Control of Volatile Organic Compounds Emissions from Manufacturing

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7' Tab1e 0-4. TYPICAL INCINERATOR PARAMETERS FOR ARCO POLYMERS EM1 SSION TESTING BASED ON DATA FROM AUGUST '1981 (Provided by ARCO Chemical Colmpany from process data) 3 - Atactlc Waste Waste Liquid Waste Liquid Recirculation to Incinerator from to Incinerator from Waste Gas to Incinerator from from Monument Parameter Monument I Plant Monument I1 Plant Nonment IL I1 Plants I& I1 Plants Temperature: Range 60-68°C(140-1550F) 52-60°C(125-140°F) 107-116°C(225-2400F) 66-7l0C(150-160°F) Pressure: Average Range Maximum 960-1,030 - kPa(140-150 psig) . 998-1,070 - kPa(145-155 psig) - - 21-41 kPa(3-6 psig) - 585 kPa(85 psig) 860 kpailz5psig) Steam Rate: Average - - - 0 - Maximum - - - - - d Air Flow: Average - - IU Maxim - - - - Nitrogen Flow: Range Organic Sol ids: Average 41.2 glsec(327 1b/hr) 51.8 glsec(4ll 1 b/hr) - Organic Gases: Average Range
Table D-4. TYPICAL INCINERATOR PARAMETERS FOR ARCO POLYMERS EMISSION TESTING BASED ON DATA FROM AUGUST 1981 (Concluded) (Provided by ARCO Chemical Company from process data) - - - Waste Heat Atactic Waste to Combustion and Quench Natural Gasato Steam Production Boiler Outlet Parameter .Incinerator Air to Incinerator Incinerator from Vaste Heat Boiler -VOC Sampling Point- Temperature: Average 29"C(85OF) 1930C(380°F) 211°C(412"F) Range Steam Rate: Average u Maximum . t Pressure: Average 413 kPa(60 psig) - 1,240 kPa(l80 psig) Range - 34-69 kPa (5-10 psig) - 8.5-18 kpa(34-71 in.^^^)^ Maximum - - - - Air Flow: Average 11.34 m3/sec 24,000 scfm Maximum 16.02 m3/sec[34,000 scfm Nitrogen Flow: Range Organic Sol ids : Average Organic Liquids: Average Organic Gases: Average Range a~umber 6 fuel oil can be substituted for natural gas. bhring test period, this pressure was 10" H20. 'cut back during Atactic Waste incineration.
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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
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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
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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
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Install ed piping and ducting costs
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estimated by the same procedure as
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.ble 5-4. POLYPROPYLENE MODEL PLANT
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Table 5-6. POLYSTYRENE MODEL PLANT
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emitters, while other dryers, e.g.,
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Table 5-8. COST ANALYSIS FOR POLYPR
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other dryers may have higher or low
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Table 5-11. COST ANALYSIS FOR HIGH
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Table 5-12. COST ANALYSIS FOR POLYS
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Polymer Table 5-15. COST EFFECTIVEN
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effectiveness of polystyrene contro
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EEA. Distil lation NSPS Pi peline C
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APPENDIX A LIST OF COMFIENJERS
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APPENDIX B COMMENTS OW MAY 1982 DRA
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Mr. J. R. Famet Page 2 EPA June 16,
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October 19, 1981 Attachment to June
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Be The mocial plant does nst incEud
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1000 BRAZOS, SUITE 200, AUSTIN, TEX
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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
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 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
Page 204 and 205: The total installed capital cost of
Page 206 and 207: 3. Test Results - VOC destruction e
Page 208 and 209: Figure D-4. Petro-Tex 0x0 unit inci
Page 210 and 211: air to reduce the air flow through
Page 213 and 214: HEAT EXCHANGE1 NOTE: From Exchanger
Page 215 and 216: ' organic carbon. chromatography. T
Page 217 and 218: D.3 VAPOR RECOVERY SYSTEM VOC EMISS
Page 219: However, the calculations assume pe
Page 222 and 223: The 20 pprn level was judged to be
Page 224 and 225: REFERENCES FOR APPENDIX D McDaniel,
Page 227 and 228: APPENDIX E: DETAILED DESIGN AND COS
Page 229 and 230: characteristics: volumetric flow ra
Page 231 and 232: Footnotes for Table E-1 astandad co
Page 233 and 234: sources to the flare header were as
Page 235: Flare Tip Diameter (in.) Figure E-1
Page 238 and 239: Table E-3. CAPITAL AND ANNUAL OPERA
Page 240 and 241: Footnotes for Table E-3 aFluidic se
Page 242 and 243: 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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