Control of Volatile Organic Compounds Emissions from Manufacturing

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Polymer Table 5-15. COST EFFECTIVENESS OF RACT APPLIED TO CO~NTIN~UO~US STREAMS IN THE - POLYMERS AND RESINS INDUSTRY, BY PROCESS SECTION ACROSS LINES Process Sect iona Projected control Device VOC Redudion, Idglyr From Frm Existing ~ncontrol led Control Annualized Cost. $/yr Cost Effectiveness. $I& VOC Reduced From- Frm Existlng Uncontrolled Control Polypropylene PR Flare 563 46 25,000 44 545 la. Flare 4 .I40 338 53,800 13 160 Thermal 360 360 130.800 365 365 Incinerator High-knsi ty ~ol~eth~lene HR F1 are 2,663 266 47,960 PF Catalytic Incinerator 85 85 71,600 Polystyrene (Same as in Table 5-14)
C Table 5-16. COST EFFECTIVENESS OF RACT APPLIED TO CONTINUOUS STREAMS IN THE POLYMERS AND RESINS INDUSTRY, BY PROCESS SECTION WITHIN A PROCESS LINE Cost Effectiveness, VOC Reduct Ian, Mg/yr $/Mg VOC Reduced Projected Frm ~rom Process Control Frm Existing Annualized Frm Existing Polymer Sectiona Device Uncontrolled Control Cost, $/y r Uhcontrol led Control Polypropylene Flare Flare Thenal Incinerator High-Densi ty Flare Polyethylene Catalytic Incinerator Polystyrene OtR Condenser (st! 'en@ i n steam) #R Condenser (styrene in air) a PR = polymerization reaction; MR = material recovery; PF = product finishing. b From uncontrolled emission rate of 3.09 kg VOC/Mg product. Frm uncontrolled emission rate of 0.2 kg VOC/#g product.
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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
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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
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 and 120: Table 5-12. COST ANALYSIS FOR POLYS
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 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
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generally for large volume, variabl
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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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