Control of Volatile Organic Compounds Emissions from Manufacturing

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Table 4-6. ADDITIONAL ENERGY REQUIRED FOR CONTROL WITHrRACT IN HIGH-DltiNSITY POLYETHYLENE PLANTS Annual Stem Annual Natural Gas Annual Electricity Total Energy Process Control Consua~ption Consumpti on Consumption Consuntptf on Control Scenario Sectiona Device 1,000 lblyr flyr kbthlyr fly r bbl oillyrc fly I. Total Plant A1 1 Thermal Incinerator - - - - 70,520 3.50Q ' 110 3,500 Flare 3,080 19,000 700 4,300 - - 870 23,300 Process Sect ion Within Line la Flare 1,010 6,200 700 4,300 - - 370 10,500 PF Catalytic - . - - 4,080 200 4,080 200 Incinerator Process Section Across Lines MR Flare 3,030 18,700 700 4,300 - - 870 23,000 a MR = material recovery; PF = product finishing. b Standard cubic feet (scf) at 60°F. PF Catalytic - - 210 1,310 12,040 590 52 1,900 Incinerator C Equivalent barrels of distil late oil required considering-energy conversion efficiencies: steam: 10001b = 1.525 GJ natural gas: 106~iu = 1..0551 GJ and 1040 But(HHV)/scf at 60°F electricitv: 1 kUh = 9.476 x GJ oi 1 : 1 GJ = 0.1628 bbl oil
-- Table 4-7. ADDITIONAL ENERGY REQUIRED FOR CONTROL WITH RACT IN POLYSTYRENE PLANTS Annual Steam Annual Natural Gas Annual Electricity Total Energy . Process Control ConsumpU on Consumption ,Cons;mption*--- Control Scenario Sect iona 0evi.ce m d - - 1,000 scf/yrD -$ij7 kWhlyr flyr bbl oil/yr /Y r Total Plant MR CI MRe Condenser Process Section Uithin Line ~d - 104.500 5,120 160 5.120 (11.330) (555) (555) MRe Condenser - - - - 2,900 140 140 Process Section Across Lines md a MR = material recovery. me b Standard cubic feet (scf) at 60°F. Condenser (same as "Total la-nt") C Equivalent barrels of distil late oil required considering energy conversion efficiencies: steam: lOOOlb = 1.525 GJ natural gas: 1068tu = 1.0551 GJ and 1040 But(HHV)/scf at 60°F electricity: 1 kwh = 9.476 x lo-3 GJ oil: 1 GJ = 0.1628 bbl oil d Styrene in air at 3.09 kg VOC/Mg of product (numbers in parantheses are at 0.2 kg VOC/Mg of product). e~tyrene in steam. Nunbers are applicable for b.oth 3.09 kg VOC/Mg of product and 0.2 kg VOC/Mg of product,
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dine Series Emission Standards and
Page 3 and 4:
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
Page 15 and 16:
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
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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)
Page 37 and 38: Tab1e 2-8. CHARACTERISTICS OF VENT
Page 41 and 42: 3.0 EMISSION CONTROL TECHNIQUES Vol
Page 43 and 44: that they require for complete comb
Page 45 and 46: PILOT AND CENTER mAlri JET ELNATION
Page 47 and 48: Ground flares are usually enclosed
Page 49 and 50: flare was operated with from 130 t
Page 51 and 52: w Table 3-1 . FLARE EMISSIONS STUDI
Page 53 and 54: has become less common during the p
Page 55 and 56: Waste Gas- Stack Section Figure 3-3
Page 57 and 58: chamber temperatures ranging from 7
Page 59 and 60: = alti-
Page 61 and 62: control can be used. Any breakdown
Page 63 and 64: and, in some cases, reused in the p
Page 65 and 66: are immiscible with the coolant. Th
Page 67 and 68: 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: Tab1e 4-5. ADDITIONAL ENERGY REQUIR
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 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
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1000 BRAZOS, SUITE 200, AUSTIN, TEX
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our previous comments the TCC quest
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. . . . " . . 5. Emission Reduction
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REFERENCES Texas Chemical Council t
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' Y !. Jack R. Faner o The A~ency h
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NATION& AIR POLLUTION CONTROL Y COM
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" DEFINITION OF INCINERATION AS MCT
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-5- IN SUWRYj THE AGENCY, BY RELYIN
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STRUMS WITH RELATIVELY STABLE FLOW
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1 I CoHPlTIONS OF 10 TIMES NORMAL S
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I 1 I - gU - I I n G PROPO.SED INCI
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The use of data from the CTG for ai
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Mr. Jack R. Farmer, Chief July 19,
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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
Page 206 and 207:
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
Page 217 and 218:
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
Page 252 and 253:
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
Page 262 and 263:
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
Page 268 and 269:
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
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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
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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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