Control of Volatile Organic Compounds Emissions from Manufacturing

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-5- IN SUWRYj THE AGENCY, BY RELYING UPON AN INNACCURATE WEPRESE)ICTATION OF WE INDUSTRYj HAS DEVELOPED QUESTIONABLE MODEL PLANT COHFfGURATIONS FROM WHICH UNCONTROLLED EMISSIONS FACTORS WERE OBTAINED* As A RESULr, THE WISSIONS FROM THE INDUSTRY HAVE BEEN OVERSTATa AND .- - WE ACTUAL MISSIONS REDUCTIONS THAT W IU BE OBTAINED BY IMPLEMENTING THE C76 wru.fiost LIKELY BE MUCH SMALLER, 111, LACK OF FLEXIBILITYFOR THE STATES IN IMPLEMENTING I THE CLEAN AIR ACT REQUIRES'THATSTATE IMPLEMENTATION PLANS FOR. NOHATTAIWENT AREAS MUST INCLUDE MCr REQUI REMENTS FOR STAT1 ONARY SOURCES. EPA HAS PERMIRP) STATES TO DEFER THE 49DPIS.ION OF RACT REGULATIONS UWTL AFTER ?HE AGENCY HAS DMfO SOURCE CATEGORIES THE 06's ARE TO PROVIDE STA'TE AND LOCAL AIR POLLUTION CONTROL AGENCIES WITH q~ INFORMATION MBY DEVELOP SPECIFIC REQUIREMENTS, THE MANDATES COMBUSTION OF THE MISSIONS AT THE 98 PERCENT LEVEL AND CR THAT THERMAL INCINERATI.ON IS THE ONLY FEASIBLE AqPROACH TO EMISSIONS I CONTROL. THIS APPROACH SEVERELY CONSTRAINSTHE !STATE's ABILITY TO 'SELECT THE MOST COST-EFFECTSVE CONTROL STRAtEGIE!$ FOR STATIONARY , SOURCES UNDER THEIR JURISDIVION, IT15 m's POSIwr1ON THAT IF A c?G 3s HEEDED FOR A SPECIFIC I I SOURCE CATEGORY, IT SHOULD BE DEVELOPED COWSISTEMTWITH THE GOALS AND REQUIREMENTS 6~ THE CLEAN AIR ACT, AS SUCHr THE CTG MUST BE ABLE 70 DESCRIBE FOR 'ME STATES THE APPROPRIATE UNDER A VARIEN OF SPECIFIC CIRCUMSTANCES WITHOUT DICTATING TO THE STATES HOW TO CONTROL SOURCES UNDER THE1R JURISD [ CTI OM. THE m6 SHOUU 8- 24 PROVIDE AN ACCURATE DESCRIPTION OF THE INDUSTRYJ ITS EMISSIONS AM I I
1 BACKGiRQUNP RIE UG SHOULD DESCRIBE THE MU'SAPPROPRIATE FOR THE INTERPRET1WG HOW SOURCES MIGHT BE AFFECFEO BY THE CT6,4 BUI THE STATES PRELIM1NARY DRAFT CT6 STATES MCT FOR THESE SOURCES HAS BEEN DEFINED A PERCENT CONTROL OF PROCESS VOUT~~E ORGAN1C COMPOUND (vo6) I NCI NEWTI OM SERVI Ne AS I'HE MODEL CONTROL TECIINIOUE. THIS DEFZNEO LML OF CONTROL FOR RACT IS EQUIVALENT TO ma LeveL OF mrssraivs ewma~OR waucmoas NOR 1 IS NOT GENERALLY EMPLOY PROCESS voc mr ssrons n RS/RESINS INDUSTRY. FLARES$ HOWEVE.?, 1MTERHIRENT EMS SSlONS HH THE SELECTION 09 %BE1 ERATI OM FOR THE R86Y STRAfECY 1S ' I NCQNSI STENB WITH THE GENERALLY ACCEPTED DEFIMITIBW OF MCT, €$A'S ARGUMENT FOR MCLUDtWG BOX LE~S AS MCT IS INCONSISTENT' WITH ITS ARGUMENT FOR SELECTING INCINERATORS, WE AGREE WITH EPA THAT BQILERS AND OTHER ENCLOSED COMBUJTION DEVICES 4 INCLUDINGINCINERATORS) ARE NOT OPERATION OF I'WESE DEVICES REQUIRES THAT THEY BE SIZED TO HANDLE CONTINUOUS 8- 25 .--
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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
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
Page 17 and 18:
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
Page 23 and 24:
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
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REFERENCES FOR CHAPTER 3 Lee, K.C.,
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Reference 24, p. 34. Key, J . A. Or
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4.1 INTRODUCTION 4.0 ENVIRONME NTAL
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Table 4-1. UNCONTROLLED EMISSION RA
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C Table 4-3. UNCONTROLLED EMISSION
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the results and an analysis of cost
Page 85 and 86:
Tab1e 4-4. MODEL PLANT ENVIRONMENTA
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Tab1e 4-5. ADDITIONAL ENERGY REQUIR
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-- Table 4-7. ADDITIONAL ENERGY REQ
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5.0 CONTROL COST ANALYSIS OF RACT T
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m I W 1. Simple. continuous uanuall
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Tab1e 5-2, INSTALLATION COST FACTOR
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FOOTNOTES FOR Tab1 e 5-3 a Incl ude
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In order to prevent an explosion ha
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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 124 and 125: effectiveness of polystyrene contro
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 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
Page 175 and 176: modification or rep1 acement, based
Page 177 and 178: epresent excellent agreement for su
Page 179 and 180: Response: The following responses a
Page 181: processes (e.g ., polypropylene and
Page 184 and 185: I I I I The purpose of this appendi
Page 187 and 188: Data collection continued for each
Page 189 and 190: Test . Number ~104Velocity (scfm) (
Page 191 and 192: found for tests of incinerators at
Page 194 and 195: 7' Tab1e 0-4. TYPICAL INCINERATOR P
Page 196 and 197: I I I I I l l I averages for the mo
Page 198 and 199: Table D-5. ARC0 POLYMERS INCINERATO
Page 200 and 201: Thempies Spaced Evenly Across the T
Page 202 and 203: 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
Page 231 and 232:
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
Page 240 and 241:
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
Page 266 and 267:
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
Page 278 and 279:
Condenser ~y2 ! ;tern Area (ftL) Fi
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ased on an equation in the Chemical
Page 282 and 283:
m Equi p ent Type Check Valves Gate
Page 284 and 285:
- 1/8 - - Table E-20. INSTALLED DUC
Page 286 and 287:
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
Page 302 and 303:
Substituting the values from Table
Page 304 and 305:
Table 7. EXPONENTS USED FOR CONDENS
Page 306 and 307:
Within Line Table F-8. STYRENE'-IN-
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Control of Volatile Organic Compounds Emissions from Manufacturing

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