United States
Environmental Protection
Agency
Office of Air Quality
Planning and Standards
Research Triangle Park NC 27711
EPA-450/3-91-023
September 1992
Air
PBR3-1.
&EPA
Carbon Disulfide Emission
Control Options
control
technology center
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EPA-450/3-91-023
Carbon Disulfide Emission Control Options
CONTROL TECHNOLOGY CENTER
Sponsored by
Emission Standards Division
Office of Air Quality Planning and Standards
U.S. Environmental Protection Agency
Research Triangle Park, NC 27711
Air and Energy Engineering Research Laboratory
Office of Research and Development
U.S. Environmental Protection Agency
Research Triangle Park, NC 27711
U.S. Environmental Protection Agency
Region 5, Library (PL-12J)
77 West Jackson Boulevard, 12th Floor
September 1992 ChiCa8°' IL 60604-3590
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EPA-450/3-91-023
September 1992
Carbon Disulfide Emission Control Options
by
R. Gupta, L. Harris, and D. Tulis
TRC Environmental Corporation
100 Europa Drive
Suite 150
Chapel Hill, NC 27514
EPA Prime Contract 68D00121
Work Assignment Number 1-62
Project Manager
Deborah Elmore
Emission Standards Division
Office of Air Quality Planning and Standards (OAQPS)
U.S. Environmental Protection Agency
Research Triangle Park, NC 27711
Prepared for:
Control Technology Center
U.S. Environmental Protection Agency
Research Triangle Park, North Carolina 27711
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DISCLAIMER
This report has been reviewed by the Control Technology Center (CTC) established by
the Office of Research and Development (ORD) and Office of Air Quality Planning and
Standards (OAQPS) of the U.S. Environmental Protection Agency (EPA), and has been approved
for publication. Approval does not signify that the comments necessarily reflect the views and
policies of the EPA, nor does mention of trade names or commercial products constitute
endorsement or recommendation for use. This document was not prepared in support of any
rulemaking effort.
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ACKNOWLEDGEMENTS
This report on emissions control options for carbon disulfide was prepared for Ms.
D. Elmore of EPA's Control Technology Center (CTC) by R. Gupta, L. Harris, B. ScheU, and
D. Tulis of TRC Environmental Corporation (TRC), Chapel Hill, NC. Assisting in the project
were J. Durham of the EPA, B. Blaszczak of the CTC, and S. Samuels of TRC. The authors
would like to thank the many individuals who supplied the information necessary to make this
report possible. These include the individuals at the EPA library who ran the Chemical Abstracts
(CA) literature search; F. Vollero of Procedaire Industries; J. Jacox of Nucon International Inc.;
M. Macintosh of Argonne National Laboratory; R. Hagen of Akzo Chemicals; C.D. Cannon and
associates at BASF; T. Moore of Texaco Chemical Company; and R. Rafson of Quad
Environmental Technologies Corporation.
ui
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PREFACE
This project was funded by EPA's Control Technology Center (CTC) and prepared by
TRC Environmental Corporation (TRC).
The CTC was established by EPA's Office of Research and Development (ORD) and
Office of Air Quality Planning and Standards (OAQPS) to provide technical assistance to State
and local air pollution control agencies. Several levels of assistance can be accessed through the
CTC. First, a CTC Hotline has been established to provide telephone assistance on matters
relating to air pollution control technologies. Second, more in-depth engineering assistance can
be provided when appropriate. Third, the CTC can provide technical guidance through designing
technical guidance documents, developing personal computer software, and presenting workshops
on control technology matters. The CTC is also the focal point of the Federal Small Business
Assistance Program, and maintains the Reasonably Available Control Technology/Best Available
Control Technology/Lowest Achievable Emission Rate (RACT/B ACT/LAER) Clearinghouse and
the Global Greenhouse Gases Technology Transfer Center. Information concerning all CTC
products and services can be accessed through the CTC Bulletin Board System (BBS), which is
part of the OAQPS Technology Transfer Network (TTN) bulletin board system.
The technical guidance projects, such as this one, focus on topics of national or regional
interest and are identified through contact with State and local agencies or private organizations.
In this case, the CTC Hotline was accessed by numerous agencies seeking information on
controlling carbon disulfide emissions. The interest in this topic warranted development of a
technical document on carbon disulfide emissions control options. This document briefly
discusses various options available to public and private industry for controlling carbon disulfide
emissions, and serves as a reference source for those seeking further information.
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TABLE OF CONTENTS
Section Page
DISCLAIMER [[[ ii
ACKNOWLEDGEMENTS ............................................ ft
PREFACE [[[ iv
LIST OF FIGURES
v
1.0 INTRODUCTION
1.1 Purpose of Report
1.2 Project Methodology
2.0 CARBON DISULFIDE: BACKGROUND INFORMATION ................ 3
2.1 Physical Properties ....................................... 3
2.2 Chemical Properties ....................................... 4
2.3 Production and End-Uses ................................... 4
2.4 Health Effects Summary ................................. [\ 5
f f
3.0 EMISSION SOURCES FOR CARBON DISULFIDE .................... 7
3. 1 Viscose Process ......................................... 7
3.2 Carbon Tetrachloride Production .............................. 9
3.3 Other Processes ......................................... 10
4.0 CONTROL TECHNIQUES ...................................... 12
4.1 Absorption .................................... p
4.1.1 Method 1: Oil Absorption ............................. 12
4.1.2 Method 2: International Patent No. WO 86/02283 ........... 13
4.1.3 Method 3: Diglycolamine Agent ........................ 16
4.1.4 Conclusions ................................... 16
4.2 Adsorption .................................. 17
4.2.1 Method 1: Activated Carbon ....................... 17
4.2.2 Method 2: Synthesized Sorbent: European Patent EP 189606 .... 20
4.2.3 Conclusions ................................ 21
4.3 Ventilation and Condensation Recovery System .............. i\
4.4 Absorption/Oxidation: U.S. Patent 4,049,775 ................... ' . 24
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TABLE OF CONTENTS (continued)
Section „
Page
4.7 Control with a Bioreactor -71
4.8 Wet Scrubbing '.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'.'. 31
4.9 Current Research [[ 33
REFERENCES „,
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LIST OF FIGURES
Number Page
1. Viscose Process g
2. Oil Absorption System \\
3. Carbon Tetrachloride Production 14
4. Adsorption Recovery System 19
5. Ventilation and Recovery System 22
6. BASF Carbon Disulfide Recovery System 23
7. Wet Method of Carbon Disulfide Control 25
8. Thermal Oxidation System 28
9. Catalytic Conversion 30
10. Control With a Bioreactor 32
11. Wet Scrubbing • 34
vu
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CARBON BISULFIDE CONTROL OPTIONS
1.0 INTRODUCTION
1.1 Purpose of Report
The EPA Control Technology Center (CTC) has received a number of inquiries regarding
control options for carbon disulfide emissions. This report presents a description of methods or
techniques to control carbon disulfide emissions from a variety of source categories (Section 4.0).
The control techniques presented represent potential control options, as many of them have not
yet been proven in an industrial environment. The report also contains background information
on carbon disulfide (Section 2.0) and a discussion of carbon disulfide emission source categories
(Section 3.0).
1.2 Project Methodology
The project was initiated by a comprehensive literature search involving several computer
databases (i.e., Chemical Abstracts, PTS-Prompt, Chemical Economics Handbook, Kirk-Othmer).
The computer search provided information primarily on foreign applications by locating patents
related to control of carbon disulfide emissions. The reader should be aware that these patents
may represent carbon disulfide emissions control options that are still in research or experimental
stages. The computer search was also able to provide some information on domestic
applications; however, the bulk of the information for domestic applications came from
discussions with vendors and plant operators.
Vendors were able to supply substantial information on equipment and solvents that they
felt may be used as control options.' Industry, however, was very conservative with information
about their process conditions and particular control configurations. It should be noted that any
information ootamed from plant operators may not be complete to the extent ot supplying
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technical process descriptions/diagrams. The Chemical Manufacturer's Association (CMA)
provided significant information for this document
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2.0 CARBON BISULFIDE: BACKGROUND INFORMATION
The following four subsections outline the physical/chemical properties of carbon
disulfide, current production information and trends, major end-uses of carbon disulfide, and
health effects of carbon disulfide exposure.
2.1 Physical Properties
Carbon disulfide is a clear and colorless liquid with a mild ethereal odor; however, minor
impurities impart a disagreeable sulfurous odor. It is slightly soluble in water and an excellent
solvent for many organic compounds. The physical properties are listed below (1,2,3).
PROPERTY
latent heat of fusion kJ/kg
boiling pt at 101kPa,°C
flash point at 101kPa,*C
ignition temp in air, *C
10-s kg tune
0.5 -s lag time
critical temp, "C
critical density, kg/m3
critical pressure, k/Pa
Liquid at temp, "C
density, kg/in3
specific heat, Jfkgxk)
latent heat of vap kj/kg
surface tension, mN/m3
thermal conductivity, W/mxK
viscosity, mPaxs
refractive index
soly in HjO, g/kg sol'n
vapor pressure kPa
Gas at temp, °C
density, kg/m3
specific heat. JfkgxK)
viscosity, mPaxs
thermal conductivity, WYrnxK
0(32"F)
1293 (98.1 Ib/ft3)
984
377 (33634 caWb)
35.3 (35.3 dynes/cm)
0.429
1.6436
2.42
16.97 (0.17 atm)
4(5.25 (114.8°F)
2.97(0. 19 Ib/ft3)
611
0.0111
0.0073
1 hermocnemical data at 298 K (77°F)
heat capacity, Cp, J(mokK)
sntropy, S, J(mokK)
neat 01 formation. Hf. kJ/mol
~ ""•"' " "' -• i-"^— •— • __B^ _.. ~^-____
VALUE ~]
161.11 (-169.7'F)
57.7 (5148 cal/lb)
46.25 (114.8*F)
-30 (-22-F)
80-120 (176-248'F)
156 (31Z8'F)
273 (523.4'F)
378 (28.7 Ib/fO
7700 (76 atm)
20(68T)
1263 (95.8 Ib/ft3)
1005
368 (32832 caWb)
32.3 (32.3 dynes/cm)
0.161
0.367
1 6276
2.10
39.66 (0.39 atm)
200 (392°F)
1.96 (0.12 Ib/ft3}
(V7Q
0.0164
46JS (114.8°F)
1224 (9Z9 Ib/ft3)
i fyin
355(31671 cal/lb)
28.5 (28.5 dynes/cm)
0305
048
101.33 (1.00 atm)
400 (752°F)
1.37 (0.09 Ib/ft3)
730
0.0234
45.48
237 8
117.1 (27,988 cal/mol)
free energy of formation, W/moi ™ '15'989 «"""»
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Carbon disulfide is soluble in most organic solvents and completely miscible with many liquid
hydrocarbons, chlorinated hydrocarbons, and alcohols.
2.2 Chemical Properties
Carbon disulfide is highly flammable and is easily ignited by sparks or hot surfaces.
Greater availability of oxygen or lower pressure may cause a considerable lowering of the flash
point temperature. The flammability or explosive range of carbon disulfide with air is very wide
and depends upon the conditions. Concentrations of 4 to 8 percent carbon disulfide in air
explode with maximum violence. The upper explosive limit (UEL) and lower explosive limit
(LEL) for carbon disulfide in air are 50 percent and 1 percent, respectively (4). In practice, for
safety reasons control equipment must be designed to operate above the UEL or below the LEL.
The thermal energy released in carbon disulfide explosions is low compared to that from other
flammable substances. The maximum absolute pressure developed is reported as 739 kPa (7.30
atm).
2.3 Production and End-Uses
In 1989, carbon disulfide was primarily used as a chemical intermediate, and production
was estimated to be 340 million pounds. At one time, carbon disulfide was used mainly as a
solvent. However, most carbon disuifide 1S currently used in the synthesis of other chemical
products. Approximately 40 percent of U.S. production of carbon disulfide Ls used in the viscose
process of regenerating cotton and wood cellulose to make rayon and cellophane. Carbon
tetrachloride production also accounts for over 40 percent of U.S. consumption of carbon
disulfide. This usage level of carbon disuifide is expected to decline through the 1990s, because
the demand for carbon tetrachloride is expected to decline (its predominant end use is in the
production of fluorocarbon gases). Other products made from carbon disulfide include rubber
4
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accelerators for vulcanization, mercaptans added to fuel gases to impart detectable odors, certain
synthetic polymers, oils, fats and waxes. It is also used as a solvent for paraffins and waxes in
oil wells because it is relatively non-corrosive.
The end use pattern for carbon disulfide in 1989 is listed below (2).
Derivative Percentage
Carbon tetrachloride 43
Rayon 35
Cellophane 4
Rubber chemicals 9
Misc. 9
2.4 Health Effects Summary
No data exist that classify carbon disulfide as an animal or human carcinogen. However,
at very high levels (10,000 ppm carbon disulfide in air), carbon disulfide is highly toxic to the
central nervous system, and death can occur due to respiratory failure. Carbon disulfide can
cause neurotoxic effects through inhalation and dermal contact (1,5). Carbon disulfide can also
be highly toxic when ingested in large doses (2).
Various local effects and symptoms may occur from exposure to carbon disulfide. In
sufficient quantities, carbon disulfide vapor is severely irritating to eyes, skin, and mucous
membranes. Permanent visual impairment and retinal cell degeneration occurred in monkeys that
breathed 256 ppm for 6 hours a day, 5 days a week for 5-13 months (1). Contact with liquid
carbon disulfide may cause blistering with second and third degree burns. Skin sensitization may
occur. Skin absorption may result in localized deterioration of peripheral nerves, most often
noted in the hands. Respiratory irritation may result in bronchitis and emphysema (6).
Subjective psychological and behavioral disorders have been observed following repeated
carbon disuifide exposure. Acute exposures may result in extreme irritability, uncontrollable
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anger, suicidal tendencies, and a toxic manic depression psychosis. Chronic exposures have
resulted in insomnia, nightmares, impaired memory, and impotency. Less severe changes include
headache, dizziness, and diminished neutral and motor ability, with staggering gait and loss of
coordination (6).
Atherosclerosis and coronary heart disease have been significantly linked to carbon
disulfide exposure. A significant increase in coronary heart disease mortality has been observed
in carbon disulfide workers. The Federal Occupational Safety and Health Administration
(OSHA) has determined that a 4 ppm 8-hour time-weighted average (TWA) limit and a 12-ppm
STEL (Short-Term Exposure Limit) are necessary to reduce the risk of cardiovascular disease
among carbon disulfide-exposed workers. Studies also reveal higher frequency of angina pectoris
and hypertension (6,7).
Other specific effects of chronic carbon disulfide exposure include chronic gastritis with
the possible development of gastric and duodenal ulcers; impairment of endocrine activity,
specifically adrenal and testicular; abnormal erythrocytic development with hypochromic anemia;
and possible liver dysfunction with abnormal serum cholesterol. Chronic menstrual disorder may
occur in women. These effects usually occur as a result of chronic exposure of carbon disulfide
and are subordinate to the other symptoms (6).
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3.0 EMISSION SOURCES FOR CARBON BISULFIDE
This section presents information on the main source categories that emit carbon disulfide
(i.e., rayon production and carbon tetrachloride production)(2,3,8,9). Included in the discussion
of each source category is a technical description of the emitting process and, where available,
a mention of the specific emission points.
3.1 Viscose Process
Viscose processes emitted approximately 500 Ibs carbon disulfide per ton of rayon fiber
produced in 1989 (9). Estimates from 1989 indicate that the viscose process of regenerating
cotton and wood cellulose to make rayon and cellophane accounts for about 40 percent of the
carbon disulfide consumed in the United States (2). Most of the world's rayon is made by the
viscose process (10). In addition to being used to manufacture rayon, cellulose food casings are
also manufactured by the viscose process.
Emissions from the viscose process are often high volume/low concentration streams
(approximately 400,000 cubic feet per minute (cfm) of water-saturated air containing
approximately 100 parts per million (ppm) of carbon disulfide (11)). This can result in difficult
and costly emission control problems. Section 4.0 of this report discusses various potential
carbon disulfide control options and their limitations.
Process Description
The viscose process used to make rayon is shown in Figure 1 (10). A brief description
of the steps involved and those steps wherein emissions can be expected to occur are given
below (10, 12).
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r
Figure 1. Viscose Process*
Cellulose
sheets
Sleeping pressing
18\vt %NaOlI
Aging
Xanlhation
Shredding
Ripening
Dei
Deaenilion ••<-
Filtration
Fiber production
Stretching
>
o—DO o
Dissolving
Dilute
NaOH
Finishing
Acid Hath
*See Reference 10
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Steeping:
Shredding:
Aging:
Xanthation:
Dissolving:
Ripening:
This step converts cellulose-pulp sheets to alkali cellulose by placing the sheets
in a steeping press and filling the press with sodium hydroxide. After steeping, the
cellulose is pressed under high pressure.
This step is used to convert the alkali-cellulose to a "crumb-like" material. This
step also helps distribute the caustic more uniformly in the cellulose while heating
the "crumbs" to a temperature favorable for aging.
Aging is used to decrease and control the degree of polymerization of the
cellulose.
This is a critical step in which the alkali-cellulose crumb is reacted with carbon
disulfide to form cellulose xanthate. To control the carbon disulfide vapor that
escapes, an enclosure system is generally used for xanthation.
This step uses cold dilution in caustic solution to form the cellulose xanthate into
a clear, honey-like viscous dope known as viscose.
This step allows the clear viscose to coagulate and "ripen" to the proper xanthate
level.
Spinning/
Regeneration: In this step, viscose is extruded into a bath containing both salt and acid. The
primary goal of the spinning stage is the control of the coagulation versus
regeneration rate and the maximal use of the differences in these rates to obtain
maximum response to stretching. Carbon disulfide is released during spinning in
an open bath.
Stretching: This step allows for better molecular alignment of the viscose fibers through a
fixed amount of stretching. Since enclosure is difficult, carbon disulfide is
released from the fibers as they are stretched and cut.
Finishing: After the fibers are spun, cut and washed, finishes are applied to give the proper
frictional performance in subsequent textile processing.
3.2 Carbon Tetrachloride Production
The carbon tetrachlonde production process is also an emitter of carbon disulfide. Carbon
tetrachloride is produced by the chlorination of carbon disulfide or the chlorination of methane
or higher hydrocarbons. Since caroon disuifide is emitted only tiom me chionnauon or carbon
disulfide, only that process is discussed. In the carbon disulfide process, a mixture of carbon
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disulfide and sulfur monochloride in carbon tetrachloride is chlorinated under controlled
conditions. This yields a mixture of carbon tetrachloride and sulfur monochloride, which are then
separated by distillation. The sulfur monochloride is recycled. Carbon disulfide is emitted from
the chlorinator, the storage facilities, handling (i.e., loading of trucks, tank: cars, barges), and as
process fugitives. Figure 2 presents a diagram of this process (8).
3.3 Other Processes
Other processes that emit carbon disulfide include the manufacture of thiocyanates and
high-purity metal sulfides. Miscellaneous applications include direct uses of carbon disulfide for
the cold vulcanization of rubber, as a flame lubricant in cutting glass, and for generating
petroleum catalysts. In addition, carbon disulfide is used for dissolving free sulfur, phosphorus,
and iodine (2).
10
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Figure 2. Carbon Tetrachloride Production*
CIII.ORINATOH
CAklUJN
TETRACIII OklDE
CAIIllON
1)1 S 1)1 HI) D
CAUSTIC -
CAUSTIC
PURIFICATION
CARUON
TETRACHLORIDE
STORAGE
LOADING
'Sec Reference 8
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4.0 CONTROL TECHNIQUES
This section describes control techniques for carbon disulflde. These techniques include
existing applications as well as potential applications that are currently being researched. Certain
carbon disulflde emission streams are high-volume air streams with low concentrations of carbon
disulflde. Some of the control techniques described herein may only be applicable to low-volume
air streams with high concentrations of carbon disulflde. Therefore, the nature of the stream
needs to be considered when deciding which techniques to apply. These techniques are described
for the general case. For a process specific application, consult the particular reference cited.
A list of additional references can be found in the October 1988 edition of Pollution
Engineering (13).
4.1 Absorption
This subsection outlines the following absorption methods: oil absorption (Methods 1 and
2) and diglycolamine agent absorption (Method 3).
4.1.1 Method 1: Oil Absorption
Vendors of liquid absorption recovery systems claim that carbon disulfide emissions can
be controlled by oil absorption systems. The basic process set-up is similar for each vendor in
that a combination of carbon disulfide and an absorption liquid are mixed in an absorber tower
and then sent to a stripper tower where they are heated and the carbon disulfide flashes out. The
nature of the absorption liquid is proprietary information.
The carbon disulfide recovery system operates in two continuous stages. The first stage
involves the removal of carbon disulfide from the exhaust stream in an absorber using the
absorption liquid. The vapors are absorbed in a counter-flow packed tower absorption vessel.
in me second stage the absorption liquid that is now rich with carbon disulfide is passed from
the absorber to a series of heat exchangers. This increase in temperature enhances the release
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rate of carbon disulfide from the absorption liquid in the stripping column. The stripped
absorption liquid is recycled back into the absorber for continuous operation. The separated
carbon disulfide vapors are then condensed to the liquid phase. Figure 3 presents a process
diagram of this control technique (14). Potential applications for this control technique include
textiles, furniture finishing and manufacturing, electronics manufacturing, pulp and paper
industries, and petrochemical industries.
There are some limitations to the oil absorption method. Although oil scrubbing may be
feasible for emissions with high concentrations of carbon disulfide, a potential concern with this
method is that it may not be feasible for emissions with low parts-per-million concentrations.
A study of carbon disulfide control options at a cellulose food casing manufacturing facility has
shown that gas absorption could be used to remove carbon disulfide from its emissions.
However, the recovery of carbon disulfide from the large absorption liquid flow would be
economically infeasible. Furthermore, because the absorption liquid could not be regenerated,
using gas absorption as the only removal method would be impractical (11). In addition, CMA
is concerned that the oil absorption system will require large volumes of oil and that the fugitive
emissions of volatile organic compounds from the scrubbing oil will be significant (15).
4.1.2 Method 2: International Patent No. WO 86/02283
Title: Air Scrubbing Process
This technique (16) relates to the purification of air by scrubbing with an effective liquid
that can be recycled. This invention presents an air scrubbing process (similar to Method 1) that
utilizes a scrubbing liquid which is a complete or partial fatty oil, particularly a drying, semi-
drying or saponifiable vegetable, marine, or land animal oil or liquid fat. If the scrubbing liquid
is not entirely fatty oil, a substantial portion of the remainder of the scrubbing liquid is water
with which the oil or fat forms an emulsion. The scrubbing liquid can also include a small
proportion of a detergent or wetting agent.
13
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from
plaul
Figure 3. Oil Absorption System*
recovered solvent
ABSORPTION TOWI:R
VACUUM
PUMP
I
A
non—condcnsablcs return
recovered
solvent to
plant
DHCANTTANK
*See Reference 14
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According to the patent, carbon disulfide is one of the many pollutants that may be
purified from an air stream using this process. After treatment of the air, the scrubbing liquid
can be precipitated readily from the air stream so that no appreciable amount of the scrubbing
liquid will be lost in the air discharged from the treatment process. The patent also states that
the scrubbing liquid is readily available and inexpensive (16). The reader should be aware that
this air scrubbing process is an experimental process and has not vet been demonstrated to he
effective in an industrial setting.
Selection of Scrubbing Liquid
The following fatty oils are suggested for use for the scrubbing liquid because of their
ready availability and effectiveness.
soybean oil
cottonseed oil
groundnut or peanut oil
corn oil
safflower oil
sunflower seed oil
rapeseed oil
Reference 16 contains an extensive listing of other oils that may be used.
In order to facilitate spraying and dispersion of the scrubbing liquid containing fatty oil,
it is preferred that the oil be emulsified with water to provide a scrubbing liquid with a viscosity
lower than the viscosity of the oil. In order to condition the oil for reuse, the oil and water are
separated and pollutants removed from the air are stripped from the oil or fat. Such stripping
can be effected by the use of steam in accordance with known procedures. Steam stripping of
fatty oils is disclosed in Wecker U.S. Patent 1,622,126 (1927) (17). Stripping of fatty oils can
also be accomplished continuously by use of the deodorization procedure disclosed in Dean U.S.
Patent 2,280,896 (1942)(18). The reader is encouraged to locate these patents if this control
technique is considered.
15
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4.1.3 Method 3: Diglycolamine Agent
Diglycolamine (DGA) agent is manufactured by Texaco Chemical Company and is the
brand name for 2-(2-aminoethoxy)-ethanol. It was first introduced in the United States in 1965
and is primarily used for removal of hydrogen sulfide and/or carbon dioxide from gas streams.
DGA agent is a clear, viscous liquid at room temperature and a white crystalline solid below its
freezing point of 9.5° F (19). Although DGA agent is used primarily for hydrogen sulfide and
carbon dioxide absorption, it may be possible to use DGA agent to control carbon disulfide
emissions through a gas absorption system as discussed in Method 1 (19). Although there are
no existing applications of this technology for the purpose of carbon disulfide control, it may still
be considered as a potential control. DGA agent reacts with carbon disulfide to produce the
major degradation product N,N'-bis(hydroxyethoxyethyl) urea. The chemical equation for this
reversible reaction is
H S H
A I || I
2R— NHj + CS. ** R— N— C— N— R +
where
R = HO— CH^— CH2— O— CHj— CH2
This degradation product has a much lower toxicity than the parent compound, carbon
disulfide (19).
4.1.4 Conclusions
Absorption may be a feasible control technique for high-concentration, low-volume carbon
disulfide air emissions. However, it may not be feasible for low-concentration streams. It is
recommended that the reader further research the absorption methods presented herein prior to
considering using these methods. The selection of the absorption medium is critical to the
16
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success of the control technique. The preceding sections have identified absorption liquids that
are thought to be effective in removing and/or eliminating carbon disulfide. According to some
industrial contacts, there are certain problems with using oil absorption in that it is not as
effective as vendors claim. Also, gas absorption is equipment intensive and for that reason may
be more costly than other alternatives. For example, a study conducted by Argonne National
Laboratory showed that application of conventional gas absorption processes for carbon disulfide
removal is relatively expensive mainly due to low equilibrium carbon disulfide loadings in all
possible absorbents. There are requirements for high liquid flow and relatively low superficial
gas velocities to avoid flooding in absorption towers. From this study it was determined that
13 conventional absorption towers (12 ft in diameter) would be required for carbon disulfide
removal for a stream with a 100 ppm carbon disulfide concentration (11). Pilot plants studies
or trial plant runs may be required to determine effectiveness and suitability of this control
technique to a particular carbon disulfide stream.
4.2 Adsorption
This subsection presents adsorption methods using activated carbon and a synthesized
sorbent technique.
4.2.1 Method 1: Activated Carbon
Carbon adsorption is a traditional control technique used for solvent recovery, energy
recovery, odor removal, and regulatory compliance. This control technique employs the use of
activated carbon as an adsorption medium. Air contaminated with carbon disulfide is passed
through a bed of the activated carbon. Carbon disulfide is adsorbed onto the internal surface of
the adsorbent and the purified air is exhausted to the atmosphere. For most applications, the
adsorbent bed is then regenerated, generally with steam. In terms of carbon disulfide adsorption,
the primary problem associated with steam regeneration is the possibility of fires since the
autoignition temperature of carbon disulfide is below the temperature of steam. The carbon
disulfide is then extracted from the steam through condensation.
17
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One method of eliminating the fire problem associated with steam regeneration is to use
dry nitrogen for regeneration. In this application, hot, inert gas (nitrogen) is passed through the
adsorbent bed and desorbs the adsorbed carbon disulflde. The carbon disulfide-rich inert gas is
cooled and passed through the compressor side of a turbo unit. It is further cooled in an
interchanger and enters the expansion side where cooling as low as -80 °F is accomplished.
Condensed liquid is separated and the inert gas is passed through a mechanical pump and is
returned to the adsorber. Figure 4 presents a complete process diagram of this recovery
system (20).
There are safety concerns associated with the use of activated carbon to control carbon
disulfide emissions. Carbon disulflde differs from organic compounds typically treated by
activated carbon systems. Organic compounds typically controlled by carbon adsorption have
an explosion hazard classification of "slight" or "moderate", whereas carbon disulfide has a
"severe" explosion hazard classification. In addition, carbon disulfide exhibits a much lower
flash point than typical organic solvents treated by activated carbon systems. Air and/or rust are
listed as "incompatible materials" for carbon disulfide but are not considered incompatible for
conventional solvents handled by activated carbon systems (21). Carbon disulfide reaction
products of activated carbon systems are much more corrosive than for typical volatile organic
compounds. Sulfuric acid is produced by the contact of reduced sulfur compounds on activated
carbon systems. Furthermore, the presence of sulfuric acid requires extensive custom design and
exotic metallurgy for pipes, condensers, heat exchangers, valves, etc. to control corrosion (21).
In addition to the above concerns, carbon disulflde exhibits a much higher vapor pressure
than typical organic solvents. At stack conditions, carbon disulfide vapor pressure is
approximately 450 mm Hg; at 25°C it is 350 mm Hg. Vapor pressure of typical organic solvents
range from 2 mm Hg to 76 mm Hg. The adverse effect of a high vapor pressure is that
condensation of carbon disulfide would require extensive refrigeration rather than conventional
water cooling to condense the vapor after column stripping (21).
18
-------
Figure 4. Adsorption Recovery System*
< 1 III «««>»«< KCX:K<>S
• • • r
I - OO
I
TUR HO
COMI'KICSSOR
EXPANDER
VACUUM
PUMP
ililKtitt
COOLER
LOW TEMP
CHILLER
KILTER
Slllllllll IIIIIIIIIIIIIMIIIIIlltllllllMllllV-
SOLVENT
STORAGE
SLAIILOWliU
I
'See Reference 20
-------
Studies performed by Argonne National Laboratory using various activated carbons for
carbon disulfide removal indicated that this method is definitely superior to other methods for
removal and recovery of carbon disulfide from air. Carbon has a great affinity for carbon
disulfide. It was concluded that activated carbon may make efficient adsorption and recovery
possible if the other known problems (H2S and H^O poisoning, water loading, and fire hazard)
can be overcome (11). Further study of the carbon adsorption method was recommended by
Argonne National Laboratory.
4.2.2 Method 2: Synthesized Sorbent: European Patent EP 189606
This patent (22) discusses an invention that involves impregnating a solid material suitable
for selective and quantitative removal of carbon disulfide. Some of the solids that can be used
for the impregnation treatment are silica gel, alumina, clay mineral and zeolites. The active
agents for the impregnation procedure which have been found to be effective are amines and
amine complexes of their derivatives. For the impregnation procedure, the solid is mixed
homogeneously with the active agents at temperatures below 200 °C. The loading of the solid
material can be controlled by the initial amount of the active agent in contact with the solid.
Afterward, the mixture can be thermally treated (below 300 °C) and dried in air or in an inert
atmosphere. This thermal treatment determines the ultimate loading of the active agent on the
solid. After a reconditioning of the impregnated material (flow of dry inert gas), the material is
activated. This creates high selectivity for the impregnated solid for adsorption of carbon
disulfide. The adsorbed carbon disulfide can then be quantitated down to the ppb range with a
universal S-monitor (22).
The patent described above is only a potential option that should be further researched
before being used. At this point, the synthesized sorbent method is experimental technology
-------
4.2.3 Conclusions
Adsorption is a traditional and feasible control technique and is relatively easy to operate.
However, for carbon disulfide, it is imperative that steam is not used in regeneration due to the
relatively low autoignition temperature of carbon disulfide. Some other regeneration alternatives
have been presented (i.e., nitrogen desorption). Although nitrogen desorption solves the problems
of using steam, it introduces additional problems (i.e., storage, handling). Carbon adsorption, as
well as the newer synthesized sorbent process, present beneficial, and potentially useful, control
technologies for carbon disulfide emissions. As previously mentioned, Argonne National
Laboratory determined that activated carbon may make efficient adsorption and recovery possible.
4.3 Ventilation and Condensation Recovery System
A ventilation and recovery system is used by the Shanghai Number 12 Viscose Rayon
Factory (12). Since 1972, carbon disulfide vapors from the spinning process (see Section 3.1)
have been controlled by a system of exhaust ventilation and recovery. The recovery of carbon
disulfide is achieved after the capture of the vapor in the ventilation pipe by three successive
cooling condensers and a collection system. Figure 5 presents a schematic of this control
technique (12). During the early 1980s, the average rate of recovery (efficiency) reached 48
percent of all carbon disulfide added in production. A similar carbon disulfide control/recovery
system has been in operation at the BASF Corporation, Fibers Division, Lowland, TN, since
1956 (23). This system employs carbon disulfide condensation through a cold caustic solution
and carbon disulfide recovery in a receiving tank. It works most efficiently when carbon
disulfide concentrations are at very high levels in a low-volume stream. The collected carbon
disulfide is then transferred to a storage chamber as pure carbon disuifide. Eleven to twelve
percent total carbon disulfide is recovered for reuse. An additional 20-30 percent of the carbon
disulfide is converted to hydrogen sulfide. Figure 6 shows a diagram of the carbon disulfide
recovery system used by BASF (24). Recovery techniques are applied by BASF to high
concentration areas of me spinning-process instead of to the low concentration high volume
exhaust stream at the final steps of the process (24).
21
-------
Figure 5. Ventilation & Recovery System*
SIJll'URIC ACID BATH
I. PRIMARY COOUNG CONDENSER
II. SECONDARY COOUNG CONDENSER
III. TERMINALCOOLING CONDENSER
CS2
COMJiCflNO
4 TANK 4
EXHAUST
CS2
TO BE REUSED
'See Reference 12
-------
Figure 6. BASF Carbon Disulfide Recovery System*
I.YH
fib Chem
COOLI.YI2
KOMUUM OUT)
VMK1RS
(PROM SPINNING ROOM)
N.
TO ATM
NON-CONDENSING
SEAI.TANK
TOCS2
STORAGE
TANK
'See Reference 24
-------
This particular control technique has already been applied at several existing sites. It can
be concluded that it is a feasible option for high concentration streams (15). It should be noted,
however, that this arrangement was designed specifically for the rayon production process and
may not be suitable for other sources. It should be noted that refrigerated condensers are
currently being used in a carbon disulfide production process (25); however, this technique poses
a disposal problem if the carbon disulfide is not to be recycled back into the process.
Ventilation and recovery systems could involve prohibitively large energy requirements
for cooling. For example, cooling the enormous volumes of water-saturated air typical of viscose
plant exhaust would be economically and technically infeasible for low concentration carbon
disulfide emission streams (15). However, condensation technology is an option that may be
considered for areas where emission streams with very high carbon disulfide concentrations can
be captured.
4.4 Absorption/Oxidation: U.S. Patent 4,049,775
The method discussed in the patent, developed at the Institute of Synthetic Fibers, Lodz,
Poland, is experimental and is being tested on an industrial scale at CHEMITEX-WISTOM
Synthetic Fibre Industry Plant, Tomaszow Mazowiecki, Poland (26). This patent discusses a
process that removes hydrogen sulfide, carbon disulfide, and sulfur dioxide from the polluted
air in one operation by absorbing and oxidizing the gases in a bath. The specific installation
discussed in the patent is used to remove hydrogen sulfide and carbon disulfide from the
ventilation system air in viscose fiber plants. The installation has a capacity of one million cubic
meters per hour and an alkaline bath (pH= 9.6 - 9.8) with a redox system being used for
absorption purposes. The carbon disulfide is absorbed by the bath in the presence of hydrogen
sulfide and is subjected to hydrolysis. The carbon disulfide reaction and hydrogen sulfide
absorption products are oxidized with atmospheric air to sodium thiosulfate, elemental sulfur and
a small amount of sulfates. This technology can reduce carbon disulfide concentrations of 200-
600 mg carbon disuifide per cubic meter by about 70 percent. Figure 7 presents die process
description for this technique (26).
24
-------
Figure 7. Wet Method of Carbon Bisulfide Control*
1
0,0
/ /
^\^"
ii
I
r^
/
\
\
•xx
efc
^"-^,
8
chimney 150
10-S pl'Js '
high, 5-dfecharge of bath solition' from the tow. 1-bath solution
n reSe™0ir' 8-3parger dr in!st' 9-bat)l ^dution exponents' inlet
"See Reference 25
25
-------
The plant equipment is comprised of 5 towers with 7.8 meter diameter plates. The
cylindrical section of a 5 meter high tower ends in a 5 meter high tapered section feeding the
gases into the chimney. A liquid condenser is positioned between the cylindrical and tapered
sections. The gases are fed into the tower by a fan that delivers from 250,000 to 300,000 cubic
meters per hour, which is equivalent to an average flow rate of gases through the tower of
between 1.5 to 1.8 meters per second. The absorption bath is pumped from the reservoirs
situated below ground level. The bath solution flows down the towers into the reservoirs where
it is regenerated. Bath regeneration is achieved by subjecting it to oxidation with air. The air
is fed by compressors with an output of 1650 cubic meters per hour. The purified air is emitted
to the atmosphere by a scattering chimney 150 meters high (26).
As this is a foreign installation, it is difficult to judge its feasibility for a domestic
application. As previously stated, this technology is currently experimental. The patent does
claim a 70 percent reduction of carbon disulfide emissions and an emission rate of 106 m3 carbon
disulfide/hour. Further investigation into the nature of the bath and its effectiveness for carbon
disulfide is recommended.
4.5 Regenerative Thermal Oxidation
This control technique involves incineration of the gas stream containing carbon disulfide.
The basic construction for this control option admits process gas into the thermal oxidation unit
through an inlet manifold. A flow control valve directs this gas into an energy recovery chamber
in inlet (preheat) mode. The process gas and contaminants are progressively heated in the
stoneware bed as they move toward the purification chamber. High temperature thermal
oxidation is accomplished in this central chamber. Gas or oil burners maintain a preset
destruction temperature of up to 1100°C (2012T) with a residence time of up to one second.
Carbon disulfide present in the gas stream will autoignite, releasing energy in the stoneware bed.
From the central chamber, the purified process gas stream passes through an energy
recovery in outlet (heat recovery) mode. The cleaned gas can be handled by a standard fan
-------
located in the clean gas side. Figure 8 presents a schematic of this technique (27). Several
applications for this process include chemical processing; metal coating; petrochemical industries;
pulp and paper industries; and paint, solvent, and ink manufacturing.
According to equipment vendors, this technique is feasible and has many applications for
industry pollutant control. However, it may be cost prohibitive as the process equipment would
need to be made of Hastalloy or Stainless Steel due to the corrosive nature of carbon disulfide.
In addition, substantial energy costs are associated with using this option for viscose
processes (15). Another potential drawback of using thermal oxidation is that sulfur dioxide is
an oxidation by-product of carbon disulfide. Control of the resulting sulfur dioxide emissions
is a concern.
4.6 Catalytic Conversion: U.S. Patent 4,374,819
This patent discussed a system that relates to a multi-stage process for removing noxious
sulfur containing gases, notably hydrogen sulfide, sulfur dioxide, carbonyl sulfide and carbon
disulfide, from waste gas streams (28). This control technique employs the Claus reaction for
sulfur recovery:
SO2 -» 2HjO + 3/2 S
The Claus process has been used to remove hydrogen sulfide from gas streams by reacting
hydrogen sulfide with sulfur dioxide in the presence of a catalyst (i.e., bauxite, alumina, cobalt
molybdates) (28). The first stage involves a Claus reaction, but uses a novel catalyst which also
permits the reduction and/or elimination of the carbon disulfide from the gas stream through the
following reaction:
CS2 + S02-» Sx + C02
-------
Figure 8. Thermal Oxidation System*
Stoneware
Refractory
lining
Outlet
plenum
Burner
Stack
Purification
chamber
nergy recovery
chamber
/aive
"See Reference 27
28
-------
In this first stage, the gas stream is passed through a reactive zone having a temperature
between 150 °C to 350 °C in the presence of a pre-treated novel catalyst having the following
formula:
In this formula, Ln is yttrium or a rare earth element, T is cobalt, iron or nickel, and x and y are
independently numbered from 0 to 3. The catalyst is non-crystalline and has a surface area of
about 10 mVg to about 40 m2/g. The preferred catalyst is one in which Ln is lanthanum; T is
cobalt; and x and y range from 1 to 3, including non-integers. The first stage yields a product
stream having a reduced content of sulfur-containing gases, specifically including substantial
reduction and/or virtual elimination of carbon disulfide.
An intermediate stage is a Glaus reaction which may take place in one or more reaction
zones in the presence of known catalysts such as bauxite, alumina or cobalt molybdates. The
final stage is required to reduce the hydrogen sulfide concentration to about 10 ppm. This stage
involves the air oxidation of hydrogen sulfide at a temperature between 150 °C to 300°C in the
presence of a catalyst usable in the first stage. Figure 9 presents a diagram of the three
stages (28). For carbon disulfide removal, only the first stage needs to be executed.
In general, this technology applies to commercial processes involving very high
concentrations of sulfur gases. It is used primarily to control hydrogen sulfide emissions from
sulfur recovery plants associated with oil refining operations. The process gases are characterized
as containing 15 percent to 20 percent carbon dioxide and essentially no oxygen (15).
This option may also be very costly because the equipment must be constructed of
HastaUoy or Stainless Steel. The other primary problem with this option is that the carbon
disulfide is not recoverable. If the particular process requires a recycle stream of carbon
disulfide. this control opaon would not be feasible. Although tneoreacally it appears that tnis
29
-------
Figure 9. Catalytic Conversion*
CLAUS REACTOR AT 328°C
WITH CATALYST OF THIS
INVENTION
CLAUS PLANT
TAIL GAS
(16,600 PPM TOTAL
SULFUR GASES)
COOLED
TO 25.9°C
,,, H
J%
COS-f-SO^
COS + !%<3
Sx
FOR FINE TUNING OF
RATIO
1st STAGE
OXIDATION REACTOR AT 1 9 1 °C
WITH CATALYST OF THIS INVENTION
4170ppm H2S + SO2
78ppm COS and
Non-Detectable CS2
Cooled to23.9°C
(3% H20(g))
/
SULFUR
PRODUCT
Ipi?
CLAUS REACTOR
WITH BAUXITR
CATALYST AT 12TC
*
v:
>
\.2J-..^
1
\)
\
SULFUR
PRODUCT
FINAL STAGE
TOTAL < 300ppm
SO2 < 250ppm
H2S < lOppm
"See Reference 23
-------
method may be used to control carbon disulfide emissions, there have not been any proven
practical applications yet.
4.7 Control with a Bioreactor
This method, entitled the Waagner-Bio/Glanzstoff Austria Process, employs a fixed bed
bioreactor that is designed as a counter current gas-liquid reactor. The reactor is equipped with
commercially available packing materials such as polyethylene and polypropylene of different
specific areas. The reactor is also equipped with an immobilized mixed culture of
microorganisms, generally Thiobacillaceae. The packing material carries the immobilized
microorganisms. The gas containing the contaminants (Le., carbon disulfide) flows counter-
current to the water/activated sludge suspension through the reactor. As the crude gas passes
through the reactor, the hydrogen sulfide and carbon disulfide transfer into the liquid surrounding
the cells and then further through the microorganism cell walls due to the favored rapid oxidation
of the hydrogen sulfide and carbon disulfide by the metabolism of the sulfur-oxidizing
microorganisms. The oxidation products are released through the cell walls into the liquid and
are removed continuously by the circulating flow of the water/activated sludge suspension and
are neutralized by the addition of sodium hydroxide. The formed sulfate is removed from the
settler by the continuous addition of water. Figure 10 presents a process diagram of this method
(29).
This control option has not been proven on an industrial scale, and all data are from pilot
plant studies. Further investigation into the capability of this option on actual industrial sites is
needed. Theoretically, this option appears to be feasible. However, there is concern that this
technology may not be feasible for low concentration, high volume streams (15).
4.8 Wet Scrubbing
Based on more than a decade of wet scrubbing experience, an odor control system has
been developed that treats air flows from 500 to 70,000 cfm (30). This method uses a packed
31
-------
Figure 10. Control With a Bioreactor*
VI
PURIFIED GAS
H20
-o-
P3 B2
P4 B3
V1 blowei P3 pump for alkali
Rl bioreauor B2 alkali lank
M circulaiion pump P4 lap water pump
Ii 1 sedirncnler B3 lap water lank
P2 reflux pump
___
•Sec Reference 29
-------
tower concept In operation, scrubbing spray is created by controlled mixing of sodium
hypochlorite (bleach) and/or other chemicals with tap water that has been pretreated to remove
hardness. The mixture is then fed to a nozzle located at the inlet of each reaction tower. While
odorous air is vented into a reaction tower, the nozzle sprays a fog of very fine droplets which
travel concurrent with the air. The nozzle produces droplets with mean diameters of 10-12
microns, which are ideal for effective odor removal. Enhanced by long gas-liquid contact times
(typically 10 to 30 seconds), the small fog droplets achieve optimal contact As a result, odor
molecules are completely reacted and clean air is exhausted to the atmosphere. The control
mechanism for this process involves non-liquid absorption and subsequent condensation in a
packed tower.
A cellulose food casing facility tested this wet scrubbing method at: its facility for carbon
disulfide removal and determined that it was not feasible on its air stream (31). However, this
wet scrubbing method may have the potential to control carbon disulfide emissions upon further
study. This method is currently employed at more than 65 wastewater treatment plants in the
United States (30). Figure 11 presents a diagram of the control system (30).
4.9 Current Research
Researchers at Argonne National Laboratory, in Chicago, Illinois, in conjunction with the
Illinois Department of Energy and die Department of Commerce and Community, have examined
the following four possible options for controlling carbon disulfide emissions.
1. gas absorption
2. gas adsorption
3. membrane separation
4. catalytic conversion
Options 1, 2 and 4 have been presented in Sections 4.1, 4.2, and 4.6, respectively. Option 3,
membrane separation, involves the separation of a gas or liquid through the use of a permeable
membrane. The driving force for transport is either pressure or concentration (32).
-------
Figure 11. Wet Scrubbing*
J_l
INLET ODOROUS AJR DUCT
LIQUID
METERING
PANEL
DRAIN
LINE
NOZZLE
REACTION CHAMBER
EXHAUST
FAX
V
OUTLET
DUCT
t
EXHAUST'
STACK
"See Reference 30
-------
The following conclusions have been reached concerning the above carbon disulfide
control options based on studies conducted at a cellulose food casing facility. Gas absorption
was determined to be relatively expensive and was concluded to be infeasible. Results of studies
showed that although ways to alleviate the foe hazard danger must be developed, carbon
adsorption presents the best current possibility for carbon disulfide recovery. Pursuing the
membrane separation option is not recommended at this time because it was determined that
existing ceramic membranes cannot remove carbon disulfide from air effectively, even at high
carbon disulfide emissions. Finally, it was determined that because the catalytic incineration
process would requke a catalytic reactor to convert sulfur dioxide to sulfur trioxide and a sulfuric
acid plant, there is little economic incentive to choose this option for carbon disulfide emission
control (11).
35
-------
REFERENCES
1. Agency for Toxic Substance and Disease Registry (ATSDR). " Toxicological Profile for
Carbon Disulfide, Draft for Public Comment", U.S. Public Health Service February 15
1991.
2. Chemical Products Synopsis. Carbon Disulfide. Mannsville Chemical Products, Asbury
Park, N.J., (908) 776-7888, September 1990.
3. Timmerman, R.; "Carbon Disulfide" in Kirk-Othmer Encyclopedia of Chemical
Technology. Vol 4, John Wiley and Sons Inc., NY, 1978, pp 742-754.
4. Memorandum from J.M. Stewart, Courtaulds Fibers, Inc., to Susan R. Howe, Chemstar
Division, Chemical Manufacturers Association, Washington, DC, April 8, 1992.
5. Hazardous Substance Data Base (HSDB), Carbon Disulfide. Bethesda, MD: National
Institutes of Health, National Library of Medicine. 1990.
6. Sittig, Marshall, Handbook of Toxic and Hazardous Chemicals and Carcinogens. Second
Edition, Noyes Publications, Park Ridge, New Jersey, 1985.
7. Federal Register, Volume 54, No. 12, January 19, 1989, p. 2535.
8. U.S. Environmental Protection Agency. Locating and Estimating Air Emissions From
Sources of Carbon Tetrachloride. EPA-450/4-84-007b, RTP, NC. March 1984.
9. Pacific Environmental Services, Inc. Emission Factor Documentation for AP-42:
Section 5.19 Synthetic Fibers. Prepared for U.S. Environmental Protection Agency,
Office of Air Quality Planning and Standards, Research Triangle Park, NC.
10. Lundberg, J.; Turbak, A.; "Rayon" in Kirk-Othmer Encyclopedia of Chemical Technology.
Vol 19, John Wiley and Sons Inc, NY, 1978-1984, pp 855-880.
11. Dr. M.J. Mclntosh, Removal and Recovery of Carbon Disulfide Emitted bv the Viscose
Process, Energy Systems Division, Argonne National Laboratory, April 1992.
12. Youxin, L.: Dezhen, Q.; 1985. "Cost-benefit Analysis of the Recovery of Carbon
Disuifide in the Manufacturing or Viscose Rayon." Scandinavian Journal of Work
Environmental Health: Vol 11, No 4; pp. 60 -63. ~ '
13. Young, R. (editor;; Pollution Engineering. Volume XX, No. 10, pp. 166-348. October
1988.
-------
14. PROCEDAIR INDUSTRIES. VOC Vapor Recovery System Brochure liiquid
Absorption, Contact: Frank Vollero [(201) 455-8821], Cedar Knolls, New Jersey.
15. Comments of the Chemical Manufacturers Association Carbon Disulfide Panel on EPA's
Draft Report on Carbon Disulfide Emission Control Options, December 20, 1991.
16. International Patent WO 86/02283 (April 24, 1986), Cox. J.P.; Duffy R (identified
through Chemical Abstracts (CA) library literature search).
17. Wecker U.S. Patent 1,622,126 (1927), cited in International Patent WO 86/02283 (April
24, 1986), Cox, J.P., Duffy, R. F
18. Dean U.S. Patent 2,280,896 (April 28, 1942), cited in International Patent WO 86/02283
(April 24, 1986), Cox, J.P., Duffy, R.
19. Texaco Chemical Company. Diglycolamine Agent Brochure, Pub No 102-0108 988
[(512) 483-0136], Austin TX.
20. NUCON International Inc., Braysorb Brochure Bulletin: IOB7-4/90 1990 Contact- Jaclc
Jacox [(614)846-5710], Columbus Ohio. ' '
21. Viskase Corporation. Rationale for Conclusion that Carbon Adsorption Technolooy is
Not Safe and Therefore Infeasible for Control of Carbon Disulfide Emission a°t the
Viskase Corporation, Bedford Park Facility.
22. European Patent 0189606 (January 2, 1985), Vansant, E.; Peeters, G.; De Bievere P • Van
Gompler. R. (identified through Chemical Abstracts (CA) library literature search).
23. Memorandum from D.A. Tulis, Alliance Technologies Corporation, to D.M Michelitsch
Control Technology Center, U.S. Environmental Protection Agency October 10 1991'
Meeting Report: Carbon Disulfide Emissions Control Options: Meeting with members
of the BASF organization.
24. Memorandum from C.D. Cannon, BASF Corporation, Fibers Division to DM
Michelitsch, Control Technology Center, U.S. Environmental Protection Agency October
16, 1991. BASF Carbon Disulfide Recovery System.
25. Hagen, R.; 1991. Telephone conversation between Rudy Hagen of Akzo Chemicals and
David Tulis of Alliance Technologies Corporation.; Chapel Hill. N C July 1Q91 TAkzo-
(205) 675-1310]. " y L
26. U.S. Patent 4,049,775 (October 10. 1975), Majewska. I; Grams W • Rybicki ^ •
Banasiak, I; (to Instytut Wlokien Chermcznvch, (identified through Chemical Abstracts
(CA) library literature search).
-------
27. PROCEDAIR INDUSTRIES. VOC Control System Brochure 2: Regenerative Thermal
Oxidation, Contact Frank Vollero [(201) 455-8821], Cedar Knolls, New Jersey.
28. U.S. Patent 4,374,819 (Feb 22, 1983), Palilla, F.; Frank, C; Gaudet, G.; Bagloi, J.; (to
GTE Laboratories Inc) (identified through Chemical Abstracts (CA) library literature
search).
29. Berzaczy, L.; Nierdermayer, E.; Kloimstein, L.; Windsperger, A.; 1988. "Biological
Exhaust Gas Purification in the Rayon Fiber Manufacture (The Waagner-Biro/Glanzstoff
Austria Process.); Chemical Biochemical Engineering Vol 2, No. 4; pp 201-204.
30. Quad Environmental Technologies Corporation - CHEMTACT Brochure Contact- Rob
Rafson [(708) 564-5070], Northbrook, Illinois.
31. Memorandum from J. Webster, Teepak, to S. Howe, Chemical Manufacturers Association
Washington, DC, March 18, 1992.
32. Chilton, C; Perry, R.; Chemical Engineers Handbook. McGraw-Hill Book Company
New York, New York, 6th edition, 1984.
-------
-------
1. REPORT NO. ~~~~
EPA - 450/3-91-023
TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing
2.
4. TITLE AND SUBTITLE
Carbon Bisulfide Emission Control Options
7. AUTHOR(S)
Ravila Gupta, Lula Harris, and David Tulis
9-
6. PERFORMING ORGANIZATION CODE
8. PERFORMING ORGANIZATION REPORT N
G ORGANIZATION NAME AND ADDRESS
T.RC ENVIRONMENTAL CORPORATION
100 EUROPA DRIVE
SUITE 150
CHAPEL HILL, NC 27514
12. SPONSORING AGENCY NAME AND ADDRESS
Emission Standards Division
— — *•— »*•«.* \»»j ••*•*• »Awj.wu \.I"1/XJJ
Office of Air Quality Planning and Standards
U.S. Environmental Protection Agency
Research Triangle Park, NC 27711
3. RECIPIENT'S ACCESSION NO.
5. REPORT DATE
September 1992
1. CONTRACT/GRANT NO.
EPA - 68-DO-0121
3. TYPE OF REPORT AND PERIOD COVERED
4. SPONSORING AGENCY CODE
15. SUPPLEMENTARY NOTES
BSD Work Assignment Manager: Deborah M. Elmore
MD-13 (919) 541-5437
16. ABSTRACT "~~—" — •—.
The EPA Control Technology Center, OAQPS, has received numerous
inquires regarding control options for carbon disulfide emissions
to r««JJ°r P"Sen^S a Description of methods or techniques used
to control carbon disulfide emissions from a variety of source
categories, and discusses the feasibility of application of each
technique presented. This report briefly discusses various
options available to public and private industry for controlling
hh^011 di^ulfi^e emissions, and serves as a reference source for
those seeking further information.
17.
a.
DESCRIPTORS
KEY WORDS AND DOCUMENT ANALYSIS
Carbon Disulfide (CS_)
Emissions Control Technologies
Emission Source
Pollutant Control
18. DISTRIBUTION STATEMENT
-Please 'Jniimi tart
i 19. SECURITY CLASS , Hus Xeoorti
-------
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