Ef
rfaUII >M
I I I I I
I I I K I t I »:
I I I t I I I t
I I I I I I, I 1 t:
Air Pollution Aspects of Emission Sources:
COKE OVENS
I
A Bibliography with Abstracts
!• • • t 19 ^ B fc B K f, B B IS
U. S. ENVIRONMENTAL PROTECTION AGENCY
-------
-------
EPA-450/1-74-002
AIR POLLUTION ASPECTS
OF EMISSION SOURCES:
COKE OVENS
A BIBLIOGRAPHY WITH ABSTRACTS
Air Pollution Technical Information Center
ENVIRONMENTAL PROTECTION AGENCY
Office of Air and Water Programs
Office of Air Quality Planning and Standards
Research Triangle Park, North Carolina 27711
March 1974
-------
This report is published by the Environmental Protection Agency to report information
of general interest in the field of air pollution. Copies are available free of charge - as
supplies permit - from the Air Pollution Technical Information Center, Environmental
Protection Agency, Research Triangle Park, North Carolina 27711. Copies may also be
purchased from the Superintendent of Documents, U.S. Government Printing Office,
Washington, B.C. 20402.
Publication Number EPA-450/1-74-002
11
-------
CONTENTS
INTRODUCTION v
ANNOTATED BIBLIOGRAPHY
A. Emission Sources 1
B. Control Methods 9
C. Measurement Methods 31
D. Air Quality Measurements 34
E . Atmospheric Interaction (None)
F. Basic Science and Technology - 37
G. Effects - Human Health 39
H. Effects - Plants and Livestock 41
I. Effects - Materials 42
J . Effects - Economic (None)
K. Standards and Criteria 43
L. Legal and Administrative 44
M . Social Aspects (None)
N. General (None)
AUTHOR INDEX 45
SUBJECT INDEX 49
111
-------
AIR POLLUTION ASPECTS
OF EMISSION SOURCES:
COKE OVENS
A BIBLIOGRAPHY WITH ABSTRACTS
INTRODUCTION
The Air Pollution Technical Information Center (APTIC) of the Office of Air Quality
Planning and Standards prepared, selected, and compiled the approximately 235 abstracts
in this bibliography. The abstracts are arranged within the categories listed in the
Contents. The abstracted documents are thought to be representative of available lit-
erature, and no claim is made to all-inclusiveness.
The subject and author indexes refer to the abstracts by category letter and acces-
sion number. The author index lists all authors individually; primary authorship is in-
dicated by an asterisk. Generally, higher accession numbers have been assigned to
more recent documents.
Current information on this subject and many others related to air pollution may be
found in APTIC's monthly abstract bulletin.*
All of the documents abstracted by APTIC are currently on file at the Air Pollution
Technical Information Center, Office of Air Quality Planning and Standrds, Environmen-
tal Protection Agency, Research Triangle Park, North Carolina 27711. Readers outside
of the U.S. Environmental Protection Agency may seek the documents directly from
publishers , from authors , or from libraries .
*"Air Pollution Abstracts" , Superintendent of Documents, U.S. Government Printing
Office, Washington, D.C. 20402. Subscription price: $27 .00 per year; $6. 75 addition-
al for foreign mailing. (More than 6300 abstracts, subject and author indexes are in-
cluded in each issue, plus two separate indexes.)
-------
A. EMISSION SOURCES
05005
R. P. Hangebrauck, D. J. von Lehmden, and J. E. Meeker
SOURCES OF POLYNUCLEAR HYDROCARBONS IN THE
ATMOSPHERE. Public Health Service, Cincinnati, Ohio, Na-
tional Center for Air Pollution Control. (PHS Publ. No. 999-
AP-33.) 1967. 48 pp.
Rates of emissions of polynuclear hydrocarbons were mea-
sured at several sources considered likely to produce such
emissions. The sources included heat generation by com-
bustion of coal, oil, and gas; refuse burning; industrial
processes; and motor vehicles. The annual emissions of
benzo(a)pyrene in the United States were estimated for each
of the sources surveyed, to provide a rough gauge of the im-
portance of each source. Small, inefficient residential coal-
fired furnaces appear to be a prime source of polynuclear
hydrocarbons; other sources may be of local importance.
Production of polynuclear hydrocarbons was generally as-
sociated with conditions of incomplete combustion. (Author
abstract)
05108
J. D. Doherty and J. A. DeCarlo
COKING PRACTICE IN THE UNITED STATES COMPARED
WITH SOME WESTERN EUROPEAN PRACTICES. Blast
Furnace Steel Plant 55 (2), 141-53 (Feb. 1967). (Presented at
the International Congress of Charleroi, Belgium - Coke in the
Iron and Steel Industry, Sept. 1966.)
The operation of coke plants or coke-plant practice in the
United States is reviewed and compared with coke-oven prac-
tice in certain countries of Western Europe. Data on coals car-
bonized and production and yields of coke and principal by-
products in the United States have been compiled by the Bu-
reau of Mines. Similar data for European countries were ob-
tained from various publications of the Economic Commission
for Europe and official publications of the respective coun-
tries. In the United States, coke-oven operations are governed
largely by demand for blast-furnace coke which in 1964
required 85 per cent of the output of oven coke. Foundry coke
requirements amounted to roughly 5 per cent of the total.
Thus, it is estimated that approximately 90 per cent of the
coke output was used in metallurgical applications. For this
reason, coke ovens are operated principally to produce the
maximum quantity of metallurgical coke. Although metallurgi-
cal coke is the major coke -oven product in Europe, coke-
oven gas is also important in Great Britain, West Germany,
France, and other countries. Owing to the lack of adequate
crude petroleum resources in these countries, more emphasis
is placed on the extraction and processing of the crude tar and
light oil. One aspect where there are several fundamental dif-
ferences is the charge preparation. In American plants the
moisture content of the coking coal admixtures generally is
lower than in most European plants, whereas the volatile
matter is higher. Bulk density in European plants is generally
lower. Coke yields are high in Europe, whereas tar and light-
oil yields are lower Carbonizing conditions are also slightly
different, as American plants use higher wall temperatures and
faster coking rates than most of those in Europe Coke-oven
dimensions, except for width, have increased in most of the
countries and are similar exclusive of the large-capacity or
high ovens. These are just coming into commercial realization
in the United States, whereas some batteries of 5- and 6-meter
ovens have been operating for many years in several European
countries.
06582
RESTRICTING EMISSION FROM GAS GENERATORS IN
COKE AND GAS PLANTS. (Auswurfbegrenzung Generatoren
Kokereien und Gaswerke.) VDI (Verein Deutscher Ingenieure)
Kommission Reinhaltung der Luft, Duesseldorf, Germany.
(VDI 2290.) 19pp. (June 1962). Ger. (Tr.)
The purposes of this specification are: to describe the opera-
tion of gas generators and to analyze the factors influencing
the emission of gas and sulfur dioxide; to indicate measures
for reducing the emission of dust and sulfur dioxide; and to
establish conditions and guide values for restricting the emis-
sion of dust and sulfur dioxide.
08392
J. D. Clendenin
THE UTILIZATION OF COAL. Am. Chem. Soc., Pittsburg,
Pa., Div. Fuel Chem. Preprints, 9(2):222, 1965. (Presented at
the 149th National Meeting, American Chemical Society, Divi-
sion of Fuel Chemistry, Symposium on Fuel and Energy
Economics, Detroit, Mich., April 4-9, 1965.)
A brief survey is presented of current and prospective utiliza-
tion of coals including lignite, (1) in the production of metal-
lurgical, chemical and specialty cokes, (2) as fuel for process
steam, space and home heating, locomotives and ship bunkers,
(3) In the manufacture of industrial producer gas and gas for
chemical synthesis, (4) as fuel in cement and lime kiln firing,
(5) at steel and rolling mills and (6) in a variety of specialty
and/or non-fuel uses, including industrial carbons, active car-
bon, fillers, filter aids and media, water treatment, foundry
facing, road building, roofing and coating applications, bar-
becue briquets, fertilizer and soil conditioner, coal-based
plastics, etc. Insofar as possible, information is presented on
process and product research and other developments that
may affect coal utilization, favorably or unfavorably, in the
areas cited. Since economics of coal utilization cannot be
divorced from economics of coal supply and transportation,
these are touched upon briefly. (Author's abstract)
09737
Ozolins, G. and C. Behmann
AIR POLLUTANT EMISSION INVENTORY OF
NORTHWEST INDIANA. (A PRELIM- INARY SURVEY,
1966.) Public Health Service, Durham, N. C., National Center
for Air Pollution Control, APTD-68-4, 36p., April 1968.
Sources of air pollutant emissions were surveyed to quantify
the total pollution load emitted to the air over the Northwest
Indiana communities of East Chicago, Gary, Hammond, and
Whiting The emissions are reported on an annual basis and
-------
COKE OVENS
subdivided into the five major pollutants: particulates, sulfur
oxides, nitrogen oxides, hydrocarbons, and carbon monoxide.
The four major source catagories that were utilized in report-
ing emissions from area and point sources are: fuel com-
bustion in stationary sources, fuel combustion in mobile
sources, combustion of refuse, and industrial process losses.
The results of this survey are reported by city and illustrated
on the grid system established by the Northwest Indiana Air
Resource Management Program. (Authors' abstract)
11901
Edel'man, I. I. and N. D. Khizhnyak
HARMFUL ATMOSPHERIC EMISSIONS FROM A PHENOL
PLANT. ((Vrednyye vybrosy fenol'nogo zavoda v at-
mosferu.)) Text in Russian. Koks i Khim, Vol. 5:40-42, May
1968.
The emissions from a plart for the production of phenol can
be divided into those from the storage tanks for raw materials
(products of the coke and chemical industry) and intermediate
or final products, ventilatory emissions, and emissions from
various other steps in the production process: crucibles,
crystallizers, condensers, washers, scrubbers, pressurized
supply tanks, and apparatus for the separation of pyridme
sulfate. Particular attention is given here to emissions from the
phenol-cresol works (amounting to 900 kg of hydrocarbons and
1150 kg of phenol per day), the pyridine works (264 kg of
hydrocarbons and 142 kg of pyridine bases per day), and the
naphthalene works (emission of 1500 kg/day, including about
1200 kg of naphthalene). These large amounts are due prin-
cipally to the high volatility of these compounds and the fact
that many of the procedures require high temperatures. In
order to control these losses, it is suggested that the design of
the condensers working in conjunction with the scrubbers be
improved, and that the storage tanks be equipped with absor-
bers, traps and an equilibrating system. It i- also pointed out,
however, that such measures are not always desirable under
all conditions.
13219
Masek, Vaclav
ARSENIC IN COKE. (Arzen v koksu). Hutnicke Listy
(Prague), 24(5):323-325, 1969. 18 refs.
Arsenic contained in coal used in coke ovens directly in-
fluences the quality of the coke and consequently the quality
of cast iron and steel and of electiodes. The material of prima-
ry importance is black coal, in which arsenic is not evenly dis-
tributed. Arsenic content in a combustible is determined either
by change of arsenic compounds to gaseous arsenic oxides or
by transformation of arsenic compounds to volatile arsenic
trichloride. Field testing of 35 specimens showed that the ar-
senic content is very low (0.002 to 0.005 mg/cu m). The
present average value of arsenic allowed is 0.3 mg/cu m. In all
places tested, the measured value was much lower than the al-
lowable average. Dust taken from different strata at the test
locations showed greater amounts, but still within the allowed
limits.
13330
Unterberger, O. G. and M. S. Gofman
DUST FORMATION DURING IMPACT IN HAMMER
CRUSHERS. Coke Chem. (USSR) (English transl.), no. 11:44-
48, 1968. 3 refs.
A mathematical analysis of the dust yield obtained from raw
coal mixtures crushed in hammer crushers is presented. Tests
performed with a laboratory-sized hammer crusher gave
results that were in close agreement with the theoretical ap-
proach. Two fundamentally different factors of dust formation
in hammer crushers were found: (1) free-impact dust forma-
tion, and (2) dust formation resulting from abrasion as groups
of particles slid across the working face of the hammer. The
amount of dust formed by abrasion depended on the amount
of dust in the starting mixture, and that formed by free impact
was proportional to the linear speed of the hammers.
14286
Pakter, M. K., D. P. Dubrovskaya, A. V. Pershin, and G. K.
Talalaev
MERCURY IN CARBONIZATION BY-PRODUCTS. Coke
Chem. (USSR) (English transl.), no. 11:41-44, 1968. 7 refs.
The mercury content of various carbonization products from
Soviet coke and Chemical works was checked. Mercury was
present in the precipitates from tar and tar liquor,
predominately in the form of sulfides. The tar contained ap-
proximately 40% of the mercuric sulfide. When the tar was
rectified, about 40% of the mercury was released in metallic
form. Under appropriate cooling conditions, it is liberated in
the condensing apparatus. The remainder of the tar mercury
contained mainly anthracene, oil, and pitch. Nearly all the
mercury was distilled off when hard pitch was produced. It
was established that mercury collects in significant quantities
only in coal tar, in certain precipitates, and in sulfuric acid tar.
(Author conclusions modified)
14767
Markus, G. A., Yu. G. Ozerskii, and V I. Oratovskii
DISCHARGES TO ATMOSPHERE AT THE PHENOL
WORKS. Coke Chem. (USSR) (English tanslation from Rus-
sian of: Koks i Khim.); no. 1:37-39, 1969. 9 refs.
The quantity and composition of discharges from the phenol
works were determined. Discharges come from breather valves
in operational equipment as a result of evaporation from
equipment operating under a vacuum which discharges drawn-
off gases, and from spent gas leaving the unit for springing
sodium phenolates with carbon dioxide. The vacuum pump
discharges contain hydrogen sulfide and ammonia. Impurities
such as pyridine bases, phenols, neutral aromatic hydrocar-
bons, hydrogen sulfide, and ammonia enter the common col-
lector. Measurements revealed that the volume of the gas-air
mixture discharged to the atmosphere through the collector is
600-800 cu m/hr. Two- liter samples were taken over a 30-min
period and analyzed. The fluctuations of the various contents
were ascribed to changes in the composition of the raw materi-
als that were processed and in the operating conditions of the
plants. The maximum concentrations of the noxious discharges
were calculated. The results indicated that the content of
phenols, hydrogen sulfide, and other impurities exceeded the
maximum standards and must be reduced 10-20 times. It was
concluded that work should be done to reduce the volume of
discharge by strict observance of the process conditions to en-
sure that minimum discharges and effective equipment be
developed to trap noxious impurities.
15455
Stebliy, K T., N. A. Panasenko, A. Z. Tsypin, and Yu. D.
Timofeyev
EXPERIENCE OF A PLANT IN COPING WITH SULFUR
REMOVAL. (Opyt osvoyeniya tsekha seroochistki). Text in
Russian. Koks i Khim., no. 7:36-39, 1967.
Within three months it was discovered that installations at the
Knvorozhsk Metallurgical Factory had reached their maximijm
-------
A. EMISSION SOURCES
capacity tor sulfur removal in the production of sulfuric acid.
Modifications to the system, required to cope with increased
production requirements, are described. These modifications
include the use of larger pumps, better-quality pipes, improved
irrigation of scrubbers, etc. Despite a 12-13% increase in acid
yield, a 4 g/cu m loss of H2 > to the feedback gases indicates
need for higher design capacities to allow for the H2S content
of the coke gas.
16125
Masek, V.
DEPOSITION OF COAL AND PITCH DUST ON AND
AROUND COKE OVENS. Coke Chem. (USSR) (English
translation from Russian of: Kaks i Khim.), vol. 4:29-31, 1969.
The results of investigations on the amounts of dust, the com-
position, and the method of dissemination in pitch-coke batte-
ries and coke oven batteries was described. Most of the dust
deposited on the pitch-coke batteries was in the form of spher-
ical particles with a minimum diameter of 0.3-0.5 micron. The
majority of the dust particles which settled on coke-oven bat-
teries had a characteristic crystalline structure. Samples of
dust deposited on the top of and in the vicinity of five coke-
oven batteries were analyzed. No striking differences were ob-
tained under winter and summer conditions. Homogeneous
samples were collected to determine the contents of vitrain,
clarain, durain, fusain, coke, and other constituents. It was
established that the major component is vitrain. Results
showed that with increasing distance from the battery, the
deposits contain larger proportions of particles below 0.2 mm
and smaller amounts of 3,4-benzopyrene. The highest content
of 3,4-benzopyrene was found in the pitch and dust on and
around coke-oven batteries. The amount of dust deposited on
the coke-oven batteries depends on the charging procedure.
Observations showed that ramming reduces dust emissions and
loose charging increases the emissions. The results support the
conclusion that strict adherence to battery operating instruc-
tions secures a major reduction in dust pollution. A further im-
provement can be effected by adopting the smokeless charging
technique.
17583
Sellars, J. H., Hornsby-Smith, M. P., M. R. Meades, and G. E.
C. Randell
COKE-OVEN TECHNOLOGY. Coke Gas, vol 23.411-420,
Oct. 1961. 2 refs
One of the three primary sources of smoke emissions in the
coke-oven industry is the charging operation. In view of con-
siderable differences of opinion regarding the effectiveness of
different charging methods, 200 different charging operations
were observed at seven plants. The effects of oven construc-
tion, coal characteristics, charging period, coal running period,
and levelling period on charging emissions were noted. A Mass
Emission Factor (M.E.F.), e.g., the total amount of smoke
emitted, was employed to distinguish quantitatively between
operational procedures and methods used at the various plants
Low M.E.F. values were due to a combination of factors, such
as the use of a rotating chamber for controlled feeding and
sequential hydraulic operation of the conventional charging
car. The chief conclusion of the survey was the need for
adequate suction in the gas space. This can be achieved effi-
ciently and inexpensively by means of the breeches pipe
However, even with improved suction, smokelessness cannot
be guaranteed with normal charging methods The
prerequisites for this piocedure in which a steam jet in the
ascension pipe is used to draw smoke into a gas-collecting
main are as follows adequate pull, adjustment of charging rate
in accordance with the pull; means for gas extraction at both
ends of the oven chamber; a method of loading the ovens so
that a free space exists to each gas offtake; and means for
restricting the leveller bar to prevent undue admission of air.
In the future, this tyoe of charging should be the normal prac-
tice.
19209
Masek, Vaclav and Josef Sedlak
EXHALATIONS OF COKE OVEN PLANTS. (Exhalace z kok-
soven). Text in Czech. Hutnicke Listy (Prague), 25;3):149-153,
1970. 10 refs.
The total emissions escaping from all Czechoslovak coke oven
plants in 1968 was 54 thousand tons; half of it was emitted
through chimneys and half represented ground pollution. Thus,
5.5 mg kg of emissions was exhaled per 1 ton of coke
produced. The dust content in the coke oven plants at-
mosphere is often higher than the allowed limit and contains
carcinogenic aromatic compounds. The emissions by metallur-
gic coke oven plants (two fluids of all country coke oven
plants) reached 36,500 tons in 1968. The major technological
steps to solve this unsatisfactory situation are seen in improve-
ment of design of the retorts (their charging, more effective
thermal insulation of their top floor, gas desulphurization,
etc.). By 1980 this would result in 80% decrease of total emis-
sions. With the contribution of new production based on other-
wise wasted emissions, the investment would return within 5
years.
21429
Ohme, W. and Weskamp
REDUCTION OF EMISSIONS IN COKING PLANTS. (Emis-
sionsverminderung in Kokereianlagen). Text in German. VDI
(Ver. Deut. Ingr.) Ber., no. 149:243-251, 1970. 11 refs.
The sulfur containing waste gases developing in coking plants
are usually drawn of at the point of origin so that none of
these gases can escape into the atmosphere. Certain amounts
of sulfur dioxide and sulfur trioxide do escape, howe -r, at
the sulfuric acid production stage. Treatment of hydrogen sul-
fide containing gases is exclusively limited to wet catalytic
methods. The SO3 emission in new plants may not exceed 2
kg/ton of sulfuric acid. In the coke sifting and pulverization
station of coking plants, dust is produced. The dust-laden air is
usually drawn off and cleaned in cyclones and scrubbers. Dust
emission by coking plants has been limited to 150 mg/cu m.
Coke particles are carried along by I he fumes developing at
the quenching process of glowing coke, Injection of water into
these fumes reduces the particulate matter by one third. More
recently, baffles installed in the quenching towers are used for
retaining these particles. The gases developing at the charging
process are drawn off and cleaned in a subsequent scrubber.
Discharge of the coke from the coke oven causes the highest
emissions Two separate wet collectors are used for collecting
the dust from discharging of the coke from the chamber and
for collecting the dusts from the dust fan above the quenching
cart. The collectors are installed on the coke mass cart.
Developmental work is still in process to further improve this
cleaning process.
22504
Telling, Hermann
AIR POLLUTION CAUSED BY COKING PLANTS AND
GASWORKS. (Luftverunreiningung durch Kokereien und
Gaswerke). Text in German Energietechnik, 17(12):556-559,
Dec. 1967. 11 refs.
-------
COKE OVENS
Solid and gaseous pollutants emitted by coking plants and
gasworks, existing possibilities of reducing their emission,
analytical methods available for their identification, and regu-
lations governing air pollution are discussed. Ninety percent of
the emission from anthracite coking plants originates in the
furnace and slaking plants which generate coal and coke dust,
aromatic hydrocarbons, and combustible and toxic gases like
carbon monoxide, hydrogen sulfide, sulfur dioxide, and am-
monia. Emissions from these plants vary widely, depending on
technological factors, throughput, competence of operators,
and quality of coke produced. Dust generation can be reduced
by proper handling of coal, like sprinkling with water during
unloading. The emission of pollutants during filling of the
chambers can be reduced by a reduction of the filling time
through the use of proper equipment and further reduced by
combustion or purification. At best, the gaseous pollutants can
thus be reduced by 60%. The best equipment for pollution
control in coking plants was developed by the Koppers Co. In-
struments available for the determination of dust pollution
levels include the konimeter, Cast's dust balance, and the tyn-
dalloscope; gaseous pollutants are determined by methods
based on absorption of radiation, changes of conductivity,
principles of colorimetry, and gas chromatography. The
highest median monthly permissible dust precipitation is 15 g
per sq m. The financial outlay for pollution equipment comes
to approximately 10% of the initial investment in the plant.
24195
Zaichenko, V. M., V. M. Petropolskaya, M. B. Khvat, V. I.
Melinkentsova, A. A. Karyukin, and N. V. Zadoroshnaya
HYDROGEN CYANIDE IN COKE-OVEN GAS. Coke Chem.
(USSR) (English translation from Russian of: Koks i Khim,
no. 10:52-54, 1969.
One of the forms in which nitrogen is found in coke-oven gas
is a hydrogen cyanide. A hydrogen cyanide balance sheet is
presented for a 4-battery plant with large ovens and a gas
throughput of 125 thousand cu m/h. The flowsheet considered
includes the following stages: primary coke-oven gas cooling
(in horizontal- tube coolers); ammonia recovery (in saturators
or by the evaporativ processes); final cooling; recovery of
benzole hydrocarbons with coal tar wash oil; and removal of
hydrogen sulfide by the vacuum-carbonate process. Analysis
of the sheets shows that hydrogen cyanide is a nuisance in al-
most every stage of the recovery and sulfur removal
processes. Its most serious effects are atmospheric pollution,
equipment corrosion, loss of product quality, and increased
consumption of sulfur removal reagents. The only way to
overcome these difficulties is to remove the hydrogen cyanide
before the gas enters the saturator or final gas cooler, i.e., at
the point where the hydrogen cyanide content of the gas is at
a maximum.
25214
Kutuzova, L. N., A. F. Kononenko, and Z. G. Sashevskaya
COMPOSITION OF DISCHARGES FROM COOLING
TOWERS FOR TERMINAL COOLING OF COKE-OVEN
GAS. (Sostav vybrosov iz gradiren konechnogo okhlazhdeniya
koksofogo gaza). Text in Russian. Koks i Khim., no. 7:47-49,
1970. 4 refs.
A study was made of the concentrations and quantities of
harmful impurities discharged by cooling towers of the
Zaporozhsk By-Product Coke Plant. Emissions into the at-
mosphere were established as follows (mg/cu m): hydrogen
sulfide, 28-57; hydrocyanic acid, 139-242; ammonia, 20-28;
pyridine, 12-28; naphthalene, 0.8-2.15; phenol, 4.5-6.4;
hydrocarbons, 78-185, and; carbon disulfide, 13.5-26.9 (air flow
rate, 197-220 thousand cu m/hr). Gaseous emission rates were
found to be as follows (kg/h: hydrocarbons, 24.4; H2S, 7.39;
HCN, 7.39; C6H6OH, 1.15; pyridine, C10H8, 0.36; CS2, 3.84;
and NH3, 4.75. Analogous data are also given for water
discharges.
25215
Kolyandr, L. Ya. and I. A. Fayda
SULFUR COMPOUNDS IN RAW BENZENE OF COKE-
CHEMICAL PLANTS OF THE SOUTH. (Sernistyye
soyedineniya syrykh benzolov koksokhimicheskikh zavodov Yu-
ga). Text in Russian. Koks i Khim., no. 9:36-38, 1970. 6 refs.
Head fractions, benzene, toluene, xylene, and heavy benzene
fractions produced at the Zhadanovsk By-Product Coke Plant
were analyzed for total sulfur content, as well as sulfur in the
form of carbon disulfide and thiophene. The head fraction (up
to 78 C) contained 33.2% total sulfur, 32.5% carbon disulfide,
and 0.04% thiophene. Corresponding values for the other frac-
tions were 0.59-0.62%, 0.01% (benzene fraction only), and
0.56-0.60%, respectively. It has been established that the
average relative sulfur content in raw benzene produced in by-
product coke plants in the South in 1965 was 123.7% as com-
pared to 100.0% for 1955; the increase resulted from a 4.4% in-
crease in batch sulfur content. Thiophene content of raw
benzene currently ranges as high as 1.5% and is expected to
reach close to 2% in the near future. Special efforts to deal
with this problem are urged.
26314
Kutuzova, L. N., A. F. Kononenko, and G. P. Sokul'skiy
COMPOSITION OF INDUSTRIAL EMISSIONS OF A
BENZENE RECTIFICATION INSTALLATION. (Sostav pro-
myshlennykh vybrosov tsekha rektifikats benzola). Text in
Russian. Koks i Khim., no. 8:42-44, 1970. 6 refs.
Aerodynamic losses from a standard petroleum-products
storage tank were established at about 2.5 tons per year, while
total emission of harmful substances (benzene hydrocarbons,
hydrogen sulfide, carbon disulfide, phenols, and cyanides)
from the fractionation facilities of the Zaporozhsk Coal-Tar
Chemical Plant was estimated to be about 1500 tons per year.
Losses at various stages of the fractionation process were
measured, and results are tabulated.
26441
Oglesby, Sabert, Jr. and Grady B. Nichols
A MANUAL OF ELECTROSTATIC PRECIPITATOR
TECHNOLOGY. PART II - APPLICATION AREAS.
Southern Research Inst., Birmingham, Ala., NAPCA Contract
CPA 22-69-73, 875p., Aug. 25, 1970. 118 refs. NTIS: PB 196381
The application of electrostatic precipitators is reviewed for
the electric utility industry, the pulp and paper industry, the
iron and steel industry, the rock products industry, the chemi-
cal industry, in cleaning municipal incinerator dusts, for the
petroleum industry, and in the nonferrous metals industry.
Particular emphasis is placed on the dust and gaseous emis-
sions of the processes discussed. This is followed by a tabula-
tion of input and design parameters for precipitators operating
on various types of dust control problems and an analysis of
critical design parameters and test results. Cost data are also
presented. The electrolytic reduction of aluminum, the produc-
tion of copper, primary lead, and zinc reduction are discussed
in the area of the nonferrous metals industry. In the petroleum
industry, catalytic cracking and detarring are indicated as ap-
plication areas. Refuse properties are discussed, as well as
-------
A. EMISSION SOURCES
types of incinerators. Sulfuric acid production, the production
of elemental phosphorus, phosphoric acid, and carbon black,
warrant the use of precipitators in the chemical industry. In
the rock products industry, the manufacture of Portland ce-
ment and the gypsum industry present problems. Coke ovens,
sinter plants, blast furnaces, open hearth furnaces, basic ox-
ygen converters, electric arc furnaces, scarfing machines, and
iron cupolas are areas of application in the iron and steel in-
dustry. In the pulp and paper industry, precipitators are in-
dicated for the recovery of boiler paniculate emissions and
sulfate process flue gases. Fly ash precipitators are needed in
the electric utility industry
27900
Smith. William M.
EVALUATION OF COKE OVEN EMISSIONS. Preprint, Air
Pollution Control Assoc., Pittsburgh, Pa., lOp , 1970. 3 refs.
(Presented at the Air Pollution Control Association, Annual
Meeting, 63rd, St. Louis, Mo., June 14-18, 1970, Paper 70-94.)
The composition and effects of coke oven emissions are evalu-
ated The polynuclear aromatic content of coke oven volatiles
is determined by placing the sampling unit near the larry car.
Unsubstituted polynuclear aromatics constitute between 2-3%
of the collected volatiles or between 4-6% of the benzene solu-
ble portion of the collected volatiles emitted during the charg-
ing operation. The investigation of different types of control
equipment installed at various coke oven plants in the Ruhr
valley showed that the fume control equipment on the larry
car was not operable a significant part of the time; when the
equipment was working satisfactorily, employee exposures
were less than with the uncontrolled larry cars. Studies were
also conducted to determine the most non-powered, half-mask
respirator for use in reducing the exposure to coal tar pitch
volatiles. Mechanical-filter respirators were more effective
than the chemical-cartridge respirators. Further research on
the characterization of coke plants emissions included the
development of a more refined method to permit the quantita-
tive measurement of 4 and 5-nng polynuclear aromatic
hydrocarbons, the determination of polynuclear aromatic
hydrocarbons and composition of coal tar pitch volatiles at a
number of widely scattered coke plants, and the determination
of the polynuclear aromatic hydrocarbon content of samples
taken at various distances from coke oven batteries
28641
Medvedev, K. P. and V. M. Petropolskaya
FACTORS DETERMINING THE AMOUNT AND COMPOSI-
TION OF ORGANIC SULPHUR COMPOUNDS IN COKE-
OVEN GAS. Coke Chem. (USSR) (English translation from
Russian of: Koks i Khim., no. 7:32-35, 1970. 1 ref.
A study of the basic factors responsible for the total organic
sulfur contents of raw and return coke-oven gases showed that
free-space temperature is the most significant influence on the
organic sulfur content of raw coke-oven gas. The lowest
recorded value (757 C) corresponded to the lowest organic sul-
fur content, and the highest values (797-806 C) to the highest
contents. The next most important factor is the volatile yield
of the charge; as it increases from 25.5 to 266%, only 1.1%,
the organic sulfur content of the raw gas goes from 535 to 903-
943 mg/cu m. The organic sulfur content of the return coke-
oven gas depends on the original amount in the raw gas and
the condensation and recovery techniques applied. By simul-
taneously lowering the temperatures of cooling towers and in-
creasing wash oil circulation rates, it is possible to reduce the
organic sulfur in the return gas to 300-350 mg/cu m. The
residual organic sulfur content can be reduced to 160-260
mg/cu m by compressing the return gas at 18-20 atm.
29627
Grosick, H. A.
AMMONIA DISPOSAL-COKE PLANTS. Blast Furn. Steel
Plant, 59(4): 217-221, April 1971. 1 ref. (Presented at the
Western States Blast Furnace and Coke Plant Association
Meeting, Chicago, 111., Jan. 29, 1971 and at the Eastern States
Blast Furnace and Coke Oven Association Meeting, Pitt-
sburgh, Pa., Feb. 19, 1971.)
The system of ammonia destruction proposed in 1958 as an al-
ternate to sulfate production consisted of washing thee am-
monia from the coke oven gas by means of water, distilling
the ammonia from the water, dephlegmating the vapors to a
concentration which could be burned, incineration of the
vapors in a combustion furnace and venting of the products of
combustion to the atmosphere by means of a stack. Certain
variations are proposed as a direct result of the increased
stringency of air and water pollution regulations, and in order
to minimize operating difficulties and reduce initial investment
and operating costs,. It is recommended that the gas outlet tem-
perature from the primary coolers by held as low as possible
to minimize the amount of naphthalene remaining in the gas. It
is also important that the efficiency of tar removal be main-
tained at a high level to minimize tar deposition in the
naphthalene scrubbing system. Operation of the naphthalene
scrubber without gas cooling appears to be less troublesome
and less expensive than with cooling since there is little con-
densate to be separated from the oil and the heat transfer sur-
face required for oil cooling is much greater than that required
for water cooling in the first stage of the ammonia washer.
Other variations are also cited which pertain to the ammonia
washers and benzol washers. Critical operating conditions are
mentioned, and pollution problems associated with ammonia
destruction are discussed. Of the acid gases removed,
hydrogen sulfide is of particular importance since all of the
hydrogen sulfide absorbed with the ammonia will be distilled
from the scrubber liquor with the ammonia vapor and burned
in the combustion furnace to sulfur dioxide. Many potential
customers have been concerned that the combustion of am-
monia might produce an mordinantly high quantity of oxides
of nitrogen. Stream pollution associated with the crude am-
monia liquor and its control are also discussed.
29781
Gils, Walter
MARKET DEVELOPMENT IN GAS ECONOMY. (Die Mark-
tentwicklung in der Gaswirtschaft). Text in German. Gas Was-
serfach Gas Erdgas (Munich), 112(5):215-219, May 1971.
(Presented at the Gasfachlichen Aussprachetagung, Wuerz-
burg, West Germany, 1970.)
The natural gas consumption in West Germany in 1969 was
22.7 billion cu m/4300 kcal/cu m, an increase over the previous
year of 42%. The gas supply from coking plants, remote gas
supply companies, and local gas works has doubled over the
past ten years. Natural gas is widely used in households and
industry. Since gas heating does not contribute to air pollution,
it is gaining popularity rapidly. Natural gas is also used in
remote heating plants, houses, and industry (boiler plants,
production plants in the cement and potassium industry, and
power plants). Another further application is the total energy
obtained when power is produced with the aid of a gas turbine
or gas motor and where the waste heat is used for the drying
processes.
-------
COKE OVENS
30026
Kutuzova, L. N., V. D. Sulima, V. N. Kutuzov, and P. L.
Saltan
DECONTAMINATION OF POLLUTED AIR FROM HARD
PITCH PRODUCTION PLANT. Coke Chem. USSR (English
translation from Russian of: Koks i Khem.), no. 10:49-51,
1970.
Polluted air from a pitch preparation plant was passed through
a water cooler and a 100-liter trap, where it was bubbled
through a layer of condensate to remove the aerosol and
moisture. From the trap, the air entered a 24-liter catalytic
reactor for oxidation of the residual pollutants. All catalysts
investigated (bauxite, iron oxide, copper-chromium oxide) ox-
idized tarry matter quite effectively, including its polycyclic
aromatic hydrocarbons. In addition to reducing the residual
tarry matter to a few mg/cu m, the catalytic reactor lowered
the waste gas temperature to 400-600 C At these tempera-
tures, the risk of synthesizing the carcinogenic hydrocarbons
is avoided.
36379
Roussel, A. A. and H. Stephany
CONTINENTAL REPORT: EUROPE. International Union of
Air Pollution Prevention Associations, Intern Clean Air
Congr., Proc. London, England, 1966, p 29-34. (Oct 4-7,
Paper II/6.)
The problem of air pollution in Europe is reviewed with
respect to emission sources, geographical and population fac-
tors, specific pollutants, research programs, and legislation.
Major emission sources include industrial plants, power sta-
tions, iron works, metallurgical plants, coke oven plants,
petroleum refineries, cement plants, chemical processing,
domestic heating, and motor traffic. The most important emis-
sions include dusts, fumes, sulfur dioxide, soot, and carbon
monoxide. Air pollution control legislation is reviewed for Ger-
many, Britain, Belgium, the Netherlands, Italy, and France.
37713
Masek, Vaclav
NEW FINDINGS CONCERNING THE PROPERTIES OF FLY
DUST FROM COKING PLANTS. PART !: PHYSICAL-
CHEMICAL PROPERTIES. (Neue Erkenntnisse ueber die
Eigenschaften des Flugstaubes aus der Kokerei. Teil I
Physikalisch-chemische Eigenschaften). Text in German. Zbl.
Arbeitsmed , 22(2):38-47, Feb 1972. 20 refs.
With every ton of coke that is produced, 0.5 to 2.0 kg fly ash
are obtained as a waste product. The properties of this fly dust
were studied on three samples taken in summer 1970 from the
NHKG- coking plant in Ostrava-Kumce. The sorption proper-
ties were examined at temperatures between 22 to 20 C after
boiling the dust sample is distilled water at a pressure of '.00
to 150 mm Hg and withdrawing the water afterwards The ion
exchange capacity of the dusts was determined by conduc-
tometry according to Sandhoff Furthermore the electrokmetic
potentials, the magnitude of adsorption of several gases and
vapors, the catalytic properties, and the crystalline quartz
modification was determined. The sorption properties of the
dust in most cases did not reach the capacity of ordinary fil-
tering paper They also have a relatively low exchange capaci-
ty in particular for sodium, potassium, and ammonia. The elec-
trokinetic potentials of the particles aie positive, however, and
rather low. Like the sorption properties the adsorption capaci-
ty for gases and vapors is very low At the dissociating
hydrogen peroxide reaction, the contact catalytic properties of
all dust samples were rather weak The fly dust had very little
activity.
38526
Thoenes, Hans Willi and Wolfgang Guse
CARBON MONOXIDE EMISSION IN INDUSTRIAL AREAS.
(Kohlenmonoxid-Emissionen aus Industriebetrieben). Text in
German. Staub, Reinhaltung Luft, 32(2):50-52, Feb. 1972. 3
refs.
The carbon monoxide emission by steam boilers, cupola fur-
naces, the chemical and petrochemical industry, and coking
plants is discussed. The Federal Republic of Germany has
1800 cupola furnaces which emit considerable amounts of CO.
For instance, as continuous and discontinuous measurements
showed, a cupola furnace with a nominal capacity of 15
tons/hr produces 20,000 cu m waste gas/hr of which 4% by vol
(982 kg/hr) are CO. An observation of the firing process
revealed that the CO concentration decreased drastically
whenever overhead firing occurred during charging. In the
chemical industry CO emissions occur when the gas pipes are
leaky or at cleaning or scrubbing processes of the organic
products for which CO was used, e.g., methanol or formal-
dehyde. According to U. S. statistics, 50 g CO are emitted/kg
formaldehyde produced. In coking plants CO is emitted during
the charging of the furnace. Measurements revealed that con-
centrations of more than 5.4% by vol are not emitted longer
than 1 min
38657
Fuhrmann, N.
PROBLEMS OF ENVIRONMENTAL PROTECTION IN
BASIC-INDUSTRY PROCESSING PLANTS. (Probleme des
Umweltschutzes bei verfahrenstechnischen Anlagen der
Grundstoffmdustrie unter besonderer Beruecksichtigung geset-
zlicher Vorschnften zur Luftreinhaltung und Laermbekaemp-
fung) Text in German. Aufbereitungs-Technik, 12(12):757-763,
Dec. 1971. 25 refs.
Branches of industries such as cement plants, soft and hard
coal briquetting plants, cokeries, and iron ore sintering plants
are large air polluters. Great efforts have been undertaken to
reduce emission. In the cement industry, for instance, the
average dust emission dropped from about 3.5% in the year
1950 to 0 15% of the clinker production in 1967. Over the same
period the clinker production rose from 11 million tons to 33
million tors. The technical directives limit the dust emissions
by cemenl grinding stations to 150 mg/cu m The gaseous
emissions from cement plants are negligible. The soft coal
briquetting plants of the German Democratic Republic emitted
about 260.000 tons of dust in 1967 In hard coal briquetting
plants the emission of benz.o-3,4-pyrene must be mentioned in
addition to the dust emission. Cokeries emit dusts, tar
aerosols, and gases, particularly hydrogen sulfide and sulfur
dioxide. In 1956 the SO2 emission by these plants amounted to
56,000 tons. Through scavenging of the gases, the SO2 emis-
sions can be greatly reduced. In iron ore sintering plants, dust
and SO2 are emitted. The SO2 concentration in the uncleaned
gas may reach 10 g/cu m. At an annual production of 20 mil-
lion tons of sinter, about 210,000 tons of SO2 are emitted.
These plants also emit fluorine. The federal government
drafted a law expanding its constitutional rights to include the
fields of water pollution, maintenance of clean air, and noise
abatement. Flmission limits for basic industry processing plants
are included in the technical directives pertaining to air.
40159
Brandt, A. D. and D. M. Anderson
MEASURES AGAINST AIR POLLUTION CAUSED BY IN-
DUSTRIAL SOURCES. (De strijd tegen de luchtvervuiling af-
komstig van industnele bronnen). Text in Dutch. Polytech.
-------
A. EMISSION SOURCES
Tijdschr., Ed. Procestechniek (The Hague), 27(7):231-237,
1972. 26 refs. (Presented at the Environmental Control
Seminar, Rotterdam, Netherlands, May 25-26, 1971).
A general survey is given of air pollution from industrial
sources in the United States, with special regard to particulate,
gaseous, and fluorine pollution. The contribution of industry to
air pollution was 14% with 30 million tons in 1968. Particulate
pollutants are most important, followed by sulfur dioxide,
hydrocarbons, carbon monoxide, and gaseous and particulate
fluorine compounds. To effectively control air pollution, im-
proved source localization techniques are required. General
principles and uses of pollution control equipment such as
cyclones, tissue filters, scurbbers, and electrostatic filters are
reviewed. Contributions of several industries to particulate and
gaseous pollution in 1967 are reviewed. Quarrying, gravel, and
sand processing was the major source of particulate emissions
with 4.6 million tons, followed by grain mills with 2.952 million
tons. Compared to other industries, a high proportion of the
emission sources is localized in the iron and steel industry,
(1.490 million tons). Cokeries are a major source of HC emis-
sions. The respective contributions by the paper and asphalt
industries were 633,000 and 522,000 tons. The joint share of
the cement and lime industries is 744,000 tons, followed by
foundries with 217,000 tons. Brick manufacturing was respon-
sible for the bulk of fluorine emissions. The chief sources of
sulfur dioxide, carbon monoxide, and hydrocarbon emissions
were primary nonferrous smelting (2,940,000 tons from the
copper industry alone), petroleum refining (6.2 million tons),
and petroleum products processing (1.1 million tons), respec-
tively.
40340
Mallette, Frederick, S.
A NEW FRONTIER: AIR POLLUTION CONTROL. Proc.
Inst. Mech. Engrs. (London), 1954:595-615, April 9, 1954. 60
refs.
Areas in the United States and Canada where definite accom-
plishment of significant developments were made m air pollu-
tion control are discussed. Legislative developments which
brought about reduced air pollution are presented. Model or-
dinances include those in St. Louis, Mo., Pittsburgh, Pa., New
York City, and Los Angeles County, Calif. The influence of
meteorological factors upon the dispersion or accumulation of
air pollutants is apparent, but an understanding of the funda-
mental factors, other than wind, is just being reached. Tem-
perature, lapse rates, stability, and smog influence pollution.
The highlights of the Donora, Pa. smog of 1948 are presented.
A description of the control procedures and equipment
presently in use there are given, together with a statistical
analysis of the air sampling and meteorological data which is
collected. The development of instrumental methods and
socio-ecomonic aspects are also discussed. Problems of the
iron and steel industry include emissions from coke ovens,
blast furnaces, open hearth furnaces, bessemer converters,
and electric furnaces. Power production, chemical processing,
and the rubber industry also cause pollution.
41877
Herrick, R. A.
BACKGROUND INFORMATION FOR ESTABLISHMENT OF
NATIONAL STANDARDS OF PERFORMANCE FOR NEW
SOURCES: IRON AND STEEL INDUSTRY. Environmental
Engineering, Inc , Gainesville, Fla., and Herrick Associates,
Reston, Va., Environmental Protection Agency, Division of
Abatement Contract CPA-70-142, 107p., March 8, 1971. 40
refs.
Process conditions common in iron and steelmaking are out-
lined. Emissions of particulates, sulfur oxides, nitrogen oxides,
fluorides, polycyclic organic matter, total reduced sulfur,
odors, carbon monoxide, and visible emissions are discussed
for the processes and the optimum control devices are
identified where possible. The basic oxygen furnace and the
electric furnace are expected to become the only significant
factors in steel production over the next 20 years. There are
no EOF installations in the U. S. that do not have air pollution
control devices. Control in electric furnace steelmaking is
usually handled by canopy heads and sometimes by roof
evacuation. The gases from both processes are usually con-
ducted to gas cleaning systems. Recommended standards of
performance for the EOF can be written in terms of particu-
late emissions. A concentration no greater than 0.020 grs/scf
should be the maximum. Gas cleaning installations cannot in
most cases maintain acceptance specifications. Electric fur-
nace steelmaking should be restricted to a standard of one Ib/t
of steel produced.
43346
Parker, Albert
ESTIMATES OF AIR POLLUTION IN THE UNITED KING-
DOM IN THE YEAR 1970- 71. Clean Air, 1(6):18-19, 1972. 1
ref.
Energy generation and smoke and sulfur oxide emission from
fuel combustion and emissions of carbon monoxide, hydrocar-
bons, aldehydes, nitrogen oxides, and SOx from petrol and
diesel engines are estimated and tabulated for the United
Kingdom in 1970-1971. Smoke and SOx concentrations
generated by combustion of coal for fuel in domestic heating,
railways, coal mining, electric power stations, coke ovens, the
gas supply industry, carbonization plants, and fuel plants
equaled 0.72 and 3.40 million metric tons, respectively. Coke
combustion for domestic and industrial sources contributed
0.17 million metric ton of SOx. The use of oil for power
sources in domestic, industrial, and commercial sources, the
gas supply industry, road transport, railways, and marine craft
resulted in emissions of 6.07 million metric tons of SOx.
Equivalents for hydro-electricity, nuclear power generation,
and natural gas are included. Petrol and diesel engines, respec-
tively, emitted 6.7 and 0.11 million tons of CO; 0.34 and 0.021
million tons of hydrocarbons; 0.01 and 0.003 million tons of al-
dehydes; 0.23 and 0.07 million tons of NOx; and 0.025 and 0.04
million tons of SOx. The amount of lead in the compounds
discharged in exhaust gases from petrol engines was estimated
at about 6000 tons
44028
Bhattacharya, R. N. and P. Bhattacharya
ANALYSIS OF COKE OVEN GAS BY VAPOUR PHASE
CHROMATOGRAPHY. Indian J. Technol. (India), 9(6):219-
223, June 1971. 11 refs.
A simple, rapid, and accurate method for the analysis of gas
obtained during the carbonization of coal is described. Coke
oven gas consists primarily of hydrogen, methane, carbon
dioxide, carbon monoxide, ethane, propane, and various
olefins. Complete analysis of the individual components
present in the sample is done by a combination of gas-solid
and gas-liquid chromatographic techniques employing different
columns, e.g., alumina, dinonylphthalate, and beta, beta-ox-
ydipropiomtrile. Quantitative data on typical gas samples ob-
tained from test runs carried out in pilot plants are presented.
Details of the procedure adopted for the collection of samples
and preparation of the stationary phases and column packing
are given. (Author abstract modified)
-------
8
COKE OVENS
45461
Smith, William M.
EVALUATION OF COKE OVEN EMISSIONS. J. Occup.
Med., 13(2):69-74, Feb. 1971. 1 ref. (Presented at the American
Iron and Steel Institute, General Meeting, 78th, May 28, 1970.)
In 1965 the American Conference of Governmental Industrial
Hygienists adopted a tentative threshold limit value for em-
ployee exposures to the benzene-soluble fraction of coal tar
pitch'volatiles. Comparison of glass fiber, cellulose acetate
membrane, and silver membrane filters for the collection and
measurement of the benzene-soluble fraction, made by the
State of Pennsylvania, established that silver membrane filters
were most effective. The sampler and methods of collection
and analysis are described. An American Iron and Steel In-
stitute research program evaluated the efficiency of silver
membrane filters, and an attempt was made to determine the
composition of the benzene-soluble fraction with particular
emphasis on polynuclear aromatics. A six-man survey team
was organized by AISI to go to Germany to investigate the ef-
fectiveness of the different types of control equipment in-
stalled at various coke plants in the Ruhr Valley. An ac-
celerated respiratory protection program is described, and
results are given of extended research on the characterization
of coke plant emissions. The design and testing of a powered
air purifying respirator for coke oven workers are considered,
as well as the criteria for the threshold limit value for coke
oven emission.
46920
Masek, Vaclav
NEW FINDINGS CONCERNING THE PROPERTIES OF FLY
DUST FROM COKING PLANTS. III. PITCH COKING.
(Neue Erkenntnisse ueber die Eigenschaften des Flugstaubes
aus der Kokerei. Teil III. Pechkokerei). Text in German. Zbl.
Arbeitsmed., 22(9):276-281, 1972. 11 refs.
Fly dust samples from the vicinity of a pitch coking plant were
used for determination of the current potential, the contact-
catalytic influence on the hydrogen peroxide-dissociation, the
sorption properties of original, hydrolyzed, and aged dusts, the
gas vapor adsorption, the importance as a nutritive substance
for plants, the influence on the inversion of sucrose by mver-
tase, and the radioactivity. For determination of the current
potential a standard chloride solution was prepared with which
the dust samples remained in contact for three days. For the
three samples, current potentials of plus 4 mV, plus 3 mV and
minus 4mV were calculated. All samples were rather inactive
catalytically primarily the sample from the upper part of the
block. The original, hydrolyzed, and aged fly dust samples all
had rather low sorption properties. The nutritive substances
contained in the fly dust samples were liberated to a minor ex-
tent only in aqueous solutions. None of the dust samples in-
fluenced the enzymatic reaction of sucrose inversion by inver-
tase. Thus the dusts found in the vicinity of pitch coking
plants must indeed be counted as undesirable components of
the atmosphere.
48279
Pitt, R. S.
STEELMAKING AT PORT KEMBLA. Iron Steel, 45(5):527-
534, 535-540, Oct. 1972.
The Port Kembla steelworkers in Australia are discussed. The
development of the steel industry in Australia, the growth of
steel consumption, and the layout of the plants are reviewed.
The steelworks complex consists of sinter plants, coke oven
batteries, blast furnaces, open hearth and electric steelmaking
shops, an ingot mould foundry, plate an/ hot strip mills, and a
steel strapping line. The operation and cooling of the furnaces
is described. A tar and naphthalene recovery plant, gas clean-
ing systems including dust catchers and wet scrubbers for the
furnaces, rolling and finishing services, plate finishing and tin-
plate production, and personnel training are reviewed. The
Port Kembla Works are in the process of expansion, having al-
ready increased the steelmaking capacity by the addition of
new blast furnaces, a basic oxygen plant, and rolling and
finishing services. Costs of installing the new facilities are
reviewed.
48336
Enik, G. I., T. I. Markina, and I. L. Vangnits
SIFTINGS OF STAVROPOLIC COALS AS RAW MATERIAL
USED TO PRODUCE SMOKELESS FUEL. (Otsevy Stavropol
skikh ugley kak syr ye dlya polucheniya bezdymnogo topliva).
Text in Russian. Tr. Inst. Goryuch. Iskop., Moscow, 26(1):68-
73, 1971. 9 refs.
A new cokery was designed for the conversion of sittings
from Stavropol coals into smokeless coke by applying a con-
tinuous coking process with oxidative pyrolysis. The sittings,
with 40-70% below 13 mm, contained 17-32% of ash and 37-
43% of volatiles. Sittings from different mines were mixed to
secure good agglomeration and sufficient strength of the coke.
Coking was done in a temperature range of 600-700 C. The
thickness of the plastic layer was 6-13 mm; the swelling num-
bers ranged from 8 to 40. The coke had a volatile content of
about 0.6-11.4% and an ignition temperature of 350-380 C. The
coke was in the form of 13-50 mm large particles.
-------
B. CONTROL METHODS
01767
G. N. Lebedeva, V. S. Patrikeev, S. B. Kotlik, V. R.
Shevchenko, and N. P. Pervushina
THE AMMONIA METHOD FOR REMOVING HYDROGEN
SULPHIDE FROM COKE-OVEN GAS. Coke and Chem.
USSR English transl. (3) 32-7, 1966.
A laboratory-scale system for the ammonia purification of
coke-oven gas with a high H2S content (28g/cum) was
developed. It consists of successive recovery of H2S from the
gas in a cyclic process by contact with ammonia water. Am-
monia was added at a rate sufficient to replenish the desul-
furizing cycle. Under these conditions H2S recovery reached
97% at 20-26 C but fell to 85% at a temperature of 28-30 C.
Ammonia entrainment with the acid gases was 2.5%. Calcu-
lated as percentage of the ammonia in the coke-oven gas, the
ammonia entrainment with the acid gases was 10%, and thus
the ammonia content of coke-oven gas was many times greater
than the amount required to recover H2S.
02025
R. L. Cooper and G. W. Lee
ALLEVIATION OF AIR POLLUTION IN THE COKING IN-
DUSTRY. Proc. (Part I) Intern. Clean Air Cong., London,
1966. (Paper V/l). PP. 117-9.
The problem of air pollution at coking plants is the subject of
investigation by the industry, its Research Association and the
Alkali Inspectorate. A method has been devised for estimating
smoke emission during oven charging and used to demonstrate
the effectiveness of measures adopted for its mitigation mea-
sures that include modifications of charging procedure and the
use of breeches pipes for those batteries operating with single
collecting mains. Grit emitted from quenching towers is
minimized by installing grids or sprays and dust emitted during
the handling of coal and coke is reduced by the use of sprays,
hooding and dust extraction equipment. A method is being
developed to assess the relative magnitude of grit and dust
pollution from sources in the neighbourhood of coking plants.
To enhance the industry's contribution to clean air, investiga-
tions are being conducted into the production of reactive oven
cokes for the open grate and domestic boiler. (Author abstract)
02728
A. D. Brandt
CURRENT STATUS AND FUTURE PROSPECTS-STEEL IN-
DUSTRY AIR POLLUTION CONTROL. Proc. Natl. Conf. Air
Pollution, 3rd, Washington, D.C., 1966. pp. 236-41.
Air pollution control at blast furnace operations, in general, is
excellent. The most important single contributor of particulate
air pollutants in the steel industry today, namely, the steel-
making furnaces, is being brought under control rapidly and
effectively as a result of the change in steel-making technology
whereby uncontrolled conventional open hearth furnaces are
being replaced by Basic Oxygen Furnace equipped during con-
struction with adequate air pollution control facilities The na-
ture of the equipment and procedure currently employed in
making coke for the steel industry does not permit complete
control of the air pollutants created by such operations. A
technological breakthrough is essential to the attainment of
adequate and satisfactory air pollution control at coke-making
operations. Technological improvements are needed to permit
effective and practicable control of the sporadic air pollution
created when high winds blow across stock piles of coal, ore
and stone. The steel industry has made noteworthy progress in
air pollution control in recent years and presently is engaged in
a program of control which will make steel plants relatively
free from major particulate air pollution problems by the end
of the next decade. (Author summary)
03204
W. Ehnert.
THE BEHAVIOR OF NITRIC OXIDE DURING ELECTRO-
STATIC GAS PURIFICATION. Uber das Verhalten des
Stickstoffmonoxids bei der elektrostatischen Gasreinigung.
Brennstoff-Chem. (Essen) 9(7):273-274, Sept. 1966. Translated
from German as JPRS R- 8584-1).
The effects of field intensities, ionizing-electrode diameters,
period of stay of the gas in the electrostatic purifier, concen-
trations of nitric oxide in the gas, and the presence of unsatu-
rated compounds upon the decomposition of nitric oxide were
measured by means of an experimental electro-filter situated
in coke oven plant. Within the range of 3 to 3.8 kv/cm, the
quantities of NO decline with increasing field intensity, this
decline amounting to only about 10 to 20% at the field
strengths of 2 to 3 kv/cm which are commonly used in coke-
oven installations. Industrial-economic considerations however
place a limit on the extent to which voltages can be increased
in practice. The period during which the gases remain in the
filter is a factor in the icduction of NO content, but a doubling
of this period from 6 to 12 seconds results in a maximum in-
crease in the decomposition rate of only 25%. The reduction m
NO tends first to decline and then to increase as the diameter
of the ionizing electrode is increased. The most effective fac-
tor in the reduction of NO contents is the addition of unsatu-
rated compounds; thus the addition of 2.5 ml cyclopentadiene
cu/m of gas increases the loss of NO by a factor of 4 under
certain experimental conditions. The experiments show that
current commercial coke-oven practice results in reductions of
about 20% in NO content, and that an increase in the field
strengths together with a rise in the unsaturated-compound
contents can effect reductions of 50-60%.
03238
A. Z. Tsypin
WASHING THE GRID PACKINGS OF SULPHUR SCRUB-
BERS. Coke Chem. (USSR) (English Transl.) (4) 42-5, 1966
This paper describes washing, in a plant in Knvoi Rog, the
pinewood packing of sulfur scrubbers with soda solutions in
four cycles with maximum g/1 alkalimties of 10, 20-25, 30-35,
and 50, taking 30-35 days for the complete process, the length
of each cycle being determined by the change in the total con-
tent of fatty and tarry substances in the solution. Moisture,
-------
10
COKE OVENS
Na2CO3 and impurities NaCl and Na2SO4 were determined in
the soda being used. The foam-forming capacity of the wash-
ing solution was also determined once a day. Various impuri-
ties removed by the washing were determined at various inter-
vals. The author suggests bringing in a working solution from
outside containing working concentrations of ballast salts to
wash the packing without leaching. He also suggest that a
study should be made of the feasibility of using foam-breaking
additives and using ballast salts in the form of an imported
solution for starting up a plant.
04396
L. H. Engels
FEED GAS CLEANING IN COKE-OVEN LARRY CARS.
STAUB (English Transl.) (Duesseldorf) 26, (11) 23-31, Nov.
1966. Ger. (Tr.)
The problem of feed gas cleaning in coking plants is outlined.
After a description of technological processes occurring in
coal carbonization, various methods for gas removal and gas
cleaning are shown, and especially difficult operating condi-
tions and the problem of output measurements to assess the
efficiency of the method used are also discussed. Factors in-
fluencing the efficiency of known dust cleaning methods (size
and design of ovens , type and composition of coal etc.), and
the measuring results available are considered. Finally, the
costs of investment, maintenance and operation are given.
(Author summary)
04581
I. M. Khanin, V. I. Yakovlev, M. B. Kartsynel
A SPRAY-TYPE BENZOLE SCRUBBER WITH RADIALLY-
SLOTTED GAS DISTRIBUTORS. Coke Chem. (USSR) (English
Transl.) (1) 30-5, 1965. Russ. (Tr.)
The aim was to present the results of a study of the
aerodynamics of a new stage-type benzole scrubber with radi-
ally- slotted gas distributors. It has been found that: 1. The
radially-slotted distributors distribute the stream quite evenly
across the scrubber, irrespective of how the gas is supplied
(radially alpha equlas 0 degrees, along a secant alpha equal 35
degrees, or tangentially alpha equals 90 degrees); 2. Increasing
the number of plates in the top and bottom rows of the dis-
tributors from 8 to 16 does not affect the distribution of the
gas; 3. The gas distribution through the scrubber is impaired
by increasing the depth of the slots between the two rows of
plates. Although reducing the depth of the slots improves the
distribution, it also increases the resistance of the scrubber; 4.
The distribution of the gas improves noticeably as it passes
through the distributors. There is no doubt that recovery im-
proves as the number of distributors (and, consequently, the
number of stages as well) increases; 5. Increasing the flow rate
of the gas does not substantially affect the pattern of its dis-
tribution across the scrubber. However, the resultant increased
turbulence of the gas jets emerging from the distributor slots
improves the absorption; and 6. The resistance of a commer-
cial stage-type scrubber with a gas throughput of 84670 cu m/h
would be 53 mm water gauge. (Author conclusions modified)
04634
T. P. Varshavskii, A. M. Denisov, L. E. Zlatin, and K. V.
Zolotarev
SMOKELESS CHARGING OF COKE OVENS. Coke Chem.
(USSR) (English Transl.) (6) 26-31, 1965. Russ. (Tr.)
A pilot-commercial smokeless charging plant has been built on
No. 1 battery at the Kemerovo Coke and Chemical Works
along the lines of those at VUKhIN and the Magnitogorsk In-
tegrated Iron and Steel Works. A new smokeless oven charg-
ing system has been devised and introduced on the No. 1 bat-
tery at the Kemerovo Coke and Chemical Works based on
separate consecutive emptying of the charging-car hoppers
(4,3,2 and 1) with suction of the charging gases only into the
coke side collecting main. The possibility of the saleable tar
being contaminated with ash or heavy tar products has been
eliminated. 4.0 tons/day of high-ash tar was obtained from the
coke side collecting main. The nitric oxide content of the raw
gas from No. 1 battery is 16.5 cc/cu meter. Accordingly it is
vital to solve the problem of how to remove the nitric oxide
from the charging gases or how to isolate and utilize them
without purification. The satisfactory operating results of the
plant enable this system to be recommended for works which
do not supply gas to nitrogenous fertilizer undertakings.
(Author conclusions)
05432
A. C. Bureau and M. J. F. Olden
THE OPERATION OF THE FRODINGHAM DESULPHURIS-
ING PLANT AT EXETER. Chem. Eng., (206):CE 55-CE, Mar.
1967.
Data are presented on the operation of a desulfurizing plant
for coke oven gas whose design was based on pilot plant stu-
dies. Coke oven gas was desulfurized by 16-100 mesh iron
oxide in a reactor at 350-400 C. The iron sulfides formed were
oxidized in a fluidized regenerator with air for reuse. The
ffluent sulfur dioxide was recovered as sulfuric acid in a con-
tact plant. The removal of hydrogen sulfide reached 99.9%
with inlet concentrations of 533-640 grains per 100 cu ft. With
the organic sulfur, concentrations at the inlet of 12.9-19.0
grains per 100 cu ft, the removal was 68-79% of the total. Of
the organic sulfur, the thiophene removal was from 26-46%.
Continuous, concurrent removal of hydrogen sulfide and the
organic sulfur compounds was proved to be feasible during the
operation of the plant which was closed for economic reasons.
It was apparent that a redesign and simplification of the
process would be necessary to obtain guaranteed continuous
operation. Also, the preferred method of gas production today
is based on the use of light distillate in a process which in-
cludes desulfurizing and detoxification stages without a sub-
sidiary plant.
06576
RESTRICTING EMISSION OF HYDROGEN SULPHIDE AND
OTHER SULPHUR- CONTAINING COMPOUNDS, EXCEPT
SULPHUR DIOXIDE, FROM GAS GENERATORS IN COKE,
GAS, AND COAL-CONSTITUENT PROCESSING PLANTS.
(Gasauswurfbegrenzung Schwefelwasserstoff und andere
schwefelhaltige Verbindungen ausser Schwefeldioxyd Kon-
kereien und Gaswerke, Kohlenwertstoffbetriebe.) VDI (Verein
Deutscher Ingenieure) Kommission Reinhaltung der Luft,
Duesseldorf, Germany. (VDI No. 2109.) (May 1960). 21 pp.
Ger. (Tr.)
In coke and gas plants, dust, tar, mist and gas are emitted dur-
ing several production stages. This VDI Specification concerns
the emission of hydrogen sulphide and other sulphur contain-
ing compounds not including sulphur dioxide, by coal-con-
stituent processing plants. The essential points treated herein
are the occurrence of hydrogen sulphide and other sulphur-
containing compounds not including sulphur dioxide; measures
for the reduction of emissio(; and guide lines for the restric-
tion of emission. Careful maintenance and control in operation
must make sure that all equipment, lines and installations are
tight. In case of operational failure, devices must exist which
prevent the gases containing hydrogen sulphide from escaping
-------
B. CONTROL METHODS
11
into the open air. This may be effected, for example, by
reconducting such gases at a suitable point into the gas system
of the coke plant. Ventilation gases existing in current opera-
tion must be prevented from constituting a risk in a similar or
other manner to such an extent that the permissible immission
concentration is not exceeded. During cleaning and repair, any
waste-water containing hydrogen sulphide must be adequately
diluted, if necessary
06577
RESTRICTING EMISSION OF SULPHUR DIOXIDE FROM
COKE OVENS AND GAS PLANTS. (Gasauswurfbegrenzung
Schwefeldioxyd Kokereien und Gaswerke Koksofen (Abgase).)
VDI (Verein Deutscher Ingenieure) Kommission Reinhaltung der
Luft, Duesseldorf, Germany. (VDI 2110.) 20 pp. (Aug. 1960).
Ger. (Tr.).
This specification concerns the emission of sulfur dioxide with
the waste gases created by the firing of the coke ovens. The
essential points treated herein are the type, composition and
calorific value of the different underfeed gases as well as
guide values for sulfur-dioxide emission; measures for reduc-
tion of emission and low-layer concentration of sulfur dioxide;
and guide lines for the restriction of sulfur-dioxide emission.
06585
RESTRICTING EMISSION OF DUST, TAR MIST AND GAS
WHEN CHARGING COKE OVENS. (Auswurfbegrenzung fur
Staub, Teernebel und Gase beim Fullen von Koksofen;
Kokereien und Gaswerke.) VDI (Verein Deutscher Ingenieure)
Kommission Reinhaltung der Luft. Duesseldorf, Germany.
VDI 2302.). 32 pp. (June 1962). Ger. (Tr.)
This specification concerns the restriction of emission of dust,
tar mist, and gas when charging coke ovens with coking coal.
The technology, emissions, and the reduction of escape gas
emission by reconducting the escape gases into the raw gas,
combustion, and scrubbing are reviewed.
06650
Kuleshov, P. J.
AERODYNAMIC INVESTIGATION OF ELECTROSTATIC
PRECIPITATOR C-180 MODEL. U.S.S.R. Literature on Air
Pollution and Related Occupational diseases, Translated from
Russian by B. S. Levine, Vol. 7, 21-30, 1962. (Koks i Khim.)
(12) 30-5, 1958. CFSTI: 62-11103
The purpose was to arrive at practical changes which might ef-
fect better gas flow distribution over the electrofilter cross
section and thereby reduce its pressure drop and enhance its
gas purifying efficiency. The A model was made of plastic
material on 1.10 scale. Air flow through the model precipitator
was created by a fan which forced through the model over
1000 cu m of air per hour. The effects of 'live' area of the
lower perforated distribution screen of the inflow conduit in-
side location of the double T-shaped supports on gas flow dis-
tribution and on pressure drop reduction were studied. As a
result of such investigation the following 2 changes have been
introduced; a) the inside protudmg angular downward directed
part of the gas inflow condiut has been abolished; b) the
original perforated gas distributing screen No. 1 which had an
open area amounting to 18% of the total screen area was
replaced by screen No 2, the open area of which amounted to
28% and in some cases by screen No. 3, with an open area of
35.0%
06651
Kuleshov, P. J.
RAISING THE EFFICIENCY OF ELECTROSTATIC
PRECIPITATORS, TYPE C - 140. (Koks i Khim) (4) 45-9,
1956. U.S.S.R. Literature on Air Pollution and Related Occu-
pational Diseases, Translated from Russian by B. S. Levine,
Vol. 7, 30-7, 1962. CFSTI: 62-11103
A criterion for the determination of gas flow distribution over
the cross section of a precipitator by a single value is
described. The comparison of individual tests and the
complete evaluation of their characteristics were of im-
portance; the coefficient of uneven gas flow distribution -
C.U.D., was developed to characterize the deviation in rate of
gas flow from the median. Several ways of gas delivery were
studied in an attempt to lessen their effect on gas flow
velocity distribution. Most of the research was on appropriate
perforated screen construction. Several types of distributing
screens were studied; with a 'live' (perforation) areas of
geometric dissimilitude. The effect of fastening the lower ends
of precipitating electrodes on the productivity of the electro-
static precipitators was studied. The upper distributing screen
had no effect on the distribution of the gas flow across the
electrostatic precipitator, and should be removed. Removal of
the gas delivery extension from inside the electrostatic
precipitator reduced the pressure drop and improved the gas
flow distribution A distribution screen with a variable 'live'
area (geometric dissimilitude type) and with larger openings at
its periphery considerably improved the gas flow distribution.
The best gas flow distribution over the electrostatic precipita-
tor cross section was attained with a screen having a large
(32%) and even 'live' (opening) section over its entire area and
a ring-shaped slit at its periphery. The resistance of this screen
was low, it was easily machined and its installation is recom-
mended in all industrial electrostatic precipitators. The installa-
tion of this screen in an industrial electrostatic precipitator in-
creased its productivity by 100% without noticeable lowering
in its gas purifying efficiency. Such increases in the produc-
tivity of the electrostatic precipitators makes possible a 40%
saving in equipment investment. Fastening of the precipitating
electrodes onto the partition walls considerably improved the
gas distribution and lowered the hydraulic resistance (pressure
drop)
06652
P. J. Kuleshov
CONSTRUCTION DEFECTS IN TUBULAR ELECTRO-
STATIC PRECIPITATORS (ELECTROFILTERS). U.S.S.R.
Literature on Air Pollution and Related Occupational Diseases,
Vol. 7, 38-44, 1962. (Koks i Khim.) (1) 43-6, 1958. Russ. (Tr.)
The construction defects in the tubular electrostatic precipita-
tors C-140 and C-180 used in coke-chemical plants are
analyzed and suggestions are made for their elimination. The
defects reviewed are: insulating boxes and insulators; corona-
electrodes and field tension; inoperative electrodes; gas dis-
tribution, cut-off slide gates or valves; oxygen content deter-
mination; gas load and designed production capacity.
06654
Semenov, P A., Yu. V Tumanov, and O. S. Chekhov
A VENTURI APPARATUS FOR AMMONIA ABSORPTION
FROM COKE GAS WITHOUT AN ATOMIZER. U.S.S.R.
Literature on Air Pollution and Related Occupational Diseases,
Vol. 7, 47-53, 1962. (Koks i Khim.) (8) 34-7, 1960. Translated
from Russian. CFSTI: 62-11103
-------
12
COKE OVENS
The most advantageous way of ammonia absorption from coke
by sulfuric acid by means of Venturi absorbers (minus the
atomizers) is discussed. The injection liquid is carried by the
gas flow itself. Mass transfer in the gaseous phase was studied
by the method of water absorption of ammonia from the air-
ammonia mixture. Simultaneously the pressure drop was stu-
died in relation to the flow rate of the gas through the Venturi
throat and rate of spray. Ammonia concentration was varied
from 0.5 - 2.0% by volume. Velocity of air ammonia mixture in
the Venturi tube throat ranged from 30.0 to 72.5 m/sec. Three
types of venturi apparatus were investigated; the throat diame-
ter in each measured 20 mm, length of throat 3 mm, and the
conical diffusor angles were 8, 17 and 30 deg. With the spray
rate equal in all cases and varying the gas flow rate the
productivity coefficient of the three apparatuses in all in-
stances was the same; the conical diffusor angle had no effect
on the degree of ammonia absorption. The data on mass
transfer obtained with experiments in water absorption of am-
monia can be applied with reasonable accuracy to ammonia
absorption with weak solution of sulfunc acid. Resistance in
the atomizer tube falls with the increase in the conical diffusor
angle suggesting that an angle of 30 degrees should be used in
all types of Venturi absorbers operating at spray density ex-
ceeding 3-4 1/cu nm; this resulted m a reduced loss in pressure
and smaller apparatus dimensions. Ammonia absorption from
gases should not be conducted at high gas flow rates; the
productivity coefficient increased to an insignificant degree
whereas the pressure drop sharply rose. Ammonia absorption
from coke gas by sulfuric acid is most advantageous when per-
formed in two stages; at rate of gas flow through the Venturi
throat amounting to 40.0 m/sec and rate of water spray
amounting to 6 - 7 u/cu nm of acid per stage, the productivity
coefficient of the entire apparatus would range between 99.0 -
99.5% at total pressure drop of 350 - 400 mm of water.
06655
Varshavsky, T. P., R. G. Agapov, F. A. Mustafm, and V. A.
Permyakov
REDUCING GAS EMISSION DURING COKE OVEN CHARG-
ING. 'AU.S.S.R. Literature on Air Pollution and Related Oc-
cupational Diseases, Vol. 7, 56-63, 1962. (Koks i Khim.) (i) 23-
30, 1956. Translated from Russian. CFSTI: 62-11103
A method for loading coke ovens by steam injectors, which
might cut down air pollution to a minimum by reducing coal
gas and dust escape from the hatches and risers is described.
A procedure was developed for charging coke ovens equipped
with single gas collecting main by unloading one bunker at a
time with the other hatches closed which improved con-
siderably working conditions on top of coke ovens. The
procedure is applicable only to coke oven charging with coal
of not more that 6% moisture. A new procedure for charging
coke ovens with 2 gas collecting outlets by unloading the first
and third bunkers first was recommended and is currently in
use industrially. Coke oven charging by steam injection caused
coal dust to be carried way into the gas collecting mains;
therefore, the method of steam injection is not currently used
in the Eastern U.S.S.R. coke-chemical plants.
06656
I. Ya. Mezentsev
SMOKELESS COKE OVEN CHARGING. U.S.S.R. Literature
on Air Pollution and Related Occupational Diseases, Vol. 7,
64-8, 1962 Koksikhim. (4) 28-30, 1958. Translated from Rus-
sian. CFSTI: 62-11103
The advantages and disadvantages of steam injection used at
the Moscow Coke-Chemical and the Zaporozhie Coke-Chemi-
cal Plants to attain smokeless coke oven charging were deter-
mined. Coke oven batteries with 2 gas collecting mains were
investigated. 976 coke ovens were tested in the Zaporozhie
plant. The first and second bunkers held 5.5 tons of coal each,
the third bunker 6 tons. 923 ovens in the Moscow Coke-
Chemical Plant were tested. First, two end bunkers were emp-
tied and the hatches covered; the middle bunker was then
emptied. The first and third bunkers contained 6.25 tons each
the middle 4.4 tons. A third procedure was also tested. In the
first bunker - 6.3 tons, in the second - 4.5 tons, and in the
third - 6.2 tons. The end bunkers were simultaneously un-
loaded and 22 seconds later the central bunker was emptied.
Coal dust was directly proportional to time of steam injection.
Coal dust and ask were carried off if the coal contained 8.5%
of moisture; if 91% of the coal particles measured 3 mm or
less in diameter and the partial vacuum at the bottom of the
riser was 19 mm, 3.5 kg/min of coal dust were carried away.
The injection steam pressure must produce a partial vacuum at
the bottom of the riser of not less than 19 mm if charging is to
be attained without any gas escape. The Moscow Coke-Chemi-
cal Plant procedure can be used with coal containing 7%
moisture. Charging by the Moscow Coke-Chemical Plant
procedure tested at the Zaporozhie Coke-Chemical Plant with
coal moisture content of 8 and 10% had lengthened the loading
time, increased the work intensity of the levelling bar, greatly
increased the rate of coal dust pick-up, and increased the rate
of coal dust pick-up, and increased the ash concentration in
the separated tar to 0.153% as against 0.115% by the usual
procedure. The efficiency of smoke abatement was con-
siderably higher with the Moscow Coke-Chemical Plant
procedure lhan by that of the Zaporozhie Coke-Chemical
Plant. The most promising procedure was the third which con-
sumed considerably less time than either of the other two.
08178
Belousov, S. P , A. S. Dun, and I. I. Nikberg
THE USE OF BATTERY COMBUSTION CHAMBERS IN
THE PURIFICATION OF INDUSTRIAL EMISSIONS INTO
ATMOSPHERIC AIR.Gigiena i Sanit., 24(4):70-71, 1959. Trans-
lated from Russian by B. S. Levine, U.S.S.R. Literature on Air
Pollution and Related Occupational Diseases, Vol. 4, p. 54-56,
Aug. 1960. CFSTI: TT 60-21913
The gas punfymg installation described is of the type used in a
Soviet coke-pitch plant. The coke was roasted in batteries of
open flame furnaces of the OYuzhkokremontO system, each
battery consisted of 10 - 15 open flame furnaces. Reconstruc-
tion of the battery furnaces was carried out which consisted in
rebuidling part of t he furnace into purification installations of
the supplemental combustion chamber type. Thus, the exhaust
gases coming from the furnace flues were passed through the
supplemental combustion chambers before entering the
smokestacks. The supplemental combustion of pitch-coke
waste products is accomplished at 1150 - 1500 deg. This high
temperature is attained by sucking in extra air through special
openings in the supplemental combustion chamber.
08183
Ganz, S., and M. A. Likshin
COKE GAS PURIFICATION FROM HYDROGEN SULFIDE
IN HIGH SPEED ROTARY ABSORBERS. Zh. Prikl. Khim.,
31(2):191-197, 1958. 1 ref. Translated from Russian by B. S.
Levine, U.S.S.R. Literature on Air Pollution and Related Occu-
pational Diseases, Vol. 4, p. 85-93, Aug. 1960. CFSTI: TT 60-
21913
The high speed horizontally rotating absorber used in this
study was equipped with stationary discs, each of which had
-------
B. CONTROL METHODS
13
12 paddles set at an angle. Studies were made of the effect of
the hydrodynamic, as well as the physico-chemical conditions
on the absorption rate. The effect of the hydrodynamic factors
was studied with reference to the construction of the discs,
their peripheral velocity, the volume rate of the gas flow, the
height (volume) of the liquid in the horizontal absorber, and
the rate of the horizontal movement of the liquid in the ab-
sorber. The effect of the physico-chemical factors was studied
with reference to temperature, chemical absorption capacity of
the solution and the H2S concentration in the gas. The greater
number of experiments was carried out with a sodium arsenite
solution containing 8 4 g/1 As203. The results of the investiga-
tion indicated that the absorption rate of H2S by sodium ar-
senite solution in a high speed rotary absorber was con-
siderably greater than in tower systems. H2S absorption in a
rotary apparatus requires considerably lower reaction volumes,
less metal, smaller capital investment and less electric power
for its operation.
08428
A. R. Kuzmenkov, V I. Suryadnyi
THE UNIFORM SPRAYING OF PACKED SCRUBBERS.
Coke Chem. (USSR) (English Transl.), No. 4:44-46, 1967.
The degree of wetting of the packing and overlap of the cones
from 1 to 10 sprays was determined. The projections of three
adjacent cones had only one common point of intersection.
The arrangement adopted for the sprays was one in the mid-
dle, and the remainder around the periphery. The geometric
dimensions needed for the calculations are given in terms of
the radius of the spray cone R(sub c). The results of the calcu-
lations are tabulated. The degrees of wetting and overlap of
the cones have been depicted graphically. High degrees of
wetting, equal to 85.3 and 86.8 per cent, and minimum degrees
of overlap of the cones, equal to 10.3 and 12 per cent, can be
achieved with six or eight sprays. The cone radius R(sub c) de-
pends on the height of the spray above the packing and the
hydraulic conditions inside the spray In eddy sprays the cone
is stable with a constant angle of opening of 90 deg under
auto-modelling conditions. The height of the sprays above the
packing was calculated and checked under commercial condi-
tions.
13491
Vorobev, D D., V. N. Ilyashenko, M. S. Komarovskii, N. P
Slavgorodskaya, I. I. Rozhyatovskn, E. N. Kucheryavyi, and
E. I. Shuleshov
THE USE OF QUARTZ FILTERS IN AN AMMONIA PLANT.
Coke Chem. (USSR) (English Transl.), No. 8:38-41, 1968.
To be effective the sand particles in a sand filter should be
0.5-1.0 mm and tar particles 5-10 micrometers in size. The
linear filtration speed should be about 5 m/hr and the extent of
tar accumulation in the filter should not exceed 50 to 60 kg/cu
m of sand. The filter washing rate for periodic removal of tar
from the sand should be in the range of 15 to 20 1/sq m at a
washing temperature of at least 60 C and a consumption equal
to three times the volume of the sand charge. Giprokoks
designed a quartz filter meeting these requirements for use in
removal of coal tar from weak ammoniacal liquors. The filter
was used in a number of works and evaluated after four
months. The average coal tar content of the liquor was 234
mg/1, and only 14 mg/1 remained after filtration. The filter
was washed every 48 hr, and 48 kg of tar were removed each
time. During the four months, approximately 78,000 cu m of
liquor were purified and 17 tons of tar returned to production.
Given good filter operating and washing conditions, it is esti-
mated that 95% of the tar can be removed from the liquor in
96 hr if the initial liquor has an average tar content of 200
mg/1. The equation used in determining maximum permissible
tar capacity/cu m of sand is given.
13718
Trofimov, A. I.
REMOVAL OF NITROGEN OXIDES FROM COKE OVEN
GAS. (Ochistka koksovogo gaza ot okislov azota). Text in
Russian. Koks i Khun., no. 2:42-43, 1966.
An arrangement for removal of nitrogen oxides from coke
gases, installed at the Yasinovskiy Coal-Tar Chemical Plant, is
described. It converts NO to NO2 (in 110-120 sec at 70-80 C
and 15-16 bar), which in turn reacts with olefins to form a
resin which, after cooling to 30-40 C, is washed in a scrubber
filled with residue from 50 x 50 mm Raschig rings. The instal-
lation was designed for operating with a 0.8% oxygen content
in the coke gas, but 0.4-0 5%> oxygen is found sufficient,
precluding the need for introducing air. Operational reduction
of nitrogen oxides is from 12-18 to 2-3 cc/cu m. This arrange-
ment was installed at a cost of 234,000 rubles.
14420
Menyakin, E. S.
NOXIOUS EMISSIONS FROM PITCH COKE PLANTS. Coke
Chem (USSR) (English Transl.), no. 12:18-19, 1968.
Several steps were taken in the pitch coke plant at the
Cherepovets Iron and Steel Works to prevent the discharge of
steam and gases and to replace manual operations with
machinery and instruments Pitch coke oven doors were made
airtight by two doors with massive flash plates riveted to their
faces. A prolonged check on the performance of the doors
showed them to be fully airtight. The door lute material was
changed from clay ends to a lute based on the blast furnace
trough lining compound to lessen the amount of gas given off
when cleaned. Machinery was modernized for mechanical
cleaning. All the machinery was controlled from a cabin, thus
reducing the time the operator spends m the gas-polluted zone.
Waste air was directed to the raw pitch-coke gas pipe, thereby
preventing carcinogenic substances from getting into the at-
mosphere. They are either collected in special apparatus or
mixed with coke oven gas and burned in furnaces at elevated
temperatures. By taking these steps, the gas emissions were
greatly reduced. The jobs of workers in unhealthy sections
were made easier and labor productivity rose The number of
production workers per shift was cut from 13 to 9. The two
proposed methods are recommended for use m pitch coke
plants at other works.
14437
Zlatin, L. E., A. D. Mamatov, L. A. Kabrin, I. V. Maigov, Yu.
D. Yukhnovets, T. P. Varshavskii, E P. Starke, and N. A.
Zhukov
THE SMOKELESS CHARGING OF OVENS. Coke Chem.
(USSR) (English transl.), no. 12:12-15, 1968. 3 refs.
A new method was developed for the smokeless charging of
coke ovens. The charging gases are sucked into the coke side
collecting main only, with the coal blend emptied from the
charging car hoppers in a 4, 3, 2, 1 sequence. The high-ash tar
that is obtained during charging is collected separately rather
than mixed with saleable tar A technique was developed and
adopted for utilizing the high-ash tar to oil the coal blend. The
nitrogen oxide content of the saleable gas did not rise, because
charging gases pass into a separate pipe system to heat the
battery. The satisfactory performance of the smokeless charg-
ing system enables it to be recommended for adoption at coke
-------
14
COKE OVENS
and chemical works supplying coke-oven gas to nitrogenous
fertilizer plants. (Author conclusions modified)
14779
Kernan, John J.
SMOKELESS COKE OVENS. (Assignee not given.) U. S. Pat
3,462,346. 6p., Aug. 19, 1969. 4 refs. (Appl. Sept. 14, 1965, 6
claims).
Because retort (by-product recovery) processes are much more
costly, interest is again centering on non-recoveiy processes
for manufacturing coke. A new coke oven reduces the smoke
and atmospheric contamination produced by earlier non-
recovery processes and requires no external source of heat
other than that produced in the oven. Green coal and hot coke
are cooked in adjacent chambers, and smoke resulting from
the incomplete combustion of the green coal is lead to the hot-
coke oven where it is almost completely burned before passing
to the stack. Before passing through the stack, hot gases from
both chambers are passed underneath the chamber containing
green coal so that both the bottom and the upper portions of
coal are heated. As a result, the speed of the coking process is
materially increased.
15271
Andersen, Holger C.
CLEANING OF INDUSTRIAL GASES WITH PRECIOUS
METAL CATALYSTS. (Industrielle Gasreinigung mil
EdelmetahTatalysatoren). Text in German. Dechema Mono-
graph., 40(616-641)-325-33, 1962. 28 refs.
The applications of platinum metals as catalysts for removing
acetylene from olefins, cleaning coke-oven gas, and treating
residual gases from the nitric acid production are reviewed. Of
the family, platinum palladium is particularly suited for the
hydration of acetylene so that only a few ppm remain. Recent
laboratory tests indicate that at gas throughputs of up to 4500
standard cu m/hr/cu m catalyst, the addition of hydrogen can
be reduced to a mole ratio between hydrogen and acetylene of
2. In the case of coke-oven gases, acetylene, nitrogen oxides,
carbon oxysulfide, and diolefins are converted into harmless,
easily removable compounds by palladium and ruthenium
catalysts. Catalytic treatment of residual gases from nitric acid
production has three goals: the lemoval of noxious com-
ponents, recovery of the nitrogen in pure form for re-use at
the ammonia synthesis, and production 01 heat. Recent labora-
tory tests show that the process can reduce the nitric oxide
content of waste gases to 9 ppm.
156920
Hasebe, S, Takeshi Tsunemoto, Kenjiro Takeshita, and Seiji
Arita
DESULFURIZATION OF COALS IN COKING PROCESS.
(Sekitan no kokusuka katei ni okeru datsuryu). Text in
Japanese. Nenryo Kyokaishi (J. Fuel Soc Japan, Tokyo),
48(512):892-898, Dec. 20, 1969. 8 refs.
In carbonizing coal at high temperatures, 50 to 90% of the sul-
fur content remains intact. The remaining content of inorganic
sulfur is 62 to 66% and that of organic sulfur, 45 to 75%. Inor-
ganic sulfur can be eliminated to a considerable extent by cok-
ing coal, but the elimination of organic sulfur is extremely dif-
ficult. Several experiments were conducted using Miike and
Matsushima mine coals. Since the most suitable temperature
for desulfurizing coal is 400 to 600 C, an effective desulfuriz-
ing agent and catalyst in this temperature region was sought.
The suitable temperature for the desulfurization using
hydrogen gas was about 800 C, above which the bonding of
sulfur with coal became a great problem. Active hydrogen was
supposed to be more effective than the molecular hydrogen.
Carbonization of coal in the presence of tetraline, isopropyl al-
cohol, or cyclohexane as a source of active hydrogen was ex-
amined. Tetraline was more effective than hydrogen gas in the
temperature region from 500 to 600 C. After transforming or-
ganic sulfur to pyrite sulfur in the presence of the compound,
sulfur was removed by thermal decomposition. Carbonization
with some inorganic compounds other than iron compounds
was examined. Strong bases such as potassium hydroxide and
sodium hydroxide can remove the sulfur, but their unfavorable
effects on the gain and quality of coal prevent their utilization.
Calcium hydroxide increases the sulfur content of coal ob-
tained by fixing the sulfur as sulfur compounds, which can not
be removed by washing with water or acid.
16157
Kipot, N. S., A. I. Brodovich, and B. S. Filippov
REMOVAL OF NITRIC OXIDE FROM COKE-OVEN GAS.
Coke Chem. (USSR) (English translation from Russian of'
Koks i Khim.), no. 3:38-43, 1969. 47 refs.
Although the amount of nitric oxide in coke-oven gas is small,
even the slightest trace reduces the efficiency of equipment
for fertilizer manufacture and creates the risk of explosion.
Current methods of nitric oxide removal are those that involve
compression of coke-oven gas or those that are carried out at
normal pressures (800-1000 water guage). When the compres-
sion method is carried out in hollow reactors, 70-90% of the
nitric oxide can be removed at 100 C and 10-12 atm. When
carried out with molybdenum or tungsten sulfide catalysts,
nitric oxide is virtually entirely removed at 180-250 C and 16
atm. The best available method for removing nitric oxide from
uncompressed gas is purification in electrostatic brush-
discharge precipitators. In this process, nitric oxide is oxidized
inside the precipitator, on an almost stoichiometric basis, to
nitrogen dioxide. The nitro-resms formed by the reaction of
the nitrogen dioxide with the unsaturated hydrocarbons
present in the ga^ are speedily deposited inside the precipita-
tor The nitric oxide content of the coke-oven gas is reduced
from 0.5 to 0.006 ppm. This method should receive further
study in the Soviet Union where the introduction of smokeless
coke has increased the nitric oxide content of coke-oven gas.
16260
Pozin, M. E , E. Ya. Tarat, L. Ya. Tereschenko, and I. N.
Orekhov
ABSORPTION OF HYDROGEN SULFIDE BY ARSENICAL
SODA SOLUTION UNDER TURBULENT (FOAM) CONDI-
TIONS. J. Appl. Chem. USSR (English translation from Rus-
sian of: Zh. Prikl. Khim.), 39(8): 1601-1607, Aug. 1966. 15 refs
Investigations were undertaken of the rate and degree of ab-
sorption of hydrogen sulfide by arsenical soda solutions in a
foam apparatus with sieve plates in order to establish condi-
tions for purifying coke-oven gas. Empirical equations were
derived to express the dependence of the coefficient of ab-
sorption on the gas phase velocity and foam height. These
equations can be used in design calculations and to determine
the influence of liquid-phase processes on the absorption rate.
When hydrogen sulfide concentrations exceed a certain limit,
the dissolution rate is higher than the neutralization rate, and
the absorption rate diminishes sharply. Calculations show that
for a given degree of hydrogen sulfide removal, the volume of
the foam absorber needed is smaller in the ratio of 7.5 to 1
than the volume of a packed scrubber. A foam absorber with
13-18 trays is required to reduce hydrogen sulfide content in
coke-oven gas to 1.5-2 H2S/cu m; one of 38 trays is necessary
-------
B. CONTROL METHODS
15
to reduce hydrogen sulfide to the permissible domestic level.
The foam absorption process appears promising, since the rate
of diffusional transfer of H2S from the gas to the liquid phase
determines to a considerable extent the total rate of chemical
absorption.
16602
Bondarenko, I. P. and Ye. Kh. Zemskaya
EFFECT OF TEMPERATURE ON THE OPERATION OF
THE ARSENIC-SODA DESULFURIZATION PROCESS. (O
vliyanii temperatury na rabotu mysh'yakovo-sodovoy
seroochistki). Text in Russian. Koks i Khim., no. 6:54-56,
1965.
In addition to the Na2CO3/As203 ratio and the pH value of
the absorbent solution, and the consumption of air for
regeneration of the saturated solution, temperature should be
considered a basic parameter of the industrial arsenic-soda
process of desulfurization of waste gases. Many years cf ob-
servation of seasonal variations of the process parameters at
the Zhdanov coal-tar chemical plant where the ambient tem-
perature may drop to 3 C in winter and rise to 40 C in summer
suggested the possibility of their close correlation. This sur-
mise was confirmed by the results of two series of concurrent
parallel plant tests. In both series, samples of uncleaned coke
gas were taken directly from the flue through a branched pipe
fastened to a single tap hole and the H2S-concentrations, in
gram/cu m, in the purified gas in either branch were measured.
In one series, gas in one of the branches was pre-cooled to 10
to 15 C, while that in the other branch was pre-heated to 40 to
50 C before entering the respective jars filled with identical ar-
senic-soda absorbent solutions of the same temperature. In the
other series, gas of the same temperature in both branches
was passed through the respective absorbent solutions kept at
the temperature of 35 and 52 C, respectively. The H2S- con-
centrations in the purified gas measured in the first series
(given in the form of ordered pairs (pre-cooled, pre-heated))
were: (2.42, 1.23) (7.90, 4.82) (3.32, 1.60) (3.68, 3.20) (5.58,
2.47) (4.84, 2.03) (2.51, 1.47) (3.26, 3.02), and in the second se-
ries: (9.37, 3.61) (3.32, 0.96) (3.14, 0.86) (3.10, 1.16) (2.87, 1.07)
(2.69, 2.04). These results showed that in every case the coeffi-
cient of H2S absorption increases with the operating tempera-
ture of the absorption process. After the temperature of the
absorbent solution of the arsenic-soda desulfurizer of the Zh-
danov plant had been raised from 40 to 50 C, this not only in-
tensified the elimination of H2S and the regeneration of the
saturated absorbent, but also injured the stability of that solu-
tion when its As203-content is high, lessend the deletorious ef-
fect on that solution of organic compounds such as benzene,
naphthalene, resins, or absorbent oil remaining in the gas after
the preceding stage of purification and lowerd the Na2CO3
consumption while making it more uniform throughout the
year.
16642
Guentheroth, Hans
NEW EXPERIENCES WITH VENTURI SCRUBBERS FOR
FINE CLEANING OF GASES FROM COKING PLANTS.
(Neuere Erfahrungen mil Venturi- Scrubbern fuer die Fein-
streinigung von Gasen im Kokereibetrieb). Text in German.
Dechema Monograph, 48(835-858):329-345, 1963. 4 refs.
The use of PA(Pease-Anthony) venturi scrubber for the
separation of tar and naphtalene is described. Coke oven gas is
cooled to 35 C, pre-scrubbed, and passed to the PA venturi
scrubber, where oil is used as the scrubbing liquid. An average
of 0.7 cu m/1000 standard cu m gas are supplied to the
scrubber and circulated. About l/20th of the scrubbing oil is
removed per hour for regeneration. The venturi scrubber is
operated with a differential pressure of 240-300 mm water. Tar
mists are removed to a residual concentration of 38 mg/stan-
dard cu m gas; the napthalene is absorbed to a residual
amount of 160 mg/ standard cu m corresponding to a
napthalene dew point of 11 C. This degree of purity is
adequate for metallurgical plants, since the temperature in the
final coolers is 23 C and never drops below 11 C m the dis-
tribution network. It is inadequate for long distance transmis-
sion of gas. Such venturi scrubbers were installed by a steel
manufacturing company in Gary, Indiana. Two test series stu-
dying the efficiency of this type of venturi scrubber for the
separation of tar showed the great influence of saturation and
cooling. The performance of the scrubber could be improved
by pre-cooling the gas prior to its passage through a saturating
device. After saturation with scrubbing liquid, the gas is
further cooled before it goes to the actual PA venturi
scrubber. In conclusion, a novel process for the removal of
CH and soot is described from which the gases leave with a
residual soot content of 1 mg/standard cu m.
16943
Francis, Wilfrid
THE REMOVAL OF SULPHUR COMPOUNDS FROM IN-
DUSTRIAL GASES. Engineering (London), vol. 172:180-182,
Aug. 10, 1951. 3 refs.
Six processes are described for recovering sulfur from coke-
oven and refinery gases. The I. G. active charcoal process is
applicable to many types of gas and is based on the low-tem-
perature oxidation of hydrogen sulfide in thhe presence of ac-
tive charcoal. High-quality sulfur is produced; the main limita-
tion is the maximum concentration of H2S permitted,
equivalent to 8 grams/cu ft. The Girbotol process is another
physical process in which a solution of triethanolamine is used
as the scrubbing medium. The process is simple, the solution
used long-lasting, and the treated gas contains high proportions
of H2S that is readily convertible to either sulfur or sulfuric
acid. In the Seaboard process, the gas is passed up a scrubbing
tower; a dilute solution containing 2-4% sodium carbonate
passes down the tower and dissolves the H2S to form sodium-
H2S and sodium bicarbonate from which sulfur can eventually
be recovered. Some problems arise from the use of dirty gas
and the corrosion of metal parts. In the Ferrox process, a
development of the Seaboard process, the H2S is removed by
scrubbing with a dilute solution of sodium carbonate contain-
ing a fine suspension of iron oxide. The sulfur product is of
poor quality and some aeration and oxide- handling problems
arise, but its most likely application is for combustion to sulfur
oxides for use in a contact sulfuric acid plant. The Thylox
process is similar to the Ferrox process except that arsenious
oxide is used in solution in place of iron oxide in suspension;
the sulfur and waste liquors can be used for msecticidal pur-
poses. The caustic-soda wash process, where the soda
removes the H2S as sodium-H2S, may be used where high
concentrations of H2S are present. The mercaptides formed in
the presence of organic gases must be removed completely
from solution in order to sell the hydrosulfide solution readily.
17259
Danielevich, Yu. I. and Yu. K. Tupitsin
REMOVAL OF TOXIC IMPURITIES FROM GASES. Coke
Chem. (USSR) (English translation from Russian of: Koks i
Khim), vol. 6:45-46, 1969.
A technique and equipment for the removal of toxic organic
impurities from waste gases minimized the fuel consumption
-------
16
COKE OVENS
needed to purify waste gases with a limited content of com-
bustible substances by oxidizing decomposition products to
carbon dioxide and water by using O2 in waste gases. The
equipment included a vortex burner, a conical embrasure, and
u cyclone firebox which is an internally lined metal casing
preferably oblong, 2.5-4.0 m in length. The combined volume
of gases was 110,000 cu m/hr. The actual gas consumption was
1 cu m per 60-90 cu m of waste gases. The limiting thermal
load was 6,000,000 kcal/hr sq m cros section. The unit was air
tight. The equipment operates under pressure and the final
products can be used as heating gases. An experimental
technique involved the removal of toxic impurities from waste
air containing 7-11% O2 and 2.7% CO2 from fatty acid produc-
tion. Thirty to forty percent of the waste air was admitted via
the burner, the remainder being directed into the cyclone
firebox. In the firebox, combustion products were mixed with
cold waste gases producing a mixture temperature regulated by
flow rates of the gases passing through the burner.
17318
Knz, Milan, Josef Vejvoda, and Bedrich Kedron
EMISSIONS FROM GAS PLANTS, COKING PLANTS, AND
THERMAL POWER STATIONS AND MODERN METHODS
OF THEIR LIQUIDATION. (Exhalace z plynaren, koksoven,
tepelnych elektraren a moderni zpusoby jejich likvidace). Text
in Czech. Ustav Vyzkum Paliv Monograph, no. 6, 156p., 1969.
Air pollution in Czechoslovakia as caused by gas plants, cok-
ing plants, and thermal power stations is studied. Future
developments in these areas up to 1980 are indicated and ap-
propriate control methods are suggested. The number of Lurgi
gas plants, which are the major sources of town gas, are not
expected to increase, though existing plants will intensify their
operations. The present volume of coke production will remain
unchanged to 1980. Enormous development is expected in the
power station industry, the capacities of which will be
designed for a brown coal with a high sulfur content. The
study discusses dust generation in the Lurgi process and the
most modern control methods used abroad. Desulfurization of
waste gases from Lurgi plants is considered with special
references to the waste gases from a recently installed Rectisol
plant. In considering measures to improve the quality of air
around coking plants, considerable attention is give to gas pu-
rification, tar separation and treatment with ammonia, and
coke-oven gas secondary cooling. A method for the desul-
furization of coke-oven waste gas by vacuum-soda is reported.
A major part of the study is devoted to the problem of remov-
ing SO2 from thermal power plants Promising dry desulfunza-
tion processes proposed for other countries, and Czechoslovak
studies on the limestone process, are described. Electrofilters
and other dust collecting systems for thermal plant fly ash are
reviewed. Also considered is the pioblem of separating arsenic
from the waste gas of one power station. Finally, provisions of
the Czechoslovak Clean Air Act of 1967 are criticized. (Author
summary modified)
17680
British Coke Research Assoc., Chesterfield (Derbyshire)
PRACTICAL SUGGESTIONS FOR THE REDUCTION OF
THE EMISSION OF SMOKE, DUST AND GRIT AT COKE
OVENS. Special Pub. 5, May 1962. 26 refs.
Suggestions helpful in dealing with atmospheric pollution
problems at coking plants in response to the Clean Air Act of
1956 are summarized. Aspects of efficient heating with
minimum air pollution are enumerated. Oven charging
techniques are considered with separate attention given to ex-
isting plants and new plants, and a method is presented for as-
sessing smoke emission in terms of a 'mass emission factor.'
Doors and door frames, oven discharging, and coke quenching
are also briefly examined. Comments are made regarding the
handling and stocking of coal and coke, and the boiler and an-
cillary plant.
17849
Ozerskii, Yu. G., G. A. Markus, and V. I. Oratovskii
RECOVERY OF PHENOLS AND HYDROGEN SULPHIDE
FROM WASTES DISCHARGED TO ATMOSPHERE. Coke
Chem. (USSR) (English translation from Russian of: Koks i
Khim.), vol. 6:41-44, 1969. 4 refs.
Given lengthy contact times between an alkaline solution and a
mixture of air and gases containing phenols and hydrogen sul-
fide, the residual contents in the gaseous phase will depend on
the dynamic gas-liquid equilibrium conditions. The latter are
dependent on a number of factors, including the alkali solution
concentration, the nature of the phenols present, the cumula-
tive phenols content of the solution, and the solution tempera-
ture. Liquid-vapor equilibrium conditions are investigated at
30-60 C for colonmetric determination by the para-nitroaniline
method. Phenol content of the gas-air mixture increases by a
factor of 3-5 as the phenolate solution temperature is taised;
as the phenols build up in the alkali solution, the gas-air mix-
ture retains a higher residual phenol content. The equilibrium
hydrogen sulfide concentiation of the gas-air mixture increases
from 1 to 5 mg per sq m as the temperature is raised from 30
to 60 C, but the equilibrium H2S concentration in the scrubbed
discharge is negligibly small, since the sulfides in the circulat-
ing solution are oxidised to form sodium sulfite and
thiosulfate.
17943
Belov, K. A. and L. N. Petrova
REDUCING BENZOLE HYDROCARBON LOSSES TO AT-
MOSPHERE. Coke Chem. (USSR) (English translation from
Russian of: Koks i khim.), no. 9:32-36, 1968.
The saturated vapor pressures "and volality of crude benzoles
and rectification products at two coke and chemical works
were experimentally determined. The saturated vapor pres-
sures were determined at temperatures between -15 and +30
C. A three-neck flask was used which was controlled by a
thermostat to maintain a constant temperature. When the
required temperature was reached, 10 ml of the test substance
injected into the flask and the pressure charge recorded. The
relationship between saturated vapor pressure and temperature
was described by the equation IgP equals A - B/T, where P is
the pressure of the saturated vapor in mm Hg, T the tempera-
ture in degrees Kelvin, and A and B are constants which were
found experimentally Benzene hydrocarbon losses through the
breather valves in storage tanks are largely governed by the
rate at which the latter are charged and the speed at which the
air space in the tanks becomes impregnated with hydrocarbon
vapors. To determine the quantity of these losses, 250 ml of
benzene was poured into a vessel, the proper temperature was
adjusted, and atmospheric air was allowed to enter. The escap-
ing hydrocarbon vapors were caught by activated charcoal.
The increase of weight of the activated carbon divided by the
volume of air expelled by the vapors from the vessel yields
the amount of hydrocarbons lost from the container. The error
of this method did not exceed 0.5%.
19203
Dancy, T. E.
CONTROL OF COKE-OVEN EMISSIONS. Iron Steel Engr.,
47(7):65-75, July 1970. 5 refs.
-------
B. CONTROL METHODS
17
The status of equipment developments for controlling emis-
sions from coke ovens are reviewed, and studies now in
progress are described. Ventun scrubbers control particulate
emission but not benzene-soluble compounds. The AISI coke-
oven charging system to reduce emissions is described. A
component testing program to provide information on ascen-
sion pipe steam ejector design, ascension pipe automation,
hopper design, feed hopper shut-off, leveling-bar door automa-
tion, and lid lifter design is reviewed. Means of controlling
emissions during the pushing operation are discussed. The
quenching operation can be a significant source of contami-
nants. It will take considerable time, manpower, and money to
reliably control emissions throughout the industry.
19253
Breitbach, Fritz and Gustav Choulat
APPARATUS FOR DECOMPOSING AMMONIA. (Carl Still,
Recklinghausen (West Germany)) U. S. Pat. 3,505,027. 6p.,
April 7, 1970. 4 refs. (Appl. June 12, 1967, 3 claims).
A process and apparatus for decomposing or destroying am-
monia emanating from coke oven plants or gas works without
forming nitrogen oxides is described. The ammonia is decom-
posed into nitrogen and hydrogen by first heating ammonia-
containing vapor clouds to the decompostion temperature of
ammonia and then passing the vapor through a decomposition
zone. The zone may be in the form of a free space or chamber
or may comprise a chamber filled with temperature resistant
filling bodies or catalysts of a suitable nature. The apparatus is
a furnace housing with an interior refractory lining surround-
ing a centrally located combustion chamber and with several
first and second passages encompassed by the lining. The ad-
vantages of this process is that no oxides of nitrogen are
produced.
19308
Leibovich, R. E., A. I. Bublik, V P. Shelest, and S. K.
Shelkov
HIGH-TEMPERATURE DESULPHURIZATION OF COKE.
Coke Chem. (USSR) (English translation from Russian of:
Koks i Khim.), no. 11:17- 18, 1969. 9 refs.
Sulfur reduction data are presented for individual grades and
blends of Donbas coal carbonized in a Tamman furnace and
heated in intervals from 1000 C to 1700 C. The figures show a
steady reductior in residual sulfur content of individual coals
and blends, the most rapid reduction occurring from 1400-1500
C. The coal which lost the highest proportion of its original
sulfur content during carbonization was the grade containing
the highest percentage (35.84) of volatile matter
19733
Shibler, B. K. and M. W. Hovey
PROCESSES FOR RECOVERING SULFUR FROM SECON-
DARY SOURCE MATERIALS. Bureau of Mines Information
Circ., no. 8076, 1962, 62p. 561 refs.
A literature survey on processes for recovery of elemental sul-
fur and sulfur compounds from secondary source materials is
presented, and the more important processes from all non-
Frasch sources are described. The text consists of concise
descriptions of the general nature of the recovery processes
and definitions of major differences between processes
proposed for treating the same or similar materials. The
bibliography represents the available English language litera-
ture on the subject through 1958, with emphasis on the period
1950-1958. In addition to several articles and publications con-
taining general information on sulfur, the text and bibliography
on processing methods are arranged under the six principal
sources of secondary sulfur, as follows: volcanic sulfur, in-
cluding all elemental sulfur deposits not adaptable to the
Frasch mining process; hydrogen sulfide as found in sour
natural gases, petroleum refinery products, and coke-oven
gases; sulfur dioxide from the roasting and smelting of metal
sulfide ores and from power plant waste gases; pyrite and
pyrrhotite obtained by mining mineral deposits or produced as
by-products from the concentration of sulfide ore; gypsum and
anhydrite occurring as deposits of calcium sulfate; and indus-
trial wastes containing sulfates, sulfites, and sulfuric acid,
such as those produced in the steel, paper, and petroleum in-
dustries. (Author summary modified)
20960
Barnes, Thomas M., Albert O. Hoffman, and H. W. Lownie,
Jr.
EVALUATION OF PROCESS ALTERNATIVES TO IM-
PROVE CONTROL OF AIR POLLUTION FROM PRODUC-
TION OF COKE. (FINAL REPORT). Battelle Memorial Inst.,
Columbus, Ohio, Columbus Labs., Contract PH 22-68-65,
149p., Jan. 31, 1970. 90 refs. CFSTI: PB 189266
The findings and recommendations from a 6-month study of
air- pollution control in the manufacture of blast-furnace coke
are presented. The provision of new or improved equipment
for control of emissions from conventional coke ovens, and
the development of new, potentially cleaner processes for con-
version of coal into blast-furnace coke were investigated. The
emissions and control methods for the various processes in
conventional coking are discussed (charging of coal to the slot
ovens, underfiring the slot ovens with coke-over gas, sealing
of slot ovens during early stages, discharging of newly
produced coke, and quenching of hot coke). Large investments
in new equipment can make a contribution to air quality at and
near conventional coke ovens; but by their very nature, such
ovens will always be emission sources to some degree. There
are no generally accepted devices or procedures for measuring
and evaluating emissions and emission controls for coke
ovens. It is urged that research instruments and procedures be
developed for measuring emissions, since they are needed to
permit quantitative evaluation of the effectiveness of control
processes and equipment. Several unconventional coking
processes that are in the pilot-plant and demonstration stages
were examined (fluidized bed operations, forming balls in a
hot retort, hot and cold briquetting, curing of briquettes, final
coking in gas-fired vertical-shaft furnaces, intermediate and
final coking in units that recirculate hot sand, traveling-grate
cokes, rotary hearth cokers, and batch-type sole-flue ovens). It
is concluded that these processes are more amenable than slot-
oven coking to the control of air-polluting emissions. Con-
tinued development and industrial trial of these processes
should be encouraged. One important contribution would be
research conducted to improve understanding of coke proper-
ties affecting performance in a blast furnace.
21624
Stemkohlenbergbauverein, Essen (West Germany),
Arbeitsgruppe Kokereiemissionen
RESTRICTION OF DUST EMISSION IN COKE QUENCHING
COKING PLANTS AND GASWORKS. (Auswurfbegrenzung
von Staub beim Loeschen von Koks Kokereien und
Gaswerke). VDI (Ver. Deut. Ingr.) Richtlinien, no. 2303, Nov.
1966. Translated from German by D. Ben Yaakov, Israel Pro-
gram for Scientific Translations, Jerusalem, 4p. CFSTI: TT 68-
50469/10
The technology of coking plants and gasworks is reviewed
with respect to the emission of dust from the quenching
-------
18
COKE OVENS
towers. The quantity of dust emitted during quenching may
vary at different points during the quenching process, from
batch to batch in the same plant, and from plant to plant, and
depends on the nature of the charge and the dimensions and
shape of the quenching tower. The former is affected by the
nature of the input coal, the final coke temperature, and the
operation of the coking oven. The higher the quenching tower,
the greater will be the draft and resulting flow velocity of the
quenching vapors; consequently, more dust will be emitted
from a higher tower. However, the tower must also be high
enough to avoid nuisance and environmental damage. Besides
design modifications, dust emission can also be reduced by
reducing the amount of drawn-in air to reduce the flow
velocity, by the impact effect of built-in grates, screens, or
baffles, and by spraying into the quenching-steam cloud.
Newly erected quenching towers must be equipped with ap-
propriate control devices, and must be designed to meet
prevailing emission limits. An appendix describes the ap-
paratus and procedure for sampling dust emission from
quenching towers.
21965
Rickles, Robert N.
WASTE RECOVERY AND POLLUTION ABATEMENT.
Chem. Eng., vol. 72:133-152, Sept. 27, 1965 112 refs.
Various methods presently available for the treatment of liquid
and gaseous effluents were discussed. Methods and processes
that have been used or proposed for the recovery of valuable
products were stated as follows: biological oxidation, biologi-
cal reduction, and chemical oxidation; sedimentation tanks,
thickness, flocculation tanks, cyclones, centrifuges, screens,
filters, and membrane sieves; foaming and flotation; adsorp-
tion; ion exchange; membrane processes solvent extraction,
and evaporation and crystallization. The extent of participation
of the various segments of the chemical processing industry in
the abatement/by- product recovery program was illustrated by
specific examples from the petrochemical industry, coal and
coke industry, phosphate fertilizers, petroleum industry, and
pulp and paper industry. The extent of government involve-
ment, both federal and state, was brought out by listings of
federal R&D agencies, state programs of air and water pollu-
tion control, state assistance provided for waste treatment
facilities, and key provisions of proposed legislation in the
area of tax relief to companies buying control or abatement
equipment. The prediction was made that when public and
governmental pressure becomes great enough, industry will
find a way to make a profit out of waste control.
22503
Koehler, Karl-Heinz
COMPARISON POSSIBILITIES IN THE OPERATION OF
GAS DESULFURIZATION PLANTS WITH SOLID PURIFIER.
(Moeglichkeiten eines Betnebverglei von Gasentschwefelung-
sanlagen mil fester Reinigungsmasse). Text in German.
Glueckauf (Essen), 101(9):568-576, 1965. 2 refs.
Gas desulfurization installations with a solid purifying agent
are designed to remove hydrogen sulfide from coke-oven gas
so that it can be used as consumer gas or for synthesis. The
purification substance used for this purpose in the Ruhr area is
a mixture of bog iron ore, Martin mass, and wood chips. An
analysis of the factors influencing the output of such installa-
tions, namely size, technical construction, the sulfur en-
richment factor of the purifying agent, and mode of operation
disclosed the existence of a correlation between the operating
life of a gas desulfurization installation and the specific mass
absorption capacity expressed by the quotient of the purifying
mass and the daily supplied quantity of sulfur. The number of
purification towers thus represented the parameter for com-
parison. Sulfur enrichment as a function of the specific ab-
sorption capacity of the purifying agent manifested a max-
imum for each number of purification towers. With an increas-
ing number of towers, the maximum shifted in the direction of
lower specific absorption capacity. This finding has to be
taken into consideration when an addition of a new tower to
an existing 3 to 4 tower installation is contemplated.
23136
Vorobev, D. D.. A. P. Sergeev, V. G. Balanov, R. I.
Davidzon, V. L Vodolazhchenko, V. P. Mikhno, and L. N.
Tyutyunnik
DUST ARRESTOR PERFORMANCE AND DUST HANDLING
IN COKE DRY-COOLING PLANT. Coke Chem. (USSR) (En-
glish translation from Russian of: Koks i Khim.), no. 1:20-21,
1970.
At a coke dry-cooling plant in the Soviet Union, dust is
removed from circulating gas to a dust-settling hopper before
the gas stream enters the waste heat boiler and again in
cyclones before it enters the exhaust fan. By fitting the hopper
with high-strength chamotte baffles, the average dust content
of the gas entering the cyclones was reduced to 3-4 g/cu m
compared to 4-6 g/cu m when the baffles were supported by
welded steel girders faced with guniting material. Erosion of
the cyclones was checked by lining internal surfaces of all
conical sections with cast stone slabs. Coke breeze and dust
from the hoppers and cyclones is discharged through a sludge
pipeline to a settling tank on a quenching tower. Blockage of
the pipe was reduced by increasing its angle of inclination and
the addition of more wash down nozzles along its length.
23143
Mitrofanov, N. I.
EXPERIENCE IN THE INTRODUCTION OF SMOKELESS
CHARGING OF COKE OVENS. Coke Chem. (USSR) (English
translation from Russian of: Koks i Khim.), no. 1:17-20, 1970.
The smokeless charging of coke ovens is possible only when
conditions are maintained which allow the gases and fumes as-
sociated with charging to be evacuated without hindrance.
These conditions are secured by adopting a strict emptying
sequence for the charging-car hoppers, avoiding the formation
of closed spaces inside the oven, and maintaining sufficient
suction in the riser pipes. Steam and gas injection are equally
effective, but they affect the rest of the plant in different
ways. The wide commercial adoption of gas injection is ex-
cluded because of the difficulty of compressing coke-oven gas,
the increased load on the exhausters, and the operating
problems associated with high pressure gas mains. Neverthe-
less, if steam happens to be in short supply and compressed
coke-oven gas is already available at some point in the plant, it
can be used instead of steam as the injectio medium. When
gas injection is used, the valves operate more reliably and last
longer; less ammonia liquor is produced, and the gas pipelines
do not need thermal insulation. On the other hand, the use of
gas injection increases the load on the gas blowers and lowers
the partial pressures of the chemical constituents, which leads
to increased losses in the return coke-oven gas. The disad-
vantages of using injection include the rapid failure of the
fittings (because of erosion on the balls, slide valves, and
other surfaces), increased Oammonia liquor yields and cor-
respondingly increased loads on the ammonium sulfate sec-
tion, and increased operating costs on the steam pipelines and
fittings The adoption of smokeless charging has reduced the
solids and gas pollution levels in the air around the plant as
-------
B. CONTROL METHODS
19
follows: the dust content has fallen from 173.3 to 15.4-38.9
mg/cu m and the carbon monoxide content, from 92.8-147.0 to
8.3-18.9 mg/cu m. The concentrations of hydrocarbons,
hydrogen sulfide, and sulfur dioxide, have also decreased. The
purity of the air in the locality has been improved, and the
working conditions for the oven-top team have been very
greatly ameliorated.
23249
Chertkov, B. A
CONVERSION OF AMMONIUM SULFITE-BISULFITE
SOLUTIONS TO AMMONIUM SULFATE AND ELEMENTA-
RY SULFUR. (Pererabotka rastvorov sul'fit- bisul'fita am-
moniya na sul'fat ammoniya i elementarnuyu seru). Koks i
Khim., no. 1:48-53, 1956. 9 rets. Translated from Russian.
Israel Program for Scientific Translations, Jerusalem, 9p. CF-
STI: TT69-55059
There is wide interest in utilizing ammonium sulfite-bisulfite
solutions to produce ammonium sulfate fertilizer since the
solution can be converted to sulfate without expenditure of
sulfunc acid. Furthermore, sulfur-containing waste gases pro-
vide an unlimited source of ammonium sulfite-bisulfite. In the
'catasulf process,' hydrogen sulfide from coke oven gas is
catalytically oxidized to sulfur dioxide, which is then absorbed
together with ammonia to form the sulfite-bisulfite mixture.
The latter is processed in an autoclave at high temperature to
ammonium sulfate and elementary sulfur. Disadvantages of the
process are that the decomposition of the sulfite-bisulfite mix-
ture in the autoclave has to be performed at high pressure and
that the autoclave must be made of heat resistant materials. As
determined by a kinetic study of the process, decomposition
of the ammonium sulfite-bisulfite solutions to ammonium
sulfate and elemental sulfur can be performed within a techni-
cally acceptable time (1.5 hr) in an open apparatus under nor-
mal pressure. For this purpose, the solution must be
vigorously mixed in the first stage of the process with a large
excess of sulfur, and at the same time heated to 100-105 deg to
accelerate the formation of intermediate ammonium
thiosulfate. After the required thiosulfate concentration is
reached, the solution must be acidified (with H2S04 or SO2) to
convert the residual sulfite to bisulfite and to accomplish
complete decomposition of the solution. Pilot-plant tests of the
technique could result in the early application of more effi-
cient methods of purifying sulfur-containing gases, including
techniques for the simultaneous utilization of NH3 and H2S
from coke oven gas.
23910
Gurtovnik, P. F., D. P. Dubrovskaya, and Ye. A. Forer
QUALITY OF COAL-TAR ABSORBENT OIL. (O kachestve
kamennougol'nogo poglotitel'nogo masla). Text in Russian.
Koks i Khim., no. 6: 47-51, 1970.
A number of coal-tar absorption oils, used for the absorption
of benzenes, have been analyzed chromatographically. The
naphthalene content as determined by standard procedures is
more than 1.5 times lower than the value obtained by chro-
matography. By fractional distillation of these absorption oils,
it is possible to increase naphthalene yield from coal tar by
12% (relative), leaving an absorption oil of improved quality
and stability in amounts up to 45% of the starting quantity.
Laboratory results have been varified in a pilot study.
23911
Khanin, I. M., V. A. Mizin, V. S. Kovalenko, A. T. Movchan,
O. G. Nelipa, and N. A. Panesenko
INVESTIGATION OF TRAY-SPRAYER REGENERATORS
FOR REMOVAL OF HYDROGEN SULFIDE FROM COKE
OVEN GAS. (Issledovaniye tarel'chatoforsunochnyk regenera-
torov tesekha ochistki koksovogo gaza ot serovodoroda). Text in
Russian. Koks i Khim., no. 6:31-35, 1970. 11 refs.
Experimental studies and prolonged-operation tests of tray
regenerators of saturated soda- potash solution point up a need
for further improvement of desorption equipment for vacuum-
carbonat sulfur removal. A new type of industrial regenerator
comprising a combination of hollow- and bubble-tower con-
figurations is proposed. This design yields a power advantage
at the same time that it improves the degree of regeneration. A
sprayer disperses the saturated solution into a space above the
bubble column, thus intensifying the desorption of hydrogen
sulfide and significantly reducing steam consumption. Empiri-
cal formulae are given for determining the degree of regenera-
tion and optimum process paramete when designing combina-
tion regenerators of this type.
24620
Kagasov, V. M., Yu. G. Yefremov, O. P. Klebnikov, D. D.
Zykov, V. P. Maykov, A. M. Furman, and P. M.
Chermchenko
EVALUATION OF THE PROCESS OF OBTAINING ARO-
MATIC HYDROCARBONS FROM COKE-OVEN GAS. (Otsen-
ka protsessa polucheniya benzol'nykh uglevodorodov iz kok-
sovogo gaza). Text in Russian. Koks i Khim., no. 6:38-40, 1970.
6 refs.
A pilot study of the extraction of benzene from coke-oven gas
is evaluated in terms of rate of recovery of benzene and other
hydrocarbons, loss of absorbing oil, and power (steam) con-
sumption. Waste gas flow rate was 90 thousand cu m/h with a
raw benzene content of 35.8 g/cu m. Chromatographic analysis
showed benzene, toluene, and xylene to comprise 98-99% of
the hydrocarbons recovered. The use of chromatrographic and
spectrophotometric studies is recommended in the evaluation
of such recovery operations.
24977
Rott, M. V., V. N. Sevostyanov, and Ya. I. Shukh
THE REMOVAL OF HYDROGEN SULPHIDE FROM COKE-
OVEN GAS. Coke Chem. (USSR) (English translation from
Russian of: Koks i Khim.), vol. 3:32-37, 1970.
A vacuum-carbonate plant was added to a coke and chemical
works in the USSR in 1960. The hydrogen sulfide removed
from the coke-oven gas is converted to sulfuric acid by a wet
catalytic process. Plant modifications introduced in the last
nine years have reduced hydrogen sulfide losses and power,
steam, and absorbent (soda and potash) consumption and in-
creased sulfuric acid yields. Among the improvements noted is
the reduction of scale formation on vacuum-pump cylinders.
This has been achieved by cooling the cylinders with purified
water, after lining and extracting the carbonate hardness salts.
Water throughput m the hydrogen sulfide gas coolers has been
increased by dividing the coolers into two independent groups,
each with its own gas and water circuits. Difficulties ex-
perienced in extracting dust and fines from the contact mass
used to oxidize sulfur dioxide to sulfur trioxide were
eliminated by purging the contact mass with air. The transfer
of sulfuric acid to storage tanks is now automated, and elec-
trostatic precipitators are being redesigned to reduce corrosion
and H2SO4 losses.
-------
20
COKE OVENS
24998
Perederii, P. K.
DEPHENOLOZING SCRUBBER PERFORMANCE. Coke
Chem. (USSR) (English translation from Russian of: Koks i
Khim.), vol. 3:38-39, 1970.
The phenol extraction coefficient of dephenolizing scrubbers
was raised from 0.746 to 0.870 by reducing the thickness of the
phenolate packing and increasing that of the alkaline packing,
increasing the force with which alkali is pumped into the al-
kaline packing, and maintaining a water load of 50-55 cu m/hr.
The increased thickness of the alkaline packing provides suffi-
cient surface area for contact between recirculating vapors and
fresh alkali; the thinner phenolate packing offers less re-
sistance to the recirculating vapors.
25216
Yermolova, V.
REPUBLICAN SCIENTIFIC-TECHNICAL CONFERENCE OF
YOUNG RESEARCH WORKERS. (Respublikanskaya nauchno-
tekhnicheskaya konferentsiya molodykh issledovateley). Text in
Russian. Koks i Khim., no. 7:59-61, 1970.
A report is given of a conference held in Khar'kov April 14-
16, 1970 and attended by young researchers, engineers, and
technicians. A total of 63 papers dealing with coal-chemistry
research and the by-product coke industry were presented,
and several of these are reviewed briefly. Removal of nitrogen
oxides from coke oven gas in electrofilters with brush dischar-
gers and the reduction of naphthalene content in coke oven
gas delivered to the gorlovsk nitrate fertilizer plant presenting
a novel method of removing naphthalene from absorbing gases
are described.
25315
Altybaev, M. and V. V. Streltsov
REMOVAL OF SULPHUR COMPOUNDS FROM GASEOUS
FUELS. Coke Chem. (USSR) (English translation from Rus-
sian of: Koks i Khim.), no. 8:43-45, 1966. 12 refs.
Studies were conducted on the role of hydrogen in intensifying
the removal of hydrogen sulfide from coke-oven and other
fuel gases by iron oxide. The hydrogen required for the experi-
ments was produced by catalytically cracking ammonia. It was
added to H2S produced in a Kipp apparatus and the gas mix-
ture supplied to an absorber containing a fluidized iron oxide
bed. Final removal of H20 was effected in an absorber con-
taining activated charcoal. In the presence of hydrogen, max-
imum purification of the gas stream took place at 350-400 C.
At hydrogen concentrations of 7-8%, all the sulfur present in
the gases passed into the absorbent. The maximum sulfur
capacity of different oxide sizes was found at 400 C. The
capacity was 20.5% for 0.15-0.25-mm fractions, 18.5% for the
waste oxide, and 16.0% for 0 25-0.42-mm fractions.
26075
Finkel'shteyn, P. K., V. P. Babenko, V. N. Kutuzov, and P.
L. Saltan
DECONTAMINATION OF USED AIR FROM AN INSTALLA-
TION FOR PRODUCTION OF HIGH-TEMPERATURE
PITCH. (Obezvrezhivaniye otrabotannogo vozdukha ustanov-
ki polucheniya vysokotemperaturnogo peka). Text in Russian.
Koks i Khim., no. 10:50-52, 1970.
Catalytic oxidation of resins, asphaltenes, carbenes, carboids,
paraffins, naphthenes, and aromatic compounds contained in
waste gases was studied experimentally. Effective removal can
be carried out at 400-600 C, thereby eliminating the possible
synthesis of carcinogenic substances associated with fire-box
oxidation. Suitable catalysts (bauxite, iron ore) are readily
available and relatively inexpensive. Irrigation of the conden-
sors of tray scrubbers to prevent direct contact of the aerosol
with the catalyst surface improved efficiency.
26606
Balla, P. A. and G. E. Wieland
PERFORMANCE OF GAS-CLEANING SYSTEM ON COKE
OVEN LARRY CAR AT BURNS HARBOR. Blast Furn. Steel
Plant, 59(l):22-26, Jan. 1971. (Presented at the American Iron
and Steel Institute Regional Technical Meeting, Chicago, 111.,
Oct. 15, 1970.)
A larry car system for cleaning emissions from slot-oven cok-
ing operations was equipped with combustion chambers with
adjustable airports and two stainless steel ventrui scrubbers.
Although this system reduced emissions, combustion of gas
was not always complete before it entered the scrubbers. By
installing gas-fired burners and enlarging airports to increase
airport to gasport ratio, scrubber efficiency was raised to
about 96% at an oven charging time of 2.5 min. Under these
conditions, scrubber emissions are about 0.7 Ib/charge (0.16
grams/scf dry) and the only visible stack effluent is a white
stream plume. Further improvement is anticipated following
the enlargement of combustion chambers and ducts.
26607
Narata, N. and S. Kanbara
A NEW DUST COLLECTION METHOD FOR COKE OVEN
QUENCHING TOWER. (Kokusu shokato no datsu shujm
hoho). Text in Japanese. (Sumitomo Metal Industry Co.,
Osaka (Japan)) Japan. Pat. Sho 45-28302. 3p., Sept. 16, 1970. 1
ref. (Appl. Oct. 15, 1966, claims not given).
The amount of water required for the rapid, effective
quenching of one batch of burnt coke (10-20 tons) causes
neighborhood air pollution. An arrangement of water supply
outlets is described which cleans and cools the steam and dust
generated in such a way that the volume of steam is reduced.
Automatic outlets for spraying are provided at the top and side
of the quenching tower; a third outlet for cleaning and conden-
sation is provided at the border of the quenching tower and
exhaust tower Water is supplied from the third outlet only
during the first 20-30 seconds of quenching, when dust is
generated. To avoid increasing the water content of coke on
the quenching wagon, the exhaust tower is not installed
directly above the quenching tower. The arrangement can easi-
ly be adapted to traditional quenching systems.
27441
Ghigny, P.
DUST SEPARATOR INSTALLED IN A COKE PLANT. (In-
stallation de depoussierage dans une cokerie). Text in French.
Tribune CEBEDEAU (Centre Beige Etude Doc. Kaux),
21(300:681-686, Dec. 1968.
The Vilvorde Coke Plant, originally built on flat swampy
wasteland along the Brussels Maritime Canal, now finds itself
becoming part of a heavily populated area, necessitating the
purchase of more adequate dust removal equipment, which is
descnbed. Use is made of a system of tubes-within-tubes, by
means of which coal is introduced into the furnace through the
innermost tube, while the waste gases are pumped out through
the ring-shaped chamber between the inner and outer tubes.
The furnace is insulated from the external environment by a
series of hoods erected above the furnace, into which the
waste gases are aspirated by the blower, which is equipped
with special rotating screens which aid in condensing the gases
-------
B. CONTROL METHODS
21
onto the dust particles contained within them, thus removing
these particles from the stream of gas. Detail are given on how
this basic idea was refined to meet the demands of engineering
practice. Tests indicated that the equipment removed 85% of
the dust from the plant emissions, and that the unremoved
dust amounted to an average of 55 mg per square meter, con-
siderably below the minmum of 300 mg established by a com-
mission of the West German government.
27563
Kalmykov, A. V , V. N. Tyukanov, M T. Gubanov, and A.
M. Dolzhenko
INDUSTRIAL INVESTIGATIONS OF THE WET DUST
CATCHER APM-IGI ON A DRYER-TUBE. (Promyshlennyye
issledovaniya mokrogo pyleulovitelya APM-IGI na trubke-
sushilke). Text in Russian. Koks i Khim., no. 12.6-8, 1970. 3
refs
An APM-IGI dust catcher with a capacity of 75,000 cu m/h
was tested in conjunction with an industrial drier. Operation
with a conical nozzle gave 95.3-96.0% coal-dust removal (a
reduction from 1.16-2.6 g/cu m to 0.02-0.04 mg/cu m), reflect-
ing a 1 5-2% greater efficiency than was achieved with a disk
nozzle. Water consumption rate was 150-175 g/cu m.
27638
Becker, Rudolf
FLUSHING WITH RESIDUAL UNCONDENSED GAS MIX-
TURE AFTER VACUUM REMOVAL OF CONDENSED COM-
PONENTS. (Gesellschaft fuer Linde's Eismaschinen A. G.,
Wiesbaden (West Germany)) U. S. Pat. 3,421,332. 7p., Jan. 14,
1969. 8 refs. (Appl. Dec. 14, 1964, 2 claims).
Regenerative heat exchangers used for removing condensable
components of gaseous mixtures are customarily freed of con-
densate by a counterflow of cold, purified gas in one or more
flushing periods. In all systems, the condensed component is
recovered in admixture with the flushing gas and is thus in
diluted form so that subsequent separation steps, e.g , absorp-
tion of fractional condensation, are required at considerable
expense. The present invention provides an economical means
of separating condensable components from gaseous mixtures
without significant material dilution. The method, which is
especially helpful in removing hydrogen cyanide, hydrogen
sulfide, carbon dioxide, and ethylene from coke-oven gas uses
a low-temperature installation in which gas components are
fractionally condensed in heat exchangers that are subjected to
an exhaust period to eliminate all residual oven gas without
substantial volatilization of the condensate. The condensate is
subsequently extracted under vacuum without admission of
any scavenging gas to the heat exchanger. A final flushing by
the gases discharged from the condensate-containing exhanger
and cooling of the condensate by pur gas (to prepare the heat
exchanger for subsequent condensation) complete the cycle.
(Author abstract modified)
28228
Mott, R. A.
PRELIMINARY PURIFICATION OF CRUDE GASES. In:
Gas Purification Processes. G. Nonhebel (ed.), London,
George Newnes Ltd., 1964, Chapt. 4, p. 77-120. 27 refs
Preliminary purification of crude gases which arise from the
carbonization of coal in coke ovens (coke-oven gas) and
gasworks retorts (town gas), or from the gasification of coal or
coke in gas producers (producer gas or water gas) and of coke
in blast furnaces (blast-furnace gas) is considered. The purpose
of such purification is to remove both vapors of tar, water,
naphthalene, and benzole and mechanically carried solid parti-
cles of tar, naphthalene, and dust. In certain of the processes
considered, preliminary purification includes the removal of
ammonia gas. Purification of the crude gases is achieved by
cooling or washing (usually with water or oil) and by electro-
static precipitation. Comparison is made between these
procedures as they apply in coke-oven practice and gasworks
practice. Separate sections deal with special features of the
purification of producer gas, water gas, and blast-furnace gas.
(Author introduction modified)
28384
Beck, Kurt-Guenther and Wilhelm Weskamp
THE INCREASE OF PRODUCTIVITY OF COKE OVEN
GROUPS THROUGH HIGHER OPERATING TEMPERA-
TURES. (Steigerung der Produktivitaet von Koksofengruppen
durch hoehere Betriebstemperaturen). Text in German.
Glueckauf (Essen), 107(2):43-51, Jan. 1971. 8 refs. (Presented
at the Imformationstagung 'Technik und Entwicklung der
Veekogung von Steinkohle' der Kommission der Eu-
ropaeischen Gemeinschaften, Luxemburg, Belgium, April
1970.)
In an experimental coking plant, coals with 20 to 30% volatiles
were coked at 1350 to 1500 C. Increasing the temperature from
1350 to about 1490 C reduced the coking time from 14 to 11
hrs and increased the throughput from 24.7 to 34.5 tons/24 hrs.
This is a throughput increase of 27.5%. The waste gases
produced in the 450-mm wide combustion chambers contained
between 7.4 and 8.4% carbon dioxide, depending on the tem-
perature in the combustion chamber and between 2.9 and 3.2
oxygen. Temperatures of the waste gases ranged from 229 C at
a combustion temperature of 1348 C to 246 C at a combustion
temperature of 1360 C. Waste gases with temperatures
between 308 C at a combustion temperature of 1343 C and 339
C at a combustion temperature of 1480 C were measured. The
quantity of waste gas produced at an air surplus at n equals
1.2 was 38,988 cu m/24 hrs at 1343 C and 56,520 cu m/24 hrs
at a combustion temperature of 1480 C.
28532
Sedach, V. S., G. S. Nosko, Ya. D. Semisalov, and N. A.
Polkovnichenko
INCREASING SCRUBBER THROUGHPUT BY MODERNIS-
ING THE NOZZLES. Coke Chem. (USSR) (English transla-
tion from Russian of: Koks i Khun.), no. 70:47-48, 1970. 3
refs.
The possibility of improving the design of the nozzles used in
benzole scrubbers was investigated in order to give better
atomization and increase the volume of liquid absorbent with
installing more nozzles. By adjusting the live sections of the
spray nozzles, it has been possible to increase the wash oil
throughput by 11%. The modernized nozzles distribute the
spray more uniformly over the top of the grid packing in the
scrubber, and their useful life is much longer. The extra power
consumed by the new nozzles is within the capacity of the
pumping equipment already provided. (Author conclusions
modified)
29217
Marling, Donald G. and George E. Balch
CHARGING PREHEATED COAL TO COKE OVENS. Blast
Furn Steel Plant, 58(5):326-329, May 1970. (Presented at the
Iron and Steel Institute, Coke in Iron Making Meeting, Lon-
don, England, Dec. 10-11, 1969.)
-------
22
COKE OVENS
The principal advantages to be derived from the charging of
preheated coal to coke ovens are that the required residence
time in the coke oven is drastically reduced, while the use of
lower cost weakly coking or high oxygen coals to be utilized
for a major portion of the coal mix can be used. A reduction
in air pollution is accomplished through the use of closed
system pipeline charging to replace conventional larry car
charging. The system appears to be readily adaptable to auto-
mation, while the improvement in battery top conditions helps
to solve the increasingly more difficult problem of finding peo-
ple for this work. Laboratory and early experimental work on
preheating are mentioned, as well as pilot plant demonstrations
and attempts at commercial operation
29240
Watanabe, Sadaharu
COKE CAKE GUIDE CART WITH DEVICE TO PREVENT
AIR POLLUTION. (Kokus keiki annaisha ni okeru gaiki osen
boshi sochi). Text in Japanese (Shinwa Trading Co (Japan))
Japan. Pat. Sho 45-38134 4p., Dec 2, 1970. (Appl. July 5,
1967. claims not given).
A device was designed to prevent air pollution caused by the
dispersion of coke dust when coke cakes are pushed out of a
coke oven. Coke dust generation can be kept to a minimum
and the dust generated will be effectively collected by a wet
type dust collector The following are installed on a track-
guided cart next (o the coke oven, the coke guide which
guides coke cakes from the oven to the quench cart, the dust
hood which absorbs dust gas rising from the coke cakes, and
the dust collector which is connected to the dust hood. Dust
gas generated during transfer of coke cakes through the coke
guide is kept to a minimum and will never be discharged into
the atmosphere Since the coke guide is shaped so that is aper-
ture gradually wmdens toward the exit and since it is made to
plunge into the dust hood to assure air-tight connection while
permitting free slide action, coke cakes will move very
smoothly through the coke guide into the quench cart, thus
giving a minimum crushing of coke cakes during the transfer
to assure minimized generation of dust gas Thus, less volume
of air is needed for dust collection As a result, a dust collec-
tor of smaller output capacity can be used with this system for
economical operation
29628
LAW-MAKERS SAY: CLEAN UP OR SHUT DOWN. Can
Chem. Process., 55(4):47-50, Apul 1971.
The major push by the Canadian government lo control air
pollution will surely come once Parliament approves Bill C-
224, the Clean Air Act Under the Act, air polluters may be
fined up to $200,000 per instance ol violating one or more of
the emission standards to be set by the Federal government
Also, the Act will empower federal authorities to fine any pol-
lution source regardless of location; this is a major departure
from current federal/provincial division of powers. Controlling
the fumes from coking is mentioned, as well as regulations
pertaining to the emissions from petroleum refineries, lead-in
gasoline, automotive emissions and aircraft exhaust smoke.
Processes for the removal of sulfur dioxide are listed tabu-
larly. The British Columbia government has offered a prize of
$250,000 for the first individual or company to come up with a
device to eliminate air pollution and odor of pulpmills
29900
Koyama, Setsu, Yasuo Saito, Shigenori Komura, Koji
Tashiro, Yasumasa Ishibashi, Shozo Sugita, Yuzo Yamashita,
and Tetsuji Hayashi
TECHNICAL DEVELOPMENT OF MITSUBISHI-LURGI GAS
CLEANING PLANT. Text in Japanese. Mitsubishi Juko Giho
(Mitsubishi Heavy Ind. Tech. Rev.), 8(2):239-249, March 1971.
Mitsubishi and Lurgi Apparatebau G.m.b.H. in West Germany
both worked on gas cleaning plants singly and jointly. Lurgi
studied the essential components of the plant, and Mitsubishi
tested various conditions on an actual plant. The problems of
gas distribution, erosion, corrosion, and construction are
discussed. Also the installation of electrostatic precipitators,
multicyclones, cyclones, stabilizers, and venturi scrubbers are
discussed. Several relationships were examined in electrostatic
precipitators, including the relation between distance of elec-
trodes and critical voltage; the relation between distance of
electrodes and the corona current in an electrostatic precipita-
tor for an electric arc furnace; the relation between distance of
electrodes and corona current under gas with talc of 5 micron
mean diameter, the relation between distance of electrodes
and migration velocity of dust particles; the relation between
sparkover voltage and specific surface area of a dust particle;
an example of the voltage measured in an actual electrostatic
precipitation for a sintering plant; and an example of the
specific electric resistance of dust. Lattice, louvei, and flap
deflectors are also discussed. Flow distribution and deviation
are described. Other topics include the relation between pres-
sure loss and cyclone performance; the effect of blow down in
a multicyclone, examples of performance of a two-stage ven-
turi scrubber, a twist layer filter, and the weight reduction ten-
dency on a dry precipitator; the evaporation speed of a water
droplet in a gas cooler; examples of the amount of sulfunc
acid measured and a corrosion test at an electrostatic
precipitator for an oil firing boiler, and the gas analysis at par-
tial burning of LD converter gas, the explosion band of mixed
gas, the relation of flow ratio to the performance of canopy
hood and lateral exhaust hood; the relation between per-
formance and dimension of canopy hood, and examples of gas
cleaning plants installed in a steel works, cement works, sul-
furic acid plants, and coke ovens
31123
Oki, Taketo, Tetsu Abe, Akira Toyama, and Shigeru Haseba
CONTACT TYPE REMOVAL METHOD FOR NO CON-
TAINED IN GAS MANUFACTURED FROM COAL, COKE,
OR OIL. (Sekitan, cokusu, abura nado o genryo t suru gasu
chu no sankachisso no sesshokuteki jokyo hoho). Text in
Japanese (Nikki Kagaku K. K. (Japan) and Kobe Seikosho K.
K (Japan)) Japan Pat. Sho 46-18383. 4p., May 22, 1971. 1 ref.
(Appl Sept. 18 1967, 1 claim)
A new nitric oxide removal method with good efficiency was
described. The catalyst is made of an iron oxide and
pretreated with hydrogen sulfide at a low temperature. The
catalyst is used for a contact reaction to selectively remove
NO while minimizing losses of carbon monoxide, ethylene,
and other useful contents of the gas The catalyst, made of r-
FE203.H20 or Fe304, or an iron oxide containing both, is
molded as it is or with a silica, alumina, magnesia, or diatom
earth carrier and treated with hydrogen sulfide at 50-100 C.
The gas manufactured from coal, coke or oil is treated at the
temperature of 150-250 C by this catalyst to remove NO con-
tained in the gas.
-------
B. CONTROL METHODS
23
31138
Jagnow, Hans-Joachim
PRODUCTION OF RICH GAS BY THERMAL
HYDROCRACKING OF MINERAL OIL MIXTURE WITH
COKE OVEN GAS AS HYDROGEN SOURCE. (Reichgaser-
zeugung durch thermische hydnerende Spaltung von
Mineraloelgemischen mil Kokereigas als Wasserstoffquelle).
Text in German. Erdoel Kohle (Hamburg), 24(6):384-389, June
1971. 2 refs
Over a period of six years, experiments were conducted in a
small pilot plant and in a scaled-down laboratory device to col-
lect data for planning large cracking plants using coke oven
gas as a hydrogen source. For the experiments, the gas recycle
hydrogenator was used. All hydrocarbons from light naptha,
with an upper boiling point of roughly 100 C, to crude oil
distillate, with an upper boiling point of about 350 C, are suita-
ble. Both cleaned and partially cleaned coke oven gas can be
used. The quality of the end product is the same in either case
However, when using uncleaned coke oven gas, the ammonia
must be removed to avoid ammonium carbonate formation
The removal of hydrogen sulfide prevents corrosions. It is also
advisable to remove benzene from coke oven gas prior to its
use. Such partly cleaned coke oven gas is free of NH3, con-
tains about 1.5 g H2S, and up to 10 g benzene/cu m. A rough
cost estimate shows that the heat price of the produced en-
riched gas is higher than the heat price of the coke oven gas.
However, coke oven gas will sell at a lower price in the fu-
ture. Thermal hydrocracking provides a large new market for
the use of this gas
31223
Kosaki, Motokiyo
ON EQUIPMENT DESIGNED TO DISPOSE OF COMBUSTI-
BLE WASTE GAS AND DISPERSE IT INTO THE AT-
MOSPHERE. (Kanensei haigasu taiki hosen setsubi ni tsuite).
Text in Japanese. Nenryo Oyobi Nensho (Fuel and Com-
bustion), 38(7): 17-26, July 1971. 5 refs.
Combustion/dispersion equipment, designed to remove the
combustibles, noxious contents, and offensive odors from
waste gases by combustion, and thereafter discharge the waste
gas for atmospheric diffusion is described. The Technical
guidelines for designing the respective component units of the
equipment or plant are also described Among the combustible
waste gases are blast furnace gas, coke oven gas, converter
furnace gas, metal refining waste gas, naphtha refining waste
gas, gasoline cracking gas, and hydrocarbon cracking gas The
main component units of the equipment include a knockout
drum, seal tank, flame arrester, ignition device, flare gas
burner, and stack with a stack support tower. The knockout
drum is designed to remove solids, liquid contents, and con-
densate from the saturated gas contained in the flare gas, and
water content given off from washing. The seal tank prevents
back fire from going from the flare stack to the flare gas line.
The tank is kept filled to a specified water level to seal the
mouth of the flare gas line, which is held underwater. The
flame arrester also prevents back fire The ignition device ig-
nites the pilot burner, which in turn ignites the flare gas burner
nozzle, located above the ground level. The ignition device al-
lows the burner to be ignited from the ground level. The flare
gas burner comes in various sizes and types, and can be
selected according to operating conditions. The stack and
stack support tower can also be built to suit the operational
conditions.
31682
Marchenko, Yu. G. and V. E. Novikov
DETERMINING THE MINIMUM LOSSES OF BENZOL
HYDROCARBONS IN THE FINAL COKE-OVEN GAS. Coke
("hem. (USSR) (English translation from Russian of: Koks i
Khim.), no. 11:30-32, 1970. 2 refs.
Based on analysis of a mathematical model of closed-cycle ab-
sorption-desorption processes in benzol (benzene) plants,
benzol losses in the final coke-oven gas can be minimized only
by controlling the wash oil circulation rate. Since the optimum
circulation rate for wash oil varies widely according to specific
operating conditions in a recovery plant, a specific mathemati-
cal model of the benzol scrubber unit must be constructed for
each case.
31777
Revzin, I. G., S. N. Ganz, Ya. I. Shukh, and I. N. Gorokhov
PRODUCTION OF THIOUREA FROM CALCIUM CYANA-
MIDE AND HYDROGEN SULPHIDE FROM VACUUM-CAR-
BONATE SULPHUR REMOVAL PLANT. Coke Chem. (USSR)
(English translation from Russian of: Koks I Khim.), no. 3:27-
29, 1970. 8 refs.
A process has been developed for making thiourea
(2CS(NH2)2) from calcium cyanamide and the hydroge sulfide
from vacuum-carbonate sulfur removal plants in the coke and
chemical works The chief merits of the proposal are that the
process is continuous, one stage is eliminated, side reactions
are reduced to a minimum, and the reaction rate is high.
Values have been determined for the basic parameters, as well
as the raw materials consumption figures. (Author conclusions
modified)
33382
Sommers, Hans and Werner Last
REMOVAL OF ORGANIC SULPHUR FROM COKE OVEN
GAS. III. TEST RESULTS WITH TWO STEP PROCESSES.
(Entfernung von organischen Schwefel au Koksofengas. III.
Ergebnisse der Versuche mit zweistufigen Verfahren). Text in
German. Erdoel Kohle (Hamburg), 24(9):578- 586, Sept. 1971.
Part I. Ibid , 24 (7).473-477, July 1971. Part II. Ibid, 24(8):525-
529, Aug 1971.
For the hydrogenation of organic sulfur compounds to
hydrogen sulfide, a four percent cobalt oxide and 12% molyb-
denum tnoxide catalyst with a five percent nickel oxide and
11.5% molybdenum trioxide catalyst were used in a two-step
removal process The catalysts had a bulk weight of 690-760
g/1 and a specific surface of about 250 sq m/g. A third catalyst
with about one percent platinum on aluminum oxide was in the
form of granules two to four mm in diameter; a fourth catalyst
had a high nickel content. At increased pressures, the first two
commercial catalysts proved to be suitable for hydrogenation.
The laboratory-made platinum catalyst was suitable at at-
mospheric pressures. Iron compounds are recommended to
replace zinc compounds for the absorption of hydrogen sulfide
once it is already formed.
34081
Lee, G W. and J P. Graham
MITIGATION OF SMOKE, DUST, AND GRIT AT COKE-
OVEN PLANTS. Iron Steel Inst., London, Spec. Kept., no.
61:51-55, 1958. 10 refs. (Presented at the Iron and Steel In-
stitute, Air Pollution Meeting, London, England, Sept. 25-26,
1957.)
-------
24
COKE OVENS
Coke oven plants and the present scale of carbonization are
examined with respect to primary sources of smoke, grit, and
dust emissions, preventive actions, and future developments.
Pollutant emissions occur during charging, carbonization, and
discharging, quenching, and handling of coke. Improvements
in the processes to mitigate emissions include efficient door
handling to obviate unnecessary exposure to heat, careful at-
tention to the design of the coke guide, oven tops, and coal
charging hoppers, the use of a double take-off, portal-type
changing cars, improved design of charge-hole cover, mechani-
cal cleaning of self-sealing doors and oven tops, dry
quenching, and the total enclosure of coke screens.
34083
Purcell, P. R. and T. H. Williams
THE EXTRACTION OF SULPHUR FROM COKE-OVEN GAS
AND THE MANUFACTURE OF SULPHURIC ACID. Iron
Steel Inst., London, Spec. Kept., no. 61:56-61, 1958. (Presented
at the Iron and Steel Institute, Air Pollution Meeting, London,
England, Sept. 25-26, 1957.)
An account of the Collin process shows that desulfurization of
the coke-oven gas, combined with the manufacture of sulfuric
acid from the recovered hydrogen sulfide by the Chemiebau
wet contact process, has been introduced with success on the
coking plant at Corby in Britain The type of process which
was installed at Corby is an absorption-desorption process
using ammonia liquor as a scrubbing agent. The absorption is
carried out in unpacked towers so that no excessive additional
load is placed on the gas exhausters, and the concentration of
the ammonia liquor of about 1.5% is such that it is m equilibri-
um with the ammonia content of the gases and no plant for the
production of concentrated ammonia liquor is required. Fol-
lowing the solution of the corrosion troubles encountered in
the early operation of the plant, it has since worked with
satisfactory consistency. Desulfurization of 70-75% is achieved
and the quantity of acid produced is just about sufficient to
meet the requirement for ammonium-sulfate manufacture in
the by-product plant.
34207
Viswanathan, T. S. and S. Visvanathan
RECOVERY OF SULPHUR FROM COKE OVEN GAS: A
CRITICAL REVIEW OF METHODS. Tisco (Jamshedpur),
15(3):104-110, July 1968. 27 refs.
Coke oven managers have long been aware of the anomaly
that while they have to buy sulfur to make the acid to fix the
ammonia in coke oven gas, they must also incur considerable
expense and trouble eliminate the sulfur to meet consumer
requirements. Dry processes for the removal of sulfur include
an oxide purification system, the Katasulf process, and a
fluidized bed process; wet processes include the Seaboard
process, vacuum carbonate or hot actification process, Alkazid
process, Thylox process, Giammarco-Vetrocoke process, and
iron suspension process, the Collin process, Tata-Collins
process, and the Stretford process. A review of the various
established methods for the removal and recovery of sulfur
from coke oven gas and their possible applicability to the Tata
Iron and Steel Works shows that the Thylox process, which
yields elementary sulfur, or the vacuum carbonate and the
Collin process, which furnish the sulfur as hydrogen sulfide,
offer economic possibilities.
34336
Zlatin, L. E., G. I. Trondina, Yu. P. Artamonov, A. L. Shtein,
and Yu. D. Yukhonovets
DEN1TRATION OF SULPHURIC ACID FOR THE PRODUC-
TION OF AMMONIUM SULPHATE. Coke Chem. (USSR) (En-
glish translation from Russian of: Koks i Khim.), no. 3:43-44,
1970. 4 refs.
At a Soviet coke and chemical plant, ammonium sulfate is
made from spent 72-73% sulfuric acid taken from the
nitrobenzene plant. The nitrogen oxides contained in this acid
contaminated the coke oven gas, rendering it unsuitable for
subsequent use for ammonia synthesis. Thorough denitration
of the sulfuric acid is now effected by adding urea to the acid
and agitating the mixture with compressed air. The com-
pressed air also serves to remove the nitrogen formed as the
urea reacts with the nitric oxides. The removal of the nitrogen
accelerates the reaction between the nitric oxides and the urea.
A sulfuric acid storage tank is used as the denitration vessel,
and the process reaches completion in three to four hours.
When the ammonium sulfate plant is operated with acid
denitrated in this way, the nitric oxide content of the coke-
oven gas remains unchanged.
34421
Litvinenko, M. S.
UKHIN IN THE CHEMICALIZATION OF THE NATIONAL
ECONOMY. Coke Chem. (USSR) (English translation from
Russian of: Koks i Khim.), no. 4:34-37, 1970.
Process developments are enabling Russian coke and chemical
plants to supply chemical and other industries with needed raw
materials and intermediates. The developments include the
long-distance transmission of coke oven gas for ammonia
synthesis, the production of phthalic anhydride and pure
anthracene, the continuous formaldehyde purification of
napthalene, the production of sodium hydrosulfide and am-
monium sulfide from hydrogen sulfide gas, the production of
mesitylene and m-xylene, the production of pure sodium thio-
cyanate, and the catalytic refining of benzene for syntheis.
Additional products will be made at coke and chemical plants
scheduled for construction within the next five years: dark
coumarone-indene resins, n-cresol, p-cresol, pitch semicoke,
prepared tar, road tar, colloidal sulfur, 2-vinylpyndme,
pyrene, acenaphthene, and acenaphthylene. Specific product
applications are cited and the need to expand the market for
aromatic products of carbonization is noted. Radical improve-
ments in recovery techniques applied to the main chemical
products of carbonization are greatly reducing air and water
pollution. The improvements involve placing the hydrogen cya-
nide and sulfide recovery plant first in the gas flow sequence.
34465
POLLUTION CONTROL PROGRESS. INDUSTRIAL CASE
STUDIES. J. Air Pollution Control Assoc., 21(11):728-730,
738, Nov. 1971.
Successful case studies of pollution control in industrial emis-
sion sources are reviewed. Odor, emitted by condensation
products from oils and pitch condensates from wood chips, in
a hardboard tempering plant was controlled by fume incinera-
tion treatment; heat recovered from the process was used to
preheat the incoming contaminated gas prior to incineration,
resulting in a 60% saving in fue'. Emissions from electric
power plants were controlled by conversion from coal to bu-
tane/propane fired boilers and by a filtering system to
eliminate fly ash. A portable sprinkler system to control fly
ash collected by precipitators on electric generating station
-------
B. CONTROL METHODS
25
grounds was nearly 100% effective in preventing stored fly ash
from being windborne. Coke ovens designed for smoke control
and automated fume control systems for electric arc furnaces
controlled emission from steel plants. A scrubbing system,
consisting of a dry cyclone collector, a wet scrubber, and a
mist eliminator, was used effectively in a coal preparation
plant. Conversion of conventional sulfuric acid plants to the
double contact process effectively reduced sulfur dioxide
emissions and increased recovery capacity. An incinerator unit
was used to dispose of residual tar fractions (fly ash and air-
borne solids) from a phenol plant. Plasticizer emissions from
the flooring operations of a cork industry were controlled by
mist eliminator elements.
35284
Carbone, Walter E.
COKE-OVEN EMISSION CONTROL. Iron Steel Engr.,
48(12):56-60, Dec. 1971.
Total emissions (dust, carbon monoxide, hydrogen sulfide, sul-
fur dioxide, benzene, and tar) from coke oven charging opera-
tions can amount to almost six tons/day. A solution to the
emission problem may be the pipeline charging of preheated
coal to coke ovens. In a typical charging system, coal no
larger than one inch is first fed to the flash-drying entrainment
section of the preheater unit. Here only particles less than
one-eighth inch are removed. Larger particles are suspended
until heated to a surface temperature of 700 F and crushed to
less than one-eighth inch by a rotating swing hammer. Coal
leaving the preheater goes to a primary cyclone where approx-
imately 80% is recovered. Effluent from the primary cyclone
is then sent to four or more secondary cyclones where the
remaining coal dust is collected. Overall efficiency of the
cyclone recovery system is 99.5% of the coal input. Coal from
the cyclones is collected on a common screw conveyor and
discharged to charging bins. A portion of the gas from the
secondary cyclones is recycled back to the combustion
chamber, and the balance sent to a wet scrubber. Since the
system is completely sealed, no emissions escape to the at-
mosphere during charging operations. The method also reduces
emissions occurring during pushing operations.
35503
Grosick, Herbert A.
SYSTEM FOR THE REMOVAL OF NAPHTHALENE FROM
COKE OVEN GAS. (Koppers Co., Inc. Pittsburgh, Pa.) U. S.
Pat. 3,581,472 5p., June 1, 1971. 2 refs. (Appl. Aug. 8, 1969,
10 claims).
In the past, residual naphthalene has been removed during the
final cooling of the coke oven gas by precipitating as crystals.
However, this can cause clogging and does not completely
remove naphthalene vapor. Therefore, on improved process
was developed for the removal of naphthalene from coke oven
gas. Coke oven gases are cooled in a primary cooler to about
100 F to condense a light oil fraction (primary cooler tar) from
the gas. The condensed tar is collected and withdrawn from
the primary cooler; the naphthalene is stripped from the tar
and is scrubbed from the cooled gas with the primary cooler
tar. (Author abstract modified)
35759
Kipot, N. S., A. I. Brodovich, and V. M Zaychenko
BRUSH DISCHARGE FILTERS USED FOR THE REMOVAL
OF NITRIC OXIDE FROM COKE OVEN GAS. (Ochistka kok-
sovogo gaza ot okisi azota v elektrofiltrakh s kistevym raz-
ryadom). Text in Russian. Koks i Khim., no. 5:31-34, 1971. 10
refs.
Removal of nitric oxide from coke oven gas by means of elec-
tric brush discharge filters was investigated on a pilot plant.
The voltage potential promotes conversion of oxygen (con-
tained in the coke oven gas) into ozone, which enhances the
oxidation of NO into nitrogen dioxide. Removal of NO from
coke oven gas is affected by the voltage potential created
within the electric filter, by the period of permanence of the
gas within the filter, and by its initial content in NO. A certain
volume of gas to be cleaned should spend at least nine
seconds within the filter under conditions of 32 kilovolt to
achieve a 93% removal of NO. The efficiency of this cleaning
process is optimal under conditions of 41 kilovolt, but in-
creased initial concentrations in NO produce negative results.
Thus, concentrations of 0.62 cu cm/cu m NO achieve a 93%
cleaning of the coke oven gas, while initial concentrations of
3.66 cu cm/cu m NO decrease the extent of the cleaning
process to 72%. Both observations were carried out with 34
kilovolt potentials. A mathematical relationship expressing the
dependence of the cleaning process upon the three mentioned
factors effects design criteria for such gas cleaning facilities
according to the cleanliness to be achieved and the initial con-
centrations in NO existent in the given gas.
37343
CONTROLLING EMISSIONS FROM COKE OVENS. En-
viron. Sci. Technol., 6(2):118-119, Feb. 1972.
Since the early 1900 s, by-product ovens have become stan-
dard and collect most of the volatile material during the coking
operation for conversion into useful products such as gas, tar,
and ammonia liquor. Coke oven emissions contain carbon
monoxide, sulfur dioxide, hydrogen sulfide, hydrogen cyanide,
and phenol. Charging contributes the largest part of the emis-
sions in the coking operation. Design and construction of a
$1.5 million prototype system for smokeless charging of coke
ovens has been sponsored jointly by the American Iron and
Steel Institute and the Environmental Protection Agency for
the past three years. The idea behind the prototype system is
that if coal is fed into an oven through a sealed feed hopper
and adequate suction is maintained by properly designed steam
jets, pressure in the oven will never be positive during charg-
ing. National Steel Corp. is hoping to solve the environmental
problems in charging, pushing, and quenching by one complete
system. A completely self-contained charging system will use
double collecting mains and a method known as charging on
the main, a sulfur removal system to produce elemental sulfur,
an ammonia destruction system, oxides of nitrogen control
system, and a closed system for coke pushing and un-
derground quenching. Another demonstration project is a coke
pellet manufacturing process designed to eliminate coke oven
emissions by eliminating coke ovens.
37674
Gobiet, Viktor
REDUCTION OF THE DUST EMISSION DURING THE
PROCESS OF PRESSING THE COKE THROUGH THE
COKE MASS PILOTING STATION BY A DUST COLLEC-
TOR. (Verminderung der Staubemission beim Druecken des
Kokses durch Entstauber-Kokskuchenfuehrungswagen). Text
in German. Glueckauf (Essen), 108(5):180-183, March 1972.
The process of pressing coke through the coke mass piloting
station produces dust in the opening of the coke oven door, in
the exit of the coke mass from the furnace chamber, in stirring
the coke in the tub of the piloting cart, and in the breaking and
falling of the coke into the quenching trough. For reducing the
dust emission, a mobile roofing with an exhaust fan and dust
collector was installed over each coke mass piloting and
quenching cart At first the dimensions of the exhaust fan
-------
26
COKE OVENS
were underestimated, and it had to be enlarged. The final ver-
sion was connected to two independently-operating rotary wet
collectors. Examination of the newly installed dust collection
system revealed that the quantity of dust-laden air being
drawn off by the exhaust fan depends on the prevailing wind
conditions. On the average, 90% of the emissions are drawn
off. The wet collectors achieve collection efficiencies of 97.5
to 97.7%. The average wind speed at the time of the collection
efficiency measurements was 10.6 m/sec; the prevailing wind
direction was south to southwest.
38832
Pustovit, Yu. A., V M. Kirillin, T. V. Shinkareva, and G. Ye.
Borodina
AN ANALYSIS OF TECHNICAL PROCEDURES TO BE AP-
PLIED FOR THE EXTRACTION OF AMMONIA AND ACID
COMPONENTS FROM COKE GAS. (Analiz tekhnicheskikh
razrabotok po izvelecheniyu ammiaka i kislykh komponentov
iz koksovogo gaza). Text in Russian. Koks i Khim., no. 1:44-
48, Jan. 1972. 8 refs.
The basic trends in the field of the extraction of ammonia and
acid components from coke gas are outlined on the basis of an
analysis of related inventions and technical solutions in the U.
S., USSR, Great Britain, and the German Federal Republic
during 1950-1967. In the next 5-10 yrs, ammonia from coke gas
will be utilized in fertilizer production, and the technology
used in manufacturing ammonium sulfate will be further
developed to obtain macrocrystalline and granulated products
The importance of processes for the extraction of acid com-
ponents is confirmed by the increasing number of related new
methods and apparatus. More than 550 patents relating to the
extraction of ammonia water, free ammonia and acid com-
ponents such as hydrogen sulfide, the production of ammoni-
um sulfate, and extraction equipment have been registered in
the four countries during 1950-1967. Nitric oxide present in
coke gas can be removed by means of ultraviolet rays on
catalysts in the presence of unsaturated compounds.
39656
Smith, Jack
COAST S LARGEST STEEL PLANT KEEPS AIR CLEAN.
Air Eng., 1(8):21- 24, Nov. 1959.
The solutions to air cleaning problems at a steel plant are
presented. The sinter plant stack was built 301 ft high to ob-
tain better dispersion of the sulfur gases emitted. As a second
step to eliminate the sulfur problem, all plant railroad equip-
ment was diesel powered. Four Thomas continuous autometers
were installed at varying distances from the mill to record sul-
fur concentrations in the atmosphere. Three devices were in-
stalled next to each blast furnace in order to clean the gases.
First, the gas goes through a primary inertial-type dust catcher
which removes 62% of the incoming dust. The gas is further
cleaned to 98.75% in a gas washer. After the gas passes
through a pair of water film electrostatic precipitators, 99.98%
of the incoming dust is removed. The coke ovens are equipped
with self-sealing doors. Baghouses and dust collectors were
designed into the raw materials system, greatly reducing the
amount of ore dust. The open hearth stacks were built higher
than customary for proper dispersal of furnace emissions. Cot-
trell precipitators were installed on the open hearth furnaces.
39751
Belin, F. T., Ya. M. Bergart, N. N. Nikolaev, S. Ya. Shapiro,
and O. I. Eliseev
A BOILER FOR HYDROGEN SULPHIDE COMBUSTION.
Coke Chem. (USSR) (English translation from Russian of:
Koks i Khim.), no. 6:52-55, 1971.
An improved design for a boiler for the combustion of
hydrogen sulfide was adapted for use in the sulfur removal
plant of a coke and chemical works. The boiler is of the
through-flow separator type connected to an afterburning
chamber. Its basic merits include intense heat transfer in the
firebox, gas exit temperatures that can be regulated against
changes in load, highly efficienct mixture formation in the
burner unit, minimum formation of nitrogen and sulfur triox-
ide, resistance to corrosion, and simple design. The com-
bustion products are cooled to 700-750 C in the boiler before
going for conversion to sulfuric acid by the wet catalytic
process.
39904
Sussman, Victor H.
AIR POLLUTION AND ITS CONTROL IN THE STEEL IN-
DUSTRY. Iron Steel Engr., 39(5):80-84, May 1962. 5 refs.
Production of one ton of steel requires the use of over 10 tons
of air. Blast furnace production of one ton of iron results in
0.6 tons of slag, 0.1 tons flue dust, 5.1 tons gas, and occasional
mushroom clouds from furnace slips. Size and power require-
ments of air cleaning systems present major economic con-
siderations. Regulatory requirement vary depending upon
population density, meteorological conditions, and topography.
Gas cleaning equipment consists of a we' scrubber and an
electrical precipitator. It is impractical to provide gas cleaning
equipment for the large volumes of dust-laden gas discharged
periodically as the result of blast furnace slips. Hydrogen sul-
fide gas emanating from slag quenching pits presents an offen-
sive odor in nearby communities. Recent modifications in blast
furnace operations such as the injection of fuel oil have con-
tributed to air pollution. The by-product coke oven releases
contaminants during charging, coking, pushing, and quenching.
Sintering plants are equipped with collectors and electrical
precipitators. In open hearth operations, variations in dust
loadings and gas discharge rates complicate the economic
design of collectors. Electrical precipitators clean gases with
98% efficiency, cleaning 700,000 cu ft/min and discharging gas
with a loading not over 0.05 grains/cu ft. Filtration methods
for cleaning open hearth gases are being studied by Harvard
School of Public Health. Air pollution problems associated
with the Bessemer converter are similar to those of the blast
furnace and open hearth. The control of sulfur and other nox-
ious gases emitted during coal burning operations is being stu-
died by the Bureau of Mines and other groups. Because air
pollution control is relatively new, standards for control equip-
ment and emission standards are incomplete. Plant manage-
ment should accept responsibility for air pollution control and
make positive provisions for control devices in new construc-
tion.
39960
O Mara, Richard F.
DUST AND FUME PROBLEMS IN THE STEEL INDUSTRY.
Iron Steel Engr., 30(10):100-106, Oct. 1953. 6 refs.
The major areas in a typical steel plant operation where some
form of dust or fume control equipment is applicable are
reviewed. Hoods, ventilating fans, and cloth filters can be
used in the screening segment of ore handling operations.
-------
B. CONTROL METHODS
27
Mechanical collectors used in combination with electric
precipitators have a recovery efficiency of 98-99% in the sin-
tering plant. Dust from the coke screening plant can be con-
trolled with hoods, ventilation, and recovery equipment. The
advent of center inlet design in blast furnace gas precipitators
has proven advantageous, however, adequate precipitation
equipment for open hearth emissions has not yet been
developed. Bessemer converters present the greatest difficul-
ties in dust control; hooding problems are discussed. Test data
indicate that electrical precipitation is applicable. The design
of control equipment, including scrubbers and electric
precipitator, for electric furnaces is considered. Other m-plant
emission sources are noted: limestone and coal handling, coke
oven gas cleaning, open hearth raw materials, department
power house, blooming mill operations (scarfing machines),
hot strip mills, pickling plant, and powdered fuel heating fur-
40232
Thring, M. W. and R. J. Sarjant
DUST PROBLEMS OF THE IRON AND STEEL INDUSTRY.
MEASURES TO STOP ATMOSPHERIC POLLUTION. Iron
Coal Trades Rev., 174(4636): 731- 735, March 29, 1957.
(Presented at the Institution of Mechanical Engineers Con-
ference, London, England, Feb. 1957.)
Control methods to remove dust and fumes from waste gases
emitted by specific processes within the iron and steel industry
are reviewed. The applicability, efficiency, cost, and operation
of electrostatic precipitators, venturi scrubbers, continuous
slagwool filters, hoods within exhaust systems, wet scrubbers,
wet impingers, bag filters, wet tower gas washers, centngugal
separation, aerodynamic separators, and overfire air jets, to
control the emissions of iron oxides, manganese oxides, and
silicon oxides are examined. The adaptation of the control
equipment and process and design modifications are examined
for the open hearth furnace, Bessemer converter, arc furnace,
cupola, blast furnace, coke ovens, reheating furnaces, and
small heat-treatment furnaces.
40266
Speight, G. E.
AUl POLLUTION CONTROL IN IRON AND STEEL INDUS-
TRY. J. Fuel Heat Technol., 19(2):20-23, March 1972.
(Presented at the International Air Pollution Control and Noise
Abatement Conference, Jonkoping, Sweden, Sept. 1-7, 1971.)
The operating principles and adaptation of various control
techniques within the iron and bteel industry are examined.
The major emissions and sources within the industry include
grit, dust, and sulfur dioxide emitted during sintering in the
blast furnace; particulates, smokes, and gases (carbon monox-
ide, ammonia, SO2, hydrocarbons, and organic compounds)
from coking plant operations; grit and drizzle from hot coke
quenching; carbon monoxide, iron ore, sinter, and coke parti-
cles from blast furnaces; iron oxide fumes and smokes in the
steelmaking process; sulfur dioxide, dusts, and fumes from
open hearth furnaces; basic oxygen furnaces; and electric arc
furnaces. Cleaning and control processes and equipment for
these processes include electrostatic precipitators, low sulfur
fuels, higher stacks for greater dispersion, temperature con-
trol, hoods, shroud exhaust systems, cyclones, dust collectors,
flares, good maintenance, wet scrubbers, baffles, gas washing
towers, bag filters, rapping mechanisms, exhaust fans, and
process modifications.
40497
POLLUTION CONTROL AGREEMENT. NO. 5, KANAGAWA
PREFECUTRE, YOKOHAMA CITY, KAWASAKI CITY, AND
NIHON KOKAN KEIHIN REFINERY POLLUTION CON-
TROL AGREEMENT. (Kogai boshi kyotei (5) Kanagawa-ke
Yokohama-shi, Kawasaki-shi to Nihon Kokan (kabu) Keihin
seitetsujo no kogai boshi kyoteisho). Text in Japanese. Kogyo
Ricchi (Ind. Location), 10(8):51-53, Aug. 1971. (Includes POL-
LUTION CONTROL AGREEMENT BETWEEN ONE-
PREF-TWO CITIES AND THE STEELWORKS: WILL THE
WHITE CLOUDS RETURN TO THE SKY OF THE AREA?
(Ikken nishi tai kokan kogai boshi kyotei - fukugen naruka,
chiiki no sora no shiroi kumo). Text in Japanese. Toshi Kaihat-
su (Urban Development), 1971:82-84, Nov. 1971 ) With the
proposed move of Nihon Kokan (Japan Steel Pipe Industries)
Kawasaki Refinery to the landfilled Ogi Island in Tokyo Bay,
Kawasaki and Yokohama cities are expected to be victimized
by the refinery s pollution more than ever. Agreements were
signed between Kanagawa Prefecture, Yokohama and
Kawasaki cities, and Japan Steel Pipe concerning protection of
environment and citizens health According to the agreement,
the major part of the refinery operation will be concentrated
to two large blast furnaces (capacity of producing 6 million
tons/yr of crude steel) which will be completed by 1978. For
specific pollution control, the refinery will use fuels containing
less than 0.5% sulfur at the present location, less than 0.65%
sulfur fuel for an electric power generator boiler, and with
blending of gas fuel, an average of 0.7% sulfur content fuel for
the total area should be achieved. Coke furnace gas fuel
should be desulfurized to less than 0.02% content; ground con-
centration of sulfur oxide in a 2 m velocity south wind should
be less than 0.015 ppm; the maximum total emission of 770 N
cu m/hr should be maintained but efforts should be made to
reduce it to 650 N cu m/hr of less than 0.012 ppm sulfur oxide
concentration. For sintering material, sulfur content should be
less than 0.15% and more than 50% actual desulfurization
should be achieved for stack gas. With regard to dust emis-
sions, maximum standards ranging from 0.005 to 0.1 g/N cu m
are designated for various emission sources, and methods of
dust control are suggested.
41042
Balanov, V. G., R. I. Davidzon, and V. F. Kossovskiy
VENTILATION OPERATION IN DRY EXTINGUISHING
COKE PLANTS. (Rabota ventilyatsionnykh ustanovok
USTK). Text in Russian. Koks i Khim., no. 3:50-51, 1972.
Improvements in air pollution control techniques at a USSR
coke plant are described. Both carbon monoxide and dust con-
centrations were high when exhaust fans with cyclones were
applied, and the air ducts and cyclones were damaged by dust
and sulfur compounds, respectively. Therefore the exhaust fan
was replaced by a blower, and a scrubber with lined plate,
using diabase solution, was found to be the most reliable
cleaning equipment. The scrubber, with an efficiency of 90%,
had a life expectancy of 5-6 years. The air duct following the
scrubber required systematic cleaning weekly, but rubberizing
the ducts extended their life. Sectional exhaust fans with dry
cyclones should be designed for new coke feed conveyors
41447
levlev, V. V , V. I. Litvinenko, and S N. Lazonn
SULPHUR LOSSES IN SULPHUR REMOVAL PLANTS.
Coke Chem (USSR) (English translation from Russian of:
Koks i Khim.), no 10:49-51, 1971. 5 refs.
-------
28
COKE OVENS
Both the arsenic-soda process and the vacuum-carbonate
process to extract hydrogen sulfide from coke-oven gas need
further development to reduce the level of air and water pollu-
tion produced and increase the output of sulfur and sulfuric
acid. The liquid effluent produced by an arsenic soda plant is
rich in sulfur- containing sodium salts and is reused in the
quenching of coke. The coke thus produced is enriched in sul-
fur 0.1% and enriched in ash 0.4%. In the arsenic-soda
process, 9000 t of sulfur and 31,000 t of sodium thiosulfate,
sulfate, and thiocyanate are lost annually. Equipment to
reclaim these saleable compounds from salts in the effluent
would also increase the value of the coke by reducing the sul-
fur and fly ash content. In the vacuum-carbonate process, SO2
and SO3 loss is mainly due to inefficient oxidation in the wet
catalytic plant. Improved catalytic oxidation, more intense
spray irrigation in the condensation towers, and improved
electrostatic precipitators are needed.
42024
McManus, George J.
HEAT OF POLLUTION DRIVE HITS THE COKE OVEN.
Iron Age, 209(26):77- 80, June 29, 1972.
Despite emissions control deadlines and commitments, steel
men say it will be physically impossible to achieve an over-
night cleanup of coke ovens. The two domestic builders of
complete ovens could not handle all the projects resulting
from a crash program. Until recently, new construction had
been held up by the uncertainty of the regulations concerning
acceptable emissions levels. A number of recently installed
systems for charging, pushing, and quenching in the coke oven
process are described. Systems have been installed which can
eliminate 93% of the hydrogen sulfide emission and yield ele-
mental sulfur or sulfuric acid. Substitutes for coke, including
briquettes from powdered coal and gas injection are under
consideration in Japan.
43752
Harima, Mikio
AMMONIA ABSORPTION, PHOSAM PROCESS. (NH3
kyushu, PHOSAM purosesu). Text in Japanese. Aromatikkusu
(Aromatics), 24(1):26-31, 1972.
A new process for ammonia gas removal is described. Am-
monium phosphate solution is used as the absorbing agent in
the so-called Phosam process. The absorbent is sprayed from
the top of the absorbing tower in a counterflow direction to
the incoming coke oven gas (COG) which has just emerged
from a primary cooler, exhauster, and a gas purifying tower in
which solid content, moisture, and tar of the COG are
removed. More than 98% of the NH3 is removed in the ab-
sorbing tower. The resulting solution is then led to a separator
to which hot steam is supplied and ammonia water is
separated from the phosphate solution which is recycled to the
absorbing tower. Anhydrous ammonia gas is generated at high
pressure by introducing steam into the ammonia fractionation
tower. The pressure loss of the absorbing tower is designed at
100 to 150 mm Aq, and the process can be designed for any
desired gas feed, NH3 recovery, and product purity.
43840
Hemming, Charles
WHAT INDUSTRY IS DOING ABOUT POLLUTION CON-
TROL. Civil Eng. (N. Y.), 41 (9):59-62, Sept 1971.
Developments in air and water pollution control by five major
industries are reviewed. Hercules, Inc. is constructing an ad-
vanced solid-waste reclamation plant in Delaware that will
convert 500 tons of refuse and 70 tons of sewage sludge/day
into marketable products. Dow Chemical Company has a
number of projects underway at its Midland, Michigan, Divi-
sion, including brine purification, the installation of detection
devices on sewers, and environmental monitoring in the form
of a specially designed van which tours potential trouble areas
around the plant. Alcoa has perfected a system for recycling
fluoride effluents in smelting operations. The fumes given off
in a aluminum smelting, heavy with particulate and gaseous
fluorides, are ducted through a bed of alumina which chemis-
orbs the gaseous fluoride. Particulate fluoride is captured in
filter bags. Recovered fluorides are recycled to potline cells
where they contribute to the continuous smelting process. The
Alcoa 398 Process is more than 99% efficient in recovering
potential pollutants. General Motors is active in planning aban-
doned-car cleanup campaigns. Allied Chemical Corporation
has developed a pipeline-charging system that controls air pol-
lution resulting from coke ovens by reducing smoke and gases
from by-products by as much as 70%.
44156
Amstislavskii, D. M., N. O. Panteleenko, and I. E. Matveeva
CORROSION PROTECTION OF SULFUR REMOVAL
REGENERATORS. (Zashchita ot korrozii regeneratorov tsek-
ha seroochistki). Text in Russian. Koks i Khim., no. 3:53,
1972.
The interior surface of the regenerator used for removal of
hydrogen sulfide from coke oven gases was cleaned by sand
blasting, then protected by a 4-coat system of primer, filler,
and two top coats, all based on an epoxide resin. A finish,
containing 70% epoxide resin and 30% coal tar, hardened with
8% polyethylene poly amine (calculated on the weight of resin),
and containing aluminum oxide as filler, was also used.
44989
Nicolau, Matei
AIR POLLUTION CONTROL ON THE WORKING PLAT-
FORMS OF COAL CARBONIZATION PLANTS. Dept. of
Commerce, Washington, D. C., Bureau of International Com-
merce, Environ Control Sem. Proc., Rotterdam, Warsaw,
Bucharest, 1971. p 292-297. 5 refs. (May 25-June 4.) NTIS: PB
COM-72-50078; GPO
Three types of technological processes cause air pollution on
the coal carbonization installations of siderurgical combines.
They are lateral charging of coal blocks into the pyrogenation
chambers of the coking batteries; quenching the incandescent
coke, and tar removal from the raw coke gas collectors.
Charging coal into the coking oven may be performed without
the generation of raw coke gas (smokeless charging of coal
pyrogenation ovens). The technological process of dry cooling
incandescent coke eliminates air pollution and, compared to
the conventional coke quenching method, presents two impor-
tant economic advantages, i.e.: the possibility of recovering
the physical heat of the incandescent coke subjected to cool-
ing; and qualitative improvement of the cooled coke. Dry cool-
ing of the coke results in a more uniform coke grain size and
in a higher mechanical strength of the coke. According to solu-
tions proposed in Romanian patents, the hot inert gas is first
cleaned before it enters the heat transfer system. The problem
of removing tars from the raw coke gas collectors has not yet
found an optimum solution on a worldwide scale. An optimum
installation leading to the solution of the problem must achieve
efficient cleaning of the tar masses and tars and their optimum
removal from the raw coke gas collector, while maintaining
perfect tightness of the entire system. It should use an auxilia-
ry fluid medium, circulating through the collector, which
-------
B. CONTROL METHODS
29
should be easily recoverable. The installation must present
complete operating safety. It should not compromise the cok-
ing process. It should enable the automation of the entire tar
mass cleaning and removal process from the collector. It
should require minimum investments and operating costs.
45308
Pakter, M. K., E. Ya. Eidelman, and A. T. Pozhidaev
GERMANIUM AND SULPHUR DISTRIBUTIONS IN COKE.
Coke Chem. (USSR) (English translation from Russian of:
Koks i Khim.), no. 4:31-35, 1971. 11 refs.
The distributions of germanium and sulfur in coke were in-
vestigated in the hope of finding ways of transferring more
germanium and sulfur to the recovery products. The germani-
um content of coke increases from the bottom to the top of
the cake, while both the germanium and sulfur contents in-
crease outward from the axis of the side walls. There is little
significant variation in either element along the coke oven or
in the vertical sulfur distribution. The observed germanium
and sulfur distributions are brought about mainly by local car-
bonization temperature conditions, thus indicating the feasibili-
ty of recovering more germanium and removing more sulfur
from the coke by moderating the longitudinal and vertical tem-
perature gradients in the cake. There is little hope that signifi-
cant changes can be brought about by reducing the width of
coke ovens. (Author conclusions modified)
45324
Kazmina, V. V.
REDUCING THE SULPHUR CONTENT OF COKE BY HIGH-
TEMPERATURE HEATING. Coke Chem. (USSR) (English
translation from Russian of: Koks i Khim.), no. 6:25-28, 1971.
3 refs.
The heat treatment of any size fraction of coke at tempera-
tures between 1300-1600 C leads to a reduction in its sulfur
content. The optimum holding time for calcination at tempera-
tures of 1300 C and higher is 30 min. The smaller size frac-
tions of coke lose higher proportions of their sulfur since the
pieces are smaller and have a larger specific surface area. Sul-
fidic sulfur is most completely removed at the lower calcina-
tion temperatures, while higher proportions of organic sulfur
are removed as the temperature is raised. The sulfur content
of large blast furnace coke fractions can also be reduced by
calcination at 1300-1600 C. When coke is calcined its reactivity
is significantly lowered. The hardness of the coke increases as
the calcination temperature is raised (Author conclusions
modified)
45426
Belonozhko, A M.
COKE AND CHEMICAL PRODUCTION WASTES AND
WAYS OF USING THEM. Coke Chem. (USSR) (English
translation from Russian of: Koks i Khim.), no. 9:48-50, Sept
1971. 8 refs.
Wastes from coke and chemical plants are a serious loss which
can damage the national economy and cause problems of air,
water, and soil pollution. Solid wastes include clinker, dirt,
flotation tailings, lime sludge, and coal waste The existing
dumps are approaching saturation More use must be made of
clinker for road building; coal wastes can be gasified, coal
sludge can be incorporated into carbonization charges; and al-
ternatives can be used instead of lime. Recommendations are
presented for producing useful chemicals from still bottoms
and solar oil. Further work is required on uses for sulfuric
acid and alkaline wastes which are regularly dumped by
chemical works. Waste chemicals from arsenic-soda sulfur
removal plants, vacuum-carbonate sulfur removal plants, and
wastes in the form of ammonium sulfate solution and tar
liquor are presently being utilized in the production of industri-
al chemicals.
45658
Mityushkm, V. G. and V. I. Var yev
MODIFICATION OF THE COKE GAS PURIFICATION
ELECTRICAL FILTER DESIGN. (Rekonstruktsiya elektrofil
tra dlya ochistki koksovogo gaza). Text in Russian. Koks i
Khim., no. 4:38-39, 1972.
A modified electrical filter design for use in cokeries for the
separation of tar from coke gas is described. The hermetically
sealed cylindric electric filter provides possibilities to minimize
electricity and heat consumption, to simplify maintenance
procedures, and to stabilize the temperature of the insulators.
The hermetically sealed design was made possible by applying
two coupled insulators, the upper one of which is sealed by
mastic, as well as by mounting the suspension insulators for
the discharge electrodes frame inside the electrostatic filters.
To avoid tar condensation on insulators, the latter are placed
in the center of the gas flow.
45688
Sieu, Ho and Piotr Wasileswski
USE OF FOAM COLUMNS FOR ABSORPTION OF AM-
MONIA FROM COKE OVEN GAS IN AQUEOUS AMMONI-
UM DIHYDROGEN PHOSPHATE SOLUTIONS. (Proba
zastosowama kolumny pianowej do absorpcji amoniaku z ga/,u
koksowniczego w wodnym roztworze fosforanu ]ed-
noamonowego). Text in Polish. Koks, Smola, Gaz, 17(3):76-81,
1972. 15 refs
Because of a much higher contact surface between the gas and
the liquid, foam columns give much better results in ammonia
absorption than the usual sieve-plate columns or columns with
pneumatic mixing. The performance of an experimental
column for ammonia absorption with an aqueous solution of
ammonium dihydrogen phosphate solution is described. The
column (1080 mm high) had three plates and was operated with
foaming of the solution with an ammonia-air mixture. The ef-
fect of foam-layer thickness on the absorption coefficient and
the absorption degree were determined. Very high values of
the absorption coefficient and the absorption degree were ob-
tained. At a gas-mixture velocity of 0.8 m/sec, the absorption
coefficient was 104 kg/(cu m)(hr)(g/cu m), and the absorption
degree was 93 4%. Increase in gas quantity leads to increase of
flow rate, absorption coefficient, and absorption degree, and
to a decrease of salt concentration in solution after completion
of the absorption process
46441
Helling, S. and H. Eckhardt
DEVELOPMENT OF A METHOD FOR STABILIZING THE
TAR FROM SOFT COAL HIGH TEMPERATURE COKING.
(Entwicklung eines Verfahrens zur Stabilisierung des bei der
Braunkohlenhochtemperaturverkokung anfallenden Teeres).
Text in German. Freiberger Forschungsh. A, 507:47-59, 1972. 5
refs
The tar obtained from high-temperature coking poses con-
siderable difficulties if used as fuel oil. Through its instability,
solid matter separates during storage and incrustations are
formed at the combustion. Its low sulfur content of 0.4%
would make it an ideal fuel, however. It was possible to im-
prove the thermo-chemical stability of the tar considerably
-------
30
COKE OVENS
The most economical and most favorable method turned out to
be the gassing the tar with ammonia. Further study of this
method showed that iron as material for the gassing column
has a negative effect on the stabilization. Glass, chromium-
nickel steel or enameled iron are better materials. With the
ammonia-gassing method, a low-sulfur fuel oil can be obtained
which has the stability of conventional fuel oils.
46642
Weber, Heinrich and Kurt Tippmer
COKING PLANT GASES TREATMENT BY SCRUBBING
WITH AMMONIA VAPORS TO REMOVE HYDROGEN SUL-
FIDE. (Verfahren zum Entfernen von Schwefelwasserstoff
aus Kokereigasen). Text in German. (Assignee not given.) Ger.
Pat. 1,494,815. 5p., April 20, 1972. (Appl. Oct. 1, 1970, 2
claims).
Ammonia scrubbing vapors are introduced to a hydrogen sul-
fide stripper column at several points to remove hydrogen sul-
fide from coking plant gases. The NH3 vapors are introduced
preferably at 40-45 C, above the packing of the H2S stripper
column top.
46945
Volkov, E. L., V. Ya. Deev, and T. M. Roslyakov
A PILOT COMMERCIAL SPRAY-TYPE ACTIFIER FOR H2S
REMOVAL. Coke Chem. (USSR) (English translation from
Russian of: Koks i Khim.), no. 4:45-46, 1971.
The extent to which hydrogen sulfide is removed from coke
oven gas depends in large measure on the performance of the
regeneration plant. The foul liquor from vacuum carbonate
H2S absorbers is actified in towers fitted with tunnel and
capped plates. Degree of actification is basically dependent on
the temperature of the liquor to be treated, which in turn is
determined by the residual pressure in the equipment and its
detailed design. A pilot commercial spray-type actifier tower is
described, including operating experience. The actifier consists
of a thermally insulated tower fitted with internal nozzles
through which the liquor is sprayed. Two slotted baffles divide
it into three sections.
46946
Volkov, E. L., V. Ya. Deev, and T. M. Roslyakov
UTILIZATION OF HEAT FROM THE TAR LIQUOR IN THE
COLLECTING MAIN. Coke Chem. (USSR) (English transla-
tion from Russian of: Koks i Khim.), no. 4:47-48, 1971.
Large amounts of energy are consumed in the removal of
hydrogen sulfide from coke oven gas with alkaline solutions.
However, the economics of sulfur removal can be improved
by utilizing waste heat from other parts of the plant. The
liquor temperature required in the actifier is no higher than 65-
70 C. A process is described whereby sensible heat from the
tar liquor in the collecting main is used to heat the foul liquor
from the absorbers. Design of the waste heat recovery unit is
indicated.
47110
Edgar, Wm. D.
COKE-OVEN AIR EMISSIONS ABATEMENT. Iron Steel
Engr., 49(10):86-94, Oct. 1972. 7 refs.
Sources of coke-oven emissions, types of emissions and con-
trols, pipeline charging of preheated coals to coke ovens, oven
pushing, and coke quenching are considered. Gas scrubbers,
incinerators, exhaust systems, and various collection system
requirements are indicated. In addition to the reduction or
elimination of coke-oven emissions, some plants are improving
the operator s environment, either by providing better working
conditions or by eliminating certain operating jobs. Perhaps
the worst environment is encountered by the lidnian on top of
the battery, and current laws require the use of respirators by
all top-side personnel. While the systems or modifications of
systems as described will be adaptable to most plants, other
operators are looking toward other processes, such as form-
coke or direct reduction, which will eliminate the need for by-
product coke ovens and, in the latter case, blast furnaces.
47794
Weber, Heinrich, Gustav Choulat, Helmut Fritzsche, and
Dieter Laufhuette
AMMONIA DISPOSAL FROM COKE OVEN GASES. (Ver-
fahren zur Verbrennung Oder Zersetzung des bei der Aufbe-
reitung von Kokerei- oder Gaswerksgas anfallenden Am-
moniaks). Text in German. (Firma Carl Still, Recklinghausen
(West Germany}) W. Ger. Pat. Appl. 2,054,336. 7p., Nov. 5,
1970. 7 refs. (6 claims).
A technique for the removal of ammonia from coke oven
gases by absorption in sulfuric acid, ammonium bisulfate, or
ammonium phosphate, mono basic, is presented. The resulting
solutions are thermally decomposed to produce NH4HSO4 or
NH4H2PO4, respectively, which are recycled to the absorp-
tion process and NH3. The NH3 is burned with air or ther-
mally decomposed by passing its mixture with combustible
gases and air through a decomposition zone. The gases leaving
this zone are burned completely with air or are used for lean-
ing of calorie-rich gases. The combustion heat is used for the
thermal decomposition of the substances from the NH3 ab-
sorption. The combustion gases are free of products from
hydrogen sulfide or hydrogen cyanide combustion.
-------
31
C. MEASUREMENT METHODS
03233
W. Thurauf and W. Ehnert
((THE FORMATION OF NITRIC OXIDE DURING COK-
ING.)) Uber die Bildung von Stickstoffmonoxid bei der Ver-
kokung und seine Bestimmung in Koksofengas. Brennstoff-
Chem. (Essen) 9(48):270-273, Sept. Translated from German as
JPRS R-8582-D.
Experiments were undertaken in order to settle the question of
where and when nitric oxide is formed during the coking
process, and the manner in which the nitric oxide content of
coke oven gas changes during the process of coking. The ex-
periments were conducted on a small scale, employing spe-
cially designed apparatus with the thermal energy being pro-
vided by an electric heater, in order to eliminate the possibility
that coking fuels are responsible for the formation of nitric ox-
ide. It was found that nitric oxide begins to form during the
first state at which gas is driven off; and that the extent to
which it continues as the temperature is raised depends on the
type of coal, its granular structure, and the temperature rise.
Formation appears to be complete by the time that the coking
coal reaches a temperature of 400 C. In the case of ground
coals, the finer the grains the lower the formation of nitric ox-
ide, and vice versa; the reverse being true for coal dust ob-
tained by sifting coal that had been stored in the open air. The
NO contents of subsequently heated alcohol extracts from
coals are approximately the same as those of the same coals
directly heated in a helium atmosphere, and are from four to
twelve times as great as the volumes contained in the distilla-
tion gases obtained during the coking process. This indicated
that approximately 90% of the NO which is formed during
coking is subsequently decomposed by reactions with the
other distillation products. NO is not formed, as formerly be-
'ieved, through oxidation during coking, but rather from the
decomposition of substances which are formed when coal is
stored in the open air.
06653
Razbegaeva, A. P.
MECHANIZATION OF THE GAS ANALYZER ORSAT.
U.S.S.R. Literature on Air Pollution and Related Occupational
Diseases, Vol. 7, 44-7, 1962. (Koks i Khim.) (4) 53-4, 1958.
Translated from Russian. CFSTI: 62-11103
A method for mechanical transfer of the combustion gases
from the burettes into the absorption tubes is described. The
apparatus consists of a water pressure flask and a rubber bulb
or balloon which form an assembly unit. Each rubber bulb is
operated by a spring type pusher activated by one of several
eccentric cams on a common shaft. The cams are set so that at
a given time interval only one pusher is brought into action.
Results of tests made with gas analyzer ORSAT manually and
by the automatic procedure show that differences between
testing procedures were within error limits normal for an ap-
paratus of this type. Adoption of the mechanical procedure of
combustion gas analysis facilitated the work of the laboratory
technicians, increased their productivity, and freed one techni-
cian for other laboratory work. The apparatus is now in con-
tinuous smooth operation.
06908
R. V. Gorskaya
DETERMINATION OF PYRIDINE IN AIR. (K voprosu ob
opredelenii piridina v vozdukhe.) Hyg. Sanit. (Gigiena i Sanit.)
30 (12), 393-6 (Dec. 1965). Russ. (Tr.)
The determination of pyridine in factory air was accomplished
by the reaction of pyridine with cyanogen chloride and bor-
bituric acid. The method was tested under industrial conditions
to determine pyridine concentrations in the air of the pyridine
shop of a coking-chemical plant. Parallel determinations were
made by the gas laboratory of the plant using cyanogen bro-
mide and aniline. A comparison of the results show that the
determination of pyridine with cyanogen chloride and barbitu-
ric acid makes quantitative results possible, while the method
used by the laboratory does not. This method also eliminates
work with highly toxic reagents, is convenient for routine anal-
ysis under industrial conditions, and possesses high sensitivity
and accuracy.
08335
Richards, Ronald T., Therese Donova, and Jack R. Hall
A PRELIMINARY REPORT ON THE USE OF SILVER
METAL MEMBRANE FILTERS IN SAMPLING FOR COAL
TAR PITCH VOLATILES. Am. Ind. Hyg. Assoc. J., p. 590-
594, Nov.-Dec. 1967. 2 refs.
A method is developed for collecting and analyzing samples
for coal tar pitch volatiles by using a silver metal membrane
filter and benzene extraction. The collection of a 1-cubic-meter
air sample and the use of a five-place analytical balance accu-
rate to 0.01 mg provides adequate sensitivity to detect 0.10 mg
of coal tar pitch volatiles per cubic meter of air. Background
information concnerning reasons for the initiation of this stu-
dy, the tentative threshold limit of 0.2 mg per cubic meter of
air (ACGIH), and previous attempts at sampling with glass
fiber filters are also discussed. Problems encountered in ob-
taining consistent results with glass fiber filters and the
benzene extraction analysis technique led to a search for a
better technique. Comparison of glass fiber filters, cellulose
acetate membranes, cellulose filters, and cellulose thimbles
with the silver membranes were made. This comparison in-
cluded weight stability with humidity changes and benzene ex-
traction and airflow determinations. The results of actual sam-
pling are listed, and other possible uses of the metal mem-
brane in industrial hygiene are discussed. (Authors' abstract,
modified)
10671
Herrick, Robert A. and Louis G. Benedict
A MICROSCOPIC CLASSIFICATION OF SETTLED PAR-
TICULATES FOUND IN THE VICINITY OF A COKE-MAK-
ING OPERATION. Preprint, Bethlehem Steel Corp., Pa., Coal
and Coke Section, 23p., 1968. 8 refs. (Presented at the 61st
Annual Meeting of the Air Pollution Control Association, St.
Paul, Minn., June 1968, Paper 68-137.)
The specific identification of the components of settleable par-
ticulate samples collected near a coke-making operation was
-------
32
COKE OVENS
accomplished. The identification technique employed is a new
application of reflected-light microscopic examination of
polished sections of the material. The inherent optical charac-
teristics of the individual particles are utilized to classify them
as coal (high-, medium- or low-voltatile), coke (coke balls,
pyrolytic carbon, slot-oven coke and char), fly ash or mineral
matter. The application of this method of analysis is unique in
that classification of particles is based on these inherent opti-
cal properties and not on shape, color or other subjective
criteria. This microscopic classification technique is based on
accepted methods and should be generally applicable by
petrographers on the basis of the photomicrographs and the
detailed procedures which are included. On the basis of the
data obtained during a six-month study near a coke-making
operation it is concluded that material handling and stockpiling
operations are major contributors to settled paniculate deposi-
tion, while coke oven charging was not a major source. This
study has shown that a broad program of engineering control
will be required to significantly reduce settled particulate
deposition in the immediate vicinity of a coke-making opera-
tion. (Authors' abstract, modified)
24621
Khalaimova, A. M., M. F. Kovalenko, and Ye. A. Zherdeva
DETERMINING THE COMPOSITION OF RAW BENZENE
BY GAS-LIQUID CHROMATOGRAPHY. (Opredeleniye
sostava syrogo benzola metodom gazozhidkostnoy khro-
matografii). Text in Russian. Koks i Khim., no. 6:35-37, 1970. 5
refs.
Results of gas-liquid chromatography of raw benzene derived
from coke-oven gas are presented. The benzene content was 3-
6% higher and xylene content 1-2% higher than indicated by
fractional distillation. Blast-furnace coke contained 8-10%
more total raw benzene than foundry coke, but less of the fol-
lowing constituents (% abs.): toluene, 3-4; xylene, 2; carbon
disulfide, 0.4; and pseudocumene, 0.5.
25030
Masek, Vaclav
THE USE OF SILVER MEMBRANE FILTERS IN SAMPLING
FOR COAL TAR PITCH VOLATILES IN COKE OVEN
PLANTS. Am. Ind. Hyg. Assoc. }., 31(5): 641-644, Sept.-Oct.
1970. 3 refs.
The application of silver metal membrane filters is recom-
mended to establish the concentration of benzene soluble frac-
tions in the workplace atmospheres of both black-coal and
coal-tar pitch coke oven plants. Long-term induction of air
through Soxhlet Schleicher-Schull filters yielded enough of the
pollutants for analysis when placed 1.5 meters above floor
level at seven sampling points. Determinations were made of
the ash content and total iron and silicon oxide concentrations
in the ash, while the size distribution curve was established,
first on a sieve set and then by optical microscopy. The con-
tent of benzo(a)pyrene was ascertained by chromatography,
and the content of benzene-soluble fractions was determined
in a Soxhlet apparatus. Using the colloidal membrane
technique, the finest of the separated impurity particles were
photographed under a Tesla BS 249 electron microscope.
When twelve silver metal membrane filters of 37 mm and 47
mm diameters with a porosity of 0.0008 mm were made availa-
ble, Soxhlet extraction was ended after five cycles of spectro-
graphic grade benzene. About 250 ml of extract was first
evaporated down to some 20 to 30 ml and then filtered through
a silver metal membrane filter of 47 mm diameter into a tarred
container. The filter was then rinsed with 10 to 20 ml of
benzene, and the container was evaporated dry at room tem-
perature. However, the pollution values thus established are
not always a reliable measure of the actual carcinogen danger
encountered in black coal coke oven plants.
29157
Schulze, Volker
GAS CHROMATOGRAPHIC OPERATING AND PRODUCT
CONTROL IN A COKING PLANT. (Gaschromatographische
Betnebs- und Produktenkontrolle in einer Kokerei). Text in
German. Gas Wasserfach (Munich), 112(4):179-182, 1971.
Gas chromatography is used in coking plants for analysis of
hydrocarbon gases. This method has the advantage that a clear
distinction can be made between benzene and benzene
hydrocarbons. Initially, gas chromatography was used to study
connections between the composition of new types of gases
and soot depositions. Small concentrations of carbon monox-
ide in the presence of considerable nitrogen are not accurately
separated by gas chromatography unless duration of analysis is
more than 20 mm. For operating control, gas chromatography
is indispensable. Direct naphthalene determination by gas
chromatography without enrichment has not yet been carried
out satisfactorily.
37217
Institution of Gas Engineers, London (England)
RECOMMENDED ANALYTICAL METHODS FOR GAS
WORKS AND COKE OVEN EFFLUENTS. Inst. Gas Eng.,
Commun., 831(2):1-30, Dec. 1970. 7 refs.
Methods are given for the determination of nitrate, sulfide,
thiosulfate, total chromium and chromate, iron, nickel, and
potassium in effluents from gas works and coke ovens and for
preliminary treatment before analysis for metals in the ef-
fluents. The methods are colorimetric (nitrate, sulfide, total
chromium and chromate, iron, nickel); precipitation (sulfide);
polarographic (thiosulfate); iodimetric (thiosulfate); flame
photometry of spectrophotometry (potassium); and the nitric
acid/sulfuric acid and nitnc acid/perchloric acid methods for
preliminary treatment.
38361
Plankert, Manfred
THE DETERMINATION OF ORGANICALLY BOUND SUL-
FUR IN COKE OVEN GAS. (Zur Bestimmung des organisch
gebundenen Schwefels im Koksofengas). Text in German. Gas
Wasserfach Gas Erdgas (Munich), 113(2):65-69, Feb. 1972. 12
refs. (Presented at the Erfahrungsaustausche der Gas-
Chemiker, Konstanz, West Germany, 1971.)
Since the concentration of organic sulfur in gas has been
limited an analytical method had to be found which permits a
fast and accurate determination in the cleaned and uncleaned
gas. A combination of the reduction method with the Draeger
indicator tube for hydrogen sulfide was tested. The gas sample
is passed through a cadmium acetate solution where the H2S
is retained. A certain measured volume is then passed over a
platinum catalyst at 1000 C. The organic sulfur is entirely con-
verted to H2S at this temperature, provided the hydrogen con-
centration and the residence time at the catalyst are suffi-
ciently large. The apparatus consists of the gas entrance sec-
tion, the measuring buret, the reactor and the indicator. The
gas entrance section has a scrubber. The reactor is composed
of a quartz tube with a length of 150 mm and a diameter of 10
mm A sample volume of about 300 ml suffices for the deter-
mination, the whole measuring process lasts less than 5 min.
Reproducible values were obtained which agreed well with the
results of parallel measurements by the method of
Roelen/Feisst.
-------
C. MEASUREMENT METHODS
33
41644
Khalyapin, S. A. and A. E. Mironov
RADIOMETRIC DETERMINATION OF SULPHUR IN
GASES. Coke Chem. (USSR) (English translation from Rus-
sian of: Koks i Khun.), no. 10:52-54, 1971. 4 refs.
A radiometnc method for the determination and in-process
control of sulfur in streams of gases generated by coke and
chemical plants is described. The radiometry principle is based
on the relationship between soft gamma-ray absorption and the
atomic number of the absorbing element. The on-stream gas
analyzer for sulfur determinations is based on the use of a
compensating source and beam amplitude modulation. Radia-
tion from two sources passes through the working and com-
parison channels in the analyzer The working channel in-
cludes an on-stream gas cell, while the comparison channel in-
cludes a compensating slide. The rotating shutter alternately
exposes the single detector, which consists of a scintillation
counter and a photoelectric multiplier, to the two beams.
When the beam intensities in the working and comparison
channels are different, the alternation produced by the shutter
leads to an alternating current signal at the output of the
system controlling a reversible motor. The amplitude of the
signal driving the meter is proportional to the sulfur content of
the gas to be analyzed. A prototype analyzer was tested at a
coke and chemical works and the instrument readings were
evaluated by comparing them with the results of simultaneous
chemical analyses on the sample gas. A t-test was applied to
confirm that there was no systematic difference between the
two sets of results. The trial results obtained with the proto-
type analyzer were fully in accordance with the theoretical
principles on which the procedure was based
-------
34
D. AIR QUALITY MEASUREMENTS
08485
Masek, Vaclav
THE EFFECT OF SOLAR RADIATION ON THE PRESENCE
OF 3,4-BENZOPYRENE IN INDUSTRIAL EXHAUSTS. ((Vliv
slunecniho zareni na pritomnost ?,4-benzpyrenu v exhalacich.))
Text in Czech. Chem. Prumysl (Prague), 17(2):99-103, 1967. 30
refs.
The determination of polycyclic hydrocarbons in industrial ex-
hausts and in the atmosphere has become increasingly impor-
tant in recent years. The main interest is focoused on car-
cinogenic substances, particularly on 3,4-benzopyrene. In the
present study, 3-4-benzopyrene was determined from samples
obtained by passing air through filter paper in the vicinity of a
coking plant in which coal tar products formed during car-
bonization leak into the atmosphere. At the same time the in-
tensity of solar radiation was recorded with a Robitzsch
pyranograph. The results showed that the intensity and dura-
tion of solar radiation had no effect on the content of 3,4-
benzopyrene in the atmosphere and in the dust in the vicinity
of the source. The discharge of tar products into the at-
mosphere must be controlled by changing the technology, e.g
by improving equipment seals and using steam injection to
reduce the vapor pressure inside the equipment. Tables and
graphs.
11015
Tanimura, Hisashige
BENZO(A)PYRENE IN AN IRON AND STEEL WORKS.
Arch. Environ. Health, 17(2):172-177, Aug. 1968.
To investigate benzo(a)pyrene in an iron and steel works,
separating and measurement methods were studied, and
amounts of benzo(a)pyrene contained in suspended and falling
particulates were collected in the plant and measured for
summer and winter sessions. The samples were separated
chromatographically and the amounts were determined spec-
trophotometrically. A great amount of benzo(a)pyrene was
found near the three high mills in the rolling mill plant, the
coke oven, the blast furnace, and the electric furnace. High
correlations were found between benzo(a)pyrene in suspended
and falling particulates. (Author's abstract)
21239
Dikun, P. P. and I. I. Nikberg
INVESTIGATION OF ATMOSPHERIC POLLUTION WITH
3:4-BENZPYRENE IN THE VICINITY OF PITCH-COKE
OVENS OF OBSOLETE PATTERN. Probl. Oncol. (USSR)
(English Translation from Russian of: Vopr. Onkol.), 4(6): 32-
38, June 1958. 6 refs.
The results of an analysis of three sets of samples taken from
the vicinity of an obsolete pitch-coke oven, at various times,
at various distances from the works, and at points lying at
various directions away from it are given. The first series were
of deposits of dusts; the second series were of sedimentation
samples; and the third series were of aspiration samples. The
analysis of all three samples showed that exceptionally large
amounts of carcinogenic hydrocarbons, in particular 3,4-benz-
pyrene, escaped into the surrounding area. Subsequently, on
special government instructions aimed at ensuring a healthy at-
mosphere, the coke ovens were equipped with special devices
to provide additional combustion of exhaust gases. Analysis
showed that after reconstruction of the coke ovens, at-
mospheric pollution in the vicinity of the pitch-coke works
sharply diminished.
26040
Kettner, H. and V. Masek
DUST AND SOOT NUISANCES AT A METALLURGICAL
COKING PLANT AND IN ITS ENVIRONMENT. (Ueber
Staub- und Russbelaestigungen auf einer Huettenkokerei und
in derer Umgebung). Text in German. Gesundh. Ingr.,
91(ll):323-326, Nov. 1970. 7 refs.
The maximum permissible dust emission in West Germany for
inhabited areas is 0.42 g/sq m/day as an average of 12 monthly
averages. For industrial areas, the tolerated level is higher,
0.85 g/sq m/day as an average of 12 monthly averages. In
Czechoslovakia, the respective levels are 150 t/sq km/year for
inhabited areas, and 10 mg dust/cu m for industrial areas.
Gravimetric dust emission measurements performed at 19 sites
of a coking plant and in its vicinity near Ostrava in
Czechoslovakia yielded levels which by far exceeded the
stipulated norms; in one case, a daily emission level of 11.3
g/sq m/day was recorded. The maximum 3,4-benzpyrene con-
tent found was 38.5 micrograms/g dust. The dust consisted of
coke and coal particles and of soot flakes. This emission
resulted even though the coking plant met all waste gas pu-
rificatio requirements prescribed by law. Thus, additional mea-
sures will have to be instituted to reduce dust emission, espe-
cially during the charging operations of coke ovens.
27406
Beeckmans, I. and R. Dewaef
STUDY OF ATMOSPHERIC POLLUTION RESULTING
FROM METALLURGICAL ACTIVITY, 1961-1967. (L'etude
de la pollution atmospherique due 1'activite siderurgique, de
1961 a 1967). Text in French. Tribune Cebedeau, 22(303):68-75,
Feb. 1969. 1 ref.
An analysis was made of a number of studies of pollution in
the industrial areas of Belgium, including studies of emissions
from ore concentration, coke, and steel plants in terms of par-
ticulate and gaseous pollutants, qualitative and quantitative
analyses of gaseous and particulate pollutants, and morpholog-
ical and granulometnc analyses of the solid-state material, the
methods of dispersion of waste materials, and the pollution
content of the soi and atmosphere within a radius of 5 kilome-
ters from the emission sources. The influence of large-parti-
cled solid pollution extends to a radius of more than 2 kilome-
ters from an ore concentration plant and more than 1.5 kilome-
ters from a coke plant. Finer particles are found about 1500 m
from ore concentration plants, while the range for sulfur diox-
ide is 1000 m. Pollution data on large and fine particulate sub-
stances, SO2, and nitrogen dioxide are extensively analyzed
for the Charleroi and Liege areas, both in the Meuse Valley,
-------
D. AIR QUALITY MEASUREMENTS
35
and a comparison is made with figures from the United States,
England, Italy, France, and Hungary.
29257
Hall, D. A. and G. R. Nellist
ATMOSPHERIC POLLUTION AT MODERN COKE WORKS.
Coke Oven Managers Yearbook, 1964, p. 96-114. 8 refs.
(Presented before the Coke Oven Managers Association
Northern Section, Nov 1962.)
Measurements of general atmospheric pollution in the vicinity
of three modern coke works are presented. These show that
the total solids deposition is much less than in industrial re-
gions and similar to that in an urban area such as Newcastle.
The amount of the deposition is only about the same as has
been suggested as resonable by a number of authorities. The
special problem of grit and drizzle deposition from the
quenching tower was studied, and the effect of the installation
of wooden baffles at one coke works measured The results
show that the baffles greatly reduce the emission of drizzle
but make only a small difference in total emission of solid
material, e.g., fine dust. In addition, the eliminators cause
coagulation of water droplets and, to a lesser extent, gnt,
which results in both materials being precipitated nearer to the
quenching tower than previously (Author abstract modified)
35081
Kutuzova, L. N , A F Kononenko, and G. P. Sokulskii
DISCHARGES TO ATMOSPHERE FROM BENZOLE PLANT.
Coke Chem. (USSR) (English translation from Russian of
Koks i Khim), no. 8:39-42, 1970 6 refs
Coke and chemical plants pollute the atmosphere with nu-
merous toxic substances, including hydrocarbons and sulfur
compounds Concentrations of benzene, toluene, xylenes,
hydrogen sulfide, and carbon disulfide were determined on a
chromatograph with a thermal conductivity detector at a
benzol refinery Chemical analyses were carried out simultane-
ously for benzene (which was determined by the combustion
method), hydrogen sulfide (which was determined by an
lodimetnc method), and carbon disulfide (which was deter-
mined by the xanthogenate method) Phenols were determined
in the discharge gas spectrophotometricaily, and hydrogen cya-
nide by the tetrathionate method
38830
Chuang. Tsm-yuan
AIR POLLUTION AND CONTROL MEASURES IN TAIPEI
CITY. (Taipei-shih kung-chi wu-jan chih hsien-chuang yu chi
kuan-chih tui-tse). Text in Chinese. Kung Ch eng (Eng J.),
44(8/9).85-109, Aug /Sept. 1971 22 refs
Air quality was measured in Taipei city to determine the level
of air pollution. The annual average dust fall was calculated at
18.51 ton/sq km/mo with a standard deviation of 6.48 tons;
however, 53% of the pollution load, excepting fuel combustion
products, is water soluble Suspended particulate matter from
steel mills, brick factories, and coking plants was also mea-
sured Approximate concentrations of 0 06 ppm for sulfur
dioxide, 6-8 ppm of carbon monoxide, and 0.026 ppm of
nitrogen dioxide were established Monitored SO2 observa-
tions also indicated radiation inversions at certain times of the
day. The problems of air pollution are aggravated by the in-
creasing population, 80% of which is concentrated in the urban
areas. Meteorologically, the situation is favorable toward
dispersion of pollutants, since periods of calm occur only
2.73% of the time and the average annual wind velocity is 3 23
m/sec. Topographic interactions, however, may have adverse
influences on wind movements and velocity. The wind
direction is generally easterly, thus bringing in pollution from
the Nankang and Neihu industries.
38895
Masek, Vaclav
NEWER FINDINGS CONCERNING THE PROPERTIES OF
FLY DUST FROM COKING PLANTS. II. THE ARSENIC
CONCENTRATION IN THE DUSTS DEVELOPING AT THE
COKING PROCESS. (Neue Erkenntnisse ueber die Eigenschaf-
ten des Flugstaubes aus der Kokerei. Teil II - Arsengehalt in
den Luftstaeuben der Verkokung). Text in German. Zentr. Ar-
beitsmed. Arbeitsschutz, 22(3):69-74, March 1972. 10 refs.
The dust and arsenic concentration in 19 samples taken at the
upper floors of the hard coal and pitch blocks of the coke-
oven furnace were measured. The soluble arsenic concentra-
tion was determined by boiling the sample with 2% sodium
hydroxide solution. The total arsenic concentration was deter-
mined by a modified colonmetric method. The obtained ar-
senic was then determined by photometry with silverdiethyl
dithiocarbamate. The average arsenic concentration of the raw
material was 0 0005% by weight, in the dusts of the air sam-
ples it was 0.014% by weight, which means that the arsenic
concentration in the emission is 28 times higher than in the ini-
tial coal used for the coking process. The dusts in the samples
taken in the upper pitch blocks contain an arsenic concentra-
tion which is 182 times higher than the concentration in the
coal. The quantities of soluble arsenic in the samples were
negligible The maximum allowable arsenic concentration in
the air of working places of 0.3 mg As/cu m was never ex-
ceeded
45231
Masek, Vaclav
BENZO(A)PYRENE IN THE WORKPLACE OF COAL AND
PITCH COKING PLANTS. J Occup. mod., 13(4):193-198,
April 1971. 3 refs.
The results of measurements of the atmospheric content of
benzo(a)pyrene (BAP) at some Czechoslovak coking plants are
presented. Various methods exist for determining BAP but
there is no acceptable standard method, nor in Czechoslovakia
is there a hygienic standard. It is hoped that the measure-
ments, taken over a period of 6 years, will help in setting stan-
dards Ways of reducing the health hazards include reducing
exhalations by modifying the charging equipment, limiting the
time workers spend in a noxious atmosphere, and subjecting
all coking plant personnel to regular medical checks. These are
only stopgap measures and a more thorough approach is
needed for the protection of people living near the plants as
well as those working in them
47099
Masek, Vaclav
NEW FINDINGS CONCERNING THE PROPERTIES OF FLY
DUST FROM COKING PLANTS. PART IV. HARD COAL
TAR DISTILLATION PLANTS. (Neue Erkenntnisse ueber die
Eigenschaften des Flugstaubes aus der Kokerei. Teil IV: Stem-
kohlenteerdestillationsanlagen) Text in German. Zbl. Ar-
beitsmed., 22(11):332-337, 1972. 11 refs. Part I. Ibid, 22(2):38-
47 Part II Ibid, 22(3)'69-74. Part III. 22(9)'276-281
In three tar distillation plants the ben7o(3,4)pyrene concentra-
tion in the fly dust was determined. Samples were taken at 20
different points on 566 impregnated Schleicher-Schuell filters
with a diameter of 11 cm. The benzo(3,4)pyrene concentration
was determined by chromatography. In all samples
-------
36 COKE OVENS
benzo(3,4)pyrene was found; the largest quantities in the sam- primarily in the fly dust fractions with diameters up to 5
pies were taken during charging and emptying of the tanks
with and from hot pitch. The benzo(3,4)pyrene was found micron.
-------
37
F. BASIC SCIENCE AND TECHNOLOGY
09930
Khanin, I. M., V. G. Deryugin, I. G. Kuprienko, B. D.
Kotlyar, A. V. Gorbunov, A. S. Zoltuev, and B. A. Boltsman
INVESTIGATION INTO THE OPERATING CONDITIONS OF
WASTE-GAS FLUES ARRANGED FOR CENTRAL
DISCHARGE OF THE COMBUSTION PRODUCTS. Coke
Chem., (USSR) (English Translation) (Gomersal), 24(8): 19-23,
Aug. 1967.
Commercial trials have been conducted at a Siberian coke and
chemical works to investigate the operating conditions of the
coke oven waste-gas glues m order to verify the experimental
results obtained on hydraulic models and the projected, mathe-
matically produced results. The following data have been
determined: the resistance coefficients of the smoke outlets on
the coke and pusher sides of a coke-oven battery, the re-
sistance coefficient when the streams from the side flues
merge at the entrace to the collecting flue; the resistance coef-
ficient when the streams from the side flues merge in the col-
lecting flue; and the degree of loading of the outside and in-
side half-flues. A comparison of the laboratory calculations
with the commercial results indicates a satisfactory level of
agreement. The flues are diagramed.
15723
Faingold, S. G., A M. Stanetskaya, L. A. Tretyakova, and N.
S. Kipot
CAUSES OF THE FORMATION OF NITRIC OXIDE IN THE
CARBONIZATION OF COALS. Coke Chem. (USSR) (English
translation from Russian of Koks i Khim.), no. 2:23-28, 1969. 10
refs.
While confirming that nitric oxide is an inevitable product of
coal carbonization, previous research has not established the
extent to which carbonization participates m nitric oxide con-
tent of coke oven gas or its relationship to the nitrogen con-
tent of coal. To resolve these questions, as well as determine
the nitric oxide content of coke-oven gas during carbom/ation,
various coal blends and different grades of coal were car-
bonized in a gas-tight oven chamber at a pressure of 600- 800
mm water gauge. The evolution of nitric oxide followed the
same pattern for all blends and coals: the content reached a
peak at 200-399 C, the beginning of carbonization, and the
peak lasted until 400 C. The quantity of nitric oxide evolved
was unrelated to the nitrogen content of the blends and coals
For example, one blend contained 2.36% nitrogen, and the
dynamic mean nitric oxide content of the coke-oven gas
equalled 2.83-3.67 ppm or 0.96-1.10 ml/kg for the blend The
nitrogen content of the blends ranged from 1.5-236% The
nitrogen content of coals varied less and the volatile matter
differed sharply, but nitric oxide formation was the same as
for blends. It is concluded that nitric oxide is formed as a
result of reactions involving the liberation of oxygen from the
air, introduced with the blend or coal and the oxygen-nitrogen-
containing compounds in the coal.
16623
Ganz, S. N., I. Ye. Kuznetsov and M. A. Lokshin
DETERMINATION OF DIMENSIONS OF HOLLOW
TOWERS FOR CLEANING COKE GAS OF HYDROGEN
SULFIDE. (K opredelemyu razmerov polykh bashen dlya
ochistki koksovogo gaza ot serovodoroda). Text in Russian.
Koks i Khim., no. 9:48-50, 1964. 1 ref.
Data on H2S elimination from coke gas in hollow atomizing
scrubbers as previously reported demonstrated the high effec-
tiveness of these devices. It was previously shown that the
rate of absorption of H2S by a Na2CO3 solution depends on a
set of physico-chemical, hydrodynamical and geometrical
parameters. New investigations using a semi-industrial test set
up enabled the determination of the effect of each of these
parameters on the rate of the absorption process and to
representation of the quantitative interrelations among these
parameters in terms of dimensionless ratios. An empirical ex-
pression was derived using the adsorption-rate coefficient; the
diameter of the atomizer; the coefficient of molecular diffu-
sion of a gas in another gas; the rate of rotation of the
atomizer, the kinematic viscosity coefficient of the liquid; the
velocity of the gas; the kinematic viscosity coefficient of the
gas; the coefficient of molecular diffusion of the gas in a
liquid; the wetting rate; the concentration of the absorbed
component in the gas; and the concentration of the absorbent
in the solution. The dimensionless coefficient is a function of
temperature and is found from the expression. A sub t equals
3O times 10 to the minus 6th power. (Pr sub 1(C sub 1 times t))
to the 2.7th power, where C sub 1 equals 50 kg/cu m Na2CO3
and t is the operating temperature of the scrubber. The dimen-
sionless expression fits well the experimental data and can be
used to calculate the principal dimensions and values of
operating parameters of hollow scrubbers for absorption of
H2S from coke gas. This is illustrated by a detailed calculation
of a hollow scrubber for cleansing of 60,000 cu m/hr of coke
gas containing 15 grams/cu m of H2S at a temperature of 30 C
and a Na2CO3 concentration in the solution of 50 kg/cu m to a
required degree of purification of 90%.
18185
Jordan, C. W , A L Ward, and W H. Fulweiler
GUM DEPOSITS IN GAS DISTRIBUTION SYSTEMS. Ind.
Eng Chem., 27(10) 1180-1190, Oct. 1935. 31 refs.
The efficacy of iron sulfide for the absorption of mtnc oxide,
together with conditions favoring its use, was determined by a
series of experiments involving the absorption of undiluted
and dilute nitric oxide by iron sulfide, and alkaline and metal-
lic sulfite absorbents. The highest activity for the absorption
was obtained by sulfided Lux iron oxide to which sufficient
sodium bicarbonate had been added to give an alkali ratio of
50%. Iron sulfide is economically feasible as an agent for the
commercial purification of manufactured gases because it can
be made from the hydrogen sulfide already present in commer-
ical gas, and it is not poisoned by sulfur of cyanogen com-
pounds, reduced by hydrogen, or affected by carbon dioxide
or carbon monoxide Though it does react with the small
-------
38
COKE OVENS
amount of oxygen present in manufactured gas, iron sulfide
can be used to advantage in removing hydrogen sulfide from
gas. As a result of the laboratory experiments, an inexpensive,
commercial process was developed for removing all of the
nitric oxide.
18197
Riese, Wilhelm
THE USE OF ACTIVATED COAL FOR THE REMOVAL OF
SMALL CONCENTRATIONS OF NITROGEN OXIDES FROM
GASES. (Ueber die Brauchbarkeit von Aktivkohle fuer die
Entfernung geringer Gehalte von Oxyden des Stickstoffs aus
Gasen.) Text in German. Brennstoff-Chem. (Essen), 21(3):25-
36, Feb. 1, 1940. 7 refs.
Laboratory experiments with 200 cm and 100 liters activated
coal showed that it is chemically, technically, and economi-
cally feasible to use it for the removal of nitrogen oxides from
waste gases of a coking plant. The waste gas develops in a
thermal cracking process during which water vapor is added.
The gas is subsequently washed under pressure with water and
lye. It is low in, but not free of, tar-forming hydrocarbons. To
achieve a high efficiency of the activated coal, the use of pres-
sure is recommended. The efficiency of the activated coal is
low if the concentration of tar-forming hydrocarbons is high.
Thus, original coking gas is less suited for activated coal treat-
ment than is coking gas converted by thermal cracking.
Generally, it can be said that activated coal can only be used
for NO removal if the gases are free of substances which soil
the surface of the coal. The situation is somewhat different if
the benzene in the coking gas is recovered simultaneously with
NO removal, since the costs of regenerating the activated coal
are partly covered by the revenue obtained from the sale of
benzene. Simultaneously with NO, NO2 is also removed to
prevent corrosion by the flue gases. The use of the activated
coal method for removal of small concentrations of nitrogen
oxides under pressure is simple and even inexpensive if the
gas is to be compressed anyway. Consumption of activated
coal is low, particularly since the coal spent by NO adsorption
from cracking gas can be used for adsorption elsewhere in-
stead of fresh coal. The reaction mechanism is probably
characterized by adsorption of nitrogen oxides on activated
coal and reaction with active C-atoms of the coal surface. In
addition, reaction of the nitrogen oxides with certain unsatu-
rated hydrocarbons and the action of oxygen may play a role
37056
Charadame, R.
THE AERODYNAMICS OF FLAMES. Preprint, Inst. of Com-
bustion and Fuel Technology of Canada, Ottawa (Ontario),
19p., 1970. 12 refs. (Presented at the North American Fuel
Technology Conference, Ottawa, Ontario, May 31-June 3,
1970, Paper Inst. F-NAFTC-1.)
Research studies carried out by the International Flame
Research Foundation and the Centre d Etudes et Recherches
des Charbonnages de France on the aerodynamics of flames
are summarized. Oil, coke-oven gas, pulverized coal, and natu-
ral gas flames were investigated. Specific research areas were
variables influencing flame properties, especially radiation; in-
teractions between pure aerodynamic phenomena and
physicochemical phenomena occurring in flames; development
of the theoretical flame model of flame jets; and tests with
both model and industrial-scale furnaces. The studies demon-
strated the importance of total momentum flux at the burner
for combustion and radiation and the importance of recircula-
tion currents in the pre-ignition phase. The total momentum
flux governs the mixing between fluid leaving the burner and
the surrounding combustion air: the more the momentum flux
increases, the more rapid the mixing becomes and the shorter
the flame While rapid mixing with secondary air retards igni-
tion, rapid mixing with recirculated gases speeds it up. The
studies described made it possible to improve the efficiency of
pulverized coal boilers, the operation of cement kilns, and gas
production from coke ovens.
45369
Dvornikov, A. G.
INCREASED CONCENTRATIONS IN CERTAIN COAL
FRACTIONS. Coke Chem. (USSR) (English translation from
Russian of: Koks i Khim., no. 9:6-7, Sept. 1971. 5 refs.
The mercury contents of fractions of some Donbass coals
were analyzed. The mercury content gradually increased from
the coarsest to the finest size fraction, reaching a maximum
for the below 0.1 mm fraction. The three finest fractions con-
tained less fusimte and vitrinite and far more pyrite than
coarse fractions. The relationship between fusinite and
vitrinite contents and fraction density was almost linear. The
mercury content of the carbonaceous clay shale increased in
the low-density fractions. However, the heaviest fraction con-
tained a high proportion of mercury in clay shale. The mercury
content of coal fractions is related inversely to their vitrinite
and fusimte contents and directly to their pyrite and clay shale
contents. The mercury found in anthracites is associated with
the pyrite present. The methods used to concentrate mercury
in the light and heavy fractions of anthracite can be used to
recover mercury from coals in the course of normal cleaning.
-------
39
G. EFFECTS-HUMAN HEALTH
00621
D.J. Von Lehmden, R. P. Hangebrauck, J.E. Meeker
POLYNUCLEAR HYDROCARBON EMISSIONS FROM
SELECTED INDUSTRIAL PROCESSES. J. Air Pollution Con-
trol Assoc. Vol. 15(7):306- 312, July 1965.
A number of selected industrial processes considered as poten-
tial sources of benzo(a)pyrene and other polynuclear hydrocar-
bons was surveyed. Polynuclear hydrocarbon emission levels
were measured directly for asphalt hot road mix preparation
and asphalt air blowing. Emissions of other pollutants, includ-
ing paniculate matter, carbon monoxide, and total gaseous
hydrocarbons were also measured, and are reported together
with pertinent data on process design and operation. Results
are discussed with reference to the type of process; the type
of equipment used, including control devices; and other fac-
tors The significance of some additional processes as con-
tributors of polynuclear hydrocarbons was examined indirectly
by collecting atmospheric samples of polynuclear hydrocar-
bons in residential areas in the vicinity of (1) a carbon black
manufacturing area, (2) a steel and coke manufacturing area,
(3) an organic chemical industry complex, and (4) a residential
and small-industry coal burning area. (Author abstract)
02561
V.B. Kapitul'Skii
PHYSIOLOGICAL CHANGES ENCOUNTERED IN WOR-
KERS EMPLOYED IN THE PITCH-COKE INDUSTRY. (O
nekotorykh fiziologicheskikh sdvigakh u rabochikh pekokok-
sovogo provizvodstva.) Hyg. Sanit. CFSTI: TT66-51160/1-3
1. Workers at a pitch-coke plant showed marked changes in
certain physiological functions as compared with a control
group. 2. Such changes were found in cardiovascular, respira-
tory, and muscle function, as well as in the central nervous
system. Changes in certain physiological indicators, such as
muscular strength, latent period of motor response to sound
and chronaxie, can be explained as due to the combined effect
of various unfavorable environmental factors. Among these
factors, aerosols of pitch and pitch distillates appear to play an
essential part, judging by the considerable changes in certain
physiological functions found in workers employed on the
preliminary processing of pitch, who perform relatively easy
tasks at normal efficient technological processes and by the
mechanization of operations involving heavy physical labor. In
addition, serious attention should be paid to individual protec-
tive measures, including respirators, goggles, antipitch pastes.
The workers should also be medically examined at regular in-
tervals.
05450
Kapitulskii, V. B. and Kogan, L. A.
A COMPARISON OF THE HYGIENE CHARACTERISTICS
OF THE SMOKELESS AND ORDINARY METHODS OF
CHARGING COKE OVENS. Coke Chem. (USSR) (Engh
Transl.) (8) 29-31, 1966
The hygienic effectiveness of a technique of smokeless charg-
ing of coke ovens is evaluated by comparing the atmospheric
contamination above a battery charged the normal way and
one using the smokeless charging method. The smokeless
charging involves the diversion of the bulk of the escaping
coke-oven gas, coal dust, and tar into the coke side gas col-
lecting main which is connected to the ovens for the charging
period. The smokeless charging reduced the dust concentration
from 143-2250 mg/cu m to 57 mg/cu m, the carbon monoxide
from 40-74 mg/cu m to 6-18 mg/cu rn, and the heat exposure
from 6.9-13.5 cal/sq cm min to 2.3-5.2 cal/sq cm min with the
time of maximum heat exposure cut from 39 to 18 percent of
the working shift. In 1964, the sick rate was 18 percent less
than for workers using the normal charging method, with the
incidence of catarrh one half and that of bronchitis one-sixth
in the case of smokeless charging, the mechanization of the
opening and closing of the charge holes has improved the con-
tamination problem on top of the ovens with further changes
indicated in trapping the dust from pushing the coke and dry
quenching.
08150
Itskovich, A. A.
THE STIMULABILITY OF THE OLFACTORY ANALYSER
IN THE HYGIENIC EVALUATION OF ATMOSPHERIC AIR
POLLUTION. In: Survey of U. S. S. R Literature on Air Pol-
lution and Related Occupational Diseases. Translated from
Russian by B. S. Levine. National Bureau of Standards,
Washington, D. C., Inst. for Applied Tech. Vol. 3, p. 106-109,
May 1960 CFSTI: TT 60-21475
The functional shifts in the human organism which resulted
from atmospheric air pollution by volatile products of the
coke-chemical industry were investigated. The effect of these
substances on the state of the olfactory analyzer in various
population groups was used as the selective index of pollution
effects. In the selective group-studies crystalline phenol and
thymol were used as the odor- emanating substances. Tests
were made on 241 individuals divided into 4 groups. Group 1
consisted of workers and technical personnel of a coke-chemi-
cal plant, Group 2 consisted of residents within 500 - 1000 m
from the production plant; group 3 consisted of school chil-
dren living in the same area; group 4 consisted of employees
of the Sanitary Institute who had no direct connection with the
source of the atmospheric air pollution. Determinations made
with the aid of the Elsberg-Levy olfactometer showed that in
66.6 percent of workers under study and of persons residing
500 - 1000 m from the coke-chemcial plant the threshold of
coke-chemical odor perception was above the normal. The
same was true of 50 percent of the youngsters of school age.
The results of olfactory threshold determinations were in
complete agreement with the anamnestic data secured from
the same population groups. The changes observed in the ol-
factory sensitivity of the groups were of a specific character
and could be regarded as effects of the coke- chemical at-
mospheric air pollutants. It was noted that persons with
pronounced changes in the olfactory sensitivity resided within
500 1000 m from the source of atmospheric air pollution
where, according to analysis, the concentrations of phenol
compounds in the air ranged between 0.167 - 0.237 mg/ cu m.
-------
40 COKE OVENS
This should be taken into consideration in the determination of air.
the limit of allowable concentration of phenol in atmospheric
-------
41
H. EFFECTS-PLANTS AND LIVESTOCK
26418
Babkina, V. M.
GROWTH AND DEVELOPMENT OF ORNAMENTAL HER-
BACEOUS PLANTS IN COKE CHEMICAL WORKS. In:
American Institute of Crop Ecology, Survey of USSR Air Pol-
lution Literature. M. Y. Nuttonson (ed.), Vol. 2, Silver Spring,
Md., American Institute of Crop Ecology, 1969, p. 8-12. (Also:
Okhrana Priorody na Urale, 1966:173-176, 1966.)
A study was undertaken to determine the effect of smoke
vented by a coke-chemical works on various ornamental
plants The air over three plots contained sulfur dioxide rang-
ing in concentration from 0.75 to 4 mg/cu m, while the fourth
plot was free of noxious gases. Test plants exposed to 0.75
mg/cu m did not differ in height from the plants grown in the
control plot. All bore fruit and produced good seed. Smoke
pollutants stimulated the growth of the Dahurian lily and of
the whiterim camomile, while phlox was severely damaged and
the hybrid peonies less so. Of the 46 tested plants, 25 reacted
slightly to 2 mg/cu m of the polluted air. Thwarted growth
processes were noted, however, with the Chinese pink, great
hellflower, Aztec mangold, and others. Dahlias and lupines
were severely damaged, producing few and freqently
deformed flowers. With 4 mg/cu m of polluted air. 25 of the 46
species perished during the developement of the cotyledons. In
most species the phase of vegetative growth was extended,
and the duration of blooming as well as the entire growth
period was shortened. A number of plants are recommended
for growing in areas exposed to sulfur dioxide.
39571
Masek, Vaclav
THE INFLUENCE OF FLY DUST FROM COKING PLANTS
ON SOME BIOLOGICAL PROCESSES OF PLANTS. (Der
Einfluss des Flugstaubes aus der Kokerei auf einige
biologische Prozesse de Pflanzen). Text in German. Gesundh.
Ing., 93(3):77-80, March 1972. 17 refs.
The influence of three typical samples of fly dust from a cok-
ing plant on enzymatic reactions, photosynthesis, chlorophyll
concentration in leaves of bean plants was studied. The
hydrolysis of starch with amylasis and of the albumen with
pepsin at 37 C and the inversion of sacharosis by invertase in
a buffered environment were also examined. None of the three
dust samples showed a signification activity in enzymatic reac-
tions. Applying the dust samples to the leaves of young bean
plants reduced the intensity of photosynthesis and the
chlorophyll concentration. In aqueous extracts, the dust sam-
ples liberated only small quantities of nutrients. Plants which
were grown in a dust suspension showed no increase of dry
substance and growth rate. A stimulating effect of the dust
samples on root growth was determined. A mixing of the dust
samples with the soil influenced the accessibility of water to
plants.
44777
Harney, Brian M., Donald H. McCrea, and Albert J. Forney
AERIAL DETECTION OF VEGETATION DAMAGE UTILIZ-
ING A SIMPLE 35-MM CAMERA SYSTEM. Preprint, Air
Pollution Control Assoc., Pittsburg Pa., p. 1-18, 1972. 4 refs.
(Presented at the Air Pollution Control Association, Annual
Meeting, 65th, Miami, Fla., June 18-22, 1972, Paper 72-160.)
A 35-mm camera bank and aerial photography were used to
detect and determine the extent of vegetative stress or damage
by various pollutants in low concentrations. Photography in-
volved the visible and near infrared bands of the electromag-
netic spectrum. Multispectral photography was also utilized.
The test site chosen included three large coal-fired power
plants and a complex of beehive coke ovens, and was subject
to relatively unpredictable and frequent ground haze condi-
tions. The film apparatus and procedure are described. Results
indicate that the use of a small hand-held, manually operated
camera is operationally and economically more advantageous
than the use of aerial photography. Color infrared film was
helpful in discriminating tree species and in haze-cutting abili-
ty. Its ability to identify stressed trees was better than conven-
tional color film in some cases, marginal in others. This pro-
perty varies with cyan contribution in the image. The air pollu-
tion damage to vegetation was not extensive. The symptoms
found indicated oxidants as the cause, with sulfur dioxide
from the power plants as a contributing factor. The damaging
effect of coke oven effluents was severe and easily detected in
aerial photographs. The major damage was localized to the
area adjacent to the coke ovens.
45389
Kozyukina, J. T. and V. I. Obraztsova
DYNAMICS OF TREE DAMAGE DUE TO COKE-CHEMI-
CAL INDUSTRY GASES. (Dinanika povrezhdayemosti
drevesnykh rasteniy gazami koksokhimicheskogo proizvodst-
va). Text in Russian. Uch. Zap. Perm. Gos. Univ., no. 256:191-
196, 1971. 11 refs.
Weekly examination of decoloration, spotting, lifetime, and
xenomorphism of leaves and tree growths (height and volume)
were made during 1968-1969 on a series of 10 to 15-year-old
trees exposed to atmospheres polluted with sulfur compounds,
phenols, ammonia, and coal dust. Injury to trees was ob-
served. Harmful changes were most pronounced in older trees,
and decreased in poplar, ailanthus, mulberry, acacia, English
elm, and were smallest in privet. A direct relation was ob-
served between the extent of xenomorphism and plant re-
sistance to polluting gases. (Author abstract)
-------
42
I. EFFECTS-MATERIALS
26313
Cherkasov, N. Kh., L. K. Gorin, and R. Ya. Kolesnikova
OPERATION OF THE CYCLE OF FINAL COOLING OF
COKE GASES. (O rabote tsikla konechnogo okhlazhdeniya
koksovogo gaza). Text in Russian. Koks i Khim., no. 10:33-35,
1970. 4 refs.
The problem of corrosion in closed-system terminal cooling of
coke gases, due to the absorption of hydrogen sulfide,
hydrogen cyanide, and other acidic gases, and the concommi-
tant interference with benzene removal were studied. Flushing
the water through absorbing resins is not effective in removing
these corrosive agents which simply act to degrade the resin.
Hence, a closed cooling system does not seem feasible.
36804
Zaychenko, V. M., I. I. Rozhnyatovskiy, E. N. Kucheryavyy,
D. D. Vorobyev, A. P. Sergeyev, M. S. Komarovskiy, and L.
F. Vasyutin
FACTORS CAUSING ACCUMULATION OF CORROSIVE
COMPONENTS IN ABSORPTIVE OIL. (Prichiny nakopleniya
korrozionno-agressivnykh komponentov v poglotitelnom masle).
Text in Russian. Koks i Khim., no. 5:28-33, 1969. 1 ref.
Factors contributing to the accumulation of corrosive sub-
stances within the recycling oil utilized in the absorption of
benzene from coke processing were investigated. Sulfides,
cyanides and thiocyanates are absorbed by the recycling oil
within the gas exchange facility (absorber) where contact
between gaseous and oily phases occurs under increased pres-
sure. The circulating oil contains approximately 50-90 mg/L
chloride ion and 110-150 mg/L sulfate ion. Accumulation of ag-
gressive compounds within the absorptive oil is enhanced by
chemical reaction occurring under the circumstances. Along
with hydrogen sulfide and cyanide, oxygen from coke gas is
absorbed as well. This oxygen produces the oxidation of
hydrogen sulfide and other sulfides to polysulfides. Polysul-
fides react readily with cyanide to produce thiocyanates.
Decrease in H2S and HCN concentrations within the absorp-
tive oil due to these reactions leads to the absorption of new
amounts of sulfides from the coke gas. Increased pressure
enhances these processes producing accumulation of corrosive
thiocyanates within the recycling oil. To prevent corrosion of
the benzene producing equipment, procedures for the removal
of H2S before the aromatic hydrocarbon absorption stage
should be developed. The countercurrent procedure with al-
kaline solutions for the capturing of H2S within the absorber
section appeals to be unsatisfactory for the mentioned pur-
poses.
-------
43
K. STANDARDS AND CRITERIA
12277
Sayfutdinov, M. M.
EXPERIMENTAL DATA PROPOSED FOR THE DETER-
MINATION OF MAXIMAL ALLOWABLE AMMONIA CON-
CENTRATION IN ATMOSPHERIC AIR. In: The Biological
Effects and Hygienic Importance of Atmospheric Pollutants,
Book 10. Translated from Russian by B. S. Levme, U.S.S.R.
Literature on Air Pollution and Related Occupational Diseases,
Vol. 17, pp. 67-76, 1968. CFSTI: PB 180522T
Air quality studies near several industries, especially metallur-
gical plants having coke oven gas and nitrate operations on the
premises showed that these were the chief sources of at-
mospheric air pollution with ammonia. Onvestigations con-
ducted with workers and with laboratory animals led to the
conclusion that the subthreshold ammonia concentration which
had no affect on the cerebral cortex biopotentials is at the 0.2
mg/cu.m level, which can be regarded as its maximal allowable
single concentration in atmospheric air. Under conditions of
chronic inhalation exposure such a concentration proved tox-
icologically inactive. On this basis such ammonia concentra-
tion can be recommended as its maximal allowable limit in at-
mospheric air.
35390
Plaks. Norman
IMPROVED PROCESSING METHODS FOR CONTROL OF
AIR POLLUTION EMISSIONS FROM COKEMAKING.
Preprint, Economic Commission for Europe, 27p., 1971. 3 refs.
(Presented at the Seminar on Problems of Air and Water Pollu-
tion in the Iron and Steel Industry, Leningrad, USSR, Aug. 23-
28, 1971.)
In the United States, the first set of Federal emission stan-
dards for coke plants will probably cover charging of the
ovens, largely because the control technology necessary will
be demonstrated sooner than the control technology for other
stages of coke production. Afterwards, there will be a demon-
stration of new technology for controlling the emissions from
pushing of coke. Standards have been established for conven-
tional slot-oven coke plants; emissions from all new installa-
tions cannot exceed the measured quantity emitted by the
demonstrated processes. The next step will be to build and
demonstrate the capabilities of air pollution control technology
applied to a continuous or formcoke plant Standards
established for a continuous coking plant should limit emis-
sions to levels considerably lower than those permitted for
slot-oven plants. All coke plants built after the standards are
promulgated will not be allowed to emit more pollutants than a
well-controlled continuous coke plant emits. By adherence to
this program, coke-plant emissions, under Federal legislation,
will, by an evolutionary process, be decreased to a level that
has been established by the application of the best technology
available. (Author conclusions)
38578
Duprey, R L.
THE STATUS OF SOX EMISSION LIMITATIONS. Chem.
Eng. Progr., 68(2):70-76, Feb. 1972. 7 refs.
The Clean Air Act, as amended, will undoubtedly result in
more stringent sulfur dioxide limitations to achieve the na-
tional ambient air quality standards In addition, many jurisdic-
tions are expected to reduce the sulfur content of fuels to less
than 0.3%, and the Environmental Protection Agency has
proposed restricting sulfur oxides emissions from new steam-
generating plants to 0.8 and 1.2 Ib/milhon Btus of heat input
for liquid and solid fossil fuels, respectively Present state and
local restrictions on fuel sulfur content, which are tabulated
together with emission standards in equivalent sulfur levels,
range from 0.3% to 2.7% for fuel oil and 0.2% to 3.6% for
solid fuel. The new restrictions will have a substantial impact
on the coal industry and petroleum refinery operations faced
with the desulfunzation of petroleum products Sulfur
recovery plants will need to operate more efficiently in remov-
ing sulfur from petroleum refining, natural gas processing, and
coke oven gas. Control techniques employing tail-gas cleaning
are available to reduce sulfur oxide emissions well below 0 01
Ib of sulfur processed Primary nonferrous smelters are faced
with regulations that require about 90% reduction in sulfur ox-
ides emissions Existing sulfunc acid plants are expected to be
restricted to 6 5 Ib of sulfur oxides/ton of acid and new plants
to 4.0 Ibs of sulfur oxides/ton of acid.
-------
44
L. LEGAL AND ADMINISTRATIVE
11914
L. N. Samoilovich, and Yu. R. Redkin
AIR POLLUTION WITH 3,4-BENZPYRENE FROM
PETROLEUM AND CHEMICAL INDUSTRIES. ((Zagryaznenie
atmosfernogo vozduha 3,4-benzpirenom predpriyatiyanii nef-
tehimirkeskoi promishlennosti.)) Text in Russian. Gigena i
Sanitariya, 33(9):10-14, Sept. 1968. 7 refs.
The 3,4-benzpyrene concentrations of 193 air samples from 2
petroleum refineries, one chemical plant, and the city of Groz-
ny, collected for 3 years by an ERV-49 aspirator and adsorbed
on the organic FPA-15 tissue, were determined after extraction
with benzene and dilution with n-octane. The refineries had
0.1-40 mKg microgram/100 cu m (with values of 0.8-40
mKg/100 cu m in coke shops), the chemical plant (pyrolysis
shop) 0.9-9.1 mKg/100 cu m, and the city sections (distance 50-
2000 m from a contact coke plant) 0.08-0 40 mKg/100 cu m
maximal 3,4-benzpyrene concentrations. The emission was the
highest during full-capacity production, with 2-4-fold increase
in a contact coke plant of refinery No 2. By order of the city
sanitary physician refinery No2 was closed down temporarily.
The furnaces were supplied with gas-forming fuel and her-
metization was carried out. It was concluded that within a 2-
km radius from a petroleum refineiy, there is considerable 3,4-
benzpyrene pollution. The most significant sources were the
coke and pyrolysis shops.
28584
Mahler, E. A J.
AIR POLLUTION. Chem. Bru., 6(5):201-203, May 1970.
The legal basis for air-pollution control in the United Kingdom
is the Alkali and Works Regulation Act of 1906. Originally
covering only the chemical industry, the scope of the Act now
includes a considerable portion of heavy nonchemical indus-
try, including ironworks, steelworks, power stations,
gasworks, coke ovens, and certain brick works. The main
provision of the Act requires works to use the best practicable
means to prevent the emission of any noxious or offensive
gases and to render unavoidabl emissions harmless and inof-
fensive. The second requirement is usually met by discharging
at such a height that ground-level concentrations are low. Rou-
tine inspections help insure compliance with the standards set
by the Chief Alkali Inspector Chemical plants scheduled
under the Alkali Act cause little neighborhood air pollution.
However, increasing production will require either develop-
ment of new processes with an inherently lower proportional
rate of emission or improvement of abatement measures.
32517
Dreyhaupt, Franz J.
IN DISHARMONY BEYOND THE GOAL. (Im Zwiespalt am
Ziel vorbei). Text in German Umwelt (Duesseldorf), 1(41:15-
17, Aug. 1971
Laws and regulations in Germany concerning the prevention
of air pollution are incomplete on federal and state levels. The
technical directives (TA) passed in 1964 require permits for the
construction, alteration, and operation of a plant only if it is
equipped with the latest air pollution control facilities. The
maximum allowable emission concentrations within the
reaches of the plant may not be exceeded by the emissions of
the plant. The list of TA maximum allowable emission concen-
trations includes dust (without differentiation between toxic
and non-toxic); nitrous gases; chlorine, hydrogen sulfide; and
sulfur dioxide. The concentration limit for hydrogen sulfide is
far too high, since it is above the odor threshold. Concentra-
tions prevailing on days of inversion weather are excluded
from consideration. The air pollution control systems in coking
plants, steel plants, non-ferrous metallurgical plants, oil refine-
ries, the chemical industry, thermal power plants, and refuse
incinerators must be improved
-------
AUTHOR INDEX
45
A
ABET B-31123
AGAPOV, R C B-06655
ALTYBAEV M 'B-25315
AMSTISLAVSKII D M *B-44156
ANDERSEN H C 'B-15271
ANDERSON D M A-40159
ARITA S B-15692
ARTAMONOV YU P B-34336
B
BABKNKO V P B-26075
BABKINA V M 'H-26418
BALANOV V G B-23136, 'B-41042
BALCH G E B-29217
BALLA P A *B-26606
BARNES T M *B-20960
BECK K G 'B-28384
BECKER R *B-27638
BEECKMANS I 'D-27406
BELIN F T 'B-39751
BELONO7.HKO A M 'B-45426
BELOUSOV, S P 'B-08178
BELOV K A 'B-17943
BENEDICT, L G C-10671
BERGART YA M B-39751
BHATTACHARYA P A-44028
BHATTACHARYA R N »A-44028
BOLTSMAN, B A E-09930
BONDARENKO I P 'B-16602
BORODINA G YE B-38832
BRANDT A D *A-40159
BRANDT, A D *B-02728
BREITBACH E 'B-19253
BRODOVICH A I B-16157, B-35759
BUBLIK A I B-19308
BUREAU, A C 'B-05432
C
CARBONE W E *B-35284
CHEKHOV, O S B-06654
CHERADAME R *f-37056
CHERKASOV N KH *I-26313
CHERNICHENKO P M B-24620
CHERTKOV B A *B-23249
CHOULAT G B-19253, B-47794
CHUANG T 'D-38830
CLENDENIN, J D 'A-08392
COOPER, R I, 'B-02025
D
DANCY T E 'B-19203
DANII.EVICH Y I 'B-17259
DAVIFJ7.ON R I B-23136, B-41042
DECARI O, J A A-05108
DhHV V YA B-46945, B-46946
DENISOV, A M B-04634
DERYUGIN, V G F-09930
DESWAEF R D-27406
DIKUN P P 'D-21239
DOHERTY, J D *A-05108
DOL7.HENKO A M B-27563
DONOVAN, T C-08335
DREYHAUFF F J 'L-32517
DUBROVSKAYA D P A-14286, B-23910
DUN, A S B-08178
DUPREY R L 'K-38578
DVORN1KOV A G 'F-45369
ECKHARDT H B-46441
EDEI.MAN, I 1 *A-11901
EDGAR W D 'B-47110
EHNERT, W *B-03204, C-03233
EIDELMAN E YA B-45308
EL1SEEV O I B-39751
ENGELS, L H 'B-04396
FAINGOI.D S G *F-15723
FAYDA I A A-25215
FILIPPOV B S B-16157
FINKEL SHTEYN P K 'B-26075
FORER YEA B-23910
FORNEY A J H-44777
FRANCIS W 'B-16943
FRITZSCHE H B-47794
FUHRMANN N *A-38657
FULWE1I.ER W H E-18185
FURMAN A M B-24620
G
GAN7 S N B-31777, *F-16623
GANZ, S N *B-08183
GHIGNY P *B-27441
GILS W *A-29781
GOB1ET V 'B-37674
GOFMAN M S A-13330
GORBUNOV, A V F-09930
GORIN L K 1-26313
GOROKHOV I N B-31777
GORSKAYA, R V 'C-06908
GRAHAM I P B-34081
GROSICK H A *A-29627, 'B-35503
GUBANOV M T B-27563
GUENTHFROTH H 'B-16642
GUR'IOVNIK P F *B-23910
GUSE W A-38526
H
HALL D A *D-29257
HALL, I R C-08335
HANGEBRAUCK, R P
HAR1MA M *B-43752
HARNEY B M '11-44777
HASEBA S B-31123
HASEBE S 'B-15692
HAYASHI T B-29900
HELLING S *B 46441
HEMMING C *B-43840
HERRICK R A 'A-41877
HERRICK, R A 'C-10671
HOFFMAN A O B-20960
HORNSBY SMITH M P A-17583
HOVEY M W B-19733
I
IEVLEV V V 'B-41447
ILYASHENKO V N B-1349!
ISHIBASHI Y B-29900
ITSKOVICH, A A 'G-08150
JAGNOW H I *B-31138
JORDAN C W *F-18185
'A-05005, G 00621
K
KABRIN L A B-14437
KAGASOV V M *B-24620
KALMYKOV A V *B-27563
KANBARA S B-26607
KAP1TUL SKII, V B 'G-02561
KAPITULSKII, V B *G-05450
KARTSYNEL, M B B-04581
KARYUKIN A A A-24195
KAZMINA V V *B-45324
KEDRON B B-17318
KERN AN J J *B-14779
KETTNFR H *D-26040
KHALAIMOVA A M *C-24621
KHALYAPIN S A *C-41644
KHANIN I M 'B-23911
KHANIN, I M *B-04581, 'F-09930
KHIZHNYAK, N D A-11901
KHVAF M B A-24195
Kli'OT N S 'B-16157, *B-35759, F-15723
KIRILLIN V M B-38832
KLEBNIKOV O P B-24620
KOEHLER K H 'B-22503
KOGAN, I A G-05450
KOLESNIKOVA R YA 1-26313
KOI.YANDR L YA 'A-25215
KOMAROVSKII M S B-13491
KOMAROVSKIY M S 1-36804
KOMURA S B-29900
KONONFNKO A F A-25214, A-26314,
D-35081
KOSAKI M 'B-31223
KOSSOVSKIY V F B-41042
KOTLIK, S B B-01767
KOTLYAR, B D F 09930
KOVALENKO M F C-24621
KOVALFNKO V S B-23911
KOYAMA S 'B-29900
K07YUK1NA I T 'H 45389
KRIZ M 'B-17318
KUCHERYAVYI E N B-13491
KUCHERYAVYY E N L 36804
KUKHONOVEFS YU D B-34336
KULFSHOV, P J 'B-06650, 'B-06651,
'B-06652
KUPR1FNKO, I G F-09930
-------
46
COKE OVENS
KUTUZOV V N A-30026, B-26075
KUTUZOVA L N 'A-25214, 'A-26314,
•A-30026, 'D-35081
KUZMENKOV, A R 'B-08428
KUZNETSOV I Y F-16623
LAST W B-33382
LAUFHUETTE D B-47794
LAZORIN S N B-41447
LEBEDEVA, G N 'B-01767
LEE G W *B-34081
LEE, G W B-02025
LEIBOVICH R E 'B-19308
LIKSHIN, M A B-08183
LITVINENKO M S 'B-34421
LITVINENKO V I B-41447
LOKSHIN M A F-16623
LOWN1E H W JR B-20960
M
MAHLER E A J *L-28584
MAIGOV I V B-14437
MALLETTE F S 'A-40340
MAMATOV A D B-14437
MARCHENKO YU G 'B-31682
MARKUS G A 'A-14767, B-17849
MARTING D G *B-29217
MASEK V A-13219, 'A-16125, 'A-19209,
*A-37713, 'A-46920, 'C-25030,
D-26040, 'D-38895, 'D-45231,
'D-47099, 'H-39571
MASEK, V 'D-08485
MATVEEVA I E B-44156
MAYKOV V P B-24620
MCCREA D H H-44777
MCMANUS G J *B-42024
MEADES M R A-17583
MEDVEDEV K P 'A-28641
MEEKER, J E A-05005, G-00621
MELIKENTSOVA V I A-24195
MENYAKIN E S 'B-14420
MEZENTSEV, I Y *B-06656
MIKHNO V P B-23136
MIRONOV A E C-41644
MITROFANOV N I 'B-23143
MITYUSHKIN V G 'B-45658
MIZIN V A B-23911
MOTT R A *B-28228
MOVCHAN A T B-23911
MUSTAFIN, F A B-06655
N
NARATA N *B-26607
NELIPA O G B-23911
NELLIST G R D-29257
NICHOLS G B A-26441
NICOLAU M 'B-44989
NIKBERG I I D-21239
NIKBERG, I I B-08178
NIKOLAEV N N B-39751
NOSKO G S B-28532
NOVIKOV V E B-31682
O
O MARA R F 'B-39960
OBRAZTSOVA V I H-45389
OGLESBY S JR 'A-26441
OHME W 'A-21429
OKI T *B-31123
OLDEN, M J F B-05432
ORATOVSKII V I A-14767, B-17849
OREKHOV I N B-16260
OZERSKII Y G A-14767, 'B-17849
OZOLINS, G 'A-09737
PAKTER M K 'A-14286, 'B-45308
PANASENKO N A A-15455
PANESENKO N A B-23911
PANTELEENKO N O B-44156
PARKER A 'A-43346
PATRIKEEV, V S B-01767
PEREDERII P K 'B-24998
PERMYAKOV, V A B-06655
PERSHIN A V A-14286
PERVUSHINA, N P B-01767
PETROPOLSKAYA V M A-24195,
A-28641
PETROVA L N B-17943
PITT R S *A-48279
PLAKS N 'K-35390
PLANKERT M 'C-38361
POLKOVNICHENKO N A B-28532
POZHIDAEV A T B-45308
POZIN M E 'B-16260
PURCELL P R 'B-34083
PUSTOVIT YU A 'B-38832
R
RANDELL G E C A-17583
RAZBEGAEVA, A P *C-06653
REDKIN, Y R L-11914
REHMANN, C A-09737
REVZIN I G 'B-31777
RICHARDS, R T 'C-08335
RICKLES R N 'B-21965
RIESE W 'F-18197
ROSLYAKOV T M B-46945, B-46946
ROTT M V *B-24977
ROUSSEL A A 'A-36379
ROZHNYATOVSKII I I B-13491
ROZHNYATOVSKIY I I 1-36804
SAITO Y B-29900
SALTAN P L A-30026, B-26075
SAMOILOVICH, L N 'L-11914
SARJANT R J B-40232
SASHEVSKAYA Z G A-25214
SAYFUTDINOV, M M 'K-12277
SCHULZE V 'C-29157
SEDACH V S 'B-28532
SEDLAK J A-19209
SELLARS J H *A-17583
SEMENOV, P A 'B-06654
SEMISALOV YA D B-28532
SERGEEV A P B-23136
SERGEYEV A P 1-36804
SEVOSTYANOV V N B-24977
SHAPIRO S YA B-39751
SHELEST V P B-19308
SHELKOV S K B-19308
SHEVCHENKO, V R B-01767
SHIBLER B K 'B-19733
SHINKAREVA T V B-38832
SHTEIN A L B-34336
SHUKH YA I B-24977, B-31777
SHULESHOV E I B-13491
SIEU H 'B-45688
SLAVGORODSKAYA N P B-13491
SMITH J 'B-3%56
SMITH W M 'A-27900, *A-45461
SOKUL SKIY G P A-26314
SOKULSKII G P D-3508I
SOMMERS H 'B-33382
SPEIGHT G E 'B-40266
STANETSKAYA A M F-15723
STARKE E P B-14437
STEBLIY K T 'A-15455
STEPHANY H A-36379
STRELTSOV V V B-25315
SUGITA S B-29900
SULIMA V D A-30026
SURYADNYI, V I B-08428
SUSSMAN V H 'B-39904
TAKESHITA K B-15692
TALALAEV G K A-14286
TANIMURA, H 'D-11015
TARAT E Y B-16260
TASHIRO K B-29900
TELLING H 'A-22504
TERESCHENKO L Y B-16260
THOENES H W 'A-38526
THRING M W 'B-40232
THURAUF, W 'C-03233
TIMOFEYEV Y D A-15455
TIPPMER K B-46642
TOYAMA A B-31123
TRETYAKOVA L A F-15723
TROFIMOV A I 'B-13718
TRONDINA G I B-34336
TSUNEMOTO T B-15692
TSYPIN A Z A-15455
TSYPIN, A Z 'B-03238
TUMANOV, Y V B-06654
TUPITSIN Y K B-17259
TYUKANOV V N B-27563
TYUTYUNNIK L N B-23136
u
UNTERBERGER O G 'A-13330
VAR YEV V I B-45658
VARSHAVSKII T P B-14437
VARSHAVSKII, T P *B-04634
VARSHAVSKY, T P *B-06655
VASYUTIN L F 1-36804
VEJVODA J B-17318
VISVANATHAN S B-34207
VISWANATHAN T S 'B-34207
VODOLAZHCHENKO V L B-23136
VOLKOV E L 'B-46945, 'B-46946
VON LEHMDEN, D J A-05005, 'G-00621
VOROBEV D D 'B-13491, 'B-23136
VOROBYEV D D 1-36804
W
WARD A L F-18185
WASILESWSKI P B-45688
WATANABE S 'B-29240
WEBER H 'B-46642, 'B-47794
WESKAMP W A-21429, B-28384
WIELAND G E B-26606
WILLIAMS T H B -34083
YAKOVLEV, V I
YAMASHITA Y
B-04581
B-29900
-------
AUTHOR INDEX
47
YEFREMOV YU G B-24620
YERMOLOVA V *B-25216
YUKHNOVETS Y D B-14437
ZADOROSHNAYA N V A-24195
ZAICHENKO V M *A-24195
ZAYCHENKO V M B-35759, '1-36804
ZEMSKAYA Y K B-16602
ZHERDEVA YE A C-24621
ZHUKOV N A B-14437
ZLATIN L E 'B-14437, *B-34336
ZLATIN, L E B-04634
ZOLOTAREV, K V B-04634
ZOLTUEV, A S F-09930
-------
-------
SUBJECT INDEX
49
ABATEMENT A-36379, A-38657, A-40340,
B-40497, K-38578, L-28584, L-32517
ABSENTEEISM G-05450
ABSORPTION A-11901, B-01767, B-04581,
B-05432, B-06654, B-08183, B-16157,
B-16260, B-16602, B-22503, B-23910,
B-23911, B-24620, B-24977, B-25216,
B-25315, B-29240, B-31682, B-33382,
B-43752, B-45688, B-46945, B-46946,
B-47794, F-16623, F-18185, 1-26313,
1-36804
ABSORPTION (GENERAL) B-23249
ACETYLENES B-15271
ACIDS A-09737, A-15455, A-21429,
A-25214, A-26441, B-05432, B-06654,
B-19733, B-24977, B-27638, B-29900,
B-34083, B-34336, B-34465, B-37343,
B-38832, B-39751, B-41447, B-45426,
B-47794, 1-26313, K-38578
ADMINISTRATION A-09737, A-36379,
A-38657, A-45461, B-21965, B-39904,
B-40497, F-37056, K-35390, L-11914,
L-28584
ADSORPTION A-37713, A-46920, F-18197
ADULTS G-08150
AERODYNAMICS A-26314, B-04581,
B-06650, B-06651, F-37056
AEROSOLS A-38657, G-02561
AFTERBURNERS B-17259, B-39751
AGE G-08150
AIR POLLUTION EPISODES A-40340
AIR QUALITY MEASUREMENT
PROGRAMS A-09737
AIR QUALITY MEASUREMENTS
A-05005, A-09737, A-14767, A-16125,
A-25214, A-26314, A-27900, A-45461,
C-08335, C-10671, C-25030, D-11015,
D-21239, D-26040, D-27406, D-29257,
D-35081, D-38830, D-38895, D-45231,
D-47099, K-12277, L-11914
AIR QUALITY STANDARDS A-13219,
B-40497, D-26040, D-38895, K-12277,
L-32517
AIRCRAFT B-29628
ALCOHOLS A-l 1901, A-14767, A-25214,
A-26314, B-17849, B-24998, B-37343,
G-08150, H-45389
ALDEHYDES A-38526, A-43346
ALIPHATIC HYDROCARBONS B-03204,
B-06577, B-15271, B-27638, B-34465,
B-44156
ALKALINE ADDITIVES B-17318,
B-17849, B-34083
ALTITUDE A-26314, B-31223, L-28584
ALUMINUM B-43840
ALUMINUM COMPOUNDS A-26441
ALUMINUM OXIDES B-33382, B-44156
AMIDES B-31777
AMINES B-44156
AMMONIA A-14767, A-22504, A-25214,
A-29627, B-01767, B-04634, B-05432,
B-06576, B-06654, B-19253, B-23143,
B-31138, B-34421, B-37343, B-38832,
B-40266, B-43752, B-45688, B-46441,
B-46642, B-47794, G-05450, H-45389,
K-12277
AMMONIUM COMPOUNDS A-14767,
A-22504, A-25214, A-29627, B-01767,
B-04634, B-05432, B-06576, B-06654,
B-19253, B-23143, B-23249, B-31138,
B-34083, B-34336, B-34421, B-37343,
B-38832, B-40266, B-43752, B-45426,
B-45688, B-46441, B-46642, B-47794,
G-05450, H-45389, K-12277
ANALYTICAL METHODS A-05005,
A-21429, A-22504, A-37713, A-40340,
A-41877, A-44028, B-03238, B-06652,
B-19203, B-20960, B-21624, B-23910,
B-24620, B-26607, B-37343, B-37674,
B-41042, B-44989, C-06908, C-08335,
C-10671, C-24621, C-25030, C-29157,
C-37217, C-38361, D-11015, D-35081,
D-38895, D-47099, G-00621, L-11914
ANIMALS G-02561
ANNUAL A-09737, D-26040, D-38830
ANTHRACENES A-05005, B-34421,
D-08485, G-00621
AREA SURVEYS A-09737
AROMATIC FRACTIONS A-27900,
L-11914
AROMATIC HYDROCARBONS A-11901,
A-14767, A-25215, A-26314, A-30026,
B-17943, B-23910, B-24620, B-26075,
B-31138, B-31682, B-34421, B-35284,
C-24621, C-29157, D-11015, D-35081,
G-05450, G-08150, 1-26313, 1-36804,
L-11914
ARSENIC COMPOUNDS A-13219,
B-08183, B-16602, B-41447, B-45426,
D-38895
ASHES A-21429, B-04634
ASIA A-44028, B-15692, B-26607, B-29240,
B-29900, B-31123, B-31223, B-34207,
B-40497, B-43752, D-11015, D-38830
ASPHALT A-05005, A-40159, G-00621
ASPIRATORS B-06585, L-11914
ATMOSPHERIC MOVEMENTS A-40340,
B-37674, D-38830
AUSTRALIA A-48279
AUTOMATIC METHODS B-26607,
C-06653
AUTOMOBILES A-05005
AUTOMOTIVE EMISSIONS A-05005,
B-29628
B
BAFFLES A-21429, B-21624, B-23136,
B-40266, B-46945
BAG FILTERS A-41877, B-39656,
B-40232, B-40266
BARLEY B-15271
BASIC OXYGEN FURNACES A-09737,
A-26441, A-41877, A-48279, B-02728,
B-40266
BELGIUM B-27441, D-27406
BENZENE-SOLUBLE ORGANIC MATTER
A-05005, A-27900, A-45461, C-08335,
C-25030, D-21239, L-11914
BENZENES A-25215, A-26314, B-17943,
B-23910, B-24620, B-31138, B-31682,
B-34421, B-35284, C-24621, C-29157,
D-35081, G-08150,1-26313,1-36804
BENZO(3-4)PYRENE A-05005, A-16125,
A-38657, D-08485, D-11015, D-21239,
D-26040, D-45231, D-47099, G-00621,
L-11914
BENZOPYRENES A-05005, A-16125,
A-38657, C-25030, D-08485, D-11015,
D-21239, D-26040, D-45231, D-47099,
G-00621, L-11914
BERYLLIOSIS B-03238, G-00621
BESSEMER CONVERTERS A-40340,
B-31223, B-39904, B-39960, B-40232
BLAST FURNACES A-05108, A-09737,
A-26441, A-40340, A-41877, A-48279,
B-02728, B-06577, B-20960, B-28228,
B-31223, B-39656, B-39904, B-39960,
B-40232, B-40266, B-40497, C-24621,
D-11015
BLOOD CELLS K-12277
BOILERS A-05005, A-29781, A-38526,
B-02728, B-29900, B-34465, B-39751
BRICKS A-40159, D-38830, L-28584
BUBBLE TOWERS B-23911
BUTANES B-34465
BY-PRODUCT RECOVERY A-11901,
A-24195, A-48279, B-16943, B-19733,
B-21965, B-22503, B-23249, B-24620,
B-24977, B-31138, B-31682, B-31777,
B-34083, B-34207, B-34336, B-34421,
B-34465, B-35503, B-37343, B-38832,
B-39751, B-41447, B-43752, B-43840,
B-45308, B-45426, B-46946, F-45369,
K-38578
CALCIUM COMPOUNDS B-15692,
B-31777, B-45426
CALIFORNIA A-40340
CAMERAS H-44777
CANADA A-40340, B-29628, G-02561
CANCER G-00621
CARBON BLACK A-05005, A-08392,
A-26441, C-08335, G-00621
CARBON DIOXIDE B-17259, B-27638,
B-28384, C-06653
CARBON DISULFIDE A-25214, A-25215,
A-26314, C-24621, D-35081
CARBON MONOXIDE A-09737, A-22504,
A-36379, A-38526, A-40159, A-41877,
A-43346, B-23143, B-35284, B-37343,
B-40266, B-41042, C-06653, C-29157,
D-38830, G-05450
CARBONATES B-03238, B-41447, B-45426
CARCINOGENS D-08485, D-21239,
G-00621
CARDIOVASCULAR DISEASES G-02561
CATALYSIS A-05005, A-30026, A-37713,
A-46920, B-15271, B-15692, B-16157,
B-24977, B-26075, B-31123, B-33382,
B-39751, C-38361
-------
50
COKE OVENS
CATALYSTS A-30026, B-15271. B-15692,
B-24977, B-26075, B-31123, B-33382,
C-38361
CATALYTIC ACTIVITY A-46920, B-39751
CATALYTIC OXIDATION A-30026,
B-15271, B-23249, B-24977, B-26075,
B-41447
CELLS K-12277
CEMENTS A-08392, A-09737, A-26441,
A-29781, A-36379, A-38657, B-29900
CENTRIFUGAL SEPARATORS A-05005,
A-21429, A-40159, B-05432, B-23136,
B-29900, B-35284, B-40232, B-40266
CHARCOAL A-08392
CHEMICAL COMPOSITION A-05005,
A-14767, A-16125, A-25214 A-27900,
A-45461, C-08335, C-10671, C-25030,
D-21239, D-27406, D-38895, D-47099,
L-11914
CHEMICAL METHODS A-37713,
B-03238, C-37217, D-35081
CHEMICAL REACTIONS A-26441,
A-37713, A-48336, B-03204, B-13718,
B-16157, B-19253, B-23249, B-31138,
B-34336, B-35759, B-45324, B-47794,
F-18185, H-39571, 1-36804, L-I1914
CHILDREN G-08150
CHLORIDES B-03238, 1-36804
CHLORINE COMPOUNDS B-03238,
1-36804, L-32517
CHROMATES C-37217
CHROMATOGRAPHY A-05005, A-22504,
A-44028, B-23910, B-24620, C-24621,
C-25030, C-29157, D-11015, D-35081,
D-47099
CHROMIUM COMPOUNDS C-37217
CHRYSENES D-08485
CITY GOVERNMENTS B-40497, L-11914
CLEAN AIR ACT K-38578
COAL A-05005, A-05108, A-08392,
A-09737, A-13219, A-13330, A-17583,
A-25214, A-38657, A-43346, A-48336,
B-02025, B-04396, B-04634, B-06585,
B-06655, B-06656, B-15692, B-17318,
B-17680, B-19308, B-21965, B-27563,
B-28228, B-29217, B-31123, B-35284,
B-37343, B-38832, B-40497, B-44989,
B-45426, C-03233, C-10671, C-25030,
D-26040, D-45231, F-15723, F-18185,
F-37056, F-45369, G-00621, K-38578,
L-11914
COAL CHARACTERISTICS A-05108,
A-09737, A-13219, A-13330, A-17583,
A-48336, F-15723, F-45369
COAL PREPARATION A-08392, A-13330,
A-44028, B-15692, B-28228, B-34465,
B-38832, B-45426, F-45369, 1-36804
COAL TARS A-27900, A-45461, B-04634,
B-06585, B-06650, B-06655, B-06656,
B-13491, B-16642, B-17318, B-23910,
B-26075, B-44156, B-44989, B-46946,
C-08335, C-25030, D-08485, D-47099,
G-05450
COBALT COMPOUNDS B-33382
COLLECTORS A-05005, A-21429,
A-40159, A-41877, A-48279, B-05432,
B-17318, B-21624, B-23136, B-27441,
B-29240, B-29900, B-35284, B-37674,
B-39904, B-39960, B-40232, B-40266,
B-46945, B-47110, G-05450
COLORIMETRY A-22504, C-37217,
D-38895
COLUMN CHROMATOGRAPHY
A-05005, A-44028, D-11015
COMBUSTION A-05005, A-29627,
B-06585, B-28384, B-39751, B-47794,
F-37056, L-11914
COMBUSTION AIR A-05108, B-08178,
B-28384, B-39904, B-40232, F-37056
COMBUSTION GASES A-05005, A-09737,
A-21429, A-22504, A-25214, A-26441,
A-29627, A-30026, A-38526, A-48279,
B-01767, B-08178, B-13718, B-14420,
B-14437, B-15271, B-17318, B-19203,
B-19253, B-23143, B-23911, B-24620,
B-24977, B-25315, B-26075, B-26606,
B-28384, B-29628, B-29900, B-31138,
B-31223, B-34083, B-34465, B-35503,
B-39656, B-39751, B-39904, B-39960,
B-40497, B-44156, B-44989, B-46642,
B-46945, B-46946, B-47110, B-47794,
C-06653, C-24621, C-37217, C-38361,
C-41644, D-21239, F-09930, F-18197,
G-05450, H-45389, 1-26313, K-38578
COMBUSTION PRODUCTS A-05005,
A-09737, A-14286, A-21429, A-22504,
A-25214, A-26441, A-27900, A-29627,
A-30026, A-38526, A-43346, A-48279,
B-01767, B-04634, B-08178, B-13718,
B-14420, B-14437, B-15271, B-17318,
B-19203, B-19253, B-23143, B-23911,
B-24620, B-24977, B-25315. B-26075,
B-26606, B-28384, B-29628. B-29900,
B-31138, B-31223, B-34083, B-34465,
B-35503, B-37343, B-39656, B-39751,
B-39904, B-39960, B-40497, B-44156
B-44989, B-46642, B-46945, B-46946.
B-47110, B-47794, C-06653, C-24621.
C-37217, C-38361, C-41644, D-11015,
D-21239, D-26040, D-38830, F-09930,
F-18197, G-05450, H-45389, 1-26313,
K-38578, L-11914
COMMERCIAL EQUIPMENT B-29900,
G-00621
COMMERCIAL FIRMS B-29900, B-39656,
B-40497. B-43840
COMPRESSED GASES B-34336
COMPRESSION A-28641, B-16157
CONDENSATION A-l 1901, B-06576,
B-26607, B-27441, B-27638, B-35503
CONDENSATION (ATMOSPHERIC)
H-44777
CONSTRUCTION MATERIALS A-05005,
A-08392, A-09737, A-26441, A-29781,
A-36379, A-38657, A-40159, B-29900,
D-38830, G-00621, L-28584
CONTACT PROCESSING B-05432,
B-31123, B-34083, B-34465, L-11914
CONTINUOUS MONITORING A-05005,
A-22504, A-37713, B-40232
CONTROL AGENCIES L-11914
CONTROL EQUIPMENT A-05005,
A-08392, A-l 1901, A-I5455, A-21429,
A-26441, A-27900, A-29627, A-38526,
A-40159, A-40340, A-41877, A-45461,
A-48279, B-02025, B-03204, B-03238,
B-04396, B-04581, B-04634, B-05432,
B-06576, B-06585, B-06650, B-06651,
B-06652, B-06654, B-08183, B-08428,
B-13491, B-16157, B-16260, B-16602,
B-16642, B-I6943, B-17259, B-17318,
B-19203, B-21624, B-21965, B-22503,
B-23136, B-23143, B-23911, B-24977,
B-24998, B-25216, B-26075, B-26606,
B-26607, B-27441, B-27563, B-28228,
B-28532, B-29240, B-29900, B-31223,
B-31682, B-34083, B-34465, B-35284,
B-35503, B-35759, B-37674, B-39656,
B-39751, B-39904, B-39960, B-40232,
B-40266, B-41042, B-41447, B-42024,
B-43752, B-44156, B-44989, B-45658,
B-46642, B-46945, B-47110, C-08335,
D-08485, F-09930, F-16623, G-00621,
G-05450, 1-26313, 1-36804
CONTROL METHODS A-05108, A-08392,
A-l 1901, A-13330, A-17583, A-19209,
A-22504, A-24195, A-28641, A-30026,
A-37713, A-38526, A-38657, A-40340,
A-43346, A-44028, A-46920, A-48279,
A-48336, B-01767, B-02025, B-03204,
B-03238, B-04396, B-04581, B-04634,
B-05432, B-06576, B-06577, B-06585,
B-06654, B-06655, B-06656, B-08178,
B-08183, B-08428, B-14420, B-14437,
B-14779, B-15271, B-15692, B-16157,
B-16260, B-16602, B-16943, B-17318,
B-17680, B-17849, B-19203, B-19308,
B-19733, B-20960, B-21624, B-21965,
B-22503, B-23143, B-23249, B-23910,
B-23911, B-24620, B-24977, B-25216,
B-25315, B-26075, B-28228, B-28384,
B-29217, B-29240, B-29628, B-31123,
B-31138, B-31682, B-31777, B-33382,
B-34081, B-34083, B-34207, B-34336,
B-34421, B-34465, B-35503, B-37343,
B-38832, B-39656, B-39751, B-39904,
B-39960, B-40232, B-40266, B-41042,
B-41447, B-43752, B-43840, B-44156,
B-44989, B-45308, B-45324, B-45426,
B-45688, B-46441, B-46945, B-46946,
B-47110, B-47794, D-29257, D-45231,
F-16623, F-18185, F-18197, F-37056,
F-45369, 1-26313, 1-36804, K-35390,
K-38578, L-11914, L-28584
CONTROL PROGRAMS A-38657,
B-21965, B-40497, K-35390
COOLING A-29627, B-26607, B-28228,
B-35503, B-44989, 1-26313
COOLING TOWERS B-41447
COPPER COMPOUNDS A-26441
CORE OVENS B-13718, B-19733, C-06908,
F-18197
CORONA B-06652, B-29900
CORROSION B-23143, B-24977, B-29900,
B-31138, B-44156, 1-26313, 1-36804
COSTS A-22504, A-26441, A-48279,
B-13718, B-20960, B-23143, B-31138,
B-40232, B-46946
CRITERIA A-14767, A-41877, A-45461
CROPS B-15271
CUPOLAS A-09737, A-26441, A-38526,
B-40232
CYANATES B-34421, B-41447, 1-36804
CYANIDES A-24195, A-25214, A-26314,
B-31777, B-34421, G-05450, 1-36804
CZECHOSLOVAKIA A-13219, A-16125,
A-19209, A-37713, A-46920, B-04396,
B-04581, B-17318, C-25030, D-08485,
D-26040, D-45231, D-47099, H-39571
D
DECISIONS B-40497, L-11914
DECOMPOSITION B-03204, B-19253.
B-23249, B-47794
DEPOSITION A-16125
DESIGN CRITERIA A-17583, A-26441,
A-45461, B-08428, B-14779, B-16260,
B-17259, B-19203, B-21624, B-23911,
B-24998, B-27441, B-28532, B-29240,
B-34083, B-35503, B-37343, B-45658,
B-46642, B-46945, B-46946
DESULFURIZATION OF FUELS
A-08392, A-13330, A-44028, B-05432,
B-06577, B-15692, B-16602, B-19308,
-------
SUBJECT INDEX
51
B-25315, B-28228, B-33382, B-34465,
B-38832, B-45324, B-45426, B-46441,
F-45369, 1-36804, K-38578
DIESEL ENGINES A-05005, A-43346,
B-39656
DIFFUSION D-38830
DIGESTERS A-11901
DIOLEFINS B-03204
DISPERSION B-31223, B-39656, D-38830,
L-28584
DISSOCIATION A-37713
DISTILLATE OILS A-09737, B-31138
DIURNAL D-26040
DOMESTIC HEATING A-05005, A-08392,
A-09737, A-29781, A-36379, A-43346
DONORA A-40340
DROPLETS D-29257
DRYING A-29781, B-29900, C-08335
DUMPS A-09737
DUST FALL C-10671, D-11015, D-21239,
D-26040, D-38830
DUSTS A-05005, A-06582, A-13330,
A-16125, A-19209, A-21429, A-22504,
A-26441, A-36379, A-38657, A-41877,
A-48279, B-02025, B-02728, B-04396,
B-04634, B-06585, B-06655, B-17318,
B-17680, B-20960, B-21624, B-23136,
B-23143, B-26607, B-27441. B-27563,
B-29240, B-29900, B-34081, B-35284,
B-37674, B-39656, B-39904, B-39960,
B-40232, B-40266, B-40497, B-41042,
D-21239, D-26040, D-29257, D-38895,
G-05450, H-45389, L-32517
EDUCATION A-48279
ELECTRIC CHARGE B-35759
ELECTRIC FURNACES A-26441,
A-40340, A-41877, A-48279, B-02728,
B-29900, B-34465, B-39960, B-40232,
B-40266, D-11015
ELECTRIC POWER PRODUCTION
A-05005, A-08392, A-09737, A-26441,
A-29781, A-36379, A-40340, A-43346,
B-17318, B-19733, B-34465, B-39960,
B-40497, D-11015, H-44777, L-28584,
L-32517
ELECTRICAL PROPERTIES A-46920,
B-03204, B-06652, B-29900, B-35759
ELECTRICAL RESISTANCE B-29900
ELECTROCHEMICAL METHODS
A-37713, C-37217
ELECTROCONDUCTIVITY ANALYZERS
A-22504, A-37713
ELECTROLYSIS B-29900
ELECTROSTATIC PRECIPITATORS
A-05005, A-26441, A-40159, A-41877,
B-03204, B-06650, B-06651, B-06652,
B-16157, B-24977, B-25216, B-28228,
B-29900, B-34465, B-35759, B-39656,
B-39904, B-39960, B-40232, B-40266,
B-41447, B-45658
EMISSION INVENTORIES A-09737,
A-26314
EMISSION STANDARDS A-21429,
A-22504, A-38657, B-21624, B-40497,
B-42024, K-35390, K-38578
ENFORCEMENT PROCEDURES B-29628,
L-11914
ENGINE EXHAUSTS A-05005
ENZYMES A-46920, H-39571
EQUIPMENT CRITERIA A-14767
ETHYLENE B-27638, B-44156
EUROPE A-05108, A-06582, A-11901,
A-13219, A-13330, A-14286, A-14767,
A-15455, A-16125, A-17583, A-19209,
A-21429, A-22504, A-252I4, A-25215,
A-26314, A-28641, A-29781, A-30026,
A-36379, A-37713, A-38526, A-38657,
A-43346, A-45461, A-46920, A-48336,
B-01767, B-03204, B-03238, B-04396,
B-04581, B-04634, B-05432, B-06576,
B-06577, B-06585, B-06650, B-06651,
B-06652, B-06654, B-06655, B-06656,
B-08178, B-08183, B-08428, B-13718,
B-14420, B-14437, B-15271, B-16157,
B-16260, B-16602, B-16642, B-16943,
B-17259, B-17318, B-17680, B-17849,
B-17943, B-19253, B-19308, B-21624,
B-22503, B-23136, B-23143, B-23249,
B-23910, B-23911, B-24620, B-24977,
B-24998, B-25216, B-25315, B-26075,
B-27441, B-27563, B-27638, B-28228,
B-28384, B-28532, B-31138, B-31682,
B-31777, B-33382, B-34081, B-34083,
B-34336, B-34421, B-35759, B-37674,
B-38832, B-39751, B-40232, B-40266,
B-41042, B-41447, B-44156, B-44989,
B-45308, B-45324, B-45426, B-45658,
B-45688, B-46441, B-46642, B-46945,
B-46946, B-47794, C-03233, C-06653,
C-06908, C-24621, C-25030, C-29157,
C-37217, C-38361, C-41644, D-08485,
D 21239, D-26040, D-27406, D-29257,
D-35081, D-38895, D-45231, D-47099,
F-09930, F-15723, F-16623, F-18197,
F-37056, F-45369, G-02561, G-05450,
G-08150, H-26418, H-39571, H-45389,
1-26313, 1-36804, K-12277, L-11914,
L-28584, L-32517
EXCESS AIR B-28384
EXHAUST SYSTEMS A-21429, B-04396,
B-23136, B-23143, B-29900, B-37674,
B-40232, B-40266, B-41042, B-47110,
F-09930
EXPERIMENTAL EQUIPMENT B-01767,
B-03204, B-04581, B-04634, B-08183,
B-20960, C-08335
EXPERIMENTAL METHODS B-04396,
B-04581
EXPLOSIONS B-29900
EXPOSURE METHODS H-26418
FANS (BLOWERS) B-04396, B-23136,
B-23143, B-37674, B-40266, B-41042
FEASIBILITY STUDIES B-20960, B-45308
FEDERAL GOVERNMENTS A-38657,
B-21965, B-29628, K-35390, K-38578,
L-32517
FERTILIZER MANUFACTURING
B-16157, B-21965
FERTILIZING A-08392
FIELD TESTS C-41644, D-21239
FILTER FABRICS A-05005, C-08335
FILTERS A-05005, A-08392, A-40159,
A-41877, B-02025, B-13491, B-21624,
B-29900, B-34465, B-35759, B-39656,
B-39904, B-39960, B-40232, B-40266,
C-08335, D-08485, G-0062I, G-05450
FIRING METHODS A-05108, A-17583,
A-19209, A-38526, B-02025, B-04634,
B-08178, B-17680, B-20960, B-23143,
B-28384, B-292I7, B-37343, B-39751,
B-39904, B-40232, B-40266, B-43840,
B-47794, D-45231, F-37056, L-11914
FLARES B-31223, B-40232, B-40266
FLOW RATES A-25214, B-04581,
B-06650, B-06651, B-06652, B-06654,
B-08183, B-24620, B-31682, F-09930
FLOWERS H-26418
FLUID FLOW A-25214, B-04581, B-06650,
B-06651, B-06652, B-06654, B-08183,
B-24620, B-29900, B-31682, F-09930
FLUORANTHENES A-05005, D-08485,
G-00621
FLUORENES D-08485
FLUORIDES A-41877, B-43840
FLUORINE A-38657
FLUORINE COMPOUNDS A-40159,
A-41877, B-43840
FLY ASH A-05108, A-26441, A-37713,
A-46920, B-34465, B-41447, C-10671,
D-27406, D-38895, D-47099, H-39571
FOOD AND FEED OPERATIONS
A-40159
FORMALDEHYDES A-38526
FRACTIONATION A-26314
FRANCE A-36379, B-03238, F-37056
FUEL ADDITIVES A-43346
FUEL CHARGING A-17583, A-19209,
A-38526, B-02025, B-04634, B-20960,
B-29217, B-37343, B-39904, L-11914
FUEL GASES A-05005, A-08392, A-09737,
A-24195, A-29781, A-41877, A-43346,
A-44028, B-05432, B-06577, B-19733,
B-22503, B-23143, B-23249, B-23910,
B-23911, B-24620, B-25315, B-28228,
B-31138, B-34336, B-34465, B-35503,
B-37343, B-40497, B-41447, B-45658,
B-45688, B-46945, B-46946, C-24621,
C-37217, F-18185, F-37056, K-38578,
L-11914
FUEL OIL PREPARATION B-33382,
B-46441
FUEL OILS A-05005, A-09737, A-41877,
A-43346, B-31123, B-31138, B-40497,
B-46441, F-37056, K-38578
FUEL STANDARDS B-40497, K-38578
FUELS A-05005, A-05108, A-06582,
A-08392, A-09737, A-13219, A-13330,
A-14286, A-16125, A-17583, A-19209,
A-21429, A-22504, A-24195, A-25214,
A-25215, A-26314, A-26441, A-27900,
A-29627, A-29781, A-36379, A-37713,
A-38526, A-38657, A-40159, A-40340,
A-41877, A-43346, A-44028, A-46920,
A-48279, A-48336, B-01767, B-02025,
B-02728, B-03204, B-04396, B-04581,
B-04634, B-05432, B-06576, B-06577,
B-06585, B-06650, B-06654. B-06655,
B-06656, B-08178, B-08183, B-14420,
B-14437, B-14779, B-15271, B-15692,
B-16157, B-16260, B-16642, B-16943,
B-17318, B-17680, B-19203, B-19253,
B-19308, B-19733, B-20960, B-21624,
B-21965, B-22503, B-23136, B-23143,
B-23249, B-23910, B-23911, B-24620,
B-24977, B-25216, B-25315, B-26606,
B-26607, B-27441, B-27563, B-27638,
B-28228, B-28384, B-29217, B-29240,
B-29628, B-31123, B-31138, B-31223,
B-31682, B-31777, B-33382, B-34081,
B-34083, B-34207, B-34336, B-34421,
B-34465, B-35284, B-35503, B-35759,
B-37343, B-37674, B-38832, B-39656,
B-39751, B-39904, B-39%0, B-40232,
B-40266, B-40497, B-41042, B-41447,
B-42024, B-43752, B-43840, B-44989,
B-45308, B-45324, B-45426, B-45658,
B-45688, B-46441, B-46945, B-46946,
B-47110, B-47794, C-03233, C-08335,
C-10671, C-24621, C-25030, C-29157,
C-37217, C-38361, C-41644, D-08485,
-------
52
COKE OVENS
D-11015, D
D-29257, D
D-45231, D
F-16623
G-00621
H-39571
1-36804, K-
L-11914, L
FUMES A-214;
A-41877, B
B-39960, B
FURNACES A
A-21429, A
A-40340, A
A-48279, B
B-20960, B
B-27441, B
B-29240, B
B-35759, B
B-39960, B
B-44156, B
C-24621, D
D-27406, D
G-00621, K
-21239, D-26040, D-27406,
-35081, D-38830, D-38895,
-47099, F-09930, F-15723,
-18185, F-37056, F-45369,
-02561, G-08150, H-26418,
:-44777, H-45389, 1-26313,
12277, K-35390, K-38578,
-28584, L-32517
:9, A-27900, A-36379,
-02728, B-34081, B-34465,
40232, B-40266
05005, A-05108, A-09737,
-26441, A-27900, A-38526,
-41877, A-43346, A-45461,
-02728, B-06577, B-19253,
-23143, B-26606, B-26607,
-28228, B-28384, B-29217,
-29900, B-31223, B-34465,
-37343, B 39656, B-39904.
-40232, B-40266, B-40497,
-45308, B-46642, B-47110,
-11015, D-21239, D-26040,
-38895, F-09930, F-37056,
-35390, L-11914, L-28584
G
GAMMA RADIATION C-41644
GAS CHROMATOGRAPHY A-22504,
A-44028, C-24621, C-29157
GAS SAMPLING A-05005
GAS TURBINES A-29781
GASES A-24195, B-01767, B-04634,
B-06585, B-06655, B-23143, 13-25315,
B-28228, B-31123, B-31682, B-34336,
B-35759
GASIFICATION (SYNTHESIS) A-08392,
A-44028, B-28228, B-38832, B-45426,
1-36804
GASOLINES A-05005, A-09737, A-43346,
B-29628
GERMANY A-06582, A-21429, A-22504,
A-29781, A-36379, A-38526, A-38657,
A-45461, B-03204, B-04396, B-06576,
B-06577, B-06585, B-15271, B-16642,
B-19253, B-21624, B-22503, B-27638,
B-28384, B-31138, B-33382, B-37674,
B-38832, B-46441, B-46642, B-47794,
C-03233, C-29157, C-38361, D-26040,
D-38895, F-18197, L-32517
GLASS FABRICS A-05005, C-08335
GOVERNMENTS A-38657, B-21965,
B-29628, B-40497, K-35390, K-38578,
L-11914. L-32517
GRAIN PROCESSING A-40159
GREAT BRITAIN A-17583, A-43346,
B-05432, B-16943, B-17680, B-28228,
B-34081, B-34083, B-38832, B-40232,
B-40266, C-37217, D-29257, L-28584
GROUND LEVEL A-26314, B-31223,
L-28584
H
HALOGEN GASES A-38657
HAZE H-44777
HEAT TRANSFER A-29627, B-26607,
B-27638, B-28228, B-34465, B-35503,
B-39751, B-44989, B-46945, B-46946,
1-26313
HI-VOL SAMPLERS A-05005, D-l 1015,
G-00621
HUMANS G-02561, G-08150
HUMIDITY C-08335
HYDROCARBONS A-05005, A-09737,
A-11901, A-14767, A-16125, A-25214,
A-25215, A-26314, A-27900, A-30026,
A-38657, A-40159, A-41877, A-43346,
A-45461, A-48279, B-03204, B-04581,
B-06577, B-15271, B-16642, B-17943,
B-23143, B-23910, B-24620, B-25216,
B-26075, B-27638, B-31138, B-31682,
B-34421, B-34465, B-35284, B-35503,
B-40266, B-44156, C-24621, C-25030,
C-29157, D-08485, D-11015, D-21239,
D-26040, D-35081, D-45231, D-47099,
G-00621, G-05450, G-08150, 1-26313,
1-36804, L-11914
HYDROCYANIC ACID A-25214 B-05432,
B-27638, B-37343, B-47794, 1-26313
HYDRODESULFURIZATION B-33382
HYDROGEN A-24195, A-37713, B-04634,
B-15692, B-31138, B-34421
HYDROGEN SULFIDE A-14767, A-15455,
A-21429, A-22504, A-25214, A-26314,
A-29627, A-38657, B-01767, B-02728,
B-05432, B-06576, B-08I83, B-16260,
B-16602, B-16943, B-17849, B-20960,
B-22503, B-23143, B-73249. B-23911.
B-24977, B-25315, B-27638, B-31138,
B-31777, B-33382, B-34083, B-34421,
B-35284, B-37343, B-38832, B-39751,
B-39904, B-41447, B-42024, B-44156,
B-46642, B-46945, B-46946, B-47794,
C-38361, D-35081, F-16623,1-26313,
1-36804, L-32517
HYDROGENATION B-16157
HYDROLYSIS H-39571
HYDROXIDES B-15692
HYGROSCOPICTTY C-08335
I
INCINERATION A-05005, A-09737.
A-26441, B-06585, B-08178, B-34465,
B-47110, L-32517
INDIANA A-09737
INDOOR D-38895, D-45231
INDUSTRIAL AREAS B-40497, D-26040,
L-11914
INERTIAL SEPARATION B-39656
INORGANIC ACIDS A-09737, A-15455
A-21429, A-26441, B-05432. B-06654,
B-19733, B-24977, B-29900, B-3408!,
B-34336, B-34465, B-38832, B-39751,
B-41447, B-45426, K-38578
INSPECTION L-28584
INSTRUMENTATION B-14420
INTERNAL COMBUSTION ENGINES
A-05005, A-08392, A-43346, B-39656
INTERNATIONAL B -38832
INVERSION D-38830, L-32517
IODIMETRIC METHODS C-37217,
D-35081
IONS A-37713
IRON A-05005, A-08392, A-09737,
A-38657, A-40159, A-41877, A-45461,
A-48279. B-02728, B-16642, B-26606,
B-29900, B-31123, B-34465, B-39656,
B-39904, B-39960, B-40232, B-40266,
D-11015, D-38830, L-32517
IRON COMPOUNDS B-33382, C-37217
F-18185, F-45369
IRON OXIDES A-41877, B-05432,
B-25315, B-31123, B-40232, B-40266,
C-25030
JAPAN B-15692, B-26607, B-29240,
B-29900, B-31123, B-31223, B-40497,
B-43752, D-11015
K
KANAGAWA PREFECTURE B-40497
KILNS A-08392, A-40159, F-37056
KONIMETERS A-22504
KRAFT PULPING A-26441, B-29628
LABORATORY ANIMALS G-02561
LABORATORY FACILITIES C-08335
LANDFILLS A-09737
LAPSE CONDITION A-40340
LEAD COMPOUNDS A-26441, A-43346,
B-29628
LEAVES H-39571
LEGAL ASPECTS A-36379, A-38657,
A-40340, A-41877, B-21624, B-21965,
B-29628, B-40497, B-42024, B-47110,
K-38578, L-11914, L-28584, L-32517
LEGISLATION A-36379, A-38657,
A-40340, B-21965, B-29628, K-3S578,
L-28584, L-32517
LIGHT RADIATION D-08485, D-38830
LIME A-08392, A-40159
LIQUIDS B-06654, B-06655, B-45426
LOCAL GOVERNMENTS K-38578
LOS ANGELES A-40340
I OWER ATMOSPHERE B-31223
LUBRICANTS D-11015
M
MAGNETOHYDRODYNAMICS (MHD)
A-43346
MAINTENANCE A-38526, B-06576,
B-14420, B-34081. B-40266, B-44156
MALES G-02561
MANGANESE COMPOUNDS B-40232
MATERIALS DETERIORATION B-23136,
B-23143, B-24977, B-29900, B-31138,
B-44156,1-26313,1-36804
MATHEMATICAL ANALYSES A-13330,
B 16260, B-23911, B-31682, F-09930
MATHEMATICAL MODELING B-31682
MAXIMUM ALLOWABLE
CONCENTRATION A-13219,
B-40497, D-26040, D-38895, K-12277,
L-32517
MEASUREMENT METHODS A-05005,
A-22504, A-37713, B-26607, B-39656,
B-40232, C-03233, C-06653, C-06908,
C-10671, C-37117, C-41644, D-38895,
G-08150
MEETINGS B-25216
MEMBRANE FILTERS A-45461, C-08335,
C-25030
MERCURY COMPOUNDS A-14286,
F-45369
METABOLISM H-39571
METAL COMPOUNDS A-14286, A-26441,
A-29781, A-43346, A-45461, B-03238,
B-08183, B-15692, B-16602, B-29628,
B-31777, B-53382, B-34421, B-40232,
B-45308, B-45426, C-25030, C-37217,
F-18185, F-45369
-------
SUBJECT INDEX
53
METAL FABRICATING AND FINISHING
A-08392, A-09737, A-48279, B-31223,
B-39960, B-40497, G-00621, K-12277,
L-32517
METALS A-OS005, A-08392, A-09737,
A-38657, A-40159, A-41877, A-45461,
A-48279, B-02728, B-15271, B-16642,
B-23143, B-26606, B-29900, B-31123,
B-33382, B-34465, B-39656, B-39904,
B-39960, B-40232, B-40266, B-43840,
C-08335, D-11015, D-38830, L-32517
METEOROLOGY A-40340, B-37674,
C-08335, D-38830, H-44777
METHANES B-06577
MEUSE VALLEY D-27406
MICROSCOPY C-10671
MINERAL PROCESSING A-08392,
A-09737, A-26441, A-29781, A-36379,
A-38657, A-40159, A-43346, B-14779,
B-15692, B-19733, B-27563, B-29900,
B-31777, B-34421, B-34465, D-27406,
D-29257, D-38830, L-28584, L-32517
MINING A-43346
MISSOURI A-40340, B-04581
MISTS B-06585, B-34465
MOLYBDENUM COMPOUNDS B-33382
MONITORING A-05005, A-22504,
A-37713, B-39656, B-40232
MONTHLY A-22504, D-38830
MULTIPLE CHAMBER INCINERATORS
A-05005
N
NAPHTHALENES A-11901, A-25214,
A-48279, B-16642, B-23910, B-25216,
B-34421, B-35503, C-29157
NATURAL GAS A-09737, A-29781,
A-41877, A-43346, B-19733, F-37056,
K-38578
NERVOUS SYSTEM G-02561, K-12277
NEW YORK CITY A-40340
NEW YORK STATE A-40340
NICKEL COMPOUNDS B-33382, C-37217
NITRATES C-37217, K-12277
NITRIC OXIDE (NO) B-03204, B-04634,
B-13718, B-15271, B-16157, B-31123,
B-34336, B-35759, B-38832, C-03233,
F-15723, F-18185, F-18197
NITROGEN B-34336, F-15723
NITROGEN DIOXIDE (NO2) B-13718,
B-35759, D-27406, D-38830, F-18197
NITROGEN OXIDES A-09737, A-29627,
A-41877, A-43346, B-03204, B-04634,
B-13718, B-15271, B-16157, B-19253,
B-25216, B-31123, B-34336, B-35759,
B-37343, B-38832, B-39751, C-03233,
D-27406, D-38830, F-15723, F-18185,
F-18197, L-32517
NITROGEN TRIOXIDE (NO3) B-39751
NON-INDUSTRIAL EMISSION SOURCES
A-05005, A-08392, A-09737, A-26441,
A-29627, A-29781, A-36379, A-43346,
B-43840, B-45426, F-09930
NOSTRILS G-08150
NUCLEAR POWER PLANTS A-43346
o
OCCUPATIONAL HEALTH A-45461,
B-47110, C-25030, D-45231, G-02561
ODOR COUNTERACTION B-34465
ODORIMETRY G-08150
ODORS A-41877, B-29628, B-31223,
B-34465, B-39904, G-08150
OIL RESOURCES A-09737
OLEFINS B-03204, B-15271, B-27638,
B-44156
OPEN BURNING A-05005, A-09737
OPEN HEARTH FURNACES A-09737,
A-26441, A-40340, A-41877, A-48279,
B-02728, B-39656, B-39904, B-39960,
B-40232, B-40266, G-00621
OPERATING CRITERIA A-14767,
A-41877
OPERATING VARIABLES A-05108,
A-29627, A-48279, A-48336, B-19203,
B-21624, B-22503, B-23143, B-28384,
B-29900, B-31682, B-31777, B-33382,
B-34083, B-34207, B-39904, B-40232,
B-40266, B-45308, B-46642, B-46945,
B-46946, B-47110, F-16623
ORGANIC ACIDS A-25214, B-05432,
B-27638, B-37343, B-47794, 1-26313
ORGANIC NITROGEN COMPOUNDS
A-11901, A-14767, A-25214, B-31777,
B-34336, B-44156, C-06908
ORGANIC SULFUR COMPOUNDS
A-25215, A-28641, B-05432, B-15692,
B-33382, C-38361, 1-36804
ORSAT ANALYSIS C-06653
OVERFIRE AIR B-40232
OXIDANTS H-44777
OXIDATION A-48336, B-13718, B-35759,
1-36804
OXIDES A-06582, A-09737, A-21429,
A-22504, A-26441, A-29627, A-36379,
A-37713, A-38526, A-38657, A-40159,
A-41877, A-43346, B-02728, B-03204,
B-04634, B-05432, B-06577, B-13718,
B-15271, B-16157, B-17259, B-19253,
B-23143, B-25216, B-25315, B-27638,
B-28384, B-31123, B-33382, B-34336,
B-34465, B-35284, B-35759, B-37343,
B-38832, B-39656, B-39751, B-39904,
B-40232, B-40266, B-40497, B-41042,
B-44156, B-45426, C-03233, C-06653,
C-25030, C-29157, D-27406, D-38830,
F-15723, F-18185, F-18197, G-05450,
H-26418, H-44777, K-38578, L-32517
OXYGEN B-04634, B-06652, B-28384,
C-06653
OZONE B-35759
PACKED TOWERS B-08428, B-24998,
B-46642
PAPER CHROMATOGRAPHY D-1 PI 5
PAPER MANUFACTURING A-26441,
A-40159, B-19733, B-21965
PARIS B-03238
PARTICLE COUNTERS A-22504
PARTICLE SHAPE D-27406
PARTICLE SIZE A-16125, B-25315,
B-29900, B-45324, C-10671, C-25030,
D-27406, F-45369
PARTICULATE CLASSIFIERS A-16125,
B-25315, B-29900, B-45324, C-10671,
C-25030, D-27406, F-45369, G-00621
PARTICULATE SAMPLING B-04396,
B-21624, D-08485
PARTICULATES A-05005, A-05108,
A-06582, A-09737, A-13330, A-16125,
A-17583, A-19209, A-21429, A-22504,
A-26441, A-27900, A-36379, A-37713,
A-38657, A-40159, A-40340, A-41877,
A-43346, A-46920, A-48279, A-48336,
B-0202' B-02728, B-04396, B-04634,
B-06583 06655, B-06656, B-08428,
B-14779, B-,, U, B-17318, B-17680,
B-19203, B-20960, B-21624, B-23136,
B-23143, B-26607, B-27441, B-27563,
B-28228, B-29240, B-29900, B-31223,
B-34081, B-34465, B-35284, B-37343,
B-37674, B-39656, B-39904, B-39960,
B-40232, B-40266, B-40497, B-41042,
B-41447, B-44989, C-10671, C-29157,
D-11015, D-21239, D-26040, D-27406,
D-29257, D-38830, D-38895, D-47099,
G-00621, G-02561, G-05450, H-26418,
H-39571, H-45389, L-32517
PENELEC (CONTACT PROCESS)
B-34083, B-34465
PENNSYLVANIA A-40340
PERMITS L-32517
PEROXIDES A-37713
PERSONNEL A-48279, B-47110
PERYLENES D-08485
PETROLEUM PRODUCTION A-09737,
A-26314, A-26441, A-40159, A-43346,
B-19733, B-21965, B-31138
PETROLEUM REFINING A-05005,
A-09737, A-26441, A-36379, A-38526,
A-40159, B-17943, B-19733, B-21965,
B-29628, B-31223, B-40497, C-37217,
D-35081, K-38578, L-11914
PHENANTHRENES G-00621
PHENOLS A-11901, A-14767, A-25214,
A-26314, B-17849, B-24998, B-37343,
G-08150, H-45389
PHENYL COMPOUNDS G-08150
PHOSPHATES B-43752, B-47794
PHOSPHORUS COMPOUNDS A-26441,
B-43752, B-47794
PHOTOGRAPHIC METHODS H-44777
PHOTOMETRIC METHODS C 03233,
C-37217, D-38895
PHOTOSYNTHESIS H-39571
PHYSICAL STATES A-11901, A-24195,
B-01767, B-04634, B-06585, B-06654,
B-06655, B-19253, B-23143, B-25315,
B-26607, B-28228, B-31123, B-31682,
B-34336, B-35759, B-45426, B-46642
PILOT PLANTS A-44028, B-05432,
B-24620, B-29217, B-31138, B-35759,
B-46945
PINTO BEANS H-39571
PITTSBURGH A-40340
PLANS AND PROGRAMS A-09737,
A-36379, A-38657, B-21965, B-40497,
K-35390, L-11914
PLANT DAMAGE H-26418, H-44777,
H-45389
PLANT GROWTH H-26418, H-39571,
H-45389
PLANTS (BOTANY) A-46920, B-15271,
H-26418, H-39571, H-45389
PLATINUM B-15271, B-33382
POLAROGRAPHIC METHODS C-37217
POLLUTION PRECURSORS B- j8
POLYMERIZATION B-13718
POLYNUCLEAR COMPOUNDS A-05005,
A-11901, A-16125, A-25214, A-27900,
A-38657, A-41877, A-45461, A-48279,
B-16642, B-23910, B-25216, B-26075,
B-34421, B-35503, C-25030, C-29157,
D-08485, D-11015, D-21239, D-26040,
D-45231, D-47099, G-00621, G-05450,
L-11914
POTASSIUM COMPOUNDS A-29781,
B-15692, C-37217
POTENTIOMETRIC METHODS A-37713
POWER SOURCES A-05005, A-08392,
A-29781, A-43346, B-39656
PRESSURE B-04581, B-04634, B-06650,
B-06651, B-06654, B-16157, B-23249,
-------
54
COKE OVENS
B-33382, B-37343, F-09930, F-18197,
1-36804
PRIMARY METALLURGICAL
PROCESSING A-05005, A-08392,
A-09737, A-15455, A-19209, A-26441,
A-36379, A-38657, A-40159, A-40340,
A-41877, A-45461, A-48279, B-02728,
B-16642, B-19733, B-26606, B-29900,
B-31223, B-34465, B-39656, B-39904,
B-39960, B-40232, B-40266, B-42024,
B-43840, B-46945, B-46946, B-47110,
D-11015, D-27406, D-38830, K-38578,
L-28584, L-32517
PROCESS MODIFICATION A-05108,
A-17583, A-19209, A-38526, A-48336,
B-02025, B-04396, B-04634, B-06655,
B-06656, B-08178, B-14420, B-14437,
B-14779, B-17680, B-19203, B-20960,
B-21624, B-23143, B-28384, B-29217,
B-34081, B-34465, B-37343, B-39751,
B-39904, B-40232, B-40266, B-43840,
B-44989, B-47794, D-45231, F-37056,
L-11914
PROFANES B-34465
PROTECTIVE MASKS A-27900, A-45461,
B-47110
PULSE RATE G-02561
PULVERIZED FUELS B-35284
PYRENES A-05005, A-16125, A-38657,
B-34421, C-25030, D-08485, D-11015,
D-21239, D-26040, D-45231, D-47099,
G-00621, G-05450, L-11914
PYRIDINES A-11901, A-14767, A-25214,
C-06908
PYROLYSIS A-48336, L-11914
Q
QUENCHING A-21429, A-41877, B-19203,
B-20960, B-21624, B-26607, B-37343,
B-37674, B-41042, B-44989
R
RADIATION MEASURING SYSTEMS
C-41644
RADIOACTIVE RADIATION A 46920,
C-41644
RADIOGRAPHY C-41644
RAPPING B-40266
REACTION KINETICS B-08183, B-16260,
B-17849, B-23249, B-31777, B-34336,
F-16623
REACTION MECHANISMS B-31777.
B-34336, F-15723
RECORDING METHODS H-44777
REDUCTION A-26441
REGIONAL GOVERNMENTS B-29628,
B-40497
REGULATIONS A-40340, A-41877,
B-21624, B-42024, B-47110, K-38578,
L-32517
RESEARCH METHODOLOGIES A-08392
RESEARCH PROGRAMS A-36379,
A-45461, B-21965, B-39904, F-37056
RESIDENTIAL AREAS D-26040
RESIDUAL OILS A-09737
RESPIRATORY DISEASES G-02561,
G-05450
RESPIRATORY FUNCTIONS A 16125,
G-02561
RESPIRATORY SYSTEM C-08150,
K-12277
RUBBER MANUFACTURING A-40340
SAFETY EQUIPMENT A-45461, B-06652,
G-02561
SAMPLERS A-05005, A-45461, B-04396,
B-06585, C-08335, C-25030, D-08485,
D-11015, G-00621, L-11914
SAMPLING METHODS A-05005, A-27900,
A-44028, A-45461, B-04396, B-06585,
B-21624, C-08335, C-25030, D-08485,
D-11015, G-00621, L-11914
SCATTERING (ATMOSPHERIC) L-11914
SCREEN FILTERS B-02025, B-21624
SCRUBBERS A-05005, A-11901, A-15455,
A-21429, A-29627, A-38526, A-40159,
A-41877, A-48279, B-02025, B-03238,
B-04396, B-04581, B-04634, B-06576,
B-06585, B-06654, B-08183, B-08428,
B-16602, B-16642, B-16943, B-19203,
B-22503, B-23911, B-24998, B-26075,
B-26606, B-26607, B-27563, B-28228,
B-28532, B-29900, B-31682, B-34083,
B-34465, B-35284, B-35503, B-37674,
B-39656, B-39904, B-39960, B-40232,
B-40266, B-41042, B-43752, B-46642,
B-46945, B-47110, F-16623, 1-26313
SEALS B-05432
SEASONAL D-11015, G-00621
SEDIMENTATION B-39656
SETTLING CHAMBERS B-23136, B-29900
SETTLING PARTICLES A-05005,
A-06582, A-13330, A-16125, A-19209,
A-21429, A-22504, A-26441, A-36379,
A-38657, A-41877, A-48279, B-02025,
B-02728, B-04396, B-04634, B-06585,
B-06655, B-08428, B-16642, B-17318,
B-17680, B-20960, B-21624, B-23136,
B-23143, B-26607, B-27441, B-27563,
B-29240, B-29900, B-34081, B-35284,
B-37674, B-39656, B-39904, B-39960,
B-40232, B-40266, B-40497, B-41042,
C-10671, C-29157, D-11015, D-21239,
D-26040, D-27406, D-29257, D-38895,
G-05450, H-45389, L-32517
SEWAGE B-43840, B-45426
SHIPS A-08392, A-43346
SILICON COMPOUNDS B-40232
SILICON DIOXIDE C-25030
SILVER COMPOUNDS A-45461, C-25030
SIMULATION B-04581, B-06650
SINGLE CHAMBER INCINERATORS
A-05005
SINTERING A-09737, A-38657, A-41877,
A-48279, B-29900, B-39656, B-39904,
B-39960, B-40266, B-40497, D-11015
SLUDGE B-45426
SMOG A-40340
SMOKES A-05005, A-17583, A-43346,
A-48336, B-02025, B-04634, B-06656,
B-14779, B-17680, B-20960, B-23143,
B-34081, B-34465, B-37343, B-40266,
B-44989, G-05450, H-26418
SOCIO-ECONOMIC FACTORS A-29781,
A-40340
SODIUM CARBONATE B-03238, B-16602
SODIUM COMPOUNDS B-03238,
B-08183, B-15692, B-16602, B-34421,
B-45426
SODIUM HYDROXIDE B-15692
SOLAR RADIATION D-08485, D-38830
SOLID WASTE DISPOSAL A-05005,
A-09737, A-26441, B-43840, B-45426
SOLVENTS A-26314
SOOT A-36379, B-16642, C-29157,
D-26040, D-27406
SOOT FALL D-26040
SOURCE SAMPLING A-45461
SO2 REMOVAL (COMBUSTION
PRODUCTS) A-38657, B-17318,
B-17849, B-23249, B-24977, B-29628,
B-34083, B-34465, K-38578
SPARK IGNITION ENGINES A-05005,
A-08392
SPECTROMETRY A-05005
SPECTROPHOTOMETRY A-21429,
A-41877, B-19203, B-20960, B-21624,
B-24620, B-26607, B-37343, B-37674,
B-41042, B-44989, C-08335, C-37217,
D-11015, D-35081, G-00621, L-11914
SPRAY TOWERS A-05005, B-02025,
B-26607, B-27563, B-28532, B-40232,
B-40266, B-46945, F-16623
SPRAYS B-08428
ST LOUIS A-40340, B-04581
STABILITY (ATMOSPHERIC) A-40340,
D-38830, L-32517
STACK GASES A-21429, A-22504,
A-25214, A-29627, A-30026, A-38526,
A-48279, B-15271, B-23143, B-24620,
B-26075, B-26606, B-29628, B-31223,
B-34083, B-34465, B-39656, B-39751,
B-39904, B-39960, B-40497, B-44156,
B-44989, B-46945, B-46946, B-47110,
B-47794, C-37217, C-38361, C-41644,
H-45389, 1-26313, K-38578
STACK SAMPLING A-45461
STACKS A-19209, A-25214, B-06577,
B-21624, B-31223, B-39656, B-40266,
F-09930, L-28584
STAGNATION D-38830
STANDARDS A-13219, A-21429, A-22504,
A-38657, B-21624, B-40497. B-42024,
D-26040, D-38895, K-12277, K-35390,
K-38578, L-32517
STATE GOVERNMENTS B-21965,
K-38578, L-32517
STATISTICAL ANALYSES A-14286
STEAM B-06655, B-23143, B-26607
STEAM PLANTS A-08392, A-09737
STEEL A-05005, A-08392, A-09737,
A-40159, A-41877, A-45461, A-48279,
B-02728, B-16642, B-26606. B-29900,
B-34465, B-39656, B-39904, B-39960,
B-40232, B-40266, D-11015, D-38830,
L-32517
SULFATES B-03238, B-23143, B-23249,
B-34083, B-34336, B-41447, B-47794,
C-37217, 1-36804
SULFIDES A-14767, A-15455, A-21429,
A-22504, A-25214, A-25215 A-26314,
A-29627, A-38657, B-01767, B-02728,
B-05432, B-06576, B-08183, B-16260,
B-16602, B-16943, B-17849, B-20960,
B-22503, B-23143, B-23249, B-23911,
B-24977, B-25315, B-27638, B-31138,
B-31777, B-33382, B-34083, B-34421,
B-35284, B-37343, B-38832, B-39751,
B-39904, B-41447, B-42024, B-44156,
B-46642, B-46945, B-46946, B-47794,
C-24621, C-37217, C-38361, D-35081,
F-16623, F-18185, 1-26313, 1-36804,
L-32517
SULFUR COMPOUNDS A-14767,
A-15455, A-21429, A-22504, A-25214,
A-25215, A-26314, A-29627, A-38657,
A-41877, B-01767 B-02728 B-03238,
B-05432, B-06576, B-08183. B-15692,
B-16260, B-16602 B-16943. B-17849,
B-19733, B-20960. B-22503, B-23143,
B-23249, B-23911, B-24977, B-25315,
B-27638, B-31138, B-31777, B-33382,
B-34083, B-34207. B-34336, B-34421,
B-35284, B-37343. B-38832, B-39751,
B-39904, B-41042, B-41447 B-42024,
-------
SUBJECT INDEX
55
.,-44156, B-45308, B-45426, B-46642,
B-46945, B-46946, B-47794, C-24621,
C-37217, C-38361, C-41644, D-35081,
F-16623, F-18185, H-45389, 1-26313,
1-36804, K-38578, L-32517
SULFUR DIOXIDE A-06582, A-21429,
A-22504, A-36379, A-38657, A-40159,
B-02728, B-05432, B-06577, B-23143,
B-34465, B-35284, B-37343, B-40266,
D-27406, D-38830, H-26418, H-44777,
L-32517
SULFUR OXIDES A-06582, A-09737,
A-21429, A-22504, A-26441, A-36379,
A-38657, A-40159, A-41877, A-43346,
B-02728, B-05432, B-06577, B-23143,
B-34465, B-35284, B-37343, B-39656,
B-39751, B-39904, B-40266, B-40497,
D-27406, D-38830, H-26418, H-44777,
K-38578, L-32517
SULFUR OXIDES CONTROL A-08392,
A-13330, A-19209, A-24195, A-38657.
A-44028, B-05432, B-06577, B-15692,
B-16602, B-17318, B-17849, B-19308,
B-19733, B-23249, B-24977, B-25315,
B-28228, B-29628, B-31777, B-33382,
B-34083, B-34465, B-37343, B-38832,
B-45308, B-45324, B-45426, B-46441,
F-45369, 1-36804, K-38578
SULFUR TRIOXIDE A-21429, B-39751
SULFURIC ACID A-09737, A-15455,
A-21429, A-26441, B-05432, B-06654,
B-19733, B-24977, B-29900, B-34083,
B-34336, B-34465, B-39751, B-41447,
B-45426, K-38578
SURFACE COATING OPERATIONS
A-08392, B-34465, G-00621
SURFACE COATINGS B-44156
SUSPENDED PARTICULATES A-05005,
A-05108, A-17583, A-21429, A-26441,
A-27900, A-36379, A-37713, A-40340,
A-41877, A-43346, A-46920, A-48336,
B-02025, B-02728, B-04634, B-06585,
B-06656, B-14779, B-17680, B-20960,
B-23143, B-34081, B-34465, B-37343,
B-39960, B-40232, B-40266, B-41447,
B-44989, C-10671, D-11015, D-27406,
D-29257, D-38830, D-38895, D-47099,
G-05450, H-26418, H-39571
SWEDEN B-01767, B-04581
TAR A-38657, A-48279, B-34465, B-35284,
B-35503, B-37343, B-45426, B-45658,
B-46441, D-45231, G-08150
TEMPERATURE A-28641, A-29627,
A-30026, A-37713, B-08183, B-15692,
B-16602, B-19308, B-23249, B-25315,
B-28384, B-31138, B-39751, B-40266,
B-45308, B-45324, B-46642, B-46945,
B-46946
TEMPERATURE (ATMOSPHERIC)
A-40340
TESTING FACILITIES C-08335
THERMAL RADIATION B-46946
THIOPHENE A-25215, B-05432
THRESHOLDS A-45461, G-08150,
K-12277
TOLUENES A-25215, B-24620, C-24621,
D-35081
TOPOGRAPHIC INTERACTIONS
A-36379, D-38830
TOXIC TOLERANCES H-45389
TOXICITY A-46920
TRAINS A-08392, A-43346, B-39656
TRANSPORTATION A-05005, A-08392,
A-09737, A-29781, A-36379, A-43346,
B-29628, B-39656
TRAPPING (SAMPLING) A-05005
TREATED FABRICS C-08335
TREATMENT AND AIDS C-41644
TREES H-45389
TRUCKS A-05005
TURBIDIMETRY A-22504
TYNDALLOMETER A-22504
U
ULTRAVIOLET SPECTROMETRY
A-05005
UNDERFIRE AIR A-05108
UNITED STATES A-05108, A-40159,
A-40340, A-45461, B-15271, B-38832,
K-35390
URBAN AREAS A-09737, A-36379,
A-40340, B-40497, D-26040, D-38830,
L-11914
USSR A-l 1901, A-13330, A-14286,
A-14767, A-15455, A-25214, A-25215,
A-26314, A-28641, A-30026, A-48336,
B-03238, B-04581, B-04634, B-06650,
B-06651, B-06652, B-06654, B-06655,
B-06656, B-08178, B-08183, B-08428,
B-13718, B-14420, B-14437, B-16157,
B-16260, B-16602, B-17259, B-17849,
B-17943, B-19308, B-23136, B-23143,
B-23249, B-23910, B-23911, B-24620,
B-24977,
B-26075,
B-31777,
B-38832,
B-44156,
B-45658,
C-06908,
D-35081,
F-45369,
H-26418,
K-12277,
B-24998,
B-27563,
B-34336,
B-39751,
B-45308,
B-46945,
C-24621,
F-09930,
G-02561,
H-45389,
L-11914
B-25216,
B-28532,
B-34421,
B-41042,
B-45324,
B-46946,
C-41644,
F-15723,
G-05450,
1-26313,
B-25315,
B-31682,
B-35759,
B-41447,
B-45426,
C-06653,
D-21239,
F-16623,
G-08150,
1-36804,
VAPOR PRESSURE A-l 1901, B-17943,
B-29900
VAPOR RECOVERY SYSTEMS A-11901,
1-36804
VAPORS A-11901, B-06655, B-19253,
B-23143, B-26607, B-28228, B-46642
VEGETABLES H-39571
VEHICLES A-05005, A-08392, A-09737,
A-36379, A-43346, B-39656
VENTILATION A-11901, B-23143,
B-39960, B-41042, B-47110
VENTILATION (PULMONARY) G-02561
VENTURI SCRUBBERS A-41877,
B-04396, B-06654, B-16642, B-19203,
B-26606, B-29900, B-40232
VOLATILITY A-11901, A-27900, B-17943,
C-25030
VOLTAGE B-03204, B-06652, B-29900,
B-35759
w
WATER B-06654, B-06655
WATER POLLUTION A-29627, B-43840
WET CYCLONES B-37674
WETTING B-08428, B-34465
WINDS A-40340, B-37674, D-38830
WOOD B-03238, B-34465
X
XYLENES A-25215, B-24620, B-34421,
C-24621, D-35081
YOKOHAMA B-40497
z
-------
-------
TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing)
1. REPORT NO.
EPA-450/1-74-002
3. RECIPIENT'S ACCESSION1 NO.
4. TITLE AND SUBTITLE
AIR POLLUTION ASPECTS OF EMISSION
SOURCES: Coke Ovens
A Bibliography with Abstracts .
5. REPORT DATE
March 1974
6. PERFORMING ORGANIZATION CODE
7 AUTHOR(S)
8. PERFORMING ORGANIZATION REPORT NO.
9. PERFORMING ORGANIZATION NAME AND ADDRESS
10. PROGRAM ELEMENT NO.
Office of Air Quality Planning and Standards
Control Programs Development Division
11. CONTRACT/GRANT NO.
12. SPONSORING AGENCY NAME AND ADDRESS
13. TYPE OF REPORT AND PERIOD COVERED
Office of Air Quality Planning and Standards
Control Programs Development Division
National Environmental Research Center
14. SPONSORING AGENCY CODE
Ti-M'angla
KI
?77ll
15. SUPPLEMENTARY NOTES
16. ABSTRACT
Bibliography contains abstracts of the available literature pertinent to
emission sources associated with coke ovens, the effects of those
emi.'t'j^ons on man and his environment, and feasible technology for
their control.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.lDENTIFIERS/OPEN ENDED TERMS C. COSATI Field/Group
13. DISTRIBUTION STATEMENT
Release unlimited
19. SECURITY CLASS (ThisReport)
None
21. NO. OF PAGES
60
20. SECURITY CLASS (This page)
None
22. PRICE
EPA Form 2220-1 (9-73)
-------
-------
-------
-------
-------
O
O -
-o n
§ *
-t 01
c c
z «
^ 2
« 5
m «"
i
rn
3> 2
« <
S -1=3
S 20
3 og-g
3" 3 3 3
ID c r-
«^?3
2 9 n
•" ?. ~<
n5?£
-3I>
~J §. O
-J J m
± 2
n
X1
rv
-a
^ J
•S-
°^
0)
tU CD
Q. —
a. _
C/l Li.
D °
to z
(T) ,-.
a. U
a> -H
•Z: °
a. to
_ n
o ai
CD -
i
f C
S w>
m —
-«r
J> m
CO
O ri
z
Z
O
------- |