J. R I^IS'ISI

Tokheim, J. J liooii'iu)

Travers, W. J .■.■;-.' o i T)2 'HO

Treneer, J. M., and Benjamin, C . b 2V''<).H1

Trewby, G. C, and Fenner, H. W ^ xvirzi

Trotter, Jas. Wilson 996,736

Trumble, Milton J j 349794

Trumble, M.J r,bo2'.47.t

Trumble, M.J I 070,361

Trumble, M. J i;i82,601

Trumble, M. J

Date
June 23, 1891

Feb. 13, 1872
Nov. 23, 1920
Feb. 19, 1895
Dec. 22, 1914
Dec. 18, 1917
Nov. 12, 1918
Mar. 26, 1918
Sept. 10, 1867
Nov. 1, 1859
May 28, 1867
May 28, 1867

Dec. 28, 192C
Oct. 3, 1882
Feb. 28, 1882
April 16, 1918
Oct. 28, 1862
May 5, 1863
Sept. 16, 1862
Nov. 16, 1869
Aug. 12, 1913
Feb. 16, 1915
Mar. 20, 1866
Mar. 19, 1867
Feb. 11, 1873
Feb. 8, 1870
Aug. 9, 1870
July 2. 1918
May 22. 1866
Nov. 20, 1866
Mar. 31, 1896
May 4, 1915
Dec. 31, 1896
Dec. 31, 1895
Sept. 24, 1901
Jan. 29, 1918
Jan. 8, 1867
Mar. 8, 1864
April 16, 1867
June 20. 1876
July 31, 1883
Mar. 24. 1885
Feb. 7. 1905
Mar. 25, 1919
Nov. 16. 1915
Sept. 25, 1888
June 8. 1920
May 2. 1843
Julv7, 1885
Nov. 17, 1885
Aug. 15. 1911
Nov. 12. 1878
July 28. 1914
April 11. 1916
Sept. 24.1918
Dec. 4. 1917
Sfpt.26. r.tii
Oct. 4. 1921
Jan. 31, 1882
May n. 1920
July 4, 1911
Aug. 17. 1920
Sept. 5. 1911
Aug. 12. 1913
May 9, 1916

Class
D

F 1.2. II

B

V

F2, II

A

S

B

A

G

V

V

K.J

F 1. 2. 3. 4, II

F 1.2, II

N

N

N

N

S

J, K2

K 1. B

F 2, 3, II

F 1

F2, II

D 1

D 1

I. E 1

1) 1

D 1

V, D

B

F

F

I) 1

L

F4,

II

F2

S

F, II

F2

S

S

B

F2. 1

W

M

D 1

D 1

I

F2. 4

F 1. II

Kl

A

A

A

I)

F2

H

S. F

H

Fl. II

F2. II

E 2, F i, U

584

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)—

Continued.

NAME Number Date Class

Tmmble, M. J 1,250,052 Dec. 11, 1917 F, S

Trumble, M.J 1,259,171 Mar. 12, 1918 F 2, A

Trumble, M. J 1,260,598 Mar. 26, 1918 F

Trumble, M.J 1,262,875 April 16, 1918 F

Trumble, M.J 1,269,134 June 11, 1918 K 2, S

Trumble, M.J 1,304,125 May 20, 1919 B

Trumble, M.J 1,304,124 May 20, 1919 A

Trumble, M.J 1,281,884 Oct. 15, 1918 B

Tschudy, Frederick 1,348,606 Aug. 3, 1920 F

Turner, C. W 1,046,683 Dec. 10, 1912 B

Turner, C.W 1,151,422 Aug. 24, 1915 B

Turner, R.D 194,275 Aug. 14, 1877 A, V

Turner, R. D 154,430 Aug. 25, 1874 A

Turner, R. D 156,899 Nov. 17, 1874 S, F

Tweedle, Herbert W. C 120,349 Oct. 24, 1871 D

Tweedle, Herbert W. C 189,401 April 10, 1877 T

Tweedle, Herbert W. C 189,402 April 10, 1877 T

Tweedle, Herbert W. C 45,363 Dec. 6, 1864 K 2

Tweedle, Herbert W. C 72,125 Dec. 10, 1867 F 2, 5, II

Tweedle, Herbert W. C 72,126 Dec. 10, 1867 F 2, 5, II

Tweedle, Herbert W. C 34,324 Feb. 4, 1862 G, F 2. 5. II

Tyler, Chas. N 38,015 Mar. 24, 1863 M

Ujhely, Heinrich 289,788 Dec. 4, 1883 D

Ujhely, H.. and Buerie, C 131,137 Sept. 3, 1872 C

Upham, Richard D 512,494 Jan. 9, 1894 E3

Van Devort, C, and Van Fleet, C 168,542 Oct. 5, 1875 F 2

Van Dyke, J., and Irish, Wm 1,095,438 May 5, 1914 B

Van Dyke & Irish 1,073,548 Sept. 16, 1913 B

Van Dyke & Irish 1,143,466 June 15, 191 B

Van Dyke & Irish 1,130,862 Mar. 9, 1915 B

Van Syckel, Samuel 191,203 May 22, 1877 F, II

Van Syckel, Samuel 140,801 July 15, 1873 F 2

Van Syckel, Samuel 152,440 June 23, 1874 F, II

Van Syckel, Samuel 126,503 May 7, 1872 S

Van Syckel, Samuel 154,772 Sept. 8, 1874 F, II

Van Syckel, Samuel 154,771 Sept. 8, 1874 U

Van Syckel, Samuel 143,945 Oct. 21, 1873 K 2

Van Syckel, Samuel 110,516 Dec. 27, 1870 F 2, I

Van Syckel. Samuel 191,204 May 22, 1877 F, II

Van Tine, Henry C 60,290 Dec. 4, 1886 D

Van Vliet, L., and O'Neill, F 1,094,762 April 28, 1914 K 1

Van Wyck, C. 1 27,603 Mar. 20, 1860 W

Van Wyck, William 65,313 May 28, 1867 S

Vander Weyde, Peter H 104,798 June 28, 1870 N

Vander Weyde, P. H 61,125 Jan. 8, 1867 A

Vander Weyde, P. H 58,005 Sept. 11, 1866 F 2, 4, 5, II

Vander Weyde, P. H 53,062 Mar. 6, 1866 F

Vaughan, Aaron C 53,709 April 3, 1866 G

Vaughan, John Ives 49,689 Aug. 29, 1865 F 1, 2, II

Van Boyen, Edgar 689,381 Dec. 24, 1901 C

Van Boyen, Edgar 690,693 Jan. 7, 1902 C

Von Groeling, A. J 1,295,088 Feb. 18, 1919 B

Von Groeling, A. J 1,327,184 Jan. 6, 1920 F

Von Groeling, A. J 1,378,066 May 17, 1921 F

Von Tilburg, F. E 1,326,230 Dec. 30, 1919 B

Vuilleumier, Rudolph 1,038,691 Sept. 17, 1912 K 1, B

Waddell, Alexander 1,249,864 Dec. 11, 1917 K 1

Wade, Henry Clay 1,336,450 April 13, 1920 B

Waitz, J. W 1,105,727 Aug. 4, 1914 J, K 2

Walker, Henry V 972,953 Oct. 18, 1910 D 1

Walker, H. V 955,372 April 19, 1910 V

Walker, W. E 1,037,280 June 17, 1919 L, K

Wallace, Geo. W 1,283,000 Oct. 29, 1918 W

Wallace, Geo. W 1,382,001 Oct. 29, 1918 F, W

KANSAS CITY TESTING LABORATORY 585

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number Date Class

Wallace, John Stewart, and Cowell, W. B . 716,132 Dec. 16, 1902 D

Warden, H. R 1,385,511 July 26, 1921 E

Warden, Henry 266,929 Oct. 31, 1882 C

Warden, Wm. G 240,937 May 3, 1881 S

Warden, Wm. G 240,036 May 3, 1881 S, D

Warden, Wm. G 110,806 Jan. 3, 1871 F 1, II

Warden, Wm. G 112,751 Mar. 14, 1871 F 1

Warfield, R. N 40,068 Sept. 22, 1863 V

Waring, Richard S 284,098 Aug. 28, 1883 T

Waring, Wilson 643,578 Feb. 13, 1900 I

Warren, Cyrus M 248,074 Oct. 11, 1881 T

Warren, Cvtus M 47,235 April 11, 1865 U

Warren, John 97,998 Dec. 14, 1869 F

Warren, John 102,186 April 19. 1870 S

Warren, John W 705,168 July 22, 1902 V

Warren, John W 666,446 Jan. 22 ISO! \

Warren M H 1,110,361 Sept. 15. 1912 B

Warth C H 1,131,880 Mar. 16, 1915 F 2, II, G

Washburn C H 1,138,266 May 4, 1915 B

Webster &Bo>-nton: I'^^l.^^O P^c- l^ ioln It t

Wehr.AustinA I'^'MI ?l^^ 99' n««fi n/

Weisenberger, P , °H?f ^l^o^m- P^

Weiser Josef 1,127,951 Feb. 9, 191o S

Weizmknn, C'has;, and Leff, D. A ^'^t^'^l^ V°\^' ^^3 k

Welles, Wm. C , 61,291 Jan lo, 186. , S

Wellman, Frank E J'?^2'?21 ?*PSn' iqln R

Wellman, Frank E J'^l^'f^^ ^^"'^ a 1^90 B

Wellman Frank E }'^^?'i^S ?^'=-, l*',\,^,^o B

Wellman Frank E VB^'ltl ^Sh fi' 9I0 B

Wellman, Frank E lH^'kfA Iw 27 1920 B

Wellman, Frank E HilHi Tu v 27 1920 B

Wellman, Frank E HIS iu v 27 1920 B

Wellman, Frank E HVA^ Aub 13 1918 B

Wel}man,F.E - .| ; fj Au^/.f ^917^ B. S

WeUman,F. E 1232 454 July 3, 1917 B

|S|;n:::::::::::::::;:;:::::::::: ,:,.,«. jun.|...- g ,

F E . ■ 1,350,482 Aug. 24, 1921

FE 877.620 Jan. 28. 1908

VYCiia. i.>.<.^ ii.<^iiv. 1 Q^7 Sfi.T Nov. 2, 19ZU A

Wells, Raymond ■; Iqtnd82 Aue 24 1926 O, C

Wells, W. C. and Wei s. F. E ^i^^ill tan 28 1908 F 1, 3, II

Wells. W. C, and Wells, F. E 877.620 Jan. z«. 1

Wells, W. C, and Wells, F. E 1.296.244 M^^'/g' ^^^ ^ C

Welsh M J U5M50 ^o^.^ ,-^,^,s Kl

Wemple, H. R fiis -107 Jan 24, 1899 C

Wendtland, August 618,307 |^"i\'i879 S

Weston, Elijah 'iq'Q78 Scot. 16, 1863 U

Wetmore, I. W • ■. , QOTRTfi Auit 16. 1921 B

Wheeler, MiUoughby MacBam 52477 Feb 6. 1866 S

Wheeler, Norman W Tcs'lOl Aue. 23. 1904 T

Whitall, Frank M 734 482 July 21. 1903 T

Whitall, Samuel 1 226'o41 Mav 16. 1917 B

White, Carter 622:936 April 11. 1890 S

Whitmg, Jas. R- • ■ • :, ^■■. 583 779 June 1, 1897 V

Whiting, J. R., and Lawrence, W. A ^12 375 Aug. 6. 1919 <>. S „

Whitman, J. C 1 125422 Jan 19. 1916 K 1. 11

Whitmore, Samuel W i;)76'l80 April 26. 1921 H.J'

Wickersham S9'607 AuR. 18. 1863 F 2

Wiegand, S. Lloyd 62'583 Mar. 6. 1867 <

Wiegand, S. Lloyd 63'777 April 9. 1867 M

Wiggins, Isaac B 23210 Mur. H. 1S69 M

Wilber, William 49*020 July 26. lHfi6 F

Wilcox, L. N M5'707 lu-c. 16. 1873 *'*

Wilkinson, Asa W.. 612'34S Jan. 9. 1894 K ;«

Wilkinson, Walter S 597 892 Jan. 26. 1 898 h •»

Wilkinson. Walter S 26*739 Jar. 3, 1860 ^.3

Willard, Franklin W '

586

BULLETIN NUMBER SIXTEEN OF

UNITED STATES PETROLEUM PATENTS (TO JANUARY, 1922)-

Continued.

NAME Number

Willard, Franklin W 27,503

Willard, Franklin W 27,327

Williams, R. A., and IJragg, J 304,390

Willis, Geo. M 918,628

Wilson, R.J 379,090

Wingett, John N 1,229,189

Wintz, Jas. P 807,983

Wirkner, George von 783,916

Wohle, Salo 1,081,801

Wolf, Herman 604,280

Wolf, Linus 1,265,573

Wolff, Albert 1,240,523

Wright, E. H., and Atwood, E. H 1,278,280

Wright, R. K 1,316,214

Wingett, J. N 1,384,878

Wynne, Edward W 901,411

Wynne, Edw. William 1,351,458

Yaley, Theodore E 1,329,450

Yaryan, Homer T 300,185

Yates, Robert 1,395,075

Young, Alex V 1,378,643

Young, W. H 62,798

Young, Wm. Herbert 1,378,307

Yunck, John A 1,345,656

Zerning, Herman 1,183,266

Zimmering, August F 313,795

Date

Class

Mar. 13, 1860

F

Feb. 28, 1860

G, S

Sept. 2, 1884

S

April 20, 1909

E 3

Mar. 6, 1888

F4

June 5, 1917

P

Dec. 19, 1905

D

Feb. 28, 1905

D 1

Dec. 16, 1913

Kl

May 17, 1898

D 1

May 7, 1918

K 1

Sept. 28, 1917

D

Sept. 10, 1918

F

Sept. 16, 1919

F

July 19, 1921

W

Oct. 20, 1908

D

Aug. 31, 1920

P, F

Feb. 3, 1920

B

June 10, 1884

F2, 5, II

Oct. 25, 1921

B

May 17, 1921

B

Mar. 12, 1867

O

May 17, 1921

B

July 6, 1920

B

May 16, 1916

J, K 2, B

Mar. 10, 1885

M

KANSAS CITY TESTING LABORATORY 587

BOOKS ON PETROLEUM, ASPHALT AND NATURAL GAS.

Abady — Gas Analyst's Manual $ 6.50

Abraham — Asphalts and Allied Substances 5.00

Aisinmann — Taschenbuch fur die Mineralol-Industrie. 8 vo.

Berlin, 1896

Alien — Modern Power Gas Producer 2.50

American Society for Testing Materials — 1921 Berky Standard.. 5.00
Archbutt and Deelev — Lubrication and Lubricants. 8 vo. Lon-
don, 1912... '.

Arnold & Darnell — Manual for the Oil and Gas Industry 2.50

Bacon and Hamor — The American Petroleum Industry 12.00

Baker — Roads and Pavements 5.00

Battle — Lubricating Engineer's Handbook 4.00

Battle — Indust'-ial Oil Engineering

Berlinerblau — Das Erdwachs, Ozokerit und Cerestin. 8 vo.

Brunswick, 1917

Booth— Liquid Fuel 3.00

Boo-man — Asphalts: Their Sources and Utilizations 2.60

Brannt — Petroleum: Its History, Origin, Occurrence, Produc-
tion, Physical and Chemical Constitution, Technology, Ex-
amination and Uses. Philadelphia and London, 1895

Butler — Oil Fuel: Its Supply, Composition and Application 2.25

Campbell — Petroleum Refining ' 8.50

Clowes and Redwood— The Detention and Measurement of In-
flammable Gas and Vapor in the Air. 8vo. London, 1916

Cooper-Kcv— Sto-aTC of Petroleum Spirit. London, 1914 _-.^^

Co -^te— Calorific Power of Gas 2.00

Cox— Field Methods J-""

Craig— Oil Finding ■- ^^Vm"; "■i"i.-"

Crew— A Practical Treatise on Petroleum. 8vo. Philadelphia,

1 QCY ■•

Danbv— Natu^'alRock Asphalts and Bitumens 2.50

Day— Handbook of the Petroleum Industry 1922 •■-■•••-- :

Delano-Twenty Years' Practical Experience of Na^ura^
Asphalt and Mineral Bitumen. 8vo. London and New
York. 1893 ., ,o

B™?4V%'e*r.'''Meurthe)-Le Petrole et ser Appl^ "

Paris, N. D - 3 00

Dowson and Larter— Producer Gas • ■

Dunn— Industrial Uses of Fuel Gas^ ..^ ^.--

EHis & Meigs- Gasoline and Other Motor Fuels ^, ^^^^

Emmons— Geology of Petroleum.. ,pf,

Franzsn- Exercises in Gas Analysis .,^1^

Frost— The Art of Roa^making. . . .^.^ , ,

Garfias— Petrol-um R?«ources of the World ^^^

of Application - ■ •■. 2.50

Gill—Short Handbook of Oil Analysis „j tupb 2.50

Gre-orius-Minerai Waxes: Preparation and Uses...

Hager— Oil Field Motors ;i 00

Hager— Practical Oil Geology

588 BULLETIN NUMBER SIXTEEN OF

BOOKS ON PETROLEUM, ASPHALT AND NATURAL GAS—

Continued.

Hamor & Padgett — Examination of Petroleum $ 6.00

Hempel — Methods of Gas Analysis 2.25

Hicks— Laboratory Book of Mineral Oil Testing 1.00

Hofer — Das Erdol (Petroleum) und Steine Verwandten. Bruns-
wick, 1888

Holde-Muller — Examination of Hydrocarbon Oils 5.00

Hubbard — Laboratory Manual cf Bituminous Materials

Hubbard — Dust Preventives and Road Binders 3.00

Jaccard — Le Petrole, L'Asphalte, et le Bitume au Point de vue

Gcologigue. Paris, 1895

Guttentag, W. E. — Petrol and Petroleum Spirits, Sources, Prep-
aration, Examination, Uses 3.40

Johnson and Huntley — Principles of Oil and Gas Production.... 4.50
Judson — City Roads and Pavements 2.00

Road Preservation and Dust Prevention 1.50

King-Knight Co. — Oil Flow in Pipe Lines (San Francisco) 3.00

Lewes — Liquid and Gaseous Fuels 2.00

Lunge — Technical Gas Analysis 4.00

Marvin — The Petroleum Industry of Southern Russia. 4to.

London, 1884

The Region of the Eternal Fire; An Account of a Journey
to the Petroleum Region of the Caspian in 1883. 8vo.
London, 1884

The Petroleum of the Future. Baku, the Petrolia of Eu-
rope. 8vo. London, 1883..

The Moloch of Paraffin. 8vo. London, 1886

The Coming Deluge of Russian Petroleum, and its Bearings

on British Trade. 1887

England As a Petroleum Power, or the Petroleum Fields

of the British Empii-e. London, 1887

Our Unappreciated Petroleum Empire. 8vo. London, 1889

The Coming Oil Age: Petroleum — Past, Present, and Fu-
ture. 8vo. London, 1889

Mills — Destructive Distillation: A Manualette of the Paraffin,

Coal-Tar. Rosin Oil, Petroleum, and Kindred Industries.

London, 1887

Neuberger — Technology of Petroleum 9.00

Neuberger and Noalhat — Technology of Petroleum. Paris 10.00

North-Oil Fuel 2.00

Paine and Stroud — Oil Production Methods 3.00

Panvity — Prospecting for Oil and Gas 3.25

Ppckham — Solid Bitumens 5.00

Pforzheimer & Co., 25 Broad St., New York City — Independent

Oil Stocks, 1921

Pogue — Economics of Petroleum, 1921 6.00

Redwood — Mineral Oils and Their By-Products 5.40

Petroleum and Its Products. (3 vol.) 13.50

Redwood and Eastlake — Petroleum Technologist's Pocketbook.... 3.00
Richardson — Asphalt Construction for Pavements and High-
ways -v 2.00

KANSAS CITY TESTING LABORATORY 589

BOOKS ON PETROLEUM, ASPHALT AND NATURAL GAS—

Continued.

Riche-Halphin — Le Petrole. Paris. 1896 $

Richardson — The Modern Asphalt Pavement 3.00

Ries- — Economic Geology 5.00

Singer — Beitrage zur Theorie der Petroleum-bildung. Zurich,

1892

Southcombe — Chemistry of the Oil Industries 3.00

Sur — Oil Prospecting and Extraction 1.00

Tecklenburg — Handbuch der Tiefbohrkunde. 6 Bde. Leipzig,

1886-1896

Thompson— Oil Fields of Russia. London, 1908 7.50

Petroleum Mining and Oil Field Development 5.00

Thomson and Redwood — Handbook on Petroleum 2.70

Tillson — Street Pavements and Paving Material 4.00

Tinkler and Challenger — The Chemistry of Petroleum and Its

Substitutes 4.50

Tower— The Story of Oils 1-00

Yieth — Das Erdol und seine Verarbeitung. Brunswick, 1892

Warner — Field Mapping for the Oil Geologist 2.50

Westcott— The Handbook of Casinghead Gas 4.00

Westcott — Handbook of Natural Gas ^

Whinery— Specifications for Street Roadway Pavemetlts 1.00

Ziegler— Popular Oil Geology 3.00

U. S. Government Publications on Petroleum, Asphalt

and Natural Gas.
BUREAU OF MINES TECHNICAL PAPERS.

No. 10. Liquified products from natural gas, their properties and

No. 25. Methods for determination of water in petroleum and its

products.
No 26 Sulphur content of fuel oils.
No! 32. Cementing process of excluding water from oil wells as

practiced in California. „ , , .., »„

No 36 Preparation of specifications for petroleum products.
No 37. Fuel oil for internal combustion engines.
No'. 38. Prevention of waste of natural gas. ,.-,.„•

No 42 Prevention of waste of oil and gas in Cahfoi ma.

No! 43! Influence of inert ga.^es on explosive '""^tures.

No. 45. Waste of oil and gas in Mid-Continent fiel.l.

No. 49. Flash point of oil.

No 51. Causes of decline of oil wells.

No 57. Petroleum and gas in Wyoming.

No. 66. Mud laden fluids in well driliing.

No! 68. Mud laden fluid in well drilling in Oklahoma.

No 70 Oil recovery in California

No' 72 Problems of petroleum nuiustry.

Mn 74 Properties of California petroleum.

No! 79. ElecTric lights for use about oil an.! gas woll«.

590 BULLETIN NUMBER SIXTEEN OF

Method of tssting natural gas for gasoline content.

Fractional distillation of natural gas at low temperature.

Composition of natural gas in 25 cities.

Explosibility of acetylene.

Inflammability of gasoline and air mixtures.

Explosions of gasoline in sewers.

Limits of inflammability of mixtures of methane and air.

Bibliography of gas manufacture.

Conditions of explosibility of methane air mixtures.

Hazard in handling gasoline.

Underground waste in oil and gas fields.

Compi'essibility of natural gas.

Oil products of carbonization of coal.

Vapor pressures of various hydrocarbons at low tempera-
tures.

Nitration of toluene.

Absorption of gases by coal.

Inflammability of mine gases.

Compression and composition of natural gas.

Construction of single tube cracking furnaces for making
gasoline.

Properties of commercial gasoline sold during 1915.

Methods of testing and properties of motor gasoline.

Recent developments in the absorption process for recover-
ing gasoline from natural gas.

Determination of unsaturated hydrocarbons in gasoline.

Oily or volatile matter in coal.

BUREAU OF MINES BULLETINS.

Physical and chemical properties of the petroleum of the
San Joaquin Valley, Calif.

Commercial deductions from comparisons of gasoline and
alcohol tests en internal-combustion engines.

Comparative fuel values of gasoline and denatured alcohol
in internal combustion engines.

Oil and gas wells through workable coal beds.

The condensation of gasoline from natural gas.

Manufacture of gasoline and benzene-toluene from petro-
leum and other hydrocarbons.

The analytical distillation of petroleum.

Extraction of gasoline from natural gas by absorption
methods.

The use of mud-laden fluid in oil and gas wells.

Methods for increasing the recovery of oil from wells.

Compression plants for extracting gasoline from natural
gas.

Oil storage tanks and reservoirs.

Cost accounting for oil producers.

Petroleum laws.

No.

87.

No.

104.

No.

109.

No.

112.

No.

115.

No.

117.

No.

119.

No.

120.

No.

121.

No.

127.

No.

1.30.

No.

131.

No.

140.

No.

142.

No.

146.

No.

147.

No.

150.

No.

158.

No.

161.

No.

163.

No.

166.

No.

176.

No.

181.

No.

183.

No.

19.

No.

32.

No.

43.

No.
No.

No.

65.

88.
144.

No.
No.

125.
120.

No.
No.
No.

134.
148.
151.

No.
No.
No.

155.
158.
206.

KANSAS CITY TESTING LABORATORY 591

BUREAU OF STANDARDS.

Action of sunlight and air upon some lubricating oils. 1911. (Stand-
ards Reprint 153.) 5c.

Behavior of high-boiling mineral oils on heating in air. 1911. (Stand-
ards Reprint 160.) 5c.

Data on oxidation of automobile cylinder oils. 1916. (Standards
Technologic Papers 73.) 5c.

Density and thermal expansion of American petroleum oils. 1916.
(Standards Technologic Papers 77.) 10c.

Effect of adding fatty and other oils upon carbonization of mineral
lubricating oils. 1911. (Standards Technologic Papers 4.) 5c.

Evaporation test for mineral lubricating and transformer oils. 1913.
(Standards Technologic Papers 13.) 5c.

Fluorescent test for mineral and rosin oils. 1911. (Chemistry Cir-
cular 84.) 5c.

Iodine number of linseed and petroleum oils. 1914. (Standards Tech-
nologic Papers 37.) 10c.

Modification of Herzfeld-Bohme method for detection of mineral oil in
other oils. 1912. (Chemistry Circular 85.) 5c.

Oil films on water and on mercury. (In Smithsoniaia Report 1913,
pages 261-273, illus.) Cloth $1.10.

United States standard tables for petroleum oils. 1916. (Standards
Circular 57.) 15c.

Determination of ammonia in illuminating gas. 1914. (Standards
Technologic Papers 34.) 10c.

Determination of sulphur in illuminating gas. 1913. (Standards
Technologic Papers 20.) 10c. .o. j ^

Industrial gas calorimetry. 1914. 150 pages illus. (Standards
Technologic Papers 36.) 40c.

Lead acetate test for hydrogen sulphide in gas. 1914. 46 pages, illus.
(Standards Technologic Papers 41.) 25c. ,„, , . rp u

Legal specifications for illuminating gas. 1913. (Standards Tech-
nologic Papers 14.) 10c. o t^ ^nr \ r,^

London sliding scale for gas. 1909. (60th Congress, S Doc. 696 ) 5c.

On definition of ideal gas. 1910. (Standards Reprint 136 ) oc.

Standard methods of gis testing. 1917. 202 pages, illus. (Standards

Standa?d"s fo/gi st?vice. 3d edition. 1915. 197 pages. (Standard.s

^'""'Supeifedes^^^t edition with title, "State and municipal regu-
lations fo\ gas," and 2d edition entitled, "Standard reguh.t.ons
for manufactured gas and gas service."

U. S. GEOLOGIC SURVEY.

Annual Reports of Geological Survey. 22d. 1901. Part 1 ^j^^^^^^
RepoH and paper on asphalt and bituminous rock depositn. 464

Bu1iS'no''!1S: "StiiiliSn of crude petroleum by capillary dif-
fusion. 1908. 10c,

592 BULLETIN NUMBER SIXTEEN OF

Bulletin No. 392. Commercial deductions from comparisons of gaso-
line and alcohol tests on internal-combustion engines. 1909. 5c.

Bulletin No. 401. Relations between local magnetic disturbances and
genesis of petroleum. 1909. 24 pages, map. 5c.

Bulletin No. 475. Diffusion of crude petroleum through fuller's
earth with notes on its geologic significance. 1911. 5c.

Bulletin No. 653. Chemical relations of oil-field waters in San
Joaquin Valley, California. 1917. 119 pages, illus. 10c.

Water Supply Papers 113. Disposal of strawboard and oil-well
wastes. 1905. 5c.

Mineral Resources of U. S. — Non-metals. Part II (yearly).

Asphalt and Bituminous rock deposits of United States. (In Geo-
logical Report 1901, pt. 1, t)p. 209-452, 52 plates, illus. maps.)
Cloth, $1.60.

Asphaltum deposits of California. (In Mineral Resources, 1883-4, pp.
938-948.) Cloth, 60c.

Asphaltum, production, importation, commercial applications, history
of paving industry, etc. (In Mineral Resources, 1893, pp. 627-
669.) Cloth, 50c.

AGRICULTURAL DEPARTMENT.

Effect of controllable variables upon penetration test for asphalts
and asphalt cements. (In Journal of Agricultural Research, Jan.
24, 1916, pp. 805-818.) 10c.

Bitumens and their essential constituents for road construction and
maintenance. 1911. (Roads Circular 93.) 5c.

Methods for examination of bituminous road materials. 1915. (Agri-
cultural Bulletin No. 314.) 10c.

Macadam roads. Construction of macadam roads. 1907. (Roads
Bulletin No. 29.) 10c.

Macadam Roads. 1908. (Farmer's Bulletin No. 338.) 5c.

Use of mineral oil in road improvement. (In Agricultural Yearbook,
1902, pp. 439-454, illus.) Cloth, 85c.

SMITHSONIAN INSTITUTION— U. S. NATIONAL MUSEUM.

Bulletin No. 102, part 6. Petroleum. A resource interpretation.

PETROLEUM TRADE JOURNALS.

Published at

California Derrick San Francisco, Calif.

The California Oil World Bakersfield, Calif.

Coalinga Oil Record Coalinga, Calif.

Gulf Coast Oil News Houston, Texas

Journal du Petrole Paris

National Petroleum News Cleveland, Ohio

Natural Gas and Gasoline Journal New York

Mining and Oil Bulletin San Francisco

KANSAS CITY TESTING LABORATORY 593

PETROLEUM TRADE JOURNALS— Continued.

Oil Weekly : Houston, Tex.

Oil News Xhicago, 111.

Oil Age Los Angeles, Cal.

Journal Inst. Pet. Technologists

Oil Trade Journal New York

Oil City Derrick Oil City, Pa.

Oil & Gas Journal (The Oil Investors' Journal). .Tulsa, Okla.

Oil and Gas News Kansas City, Mo.

Oildom New York City, N. Y.

The Oil Industry Los Angeles, Calif.

Oil News London, Chicago

Petroleum Reporter New York

International Petroleum Refiner Kansas City, Mo.

Petroleum Age Chicago, 111.

The Petroleum Gazette TitusviUe, Pa.

The Petroleum Review London

The Petroleum World — PetroleumTimes London

Journal of Gas Lighting Chicago, 111.

Gas Record ^'''^^f^' Fn: xt v

Gas Engineering New \ork City, N. Y.

IMPORTANT SCIENTIFIC JOURNALS AND SOCIETY PUBLICA-
TIONS.

(With articles on Petroleum, Asphalt and Natural Gas.)
Chemical Abstracts of American Chemical

Society Easton, Pa.

Journal of Industriai'andEngineering Chemistry.New York City, N. Y.

Journal of American Chemical Society Easton, Pa.

Chemical and Metallurgical Engineering New York L ty, IN. x.

Engineering and Mining Journal New \ork C ty. N. Y.

Engineering News Record rvr": J^ew York City, N. Y.

Journal of the Society of Chemical Industry Lonflon

American Society for Testing Materials Philadelphia, Pa.

Journal of the Franklin Institute puM^Hplnhia Pa

International Society for Testmg Materials P'^i^i'^Pj pWv N Y

Institute of Mining Engineers New York Mty, i>. i.

State Geological Survey Publications on Petroleum.

Asphalt and Natural Gas.

ALABAMA.

Circular No. 3. Concerning oil and gas in Alabama, by E. A. Smith.
Bulletin No. 10. The Fayette Gas Field.
Bulletins Nos. 20. 22, 23, 28, 31. 33, 35.

CALIFORNIA.
Petroleum Resources of California.

KANSAS.

Vol IX Oil and Gas. . ^.

Bulletin' No. 3. Oil and Gas Resources of Kansas.

KENTUCKY.
Vol. I. Series V, No. 1. Oil and Gas

594 BULLETIN NUMBER SIXTEEN OF

MICHIGAN.

Publication No. 14, Series No. 11. Occurrence of oil and gas in Mich-
igan.
Publication No. 19, Series No. 16.

MINNESOTA.
Bulletin No. 5, 1889. Natural Gas in Minnesota. N. H. Winchell.
39 p.

MISSISSIPPI.
No. 15. Oil and Gas Prospecting in Mississippi. By E. N. Lowe.

MISSOURI.

Vol. Ill, No. 4. Missouri School of Mines — Production of Oils and
Tars from Bituminous Materials.

NEBRASKA.

Vol. 4, Part 25. Natural Fuels of Nebraska.

NEW YORK.

Vol. 6, No. 30. Petroleum and Natural Gas in New York, by Edward
Orton.

OHIO. .
Bulletin No. 1. Oil and Gas.
A New Geological Map of Ohio.
Bulletin No. 12. The Bremen Oil Field.
Vol. VI. Geology and Petroleum and Natural Gas.

OKLAHOMA.
Circular No. 8. Methods of exploring for oil and gas.
Handbook of Natural Resources of Oklahoma.
Bulletin No. 2. Rock Asphalt, Asphaltite, Petroleum, Natural Gas

Asphalt in Oklahoma.

Costs of drilling oil and gas wells.

Correlation of the oil sands in Oklahoma.

Rock asphalts of Oklahoma and their use in paving.

Ponca City Oil and Gas fields.

Cushing Oil fields.

Part I, 1915. Petroleum and Natural Gas.

Part II, 1917. Petroleum and Natural Gas.
PENNSYLVANIA.

Reports I, 12, 13, 14 and J. Bituminous coal fields.

Report L for the Pittsburgh gas well and the use of gas in iron
manufacture.

Reports Q, Q2, Q3 and Q4 for reference to oil rocks in Beaver, Law-
rence, Mercer, Crawford, Erie and S. Butler Counties.

Report K for the Dunkard Creek oil wells of Green County.

Reports R, R2 for description of oil rocks in McKean, Elk and Forest
County.

Reports V. V2 for notes on the oil rocks of N. Butler and Clarion
County.

Report H2' for oil boring at Cherry Tree, Cambria County.

Report G5 for oil boring in Wayne County.

Annual Report, 1885, for report of the progress in oil and gas region,
with special facts relating to the geology and physics of natural
gas.

Grand Atlas Div. Ill, Part I, under Bituminous Coal Fields.

Annual Reports, 1886, Part IL

in Oklahoma

Bulletin No.

14.

Circular No.

7.

Circular No.

5.

Bulletin No.

16.

Bulletin No.

18.

Bulletin No.

19.

KANSAS CITY TESTING LABORATORY 595

SOUTH DAKOTA.

Circular No. 4. Possibilities of oil and gas in Harding County
Circular No. 1. Oil in South Dakota.

TENNESSEE.
Vol. II. No. 2, No. 7.

Vol. V. No. 4.

Vol. VI. No. 1.
Vol. VII. No. 1, No. 4.
Vol. VIII. No. 3.

TEXAS.

Texas University Bulletin 246. Geology of Oil and Gas fields of

Wichita and Clay Counties.
Texas University Bulletin No. 66. Thrall Oil field.
Texas University Bulletin No. 44. Review of Geology of Texas.

WEST VIRGINIA.

Coal, oil, gas, limestone and iron ore map.

Vol. I. Petroleum and Natural Gas, levels and true meridians.

Vol. la. Petroleum and Natural Gas.

WYOMING.

Bulletin No. 2. The Lander Oil Fields.

Bulletin No. 14. The Byron Oil Fields.

Bulletin No. 15. The Oregon Basin Oil and Gas Fields.

LIST OF STATE GEOLOGISTS.

Eugene A. Smith, University. Ala. II. \V. Ellis, Alhiiquci-iiue. New Mex.

N. F. Drake, Favetteville, Arlv. .7. M. Clarke, .Mbany. N. Y.

R. D. George, Boulder, Colo. .1. H. Pratt, Chapel Hill. N. C.

H. E. Gregory, New Haven. Conn. A. G. Leonard, Grand Forks. N. D.

E. H. Sellards, Tallahassee, Fla. .1. A. Bovvnooker, Coluniliu.s. Ohio.
S. W. McCallie, Atlanta, Ga. C. W. Shannon, Nornuin. (»kla.

F. W. DeWolf, Urbana, 111. U. H Hice. Beaver, Fa.
Edward Barrett, Indianapolis, Ind. C. W. Brown. Providence. U. I.
Geo. F. Kav, Iowa City, Iowa. Stephen Taber, Columbia S. C.
Raymond Moore, Lawrence. Kans. Freemen Ward, Vermillion, S. I)nk.
J. E. Barton, Louisville. Ky. W. A. Nelson. Nashville. Tcnn.

E. B. Mathews, Baltimore, Md. J. A. Uden. Austin, Texas

R. C. Allen, Lansing, Mich. G. H. Perkins, Bnrlln>;t(>n, Vt

W. H. Emmons, Minneapolis, Minn. Tlios. L, Watson, CliMrlol t.'svllle, \ a.

E. N. Lowe, Jackson, Miss. Henry Landes. Seattle, Wash.

H. A. Buehler, Rolla. Mo. I. C. White. Mor>;antown, ^^•.^»•

E. H. Barbour. Lincoln, Neb. AV. O. Hotehkiss. .Madison. \\ l.-c.

H. B. Kummel, Trenton. N. J. L. W. Trumbull. Cheyenne. \\ yo.

596 BULLETIN NUMBER SIXTEEN OF

Index

Page

Abel-Pensky Tester 476

Abel tester 476

Absorption

Method for testing natural and casinghead gas 512

Oil, specifications for 271-2

Gasoline by absorption process 399

Capacity of absorption towers 401

Charcoal absorption process 401

Literature on absorption process 589-590

Relation of gasoline in natural gas by absorption, compression and specific gravity 402a

Acetylene

Explosibility of 404

Heat of combustion of 340, 409

Acid

Tables of properties of sulphuric acid 547-9

Treat menl of benzine with acid 191, 199, 201

Treatment of lubricants with acid 195

Determination of free acids in oils 495

Determination of combined acid in oils 496

Sludge acid 195, 562

Fummg sulphuric or Nordhausen 199

Aeroplanes

Specifications for fighting grade of gasoline for 255

Specification for domestic grade of gasoline for 255-6

Specifications for lubricating oil for aeroplane engines 292

Specifications for aero machine gun oil 286

Africa, oil in 11

Aggregates

Calculation of voids in mineral aggregates 377

Mineral aggregates in asphalt pavements 376-392

Methods of grading mineral aggregates 506-7-8

Agitators and agitation 192

Cost, weight, capacity and dimensions of agitators 246

Air

Specific heat of 346

Air blowing of asphalt 368, 375

Furnace heat losses due to excess of air 337

Required for combustion of fuel oil 326, 334, 336

Air compressor oil definition of 305

Alabama, inspection laws and taxes of 259

Albert! te, properties of 380

Aluminum chloride

In production of gasoline , 230

Yields of gasoline from aluminum chloride treatment 230

Properties of aluminum chloride gasoline 231,2,3

American Society for Testing Materials closed tester 467, 471-2

Ammonia

From oil shale 354

Melting point and heat of fusion of 343

Heat of vaporization of 344

Specific heat of 345,6

From coal ' 361, 2

Ammonia compressor lubricant, definition of 305

Analyses

Outline of methods 425,6,7

Index to application of methods 427

Dielectric value or breakdown of transformer oils 309

Specific gravity 428-436

Color 437-442

Odor 442

Transparency 442

Viscosity 443-453

Melting point 454-459

Cold, pour and flow test 460, 1

Water and B. S 462

Distillation tests 463-470

Flash and burning points 472-476

Pressure-heat tests 477-9

Carbon test s 480-1

KANSAS CITY TESTING LABORATORY 597

Emulsification 4g2

Heat of combustion 483-4-5

Sulphur 486-490

Ultimate analysis 491

Doctor test 492

Olefins 493

Aromatics 494

Acid '..'.... '.\'.'.'.'.'.'.'.'.'.'.'.'.'.'.'. 495-6

h loc test . 49g

Corrosion and gumming [ _ 497

Penetration of asphalt ] 497, 8

Ductility 499

Loss by evaporation 500

Asphaltic conte nt 501

Solubility 502-3

Oxidation value 504

Wax 505

Bitumen and grading 506-7

Cementing strength 508

Gas gravity by effusion 509-10-11

Gasoline in gas. 512-13

Chemical analysis of gas 514-16

Heat of combustion of gas 517-8

Anthracite coal, properties of 381

Anticlines, diagram showing accumulation of oil and gas in 18, 20, 21, 22.

Areas

Heating area of stills 226

Heating area of cracking tubes per gallon of gasoline 226

Condensing areas for gasoline and kerosene 228

And surfaces, conversion factors for units of 554

Argentina, production of petroleum in 4,11

Arizona, inspection laws and taxes of *■. 259

Arkansas

Inspection I aws and taxes of 259

Properties of crude oil from ^°'

Aromatic ,„_

Or benzine hydrocarbons, definition of • \^

Or paraflfin hydrocarbons in petroleum hydrocarbons, method of determining .... IH^

Hydrocarbons, calculated amount of by distillation , ; • ■ }ai

1, method of determining ash in asphalt, oil and bituminous materials 4B1

And asphaltic materials lai' 9

In crude petroleum • .16-4S

Prices '.,k- ii

of ib<-»

D , °' 368-391

Pavements .jga

Method of production of blown asphalts :^y^

Air required for blowing asphalt ".j^tj

Composition of natural asphalts :^^-^

Composition of oil asphalts :y;;,

Composition of blown asphalts '■^~'^^

Composition of rock asphalt "•,-„

Properties of sheet asphalt pavement '.j-|

Composition of various types of asphalt pavements • _.

Efifect of mineral filler on penetration of asphaltic cement ^^1

Fluxing of hard asphalt 37I

Material required for asphaltic concrete. . . . . ..... ■ :-.---..\;j Iir.!

Relation of defects of an asphalt pavement to its physical properties .^ .;.

Various const ituents of asphaltic surface mixture 373 4

S^'Sn^il^n'or ^tJ^tion to melting point of asphalt produced hy «ir ,^^^

blowing • • • ■. : .(71

Purposes of specifications for an asphaltic "'"X;,,;- Vnn^rVto -i^^

ciat'.on , i.' i.-' ' ' ' ' '^ '

Characteristics of typical blown petroleum asphalts

Cross Section of sheet asphalt

Method of determining fi'ted carbon and ash in asph.i^^^ ,„,

Method of determining specific gravity of asphaltic cimen

598 BULLETIN NUMBER SIXTEEN OF

Page

Method of determining melting point of bituminous or asphaltic material by ring

and ball method 454

Method of determining melting pwinl of bituminous or asphaltic material by cube

method 455

Method of determining melting point of bituminous or asphaltic material by

General Electric method 456

Determmation of nitrogen in asphalt by Kjeldahl method 492

Method of making penetration tests of 497-8

Method of making ductility tests of 499

Method of determining amount of asphalt in crude oil or petroleum residues 501

Method of determining solubility of asphalt in petroleum ether 502

Method of determining resistance of asphaltic cement to oxidation 504

Method of determining bitumen and grading of asphaltic surface mixtures by

extraction method 507

Method of determining bitumen and grading of asphaltic surface mixtures by

burning method 506

Asphaltenes. determination of 503

Atomization of fuel oil 321,326

Atwood process for cracking 212

Automobiles

Number of : 247

Lubricating oils for 277-80

Composition of exhaust gas, air required and completeness of combustion in com-
bustion of gasoline in automobile engines 251

Graph showing amount of gasoline obtained from natural gas, from cracking and

from natural crude, and amount consumed by automobiles 247

Traction efficiency of 254

Radiation, exhaust loss, engine friction, transmission friction, tire friction and air

resistance of automobiles 254

Aviation gasoline

Specifications for (fighting grade) 255

Specifications for (domestic grade) 255

Bailers for well drilling 33

Ball and ring melting point method 454

Barrel

Content of petroleum 150

Gauging tables for standard fifty-gallon barrel 183

Baku pitch, properties of 380

Baume' gravity (see gravity)

Benton process

For cracking 208

Gasoline, fractional gravity distillation of 241

Bentonite for bleaching oil 202

Benzene (see benzol)

Hydrocarbons, definition of 185

Benzine

Definition of 191

Treatment of in refining 191, 199, 200-1

Stream gravity of, from various crude oils

U. S. P. properties of 265

Benzine by distillation 191

Control of benzine distillation by stream gravity 191

Or gasoline distillation capacity for horizontal stills 226

Benzinum purificatum, properties of 265

Benzol

Producing plants of the U. S 81

Carbon, hydrogen sulphur, nitrogen and oxygen in 184

In petroleum and its products 184

Fractional gravity distillation of 240

Properties of 248

Comparison of, with gasoline as a motor fuel 265

Ultimate composition of 184

Heat of combustion of 340

In manufactured gas 364-5

Bermudez asphalt 369

Properties of 380

Bi-products plants for coal distillation 357, 89

Bi nder course for sheet asphalt 370

Bitumen

And bituminous materials (see asphalt) . 367-392

Determination of or solubility in carbon disulphide 503

Method of determining bitumen and grading in asphaltic surface mixtures by

burning and by extraction methods 506-7

KANSAS CITY TESTING LABORATORY 599

Page
Bituminous coal

Properties of 381

Coatings for acid proofing concrete 386-7

Concrete, cross section of 388

Earth pavement, cross sectioii of 389

Substances, classification of 380-1

Surface mixtures, method of determining tensile strength of 508

Bleaching of oil 200

Bentonile for bleaching oil 202

Bloom or fluorescence ot mineral oils 199

Blown oil 3^6

Boili ng point, definition of 347

Boiling temperature (see distillation temperature, etc.)

Of various substances 344

Of hydrocarbons ***

Books, list of important books on petroleum, asphalt and natural gas 58i-8-9

Bottom settlings 202

Brick oil, defini tion of ;?^

Brick pavement, cross section of ^^

Brine, gravity of solutions ^i

British thermal units, definition of ^'

Brockie oil, definition of ™5

Bunker fuel oil, specifications for '*"'■'

Bureau of Mines can

Technical papers of cqy

Bulletins of cqi

Bureau of Standards, publications of • „■ ^

Burkburnett crude oil, gasoline obtained by cracking of

Burning oils ^9

Prices of 266

Description of 267

Sjjecifications for v 268

Specifications for long t ime burning oils

Burton process 213-4

For cracking 205

Composition of gas from ,••■'■ -i' ' 215

Still with various modifications for crackmg oil ^j^^

Butane, properties of '''' jr.j

Byerlite, composition of

Cabin Creek . .187-189

Properties of crude oil from ^ ■■,■'.' ■', 239

Water white distillate from Cabin Creek crude oiK . .. - ^„„„,„„ „j 551

Calcium chloride, gravity, composition and freezing temperature of

California 3,7. 14

Petroleum production of . . 25

Geological occurrence of oil in 42

Production of oil by pools in • ■ • • 39

Oil gushers in • ■ 184

Ultimate composition of crude oil from 'MX \

Fuel oil from .■■•,•.••••• 14

Map showing production and pipe lines in 246

Cost of refining petroleum from SO

Prices of crude oil from TT.

Large petroleum producers of ;■'..

Cracking of California oil '.:•''

Inspection laws and taxes of '.i.-'

Composition of California asphalt Ih,

Properties of crude oil from ;M7

Calorie, small and large, definition of .

Calorific value (see heat of combustion)

Calorimeter j^i

Bomb calorimeter ' • " ' •'"

Gas calorimeter

Canada . ^ 'JV

Petroleum refineries of '"'

Properties of crude oil from ^^^

Cannel coal :^_j_

Properties of •.,■,•■.■••; ' '

Oil yields from distillation ot r«u "V fi

""^Tin^ersion factors for units of .^ ■ ;;;;;;;; K.r'l^

Formula and tables for capacity of tanks • > "

Carbenes, method of determining

600 BULLETIN NUMBER SIXTEEN OF

„ . Page
Carbon

In various brands of motor lubricants 277-8

In various petroleums and products of p)etroleum 184

In benzol 184

In asphalt 184

In lubricating oil 184

Produced by cracking 226

Composition of "carbon" produced by cracking 226

Conradson carbon residue 480

Fixed carbon " 481

Method of determining carbon 480, 481, 491

Carbon bisulphide

Solubility of bituminous substances in 369, 373-4, 380-1-2

Method of determining solubility in 503

Carbon black

Uses of 408-9

Sr>ecifications for 409

From natural gas 406-7-8-9

Carbon dioxide

In natural gas 394

In exhaust gas from gasoline engines 253, 251

In flue gases, from oil furnaces 336, 7

Determination of in gas 515, 6

Properties of 343, 4, 5, 6, 409

Carbon dioxide co.-npressor lubricant, definition of 305

Carbon monoxide

In natural gas 394

In exhaust gas 253,4, 251

In flue gas 335

Determination of in gas 515, 6

Properties of 340, 345, 6, 409

Explosibility of 404

Heat losses from unburned carbon monoxide in burning fuel oil 335

Relation of, to air mixtures in gasoline engines 253

Carbon residue in lubricants and heavy distillates determined by Conradson

method 480

Carbon tetrachloride

Solubility of bituminous substances in 373

Method of determining solubility in 503

Production from natural gas 405

Carboniferous

Relation of oil to carboniferous age 5,19, 20, 23, 25, 26

Cars (see tank cars)

Car oil

Definition of 305

Specifications for 294

Casinghead (see gasoline)

Production of casinghead gasoline 400

Producers of casinghead gasoline 76-79

Cost of plant for casinghead gasoline 399

Hydrocarbons of casinghead gasoline 402

Method of determining vapor pressure of 478-9

Method of determining content of casinghead gas 512

Method of determining volume of casinghead gas 410-419

Equipment for oil wells 35

Specification for various grades of 257

Specifications for blended casinghead gasoline 258

Casinghead gas

Absorption method for testing 512

Gasoline from 399

Capacity of absorption towers for 401

Testing capacity of casinghead gas wells 410

Castor oil

Definition of 305

Lubricating projDerties of 278

Viscosity of ' 278

Catalysis, in cracking of oil 207,230-33

Caustic potash — reagent 519

Caustic soda — reagent 519

In treatment of oil 193, 195

Gravity of solutions of 550

Cement (see asphalt and bituminous cement)

Natural gas used in making Portland cement 403

KANSAS CITY TESTING LABORATORY 601

Page
Centrifuge method for determining sediment and water in crude oil and fuel

oil 462

Cerro Azul oil well 39

Chain lubricants 290

Chemical nature of the cracking of oil 204

Chemical properties (see special subject)

Of various crude oils lai, 187, 8, 9

Of petroleum hydrocarbons 184, 186, 210, 204

Of natural gas 402

Involved in cracking of oil 204

(Chemical treatment of gasoline 199

Chemical constitution of petroleum 183

Chlorine

In treatment of oil 199

Reactions in natural gas 405

Chlorination of natural gas 405

Chromometer

Saybolt, for color of oil 437

Comparison with potassium dichromate solutions 439

Claroline oil -,^^1

Cleveland flash tester 474-6

Cloud test, method of determining cloud test of lubricants and other petro-
leum products ''^^

Coal oil (see kerosene), description of ^^

Coal „-,

Products of ic-Iq

Coal distillation plants in U. S • ocX

Production and value of coal distillation products in U. S 0^19

Composition of, from various sources qciIo

Yields from distillation of coal oco

Distillation of Kentucky, West Virginia and Pennsylvania coals J«j;

Yield from distillation of cannel coal -.oioQic'-i^ 01 99

Comparison of heating value of coal, oil and gas cJl^, Jib, JA>, ^1. ^^

Relative cost of coal and natural gas -jaq i

Method of manufacture of gas from gas oil and coal •j4q_^

Distillation products of ,ji»-.roD

Coal gas 3q.^

Composition 01 364-39 1

Properties of \q\

Explosibility of • • • ; • ^eiO.l, 2. 5

Yield from coal 3g5

Benzol in ggl

Coal tar, products of

Coal tar pitch 380

Properties of 362

Composition of

Coke 4, 195, 20-1

From crude oil 360^ 1 , 2

From coal 204

From Panuco crude oil ,,••,■•■•: 277-«

Coking in various brands of motor lubricants ^^^ ^

Cold test of various lubricants

Colloidal fuel Ml

Advantages of ■ XM

Definit ion and properties of

° ^Method of determining color of crude oil and dark oils ^^,

Method of determining color of lubricants. . . . . . • --..-^ ■ ■ .j37, »»

Method of determining color of kerosene, naphtha and gasoline . ^j,,,

Of crude oil from various localities t<)i)

And odor of refined petroleum 1<.(>»

Of cracked gasoline ■ • LtK*

Removal of, in oil by fuller s earth . .|.(((

lodmetric method of determininR co or. :-■-■■ VM*

Potassium dichromate method of determining color , ,,

Union colorimeter for determining color. i;jV

Saybolt chromometer for determining color i;iK

By Lovibond tintometer !'>>•

Relation of sulphur to color. 277-8

Of various brands of mctor lubricants

Colorado

Oil shale in

Inspection laws and taxes ol

i-ji nr.i

602 BULLETIN NUMBER SIXTEEN OF

Page
Combustion

Products of, of fuel oil 326

Graph showing relation ol air to amount of carbon dixoide in the stack in the com-
bustion of fuel oil 323

Of gasoline 251

Products of, in gasoline engines of 1 gallon of gasoline 253

Combustion efTiciency of gasoline engines per gallon of gasoline 254

Composition of exhaust gas, air required, and the completeness of combustion in

combustion of gasoline in automobile engines 251

Compressor oils, properti es of 279-280, 305

Compression, (gasoline, by compression of natural gas 397-401

Concrete pavement, cross section of 392

Concrete storage tanks 133

Condensers and condensing 226-7-8

Water required 228

Area for distillates 228

Vapor lines 228

Heat absorbed in condensing '. . . 228

Condenser

Boxes, cost, weight and size of 246

Oil, definition of 305

Com adson metliod of determining carbon in oils 480

Connecticut, inspection laws and taxes of 259

Conversion

Conversion factors and tables for units of

Linear dimensions _.

Square measure 553

Volume, capacity, contents, space 554

Weight 554-5-6

Liquid measure 557

Work 150-556

Pressure 559-560

Temperature 561

Time 561

Velocity 561

Money 561

For measuring of water and oil 150

For viscosities 445-447-f

Baume', specific gravity and pounds per gallon 523-52f

For metric units 552

For Centigrade and Fahrenheit degrees 520, 521, 522

Copper chloride for gas analysis 519

Copper oxide for treatment of oil 199

Corrosion, method of making corrosion tests of gasoline and naphtha 497

Cost

Formula for determining cost of gasoline made by both skimming and cracking. . 242

Of refining oil 242-246

Cottrell process for emulsions 203

Cracking

Of petroleum 196-246

Chemical nature of 204

Of paraffin wax 20t

Classification of methods of . . ; 206

In the vapor phase 206

In the liquid phase 206

Commercial processes for 207

Benton process for , 208

Advantages of liquid phase 209

Dewar & Redwood process for 211

Development of commercial cracking 212

Atwood process for 212

Young pro ess for 212

Burton process for 213-4

Burton still for various modifications for 215

Dubbs process for 216

Commercial results of operation of Dubbs process 217-8

Cross process for 219

Operating system of Cross p-ocess 220-1

Relation of cracking plant to skimming plant 222

Commercial results of operation of Cross process 223

Comparative cots of making gasoline by cracking by various methods 223

Double unit cracking plant 224-5

Refinery engineering data bv distillation and cracking of petroleum 226

KANSAS CITY TESTING LABORATORY 603

Page

Fixed gas produced in cracking 226

Carbon produced in cracking 226

Composition of cracking still carbon 226

Operation of pressure distillate cracking systems 228

Cracking curves of petroleum hydrocarbons 234

Equilibrium cracking tests on heavy petroleum hydrocarbons 235

Cracking of Mid-Continent fuel oil 235

Cracking of heavy Kansas Crude oil 235

Paraffin base residuum 235

California oil 235

Kerosene 235. 238

Healdton crude oil 235

Gas oil 235

Mexican flux oil 235

Effect of pressure on the products of cracking kerosene and fuel oil 237

Relation of gravity to amount distilled of water white distillate before and after

cracking 23i, i

Relation between gra ity and distilling temperature of paraffin base oil before

and after cracking 239

Cabin Creek water white distillate before and after ^^

Marcus Hook fuel oil before and after cracking ._ 239

Formula for determining amount of synthetic gasoline obtained by crackmg ^4^

Formula for determining cost of gasoline made by cracking 242

Viscosity of fuel oil before and after cracking . . ., Jl''

Gasoline obtained by crackmg Mexia, Burkburnett Ranger and Mexican crude

Graph showing'fractional gravity distillation of shale oil before and after cracking . 348-350

Fractional gravity distillation of shale oil before crackmg -^^

Olefins in shale oil after cracking ^^

Fractional gravity distillation of shale oil after crackmg qcKlfi

Properties of shale oil before and after crackmg 477

Method of making cracking tests of petroleum hydrocarbons ^

Cream separator oil 7 99 23 25 26

Cretaceous formations and oil .... . • i.i.^,^, -^

Critical pressure of various gasoline hydrocarbons. :; -

Critical temperature of various gasoline hydrocarbons.

Cross process _ 219

For cracking •' 220-1

Operating system of ■ ■ ■ ■ 223

Commercial results of operatmg of .,;

Crude, oil, chart showing relative prices of ,gy

8ubf method for determining melting point of asphaltic and bitummous ^^^

material , , 3(59

Cuban asphalt, properties and composition of 287.306

Cup grease (see greasel . . ■ 187, 1H8. 190

Gushing, Oklahoma, crude oil I97 h

Cylinder oil :«Xi

Definition of lHH-9

In crude petroleum .(9

Prices of 279-280

Properties of 151 182

Cylindrical tanks 151. 153

Contents of horizontal 15.^. 157 8

Contents of bumped ends of . . 155. 6

Tables of capacity of horizontal. 15»

Construction of gauging tables for 182

Contents of vertical, of all diameters— formula 1H2

Contents of vertical, of all diameters— tables

Decane -f •'.

Heat of vaporization of 1 8<>

PropGrtiGs of f ' ' •

Critical pressure and critical temperature ol ::,c.

Dehydration of petroleum . .. ■^. 259

Delaware, inspection laws and taxes or

Demand for

Petroleum products

Gasoline

Depletion of oil wells

El^l^^silnayrd derrick for drilling oh Well,: ! ! 1 . •

Bi::^Tl^i^d'^-ess for cracking ::

•1;'

■1 .

.11

604 BULLETIN NUMBER SIXTEEN OF

Page
Dielectric strength

Relation of water content to, in transformer oils 310

Method of testing, of transformer oils ', 309

Diesel engine oil, specifications for 270

Diesel engine, fuel oil for ! 326-332

Directory of oil associations 108-9

Distillate

Oil or solar oil 193

Pressure 206-218

Pressure distillate systems of cracking 206

Water white 193, 237, 8, 9

Pressed distillate 193

Wax distillate 193-7

Distillation and distilling

Relation between gravity and distilling temperature of paraffin base oil before and

after cracking 238, 239

Refinery engineering data by distilling and cracking of petroleum 226

Relation of distilling temperature to specific gravity of various hydrocarbons .... 236

Main features of crude oil distillation 194

Properties of crude petroleum from various sources 190

Benzine, gasoline and naphtha by 191

Control of benzine distillation by stream gravityg 191

Distillation of kerosene or water white distillate from crude oil 191

Fractional gravity distillation of coal tar benzol 240

Fractional gravity, distillation of Benton process gasoline 241

Fractional gravity distillation '. 238

Benzine or gasoline distillation capacity for horizontal stiHs 226

Yields from distillation of Eastern coals 362

Method of determining water in crude petroleum and fuel oil by distillation

method 463

Method of making end point distillation of gasoline, naphtha, benzine, pressure

distillate, turpentine substitute, and kerosene 464-5-6-7

Method of making fractional gravity distillation of crude f>etroleum and petro-
leum distillate 468-9

Method of making a distillation of crude petroleum for sample of products 470

Method of making a distillation of crude petroleum for water, gasoline, kerosene

and fuel oil 470

Method of calculating amount of aromatic hydrocarbons by distillation 495

Doctor test

Method of making for gasoline or kerosene 492

Solution, formula for 492

Domes, diagram showing accumulation of oil and gas in 19, 20, 1, 2

Drafts, chart showing the influence of temperature on drafts in oil furnaces 327
Drilling

Description of oil well drilling 27-36

Standard derrick for drilling oil wells 28

Standard tools for drilling oil wells 30

Rotary or flush drilling 31

Percussion drilling 31

Portable well drilling rigs 31

Cost of well drilling by motor 35

Cost of drilling oil wells by standard methods 36-7

Drilling and operating costs for oil wells 37

Dubbs process for cracking "216

Commercial results of operation of 217-8

Ductility

Interpretation of, of A. C 375

Method of determining ductility of asphaltic and bituminous materials 499

Duodecane, critical pressure and critical temperature of 210

Dynamo oils, properties of 279-280

Ebano, Mexico field 63

Economics of petroleum 2-112

Effusion method of determining gravity of gases 509-10-11

Elaterite, properties of 380

Electricity

Cracking with ■ 206

Drilling wells with 35

Comparison of heating values of electricity with fuel oil, coal, natural gas and coal

gas 312

Elliott closed tester

Method of determining flash and burning points of lubricants, asphalt and other

petroleum products by 473

Comparison of flash point of the Elliott closed tester with other testers 476

KANSAS CITY TESTING LABORATORY 605

Page

Emulsions of petroleum 202

Dehydration of 202

Coltrell process for , 203

Emulsifying properties of lubricating oils, method oif determining -182

End point distillation 464

Energy and work, conversion factors for units of 558

Engineering — Refinery engineering data 226

Engines

Horsepower of gasoline engines 251

Relation of power, combustion efficiency and theoretical mixtures in gasoline

engines 253

Products of combustion in gasoline engines of one gallon of gasoline 253

Relation of carbon monoxide to the air mixtures in gasoline engines 253

Combustion efficiency on gasoline engines per gallon of gasoline 254

Distribution of heat energy of gasoline in gasoline engines 254

Requirements for lubricating oils for internal combustion engines 276

Operating temperatures in various parts of explosion engines 276

Engine oils, properties of 279-280

Engler viscosimeter, equivalent values of viscosity by. Redwood and Saybolt. 447-8

Equivalents, tables of 553-561

Eschka method of determining sulphur in petroleum 487

Ethane, properties of 186

Ether, petroleum 265

Ethylenes

Delinition of j^

Chemical properties of '"^

Evaporation

Loss in storage of oil by }^

Losses of oil by '"?^

Rate of evaporation of gasoline and benzol ^^"

Exhaust gas *■ „c;-j

Amount of per gallon of gasoline ocff^

Composition of in automobile engines ■^^' •'

Expansion • .,,0 .q.

Of petroleum f S2

Tables of expansion of oil i?f

Explosibility of various gases ■ ■ i otr

Explosion engines, operating temperature in various parts ot ^'o

Express, rules for shipment of petroleum products by 20

Extraction of oil from oil sands 553-5(il

Factors (see conversion factors) ,■ .; ' ■ ■ j ' ' idl^O- 21-''2

Faults, diagram showing accumulation of oil and gas in i»-^u-^> -».

Fatty acid 495

Determination of in lubricants ■ ■ • • jtu-

Method of determining amount of, in petroleum products . ■

Fatty oil, method of determining amount of, in petroleum produi ts

Filler 378

Asphalt 37fi

Dust ■ ■ ' ins" 197-200

Filtration of oi 1

Fire 128

Losses in storage of oil by 12;»

Method of prevention of fire of oil in storage j2c>

Losses from oil fires , M ' , ' ' ' '» 2V7-H

Firp test of various brands of motor lubricants , • \',\^i,-„ ,.ir»u«t

Determination of lubricants, asphal t and other petroleum pr<xlucl8 by hll.otl dosed ^_.^ ^

tester and Cleveland open tester .j

Fishing operation in oil Avells

Fixed carbon 481

Method of determining 374-5

Interpretation of, in asphaltic cement

Flash point , , . . 277-8

Of various brands of motor lubricants 37.) s

Interpretation of, of asphaltic cement. . . .^u' ripvplkn'd ODCn IosKm •'''<

Method of determining Hash point of lubricants by Cleveland open ^ ., ^

By ASTM closed tester 473

By Elliott or New \ork closed tester . . • • - / ■ p„,„kv'-Martcii8 lest. . *l^.

Method of determining (lash point of fuel oil by the Pensky MariciiH ^^^

Correction of, for barometric pressure. 47fi

Comparison of flash points by different testers ^g.

Float test of petroleum residues, method o« making j,^.

Floe test, method of making

606 BULLETIN NUMBER SIXTEEN OF

Page
Floor oil

Specifications for 290

Definition of 306

Florida, inspection laws and taxes of 259

Flour mills, fuel requirements of 403

Flow sheet of complete refinery 192

Flow test of various brands of motor lubricants 277-8

Fluorescence of mineral oils 199

Fluxinft of hard asphalt 371

Foam for fire extinguishing 131

Foots oils 197

Fractional gravity distillation, method of making, of crude petroleum and

petroleum distillates 46&-9

Freezing method for testing natural gas, for gasoline content 513

Freezing point, graph showing freezing point curves of paraffin wax 459

Freezing temperatures of hydrocarbons 186, 265

Freight, rules for shipment of gasoline and naphtha by 137-8-9

Friedel & Craft's reaction 230

Fuel oil 193. 311,347

Chart showing relative prices of 47

Prices of • 49

Content of commercial crude oils 187

Cracking of Mid Continent fuel oil , 236

Efifect of pressure on the products of cracking of 237

Stack requirements for fuel oil furnaces 326-7, 339

Advantages of, over coal for locomotives and boats 326

Use of, for boats 328

Sampling of 328

Comparison of, with other fuels 328

Heat losses in flue gases from fuel oil furnaces 329

Fuel value of producer gas compared with 339

U. S. specifications for 332

U. S. Navy fuel oil 332

Specifications for bunker fuel oil 333

Air required for 334

Ultimate composition of 334

Total heat losses due to chimney gases from 335

Heat losses from unburned carbon monoxide in burning fuel oil 335

Heat losses from hoi gases in burning fuel oil 335

Heat losses from water vapor in burning fuel oil 335

Properties and requirements of one pound of various fuel oil elements 336

Formula for calculating heating value of fuel and air required for ultimate com-
position of 336

Practical losses from fuel oil furnaces 337

Losses in fuel oil furnaces due to excess air ' 337

Transmission rates of radiant heat in fuel oil ftumaces 338

Stack design for fuel oil furnaces 339

Sources and properties of 31 1, 323

Gravity of, from various sources 312

Viscosity of ^^ oJo

Comparison of heating value of, with coal, natural gas, coal gas and electricity. . . 312

Viscosity of, before and after cracking 312

Properties of various commercial fuel oils 313

Viscosity curves of miscellaneous fuel oils 314

Properties of, from various sources 315

Comparison of, with other fuels 3 16

Graph showing relation of gravity to heat of combustion of 317

Table showing relation of gravity to B. T. U. per gallon of 318

Table showing relation of gravi ty to B. T. U. per pound of 319

Advantages of the use of over coal 320

Relative cost of coal and fuel oil for the same fuel value 320

Requirements for burning 321

Graph showing relative cost of gas and fuel oil no^^

Method of burning ■ - : 321-3

Graph showing relation of air to amount of carbon dioxide in the stack in com-
bustion of ^^3

Prices of, for the past seven years 325-

Consu mption of, by railroads qoc_" o

Miscellaneous information concerning the use of ooc

Steam required for atomization of 326

Air required for combustion of 32b

Composition of stack gases from fuel oil furnaces 32b

Products of combustion of ^"^

KANSAS CITY TESTING LABORATORY 607

Temperature of fuel oil flame Pf f|

For melting iron '[ ^26

Consumption for Diesel engines 5?^

Detengination of viscosity of, by Saybolt Universal viscosimeter. as adopted by

Method of determining viscosity of,' by Furol viscosimeter . '. V. ^^Iq

Method of determining water in, by distillation method. 1m

Method of making distillation of crude petroleum for 4-0

Method of determining flash point of, by Pensky-Martens tester .' .' .' .' .' .' ." .' .' ' ' '.[[', 475

Consumption in production of gasoline . . . 99?-99r

Requirements of United States. ... of?

Fuller's earth •'^^

Properties of 2oo

Removal of color of oil by .!......'........ 200

Furol viscosimeter, determination of viscosity oif fuel oil and road oils by 449
Gas (see casinghead)

Method of manufacture of, from gas oil and coal 36,V4

Average content of light oils in various gases .....[....... 365

Chart showing specific heat of flue gases 326

Comparative gas statistics of American cities 399

Method of making complete chemical analysis of .514-5-6

Method of calculating heat of combustion of, from chemical analysis '.'. . . . 518

American gas syndicates 110-112

Fixed gas produced in cracking [ , , 226

Geologic occurance of 19, 26

Relation of oil, gas and salt water ' 19

Hydrocarbons constituting natural gas 402-409

Comparison of heating value with other fuels 312

Relative cost of, to other fuels 312

Composition of commercial gas ^. 394

Producer gas costs 3;«)

Light oils from 360-2-4

Benzol in 360-5

Composition and properties of natural gas from various sources 396-7

Gasoline in natural and casinghead gas 397-8, 401

Carbon black from 406-10

Commercial uses of natural gas 403

Gas consumed by gas engines, brick plants, fiour mills, etc 403

Composition of, from Burton stills 2t>5

Explosibility of gases -104

Testing the capacity of gas wells by the orifice meter 419

Determining capacity of gas wells by Pilot tube •Ill

Calculation of the capacity of gas pipe lines 415

Absorption method for gasoline in natural gas 512

Freezing method for gasoline in natural gas 51-^

Specific gravity mel hod gasoline in natural gas 509

Method of determining specific gravity of 5(*9

Reagents for gas analysis 517

Methods of determining heating value of ^'*

Production of ''^^

Gas black (see carbon black)

Gas compressors, gas consumed by jj'li

Gas engines, gas consumed by r^^

Gas oil • ,,^c

Cracking of ■' T-?)

Specifications for •ifi 4

Method of manufacture of gas from .«x - •»

Gasoline 47

Chart showing relative prices of j,,

Prices of ,, >^ ,,

Casinghead gasoline manufacturers ','.,' s

Rules governing location of oil loading racks for. .

Ultimate composition of

Properties of gasoline hydrocarbons I ^ ■

Content of commercial crude oil |Jjj

By distillation j9i)

Color of cracked gasoline ijijj

Chemical treatment of ;>'in

Critical points of gasoline hydrocarbons . _ . „„,^-j„ — i

Comparative costs of making gasoline by cracking by various mcthodH ., ,^^

Distillation capacity for horizontal stills ..., ; ■,_::,

Fuel consumption in production of

608 BULLETIN NUMBER SIXTEEN OF

Page

Heat absorbed in condensing 228

Condensing surface required for 228

Aluminum chloride in production of 230

Yields of, from aluminum chloride treatment 230

Properties of aluminum chloride gasoline 231-2-3

Vapor pressure of 234

Fractional gravity distillation of Benton process gasoline 241

Olefins in cracked gasoline 233-241

Formula for determining amount of synthetic gasoline obtained by cracking 242

Formula for determining cost of gasoline made by cracking 242

Formula for determining cost of gasoline made by skimming 242

Formula for determining cost of gasoline by both cracking and skimming 242

Formula for determining cost of gasoline by cracking gas oil 242

Obtained by cracking Mexia, Burkburnett, Ranger and Mexican crudes 242

Definition of 247

Hydrocarbons constituting gasoline, with their properties 247, 2io, 184, 6

Heat of vaporization of gasoline hydrocarbons 328, 344

Origin of commercial gasoline 248

Synthetic gasoline ' . ' 248

Graph showing amount of, obtained from natural gas from cracking and from

natural crude, and amount consumed by automobiles 247

Production, consumption and stocks of, at various periods 248

Properties of, sold in 1921 249

Distillation curves of, sold in 1921 250

Combustion of ". . . 251

Composition of products of combustion of, in automobile engines 251

Effect of carbureter adjustment on gasoline consumption 251

Volatility of 234

Carbon, hydrogen, sulphu/, nitrogen and oxygen in 184

Amount of exhaust gas per gallon of 253

Calorific value of 253

Products of combustion in gasoline engines of one gallon of 253

Combustion efficiency of gasoline engines per gallon of 254

Distribution of the heat energy of, in gasoline engines 254

U. S. specification for various grades of 255

Specifications for aviation gasoline, fighting grade 255

Specifications for aviation gasoline, domestic grade 255

Specifications for motor gasoline, new navy 255

Inspection laws and taxes on 259

Possible savings in the use of 264

Comparison of gasoline and benzol as motor fuel 265

Production of natural gas gasoline 400

From natural gas and casinghead gas 399

Explosions of natural gas and gasoline 404

Method of determining color of, by Saybolt chromometer 437

Method of determining color of, by Lovibond tintometer 438

Method of determining color of, with the use of potassium dichromate solution. . . 439

Method of determining viscosity of, by Ubbelohde viscosimeter 450

Method of making an end point distillation of 464-5-6-7

Method of making a distillation of crude petroleum for 470

Method of making doctor test for 492

Method of determining corrosive sulphur in ' 487

Method of making corrosion or gumming test of 496

Freezing method for testing natural gas for gasoline content 513

Gauging

Of petroleum 113, 133

And measurement of petroleum 149, 183

Method of construction of gauging tables for oil tanks 149-151-2-3-4

Method of construction of gauging tables for horizontal cylindrical tanks with

bumped ends I54

Method of gauging horizontal cylindrical tanks with bumped ends. . ............ 153-8

Table for gaugmg contents at various liquid depths of cylindrical horizontal tanks

with and without bumped ends 155-8

Gauging tables for various types of tank cars 174-182

Gaugmg tables for standard fifty-gallon barrel 183

Gear case oil, definition of 306

Gear, chain and wire rope lubricants, specifications for 290

General Electric metliod of determining melting point of asphaltic or bitu-
minous materials 456

Geograpliic distribution of petroleum 5-18

Geological Survey publications of various states relating to petroleum, as-

phalt and natural gas 593-4-5

Geologists, list of state geologists 595

KANSAS CITY TESTING LABORATORY

609

Geology Page

Of petroleum and natural gas ,« oc

Of certain oil fields l^j°

Occurrence, economics and geology of petroleuiii; asphalt and' natural' gas iql26

Character of oil from various strata . oSIor

Of various oil fields .' otiof.

Correlation chart of oil sands of Oklahoma .........! 2^

Georgia, inspection laws and taxes of 2sq

Germany, oil production of ?

Gilsonite

Composition of ogn

Properties of oqq

Glance pitch, properties of qqq

Grading, method of determining bitumen and grading of asphaltic pavement

surface mixtures by burning and extraction 506-7

Grahamite

Composition of 359

Properties of 380

Ultimate composition of 134

Gram '....'.'.'.'.'.'.'.'.'.'.['.'.'.'.'.'.'.'.'.'. 552

Gravity

Relation of distilling temperature to specific gravity of various hydrocarbons .... 236
Relation between gravity and distilling temperature of paraffin base oil before and

after cracking 239

Of various brands of motor lubricants 277-8

General discussion on specific gravity and Baume' gravity 428

Definition of specific gravity and Baume' gravity 429

Formulae for converting specific gravity and Baume' gravity into each other by

Petroleum Association and U. S. Government standards 428

Effect of high temperature on the specific gravity of oil 429

Method of determining specific and Baume' gravity with hydrometer 4:J0

Determination of specific gravity with the picnometer ^ 433

Method of determining specific gravity with the Westphal balance 431

Method of determining specific gravity of A. C. by fluid suspension 434

Method of determining specific gravity of solid asphaltic material by displacement 435

Method of determining specific gravity of asphaltic cement 436

Method of calculating heat of combustion of oil from gravity. 484

Method of determining the specific gravity of gases by the viscosity or elTusion

method 509-10-11

Equivalents of specific gravity, pounds per gallon and Baume' gravity by U. S.

Bureau of Standards formulae 523-4-5

Tables for conversion of specific gravity, pounds per gallon, Baume gravity, by

Tag scale, with extension of tables for oils heavier than water 526-7-S

Tables for reduction of Baume' gravity readings at observed temperatures to

basis of 60° F 529-30-1-2-3-4-5-6-7

Tables for reduction of specific gravity readings at observed temperature to basis

of 60° F 538-i)-40-l-2

Tables of equivalent values for degiees Baume' and specific gravity for '"l"'^o._t;_f

heavier than water ^^^177

Specific gravity and content of sulphuric acid solutions clq

Composition of fuming sulphuric acid :•.■■• '^"^

Specific gravity, Baume' gravity, composition and freezing temperature of calcium

chloride and brine solutions ••■•••■.■ c^,

Specific gravity, Baume' gravity and composition of caustic soda solutions »»'

Greases 905

Specifications for various greases ^^

Various types of ^;,j^

Composition of commercial greases ;; « '• j " h

Gulf fields, map showing production, pipe lines in Gulf fields

Gumming iq7

Or corrosion test, method of making of gasoline and naplha 277-«

Test of various brands of motor lubricants * 293

Gun grease, specifications for 290

Gun and ice machine oil, specifications for

Gushers I'^-IO

Oil M

Cause of Mexican gushers tjx;

Harness oil, definition of Vjg

Healdton crude oil, cracking of

Heat , ■•.;-

And temperature, definition of units of

Absorbed in condensing gasoline and kerosene

Exchanges in refinery condensers

610 BULLETIN NUMBER SIXTEEN OF

Page

Losses from unbumed carbon monoxide in burning fuel oil 335

Losses from hot gases ■ 335

Losses from water vapor 335

Conversion factors for units of 561

Heat

Formation 347

Fusion and melting point of various substances 343

Fusion, definition of 347

Heat of combustion

Of various substances 340

Of coal from various parts of the United States 341-2

Of gases found in natural gas 409

Method of determining heat of combustion or calorific value of petroleum products 483-4

Method of determining heat of combustion of oil from the gravity 484

Method of determining heat of combustion of natural gas 517-8

Method of calculating heat of combustion of natural gas by oxygen consumed . . . 518

Method of calculating heat of combustion of gas from chemical analysis 518

Definition of 347

Heat of Vaporization

And boiling temp)erature of various substances 344

Definition of 347

Heat pressure test

Method of making, of motor lubricants for resistance to decomposition 478

Of various brands of motor lubricants ; 277-8

Heating areas of stills 226

Helium

In natural gas 401a

Properties of 401a

Extraction of 401a

Lifting power of 401b

Heptane

Properties of 187

Heat of vaporization of 247

Critical pressure and critical temperature of 210

Hexane

Properties of 187

Heat of vaporization of 247

Critical pressure and critical temperature of 210

Horizontal cylindrical tanks 151-183

Gauging tables for 152-183

Method of constructing gauging tables 153-4

Contents of horizontal cylindrical tanks with btimped ends 155

Formulae for contents of 151

Horsepower of gasoline engines 251

Hydrocarbons

And their properties 184-6

Paraffin or saturated 184, 186

Olefin, ethylene or unsaturated 185

Naphthene ■ 184

Aromatic or benzene 185

In natural gas 394, 396, 402

Profjerties of gaseous hydrocarbons 186

Properties of gasoline hydrocarbons : . 186

Properties of lubricating oil hydrocarbons 186

Properties of, found in natural gas 402

Hydrogen

Explosibility of 404

In crude petroleum from various states, in Byerlite pitch, Grahamite, Trinidad

asphalt, gasoline, kerosene, lubricating oil and benzol 184

Determination of, in petroleum products 491

Hydrogen chloride

In treatment of petroleum 199

In chlorination of gas , 405

Hydrogenation of petroleum 205

Hydroline oil, definition of 305

Ice machine oil, properties of 279-280

Ice plant, gas fuel required for 403

Ichthyol, definition of 306

Idaho, inspection laws and taxes of 260

Ignition temperature of gases 404

Illinois, inspection laws and taxes of 260

KANSAS CITY TESTING LABORATORY 611

Illuminating oils (see kerosene) P"e«

Description of

Method of determining sulphur in. . '.] ^oslc^^

Impsonite, properties of 4eB-y-yu

India, petroleum production in ^^

Indiana, inspection laws and taxes of ,cn

Iodine method -•'"

Of determining color of crude petroleum and lubricating oils jdo

Equivalent of color by, with other methods .... . . ,_p

Iowa, inspection laws and taxes of ?fin

Italy, petroleum production in ^

Japan, petroleum production in : ^

Journals relating to petroleum, asphalt and natural gas

Kansas

Properties of crude oil from i u-

Inspection laws and taxes of 260

Large petroleum producers of ......'..'. 75

Kentucky

Properties of crude oil from jg7

Asphaltic sandstone from 370

Inspection laws and taxes of 260

Kerosene

Prices of 49

Ultimate composition of '*!'!!!!!!!!!!!!!!!!! 184

Distillation of, from crude oil 191

Critical points of kerosene hydrocarbons 210

Cracking of ...[.'.['.[['.'.'.'.'.[ .'235, 238

Effect of pressure on the products of cracking of 237

Inspection laws and taxes on kerosene 259

Description of .* ' ,' 2(i6

Value and gravity of, from various districts 2(>6

Specifications for water white kerosene 267

Specifications for prime white kerosene ■ *■.... 267

Method of determining color of, by Saybolt chromometer 137

Method of determining color of, by Lovibond tintometer 138

Method of determining color with use of potassium dichromate '139

Method of determining viscosity by Ubbelohde viscosimeter 450

Method of making distillation of crude petroleum for 470

Method of determining flash point of, by ASTM closed tester 471-2

Method of making doctor test for kerosene 492

Heat absorbed in condensing kerosene 228

Kjeldahl method of determining nitrogen in petroleum or asphalt. . 492

Knitting machine oil, definition of 307

Laws, inspection laws and taxes on gasoline and kerosene 259

Leather oil, definition of •'07

Liberty aero oil, specifications for 292

Limestone ,

Asphaltic 3(0

Composition of Mississippi 24

Linear dimensions, conversion factors for units of 5*'

Loading racks, rules governing location of, for gasoline \-lCr-i 8

Locomotive engine oil, specifications for ^_ 295

Loom oil, properties of "' ov»

Loss on heating, method of determining, of oil and asphaltic compounds .>00

Losses . .,u

In the storage of oil '^"

In storage of oil by evaporation, by seepage and by fire -"

In oil on its way to refinery at various stages ^-^

From oil fires .,■;;.

Of oil by evaporation .,:?:

Louisiana, inspection laws and taxes of "jf '

Properties of crude oil from '"'

Lovibond tintometer , , . ■ , ■ . 1

Method of determining color of gasoline, kerosene, lubricalitii- diIs mikI n'riiufi

petroleum ill" •»

Equivalents of color by, and other melliods '" "

Lubricants and lubrication ,q

Prices of lubricating oil ,,,r,

Method of refining petroleum for I,,;^

Properties of ■< \

Description and properties of . . . ,•••.••:■ l<iit

Lubricating properties of crude oil from various locahlics ,^u..j

Economy of lubrication

612 BULLETIN NUMBER SIXTEEN OF

Page

Theory of lubrication 273

Physical properties of various types of 274

Purposes of tests of 274

Viscosity blending chart for 275

Requirements for, for internal combustion engines 276

Sources of 273

Principles of refining 273

Sammary of properties of well known brands of motor lubricants 276

Gravity, color, flow test, flash and fire, viscosity, carbon, gumming and coking

and heat pressure tests of various brands of motor lubricants 277-8

Properties of various lubricants, including cylinder oil, engine oil, turbine oil, com-
pressor oil, ice machine oil, dynamo oil, spindle oil and loom oils 279-280

Effect of automobile engines on the qualities of 280

Effect of fire distillation on viscosity of '. 281

Effect of cracking on lubricating properties of oil 282

U. S. specifications for 283-296

Various grades of, including extra light, light, medium, heavy and extra heavy. . .382-4-5

Ultimate composition of 184

Properties of lubricating oil hydrocarbons 186

Cost of making 214-5

Method of determining color of, by Lovibond tintometer 438

Method of determining color of by iodine method 440

Method of determining color of, by Union colorimeter 441

Determining viscosity of, by Saybolt Universal viscosimeter, as adopted by ASTM 443-4

Method of determining cloud, pour and cold tests of 460-1

Method of determining flash and burning point of, by Cleveland open cup 474

Method of determining flash and burning point of, by Elliott or New York closed

tester 473

Method of making heat pressure test s of motor lubricants for resistance to decompo-
sition 478

Method of determining emulsifying properties of 482

Determination of free fatty acid in 495

McAfee process 230

Machine g.un oil, specifications for air craft machine gun oil 286

MacMichael viscosimeter

Equivalent reading of, with other viscosimeters 447

Method of determining viscosity of petroleum products by 451

Ma^uder viscosimeter, eouivaletit reading of, with other viscosimeters. . . . 447

Maine, inspection laws and taxes of 260

Man jak, properties of 380

Maps 6, 8, 10, 12, 14, 16, 18

Marine engine oil, specilicalions for 288

Maryland, inspection laws and taxes of 260

Mass, conversion factors for units of 447

Massachusetts, inspection laws and taxes of 260

Mazout, definition of 307

Measure, conversion factors for units of 554-:5-6

Measurement

And gauging of petroleum 149-183

Conversion tables for units of, of oil 150

Equivalent of various units of, of oil 150

Mechanical equivalent of heat, definition of 347

Medicinal oil, specification for 299

Melting point

And heat of fusion of various substances 343

Definition of 347

Interpretation of 374-5

Graph showing relation of penetr^ion to melting point of asphalt produced by

blowing with air 375

Method of determining melting point of asphaltic and bituminous materials by

cube method 455

By ring and ball method 454

By General Electric method 456

Method of determining melting jxjint of paraffin wax by titer or English method. 457-8

Methane, properties oi 186

Method of analysis

Outline of, of petroleum and its products 425-6

Application of, of petroleum and its products 427

Metric system, fundamental units of 552

Mexia, gasoline obtained by the cracking of Mexia crude oil 24?

KANSAS CITY TESTING LABORATORY 613

Page
Mexico

Map showing production and pipe lines in 16

Petroleum production and production conditions in 59-68

Potential production of oil in . 59

Oil producing areas of 61

Number and production of wells in 63

Cause of Mexican gushers 64

Salt water in Mexican oil 64

Panuco, Mexico field 63

Topila, Mexico field ; 63

Ebano, Mexico field : __63

Undeveloped oil fields of 67-8

Production of oil by companies in 69

Pipe lines in 69

Storage capacity in „ '0

Tankers handling oil from -tq'a c

Total petroleum operations of inl

Petroleum refineries of ^|^^

Cracking of Mexican flux oil ^-Jg

Gasoline obtained by the cracking of Mexican crude oil ^4^

Composition of Mexican asphalt ^69

Michigan, inspection laws and taxes of '^"'■

Mid-Continent field „

Map showing production and pipe lines in ^

Price changes in crude oil from ^''~°

Mineral seal oil ^pa

Specifications for 300° mineral seal oil -^

Definition of ofii

Minnesota, inspection laws and taxes of ^"J

Mississippi, inspection laws and taxes of |"{

Missouri, inspection laws and taxes of * ^.

Money, conversion factors for units of ,^^

Montan wax, properties of

Montana ' lg7

Properties of crude oil from 261

Inspection laws and taxes of

Motorcycle oil 292

Specifications for ' ' jjyy

Definition of 258

Motor gasoline, specifications for

Naphtlia , ■ ' * . „f 497

Method of making corrosion and gumming tests oi ^^

Prices of c ' ',' 'C ' '■ 488-9-90

Method of determining amount ot sulphur in 137_jt_9

Rules for shipping by freight " 191

By distillation 257

Met'tod* of°dlt^°rmining color of.' by' Saybolt chroniometer .■:::::::: 4fi.,_i^i^^

Method of making end point distillation oL . . .^ . , • -^^ • • ,,-,,2

Method of making flash point of, by ASTM closed tester

Naphthene liydrocarbons IK I

Definition of ■ ■ • , , ■; : 181

National Petroleum Association standard equivalent of color

^^* Freezing method for testing natural gas for gasoline content • • ■ ■ ^ ^^^

Method of determining heat of combustion ot ','.'..'.. •«'^>

Specific heat of gases found in • • ■ '.'.'.'.'.'.,. '•*"

Heat of combustion of gases found in 1 1»» 2\

Measuring the flow of, by orihce meter 410

Production of, in the United Slates ■.■.■.".'.". 3S6. 7. 4»)2

Properties of ; ■ • ■ , / ;!!!-

Occurrence, economics and geology ot • • • ■ ^

Composition of .■. • [ UJJj:

Selling price of, in various cities. ... • .• • .mt

Com^sition of, as delivered in various cities 397

ComjDOsition of, of Oklahoma and Kansas . :»; 400

Gasoline from ■ ,' • ■ ; 1„ . i.?i

Properties of hydrocarbons found m .«(>.<

F^r'gal e^i brick plants; ice plants.' zinc plants.' cement nbn.s. sal. p.«n.s. ^^.^
flour mills, gas compressors

G14 BULLETIN NUMBER SIXTEEN OF

Page

Explosions of ■ 404

Chemical products from 405

Chlorination of 405

Comparison of heating value of fuel oil, coal, natural gas, coal gas and electricity. 312

Relative cost of coal and natural gas 321

Temperature of natural gas flame 326

Natural gasoline, specifications for 258

Nebraska, inspection laws and taxes of 261

Neutral oil

Prices of ' 49

Definition of 307

Nevada, inspection laws and taxes of 261

New Hampshire, inspection laws and taxes of 261

New Jersey, inspection laws and taxes of 261

New Mexico, inspection laws and taxes of 262

New Navy gasoline, specifications for 255

New York, inspection laws and taxes for 262

New York closed tester

Method of determining flash and burning point of lubricants, asphalt and other

petroleum products by 473

Comparison of flash points of, with other testers 476

Nitrogen

In various crude oils and Grahamite, Trinidad, gasoline, etc 184

Method of determining nitrogen in petroleum' or asphalt by Kjeldahl method. . . . 492

Nonane

Properties of <. 186

Critical pressure and critical temperature of 210

Heat of vaporization of 247

Non viscous neutral oil, definition of 307

North Carolina, inspection laws and taxes of 262-

North Dakota, inspection laws and taxes of 262

Octane

Properties of 186

Critical temperature and pressure of 210

Heat of vaporization of 247

Odor

Of refined petroleum ; 199

Determination of odor of petroleum 442

Ohio, inspection laws and taxes of 262

Oil burners

Operation of 323

Various types of 322

Oildag, definition of 307

Oil shale

Distillation products of 349-366

Properties of 381

Composition of 349^350

Occurrence of 352-3

Oil wells, spacing of and relation to production 33

Oklahoma

Properties of crude oil from 187

Inspection laws and taxes of 262

Correlation chart of oil sand of , 23

Oil producing companies of 87-93

Olefins

Method of determining 493

Definition of 185

In cracked gasoline 233, 24 1

In shale oil 355

In shale oil after cracking . . . . ; 356

Orifice meter, measuring flow of natural gas by 419-424

Oregon, inspection laws and taxes of 262

Ostwald viscosimeter, equivalent readings of, with other viscosimeters 447

Oxidation, method of determining resistance of asphaltic cement to 504

Oxygen

In crude oil from various States, Byerlile pitch, Trinidad asphalt, gasoline, kero-
sene, lubricants and benzol 184

Bomb calorimeter, method of determining sulphur in petroleum by 485

Gas compressor lubricant, definition of 305

Ozokerite, properties of 380

Panuco, Mexico field 63

KANSAS CITY TESTING LABORATORY 615

Page
Paraffin ' • 197

MelhS'oTSeTefmining meltingpoinl of. by titer or English method Z. '. '. ::::.... 457^

Graph, showing freezing point curves of 280

Properties of .... 302

Grades and uses of ^- 301-2-3

Manufacture of . '. 293

Specifications for 204

Cracking of . . ^ ■ • • • _, --^ '.'.'.'.'.'.'.'.'.'... 303

Specifications for U. S. P. paraffin

Paraffin hydrocarbons 184

Definition of 186

Detailed properties of ■ ■ j ' ' ■ ' i,' ' 'c 494

Method of determining, in petroleum hydrocarbons

^***aassification of U. S. patents on petroleum refining - 5g3_||g

List of U. S. patents on petroleum refining '.............■■ 381

Peat, properties of

""""Me^th^^of making, of asphaltic and bituminous materials • ■ ■ ■ ^9.-8

Kf^mlneralfilieronpenetrationofasphaltic cement 371

Pennsylvania , t _ ^11

Properties of crude oil from 51

Price changes in crude oil Irom ibZ

Penns^n^ ^^^^^'^sc-^meter. equivalent readings of . with other vis- ^ ,^

cosimeters

^^"^lt^';^dlt^Sng flash ix>iru of h^c^^ yy-- ^71

Comparison of flash pomts of, with other testers ^^

Pentane 210

gS'^ml..rat.resa^d critical pressures of ::::::::::::::::::::: 247

Heat of vaporization of ^

Petrolatum 29fi

Prices of . .^^ .'.'.'.'.'.'.'.v.'.'. ; ; 3()0

l^dfi'cS for y.S: F^tr«|fi^";„,„uW for converting specific ftraviVy and

p-^^-S^au'^r'^^aX^'-hSr-hy .::::::::...:: ' h^

Petroleum coke, definition of r^

Petroleum ether, properties ot ^j^

Ffcromrer^'e'terSaTion of specific gravity with the picnometer ^^^^^^

""'^Scity of gasoline pipelines ! i! i! :::::::: ^ • -^ •■•■•••••■• '"'^^

^Slf^f standard fittings for.::: .....••■•■•::::;;:;:::;:. 122

Properties of average P'Pelme "il ^

Effect of viscosity on capacity ot ^

Map of United Slates showing ■^^.^— ^^d' Gulif fields • ■ 10

Map showing pipemes n Mid Con^men ^^

Map showmg pipe mes n Eastern u mi ^^

Map showing pipe ines in Wyprnmg j^.

Map showing pipe mes in Caltfornia • ,.y

Map showing pipelines in Mexico ^^^^

In Mexico 1 13 5

Sffpl^nesoftheU^itedStates:..........;;;;:::::::::::; n«

Extent and cost of • 1 L- •! m

Color equivalents with f,..>ass.iuii 52.V4-0

^''"^S.^^n^'^^y. U- S Bi'--2^^;:^(^1^l:-nr;:of tables roro«H heavier .h„n^^ ^ ,
Tables for conversion of. by i ag bi-d .
water

616 BULLETIN NUMBER SIXTEEN OF

Pressure Page

Conversion factors for units of 559-560

Effect of, on products of cracking of kerosene and fuel oil 237

Pressure tar, properties of 380

Pressure tar asphalt, composition of 369

Prices

Petroleum and its products 44-58

Crude oil at the well 44-5-6

Road oil and asphalt 46

Chart showing relative prices of gasoline, crude oil and fuel oil 47

Of crude oil compared with other raw commodities 48

Of gasoline, naphtha, kerosene, burning oil, fuel oil, neutral oil, lubricating oil,

cylinder slock, gas and asphalt 49

Of petrolatum, medicinal oils 50

Retail prices of gasoline and kerosene 50

Of California crude oil 50

Changes in Pennsylvania crude oil 51

Changes in Mid-Continent crude oil 52-8

Production

Of petroleum by states 3

Of petroleum by districts 3

Of petroleum in the world 4

Refined products of petroleum 4

Map showing production in Mid -Continent and Gulf fields 8

Map of United States showing refineries, production and pipelines 7

Map showing production in Eastern United States 10

Map showing production in Wyoming 12

Map showing production in California 14

Map showing production in Mexico 16

Daily production of oil by pools in United States 42-3

Petroleum production and production conditions in Mexico 59-68

Potential production of oil in Mexico 59

Production of oil by companies in Mexico 69

Large petroleum producers of California 75

Oil producers of Texas 82-86

Oil producers of Oklahoma 87-93

Production, consumption and stock of gasoline at various periods 248

Propane

Properties of 186

Heat of vaporization of 247

Properties

Of petroleum : 192-246

Of methane, ethane, propane, butane, pentane, hexane, heptane, octane, nonane,

decane and undecane

Of gaseous hydrocarbons 186

Of gasoline hydrocarbons 186

Of paraffin hydrocarbons 186

Of lubricating oil hydrocarbons 186

Typical crude oil from various sources 187

Crude oil from various states 187

Publications — U. S. Government publications on petroleum, asphalt and

natural gas : 589-592

Pump equipment for oil wells 34

Pumping of oil wells 34

Quenching oil, definition of 306

Ranger crude oil, gasoline obtained by cracking of 242

Recoil oil, specifications for 287-290

Recuperator oil, definition of 305

Recuperator grease, definition of 305

Redwood viscosimeter, equivalent readings of, with other viscosimeters 447-8

Reduction

Tables for reduction of Baume' gravity readings at observed temperatures to basis

of 60° F 529-30-1-2-3-4-5-6-7

Tables for reduction of specific gravity readings at observed temperatures to basis

of 60° F 538-9-40-1-2

Refineries

Map of United States showing refineries 5-18

Petroleum refineries of United States 94-103

Petroleum refineries of Canada 103

Petroleum refineries of Mexico 103

Engineering data on distillation and cracking of petroleum 226

Calculation of heat exchanges in refinery condense rs 228

Refinery

Flow sheet for complete petroleum refinery 192

Typical refinery practice 191

KANSAS CITY TESTING LABORATORY 617

Refining Page

Of petroleum 192-246

Cost of 243-246

Cost of. in 1922 246

Method of, for lubricating oils 195

Cost of refining California petroleum 246

Method of, refining oil for road building purposes 367-8

Products of the refining of light oil from gas works 364

Methods of determining refining loss of petroleum products 494

Classification of U. S. patents on petroleum refining 562

List of U. S. patents on petroleum refining 563-586

Repress oil, definition of 305

Residuum, cracking of paraffin base residuum 235

Riiode Island, inspection laws and taxes of 262

Ring and ball method of determining melting point or softening point of

bituminous material 151

Road oil -

Prices of 4b

Specifications for "^^o

Properties of typical road oils -iog

Graph showing amount of road oil required -Joo

Method of det^ermining viscosity of, by Furol viscosimeter 449

Roily oil ^r

31

Roll oil, definition of .
Rotary or flusli drilling

Russia, properties of crude oil from '?J

Salt water in Mexican oil °^

Sands , o/,

Voids in petroleum sands 5"

Correlation chart of oil sands in Oklahoma --^^

Sand screens or strainers

^^^ Method'^ord^'e^rmining color of kerosene, gasoline, naphtha and other refined pe- ^^^

troleum by • loq

Color equivalents on Saybolt chromometer scale

Saybolt Furol Biscosimeter , . , ■, j ^,j «;i k„ 44<»

Method of determinmg viscosity of fuel oil and road oil by '■••

Equivalent readings of, with other viscosimeters

^ntco'^uronlrTi^nts'Ka and crude oil by, as adopted by ASTM H^

Equivalent readings of, with other viscosimeters ^^^

i^j^'^l^iS?^r,^»J^S^^-f ; with other viscosimeters.:: ! :::::: 447

tlTrSLZ SS^Ic^*^: in crude petroleum and fuel oil by centrifuge ^^

method ^ ., v 128

Seepage, losses in storage of oil by -((,7

Sewing machine oil, definition of

Shale oil 3J9

Composition of 352 3

Refining of ...........■■■■ ' '■ '

Olefins in : ■ ■ y ; 'r 1 ■_„; . . • ' '

Fraction gravity distillation of, before cracking ,,,

Olefins in, after cracking. ...._... ^ .^^ . .,,,

Fractional gravity distillation of, after cracking. _. . . • • • 1 j- •; ' ' -r-.rkine ;>4rt .<;*)

Grfph showing fractional gravity d stiUat.on of, before and after cracking. . .^

Properties of shale oil before and after cracking 388

Sheet asphalt, cross section of

^'''^K'for shipment of gasoline and naphtha by freight '^j^?

Rules for shipment of petroleum products by express 32

Shooting, method of shooting wells

Skimming , , . , . .„ ., , ;

Plant, relation of cracking plant to

Cost of skimming crude oil •• ';|;_

il^rti^ian Institute: publications oi :.:.'.'.'. • ■ ; 1 va

Solar oil or distillate oil ^_^ ,.

'"'^fed^^SSbil^y ^'asphalt, lubricating oil, bi.u.cn and o.hcr ' ' ^j.
petroleum products in petroleum ether.

618 BULLETIN NUMBER SIXTEEN OF

Page

Method of determining bitumen, or solubility in carbon bisulphide 503

Method of determining carbenes or solubility in carbon tetrachloride 503

South Carolina, inspection laws and taxes of 262

South Dakota

Inspection laws and taxes of 263

Properties of crude oil from 187

Space, conversion factors for units of 554-5-6

Specific gravity (see gravity)

Specific heat

Chart showing specific heat of flue gases 326

Of various substances 345

Of gases and vapors 346

Of gases found in natural gas 409

Specifications

U. S. specifications for various grades of gasoline 255

For aviation gasoline, fighting grade 255

For aviation gasoline, domestic grade 255

Motor gasoline, new navy 255

Turpentine substitute or naphtha 257

Various grades of natural or casinghead gasoline 257

Motor, natural gasoline or blended casinghead gasoline 258

U. S. specifications for burning oils ■ 267

Water white kerosene 267

Prime white kerosene 267

Long time burning oil 268

300° mineral seal oil 268

Signal oil 269

Gas oil 270

Diesel engine oil 270

Straw oil or absorption oil 271-2

Lubricating oils 283-296

Aircraft machine gun oil 286

Recoil oil 287-291

Cup grease 298

Cylinder oil 289

Floor oil 290

Transmission lubricants 288

Marine engine oil 288

Gun grease 293

Car oil 294

Gear, chain and wire rope lubricants 290

Various greases ■ 295

Locomotive engine oil 295

Transformer oils 294

Paraffin wax 294

Gun and ice machine oils '. 290

Liberty aero and motor cycle oil ' 292

Medicinal oil 299

U. S. P. petrolatum 300

For U. S. P. paraffin 303

Asphaltic cement 373-4

U S. specifications for fuel oil 332

Bunker fuel oil 333

Oil asphalt filler of National Paving Brick Manufacturers Association 378-9

For carbon black 409

Purposes of, for asphaltic cement 374

Spindle oils

Properties of 279-280

Definition of 307

Spudding in — Method of spudding in wells 32

Stack gases, composition of, from fuel oil furnaces 326

Standard Oil Company

Earnings 80

Refiners, marketers, producing companies, pipe lines and tank companies of 107

Statistics, petroleum 3-4

Steam

Required for atomizing fuel oil 326

Volume of oil vapors and steam at different temperatures 229

Still

Combination pipe and tower still for petroleum distillation 196

Heating area of horizontal stills 225

Benzine or gasoline distillation capacity for horizontal stills 226

Cost, weight, capacity and dimensions of standard crude oil stills 246

KANSAS CITY TESTING LABORATORY 619

Page

Stitchinfi oil, definition of 307

Storage

Cosi, weight and capacity of steel storage tanks I35

Of petroleum 113-183

Method of, of oil 127

Capacity in Mexico 70

Cost of storage tanks 127

Losses in storage of oil 127

Method of prevention of fire of oil in 129

Gauging of vertical cylindrical storgage tanks 135

Straw oil, specifications for 271-2

Sulphur

In crude oil from various States, Byerlite pitch, Grahamite, Trinidad asphalt,

gasoline, kerosene, lubricating oil and benzol 184

Crude petroleum 188-9

Method of making sulphur tests for turpentine substitute 491

Content of vacuum distillation hydrocarbons from crude oil 281

Method of determining sulphur in petroleum products by oxygen bomb calori-
meter 485

By Eschka method 487

By chemical bomb 486

Method of determining corrosive sulphur in gasoline 487

Method of determining amount of sulphur in naphtha and illuminating oils 488-9-90

Sulphuric acid

Composition of fuming sulphuric acid 549

Content and gravity of sulphuric acid solutions 547-8

Summer black oil, definition of 305

Surfaces, conversion factors for units of 554

Swabbing of oil wells 34

Synclines, diagram showing accumulation of oil and gas in 192-0-1-2

Tabbyite, properties of 380

Tables

Conversion tables for units of measurement of oil 150

For conversion of temperatures in ° Centigrade to and from ° Fahrenheit 520-1-2

For conversion of specific gravity, pounds per gallon, and Baume' gravity by Tag

scale with extension of tables for oils heavier than water 526-7-8

For reduction of Baume' gravity readings at observed temperatures to basis of

60° F 629-30-1-2-3-4-5-6-7

For reduction of specific gravity readings at observed temperatures to basis of

60° F 638-9-40-1-2

Of equivalent values for gravity of liquids heavier than water 543

Tables

For correction of gauged valume of oil to 60° F. 152

For gauging contents of horizontal cylindrical tanks 155-6

For gauging contents of bumped ends of hor. cyl. tanks 157-8

For gauging contents of hor. cyl. tanks up to 120 inches diameter 159-173

For gauging standard tank cars 174-182

For conversion of weights and measures 552-561

Sulphuric acid 548-9

Caustic soda 550

Brine solution 551

Tables, gauging tables for standard fifty-gallon barrel 183

Tag scale, tables for conversion of specific gravity pounds per gallon and

Baume' gravity by 526-7-8

Tag-Robinson colorimeter, equivalents of color by '*'*^Z?

Tagliabue open tester, comparison of flash points of, with other testers 4/6

Tagliabue viscosimeter, equivalent readings of, with other viscosimeters 447

Tanks

Cost of storage tanks ^^i

Important features of oil tanks ^^'

Specifications for brick and tile enclosed tanks iqc

Gauging of vertical cylindrical storage tanks 13|

Cost, weight and capacity of steel storage tanks |^5

Design of steel oil storage tanks ■ „|_c

Owners of tank cars ,,?rion

Oil tanks • • ■ • , _ V^^}.*^

Method of construction of gauging tables for oil tanks 149-151-^-.l-'i

Total capacity of horizontal cylindrical tanks without bumped ends j-^J

Total capacity of bumped ends of horizontal cylindrical tanks j^j

Contents of partially filled horizontal cylindrical tanks ici a

Method of gauging horizontal cylindrical tanks with bumped ends ._ I0.1-H

Method of constructing gauging tables for horizontal cyhndncal tanks with
bumpyed ends

620 BULLETIN NUMBER SIXTEEN OF

Page
Table for gauging contents at various liquid depths of cylindrical horizontal tanks

with and without bumped ends 155-8

Contents of horizontal cylindrical tanks of various depths 159-173

Gauging tables for various types of tank cars 174-182

Tankers handling oil from Mexico ■•>-'• 71-2

Tar, method of determininft tar in cylinder stock 503

Taxes and inspection laws on gasoline and kerosene 259

Temperature

Of oil wells 22-24

Conversion factors for units of 561

Volume occupied by oil at various temperatures based on a unit volume at 60° F. 431
Factors for temperature correction of gauged volumes of oil to 60° F. for various

petroleum products 152

Operating temperature in various parts of explosion engines 276

Tables for conversion of temperatures in ° Centigrade to and from ° Fahrenheit. .520-1-2

Tempering oil, definition of 308

Tennessee, inspection laws and taxes of 263

Tensile strength — Method of determining tensile strength of bituminous

surface mixtures 508

Tetradecane, properties of 210

Texas

Oil producers of 82-86

Projaerties of crude oil from '. 187

Inspection laws and taxes of 263

Thermal units in common use 347

Thickened oil, definition of 308

Thread cutting oil. definition of 308

Time, conversion factors for units of 561

Toluol, properties of 248

Topila, Mexico field 63

Traction efficiency of automobiles 254

Transformer oils

Method of testing dielectric strength of 309

Relation of water content to dielectric strength of 310

Specifications for 294

Definition of 308

Solubility of water in 308

Transparency of petroleum, determination of 442

Transmission lubricants, specifications for 288

Transportation

Of petroleum 1 13-183

Cost of pipeline transportation 118^9-20

Tridecane, properties of 210

Trinidad

Ultimate composition of 184

Composition of .' 369

Properties of 380

Turbine oil

Properties of 279-280

Definition of 308

Turpentine substitute

Method of making sulphur tests of -^91

Specifications for 257

Ubbelohde viscosimeter, method of determining \isccsity of kerosene and

gasoline by 450

Ultimate composition

Of petroleum and its products 184

Of gasoline _. 2.53

Undecane

Properties of 186

Critical pressure and critical temperature of 210

Heat of vaporization of 247

Underreaming of oil wells 31

Union colorimeter

Method of determining color of lubricants by _ 441

Equivalent of color by, with other colorimeters ". 441-2

United States, petroleum refineries of 94-103

U. S. P. benzine, properties of 265

U. S. Bureau of .Standards formula, equivalents of specific gravity, pounds per

gallon and Baume' gravity by 523-4-5

U. S. Department of Agriculture, publications of 592

U. S. Geological Survey, publications of 592

U. S. Government publications on petroleum, asphalt and natural gas 589-592

U. S. Navy fuel oil 332

KANSAS CITY TESTING LABORATORY 021

PagG
Unaaturated hydrocarbons

Definition of Ig5

Method of determining olefins or 493

Uses of petroleum and Its products 2

Utah, inspection laws and taxes of 263

Vapors

Volume of oil vapor and steam at different temperatures 227, 229

Area of still vapor lines ' 228

Vapor pressure of heavy oils 234

Vapwr pressure of gasoline 234

Vaporization, heat of, of gasoline hydrocarbons 247

Velocity, conversion factors for units of 561

Vermont, inspection laws and taxes of 263

Virginia, inspection laws and taxes of 263

Viscosimeters

Determination of viscosity of lubricants, fuel oil and crude paLroleum by the Say-
bolt viscosimeter, as adopted by the ASTM 443-5

Engler 446

Redwood 416

Equivalent readings of the Saybolt, with the Sayboli Furol, MacMichael, Engler,
Tagliabue, Pennsylvania Railroad, Scott, Redwood, Magruder and Oslwald

viscosimeters 447

Method of determining viscosity of kerosene and gasoline by the Ubbe'.ohde vis-
cosimeter 450

Viscosity

Effect of, on the capacity of oil pipelines 123

Effect of temperature on the viscosity of oil 126, 281

Blending chart for lubricating oils 275

Of various brands of motor lubricants : 277-8

Of vacuum distilled hydrocarbons from crude oil 281

Effect of fire distillation on viscosity of lubricating oil 281

Of fuel oils 312-314

Of fuel oil before and after cracking 312

Curves of miscellaneous fuel oils 314

Of asphaltic cement, interpretation of 374-5

Equivalent values of, by Engler, Sayboli and Redwood viscosimeters 447-8

Method of determining viscosity of fuel oil and road oil by the Furol viscosimeter 449
Method of determining viscosity of petroleum products by the MacMichael vis-
cosimeter 451

Method of determining viscosity or float test of petroleum residues 452

Method of determining zero viscosity of semi-S3lid petroleum products 453

Method of determining viscosity of kerosene and gasoline by the Ubbe'.ohde vis-
cosimeter 450

Determination of viscosity of lubricants, fuel oil and crude petro'eum by Saybolt

Universal viscosimeter as adopted by the ASTM 443-4

Method of determining viscosity of petrolatum 453

Method of determining specific gravity of gases by the viscosity or effusion

method 509-10-1 1

Viscous neutral oils, definition of 308

Voids

In petroleum sands 20

Calculation of, in mineral aggregates _377

Volatility of asphaltic cement, interpretation of 374-5

Volume, conversion factors for units of 55 -''-6

Washington, inspection laws and taxes of 263

Watch oil, definition of 308

Water

Removal of from crude oil 202

Solubility of, in transformer oil and petroleum 308

Relation of water content to dielectric strength of transformer oils 308

Method of determining water in crude petroleum and fuel oil by centrifuge mrh:)rl 4'i2

Method of determining water in petroleum and fuel oil by distillation meth )ri 16'<

Method of making distillation of crude petroleum for 1"0

Water white distillate, distillation of, from crude oil "M

Was (see paraffin or paraffin wax)

Solubility of 303

Amount of, in crude oil 303

Distillate ^3

Sweating of ^J;^

Tailings J ;'i

Pot ■- . ■ . '"'

Method of determining amount of wax in asphaltic petroleum and hiiummoiis _

p. oducts •'"•''

622 BULLETIN NUMBER SIXTEEN OF 'I

Page
Weight, conversion factors for units of '.M. .-vifeit*. ?t».'... •.•>i- .iSSC

Wells ':•:/. ■':: '

Oil wells in Mexico •.•.■^u- ■"• •■•'■ ■'"• ■ ■'• ■ .^'•■-41-2

Number and production of. in Mexico ;■....•:•. v ..;.■.'?'.•. ..•''.■•.;. • -' fit?

Drilled for pelroleum ; .■.■.•:.•. '. .'-."'. '. •..*:.;.•.'•' 4

Production of petroleum ,..._......'• 4

Temperature of oil wells .- r .•''.-•.■''- ■. ;■:'.•. , •.••.■.. ; .•.'.•. . 22-24

Depth of oil wells ■••••>,-• w'^'v ' ■ • ■'•.■ ' v '• ■ ■ • ^S"?**.

Description of oil well drilling ' • •.■..'.]■*. l'.' i*;.':*. ■. . .". :'. . : \' .... 27-.'i6

Standard derrick for drilling oil wells . . . . ' ,■■'■ gi'- '■'■'■ '■,—■•.■ '■''■ ;■;.... 28

Standard tools for drilling oil wells .' :".".";*•' '^ .''•' ;.'.''. / ?.-. .■ . . 'M

Underreaming of oil wells •■. *^?.'^^7'^':. ..*:'*■ 'M

Method of spudding in wells •. f^* .*.•* '.•=., 32

Method of shooting wells .-.-.*?»'*.*.•■. . -. .".'K :" 32

Swabbing of oil wells ;.......... 33

Pumping of oil wells • Jvl io.*<:JirC'jJ!Jv.;. . ; . ; 34

Pump equipment for oil wells .-'i-.:! rli-- .o..--ribu — 34

Rate of withdrawal of oil from wells -- , 34

Depletion of oil wells -_. • 24

Cost of well drilling by motor ■.■^'. >-A:/:,.. .;■. .J.- 35

Drilling and operating costs for oil wells vH-; •.'!.;, . . . : '. 38

Production and decline of individual wells 41

Oil wells in the United States -«. , '. 41

Pitot tube for testing open flow of gas wells 411-2-3-4-5

Westphal balance, method of determining specific gravity with 433

West Virginia

Inspection laws and taxes of 263

Properties of crude oil from . 187

Wisconsin, inspection laws and taxes of ." 263

Wood block pavement, cross section of 390

Wool oil, definition of 308

Work, conversion factors for units of 558

Wurtzilite, properties of 380

Wyoming

Map showing production and pip)elines in 12

Inspection laws and taxes of - 263

Xylol, properties of 248

Young process for cracking 212

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