Control of Volatile Organic Compounds Emissions from Manufacturing

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Table 5-13. COST ANALYSIS FOR POLYSTYRENE PROCESS SECTIONS , WITHIN A PROCESS LINE ' 1 1 1 1 Materi a1 Recovery Styrene in Steam Styrene in Ai r Ej-El VOC 3.09 kg VOC Item per My product per Mg-product I Instal 1 ed Cost, S "' -Purchased Equipment -1nstallatlon Total Instal 1 ed Annual ized Cost, $/yr -Dl rect -Operating Labor -Maintenance -Natural Gas -Electric1 ty -Stearn Subtotal Indf rect -Capital Recovery -Tax, Insurance & Admlnfstration Subtotal Recovery Credit Total (Direct + Indirect - Recovery Credit) a Includes only condenser and refrigeration unit costs. b condenser only 1-2 ft in diameter so no piping, etc. beyond that in installation cost considered necessary. C Includes 514,740 for pi ping. d Cost Is for make-up cool ants. e Frm uncontrolled emission rate <strong>of</strong> 3.09 kg VOC/Mg product. fFrw uncontrolled emission rate <strong>of</strong> 0.2 kg VOC/Mg product.
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dine Series Emission Standards and
Page 3 and 4:
TABLE OF CONTENTS ................
Page 5 and 6:
D.2 THERMAL INCINERATOR VOC EMISSIO
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LIST OF TABLES End Uses of Polyprop
Page 9 and 10:
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
Page 19 and 20:
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
Page 27 and 28:
used in maki fig shopping bags. For
Page 29 and 30:
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
Page 69 and 70: VOC -*, VENT TO VcntS~ AmOSPnERE Fi
Page 71 and 72: 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: Table 5-12. COST ANALYSIS FOR POLYS
Page 123 and 124: C Table 5-16. COST EFFECTIVENESS OF
Page 125 and 126: REFERENCES FOR CHAPTER 5 Polymer Ma
Page 127: Reference 12, pp. Reference 12, pp.
Page 130 and 131: APPENDIX A LIST OF COMMENTERS' Comm
Page 132 and 133: I I I Monsanto Company 800 N. Lindb
Page 134 and 135: Mr. J. R. Farmer Page 3 EPA June 16
Page 136 and 137: and removal. Most slurry process wi
Page 138 and 139: c.Jnissions factors- However, diffe
Page 140 and 141: COMMENTS BY THE TEXAS CHEMICAL COUN
Page 142 and 143: If not, we think they should not lw
Page 144 and 145: * Includes fugitive and miscell **
Page 146 and 147: I 1 ov&state both the missions and
Page 148 and 149: * W. Ja'dkR. Farmer , June 21, 1982
Page 150 and 151: Mv NAME IS RICHARD A. SYMULESKI , I
Page 153 and 154: -4- ISSIBNS FROM CONTIMOOUS k8L'IS~
Page 155 and 156: 1 BACKGiRQUNP RIE UG SHOULD DESCRIB
Page 157 and 158: THEREARE A N ER Of ENGINEERING BRAC
Page 159 and 160: IS CONCERN IS ?HAT BWE INCINERATOR
Page 161 and 162: , P. 0.Box 3766 June 21, 1982 Uoumt
Page 165 and 166: Mr. Jack R. Fanner., Chief July 19,
Page 168 and 169: OATL4 UNITED STATES ENVIRONMENTAL P
Page 170 and 171:
APPENDIX C. MAJOR ISSUES AND RESPON
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are improving and expanding the dat
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has acknowledged after discussion w
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the Enviroscience costs. For exampl
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would be applied to uncontrolled em
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about the imp1 ication that thermal
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APPENDIX D EMISSION SOURCE TEST DAT
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on air-assisted flares. The values
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s 0 E 0 .I- C, C, P e L L 0 0 V) V)
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Canpany and Lo~catio~n Arco Polymer
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I I b) spent catalyst, c) waste pol
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Table D-4. TYPICAL INCINERATOR PARA
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The principle underlying the Byron
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D.2.2 Environmental Protection Agen
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two to three hours for each sample.
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Table D-6. AIR OXIDATION UNIT THERM
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fuel value of the streams fed to it
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utadiene unit at Houston, Texas, an
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2. Sampling and Analytical Techniqu
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subsequent survey in September 1978
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. The thermal oxidizer is provided
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he results of the Union Carbide wor
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eing undertaken to determine the ef
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esuIts are for a butadiene plant, a
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weve large enough to mask the effec
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13. Letter and attachments f~om Bow
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APPENDIX E: DETAILED DESIGN AND COS
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Table E-I. PROCEDURE TO DESIGN 98 P
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FOlOTNOTES FOR TABLE E-1 (continued
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-- - - --- - --- Table E-2. FLARE B
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auxi 1i ary fuel, considering requi
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Table E-3. CAPITAL AND ANNUAL OPERA
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I Foot notes for Tab 1e E-3 (Conclu
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01 0 - 0 r m o D,?? 92%
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Tab1e E-5. GENERALIZED WASTE GAS CO
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Footnotes for Table E-6 a Haste gas
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TABLE E-7. CAPITAL AND ANNUAL OPERA
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E.4.1 Catalytic Incinerator Design
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Itefia - - I I I Tahl~F-R, OPERATIN
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Catalytic Incinerator Equipment Pur
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,000 - Key : 10 $ 3 0.5 1 10 100 I
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-___P___P_5-==-=- Table E-11. CAPIT
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(1) styrene in steam and .(2) sytre
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Table E-12. PROCEDURE TO CALCULATE
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characteristics given primarily in
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Table E-14. PROCEDURES TO CALCULATE
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FOOTNOTES FOR Table E-14 (concluded
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Table E-16. CAPITAL AND ANNUAL OPER
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Footnotes for Table E-16 (Concluded
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- 10 I00 1,OOC Refrigeration Capaci
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Table E-17.: PIPING AND DUCTING DES
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Table E-19. INSTALLED PIPING COSTS~
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REFERENCES FOR APPENDIX E Kalcevic,
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Reference 26, pp. 3-191, 3-212 thro
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APPENDIX F. CALCULATION OF UNCONTRO
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Table F-2 summarizes these costs fo
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C Table F-3. BASIC MINIMUM COSTS AT
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Polymer Table F-5. SUMMARY OF COST
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I ~ Inserting the above information
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I A W Tab1 e F-6. CONTROL COSTS FOR
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condenser sizes are not necessarily
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(15,770 - 1,080) ER (3.09 ' (2,875
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TECHNJCAL REPORT DATA {Please read
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Control of Volatile Organic Compounds Emissions from Manufacturing

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