Control of Volatile Organic Compounds Emissions from Manufacturing

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effectiveness of polystyrene control from a credit of $-670/Mg (for I styrene in steam reduced from 3.09 kg/Mg) to a cost of $960/Mg (styrene I I -In air reduced from 0.20 kg/Mg) . I
REFERENCES FOR CHAPTER 5 Polymer Manufacturing Industry - Background Information for Proposed Standards. U.S, Environmental Protection Agency, Research Triangle Park, North Carolina. Draft EIS. September 1983. ,. Neverill R.B. Capital and Operating Costs of Selected Air Pollution Control Systems, U.S. Environmental Protection Agency. Research Triangle Park, N.C. p. 3-7 and 3-8. Publication No. EPA-45015-80-002. December 1978. Memo from Mascone, D.C., EPA, to Farmer, J.R., EPA. June 11, 1980. Thermal incinerator performance for NSPS. Blackburn, J .We Control Device Evaluation: Thermal Oxidation. In: Chemical Manufacturing Volume 4: Combustion Control Devices. U.S. Envi ronmental Protection Agency, Research Triangle Park, N.C. Publication No. EPA-45013-80-026, December 1980. Fig 111-2, p. 111-8. Reference 4, Fig. A-1, p. A-3 Ai r Oxidation Processes in Synthetic Organic Chemical Manufacturing Industry - Background Information for Proposed Standards. U.S. Envi ronmental Protect ion Agency, Research Triangle Park, N.C. Draft EIS. August 1981. p. 8-9. EEA. Distillation NSPS Thermal Incinerator Costing Computer Program (DSINCIN). May 1981. p. 4. Reference 4, p. 1-2. Reference 6, p. 6-3 and 6-4. Reference 4, Fig. V-15, curve 3, p. V-18. Memo from Senyk, David, EEA, to EBIS Files. September 17, 1981. Piping and compressor cost and annualized cost parameters used in the determi nation' of compliance costs for the EBIS industry. Perry, R.H. and C.H. Chi 1 ton, eds. Chemical Engineers' Handbook, fifth edition, Mew York, McGraw-Hill Book Company. 1973. p. 5-31. Chontos, L.W. Fi nd Economic Pip 3i meter via Improved Formula. Chemical Engi neeri ng, 87 (12) :139-142. June 16, 1980. Memo from Desai, Tarun, EEA, to EB/S Files. March 16, 1982. Procedure to estimate piping costs. Memo from Kawecki, Tom, EEA, to SOCMI Distillation File. November 13, 1981. Distillation pipeline costing model documentation. Richardson Engi neeri ng Services. Process Plant Construction Cost Estimating Standards, 1980-1981. 1980.
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dine Series Emission Standards and
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TABLE OF CONTENTS ................
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D.2 THERMAL INCINERATOR VOC EMISSIO
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LIST OF TABLES End Uses of Polyprop
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Typical Inci nerator Parameters for
Page 11:
LIST OF FIGURES Simplified Process
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2.1 INTRODUCTION 2.0 PROCESS AND PO
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Polypropylene resins are supplied i
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Table 2-2. POLYPROPYLENE (PP) PLANT
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Fxlrus loll l'el lciiz ltlq Methano
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Tab1e 2-3. CHARACTER1 STICS OF VENT
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in addition to C3 and process dilue
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used in maki fig shopping bags. For
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I 2 CTC E%% PCS A wrcc 2 C W P U iZ
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Table '2-6. CHARACTERISTICS OF VENT
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A1 though polymers with molecular w
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A - . STYREL +VACUUH SYSTEM (8) (9)
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Tab1e 2-8. CHARACTERISTICS OF VENT
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3.0 EMISSION CONTROL TECHNIQUES Vol
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that they require for complete comb
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PILOT AND CENTER mAlri JET ELNATION
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Ground flares are usually enclosed
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flare was operated with from 130 t
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w Table 3-1 . FLARE EMISSIONS STUDI
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has become less common during the p
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Waste Gas- Stack Section Figure 3-3
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chamber temperatures ranging from 7
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= alti-
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control can be used. Any breakdown
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and, in some cases, reused in the p
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are immiscible with the coolant. Th
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3.2 .I .1 Condenser Control Efficie
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VOC -*, VENT TO VcntS~ AmOSPnERE Fi
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ABSORBlHG UQUlD WITH VOC OUT To Dis
Page 73 and 74: REFERENCES FOR CHAPTER 3 Lee, K.C.,
Page 75 and 76: Reference 24, p. 34. Key, J . A. Or
Page 77 and 78: 4.1 INTRODUCTION 4.0 ENVIRONME NTAL
Page 79 and 80: Table 4-1. UNCONTROLLED EMISSION RA
Page 81 and 82: C Table 4-3. UNCONTROLLED EMISSION
Page 83 and 84: the results and an analysis of cost
Page 85 and 86: Tab1e 4-4. MODEL PLANT ENVIRONMENTA
Page 87 and 88: Tab1e 4-5. ADDITIONAL ENERGY REQUIR
Page 89 and 90: -- Table 4-7. ADDITIONAL ENERGY REQ
Page 91 and 92: 5.0 CONTROL COST ANALYSIS OF RACT T
Page 93 and 94: m I W 1. Simple. continuous uanuall
Page 95 and 96: Tab1e 5-2, INSTALLATION COST FACTOR
Page 97 and 98: FOOTNOTES FOR Tab1 e 5-3 a Incl ude
Page 99 and 100: In order to prevent an explosion ha
Page 101 and 102: analysis of the Distil 1 ation NSPS
Page 103 and 104: Install ed piping and ducting costs
Page 105 and 106: estimated by the same procedure as
Page 107 and 108: .ble 5-4. POLYPROPYLENE MODEL PLANT
Page 109 and 110: Table 5-6. POLYSTYRENE MODEL PLANT
Page 111 and 112: emitters, while other dryers, e.g.,
Page 113 and 114: Table 5-8. COST ANALYSIS FOR POLYPR
Page 115 and 116: other dryers may have higher or low
Page 117 and 118: Table 5-11. COST ANALYSIS FOR HIGH
Page 119 and 120: Table 5-12. COST ANALYSIS FOR POLYS
Page 122 and 123: Polymer Table 5-15. COST EFFECTIVEN
Page 126 and 127: EEA. Distil lation NSPS Pi peline C
Page 129 and 130: APPENDIX A LIST OF COMFIENJERS
Page 131 and 132: APPENDIX B COMMENTS OW MAY 1982 DRA
Page 133 and 134: Mr. J. R. Famet Page 2 EPA June 16,
Page 135 and 136: October 19, 1981 Attachment to June
Page 137 and 138: Be The mocial plant does nst incEud
Page 139 and 140: 1000 BRAZOS, SUITE 200, AUSTIN, TEX
Page 141 and 142: our previous comments the TCC quest
Page 143 and 144: . . . . " . . 5. Emission Reduction
Page 145 and 146: REFERENCES Texas Chemical Council t
Page 147 and 148: ' Y !. Jack R. Faner o The A~ency h
Page 149 and 150: NATION& AIR POLLUTION CONTROL Y COM
Page 151: " DEFINITION OF INCINERATION AS MCT
Page 154 and 155: -5- IN SUWRYj THE AGENCY, BY RELYIN
Page 156 and 157: STRUMS WITH RELATIVELY STABLE FLOW
Page 158 and 159: 1 I CoHPlTIONS OF 10 TIMES NORMAL S
Page 160 and 161: I 1 I - gU - I I n G PROPO.SED INCI
Page 162: The use of data from the CTG for ai
Page 166: Mr. Jack R. Farmer, Chief July 19,
Page 169 and 170: APPENDIX C MAJOR ISSUES AND RESPONS
Page 171 and 172: generally for large volume, variabl
Page 173 and 174: control devices, such as thermal an
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modification or rep1 acement, based
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epresent excellent agreement for su
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Response: The following responses a
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processes (e.g ., polypropylene and
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I I I I The purpose of this appendi
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Data collection continued for each
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Test . Number ~104Velocity (scfm) (
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found for tests of incinerators at
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7' Tab1e 0-4. TYPICAL INCINERATOR P
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I I I I I l l I averages for the mo
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Table D-5. ARC0 POLYMERS INCINERATO
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Thempies Spaced Evenly Across the T
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probe for the temperature while a w
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The total installed capital cost of
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3. Test Results - VOC destruction e
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Figure D-4. Petro-Tex 0x0 unit inci
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air to reduce the air flow through
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HEAT EXCHANGE1 NOTE: From Exchanger
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' organic carbon. chromatography. T
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D.3 VAPOR RECOVERY SYSTEM VOC EMISS
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However, the calculations assume pe
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The 20 pprn level was judged to be
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REFERENCES FOR APPENDIX D McDaniel,
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APPENDIX E: DETAILED DESIGN AND COS
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characteristics: volumetric flow ra
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Footnotes for Table E-1 astandad co
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sources to the flare header were as
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Flare Tip Diameter (in.) Figure E-1
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Table E-3. CAPITAL AND ANNUAL OPERA
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Footnotes for Table E-3 aFluidic se
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Tab1e E-4. WtORKSHEET FOR CALCULATI
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excess air for oxygen in the waste
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Table E-6. PROCEDURE TO DESIGN THER
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I I a plant had a use for it, heat
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Footnotes for Table E-7 Wpdated usi
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Table E-8. OPERATING PARAMETERS AND
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TABLE E-9. GAS PARAMETERS USED FOR
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~ 1 1 I I l 1 I I represent June 19
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Tabl e -11 CAPITAL AND . IERATIONG
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$0.335/scfm for units with no heat
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Table E-12. PROCEDURE TO CALCULATE
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Footnotes for Table E-12 (Concluded
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i m- Table E-13. PROCEDURE TO CALCU
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I - I - 1 A nnnrrn~~nrc rn rnl PIII
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Table E-15. CAPITAL AND ANNUAL OPER
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aUpdated using Chemical ~ I nneiri
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Condenser ~y2 ! ;tern Area (ftL) Fi
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ased on an equation in the Chemical
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m Equi p ent Type Check Valves Gate
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- 1/8 - - Table E-20. INSTALLED DUC
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Reference 12, p. 6-3 and 6-4. Refer
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APPENDIX F CALCULATION OF UNCONTROL
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Table F-1 . INITIAL EMISSION CHARAC
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Table F12. SUMMARY OF ANNUAL COSTS,
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= the difference between the operat
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I 8 - a F.Z. 1 Sty rene-i n-Steam m
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(9 CE = AC - (0.9 ~ CDnA ~ x eRC) d
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Substituting the values from Table
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Table 7. EXPONENTS USED FOR CONDENS
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Within Line Table F-8. STYRENE'-IN-
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Control of Volatile Organic Compounds Emissions from Manufacturing

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