Document ppORYENaZvww8wKLXKzOJveX

JOSEPH B. ZELLER JEROME H. HECKMAN CHARLES H. MEEHAN WILLIAM H. BOROHESANI, JR. ROBERT R. TIERNAN MALCOLM D. MACARTHUR WAYNE V. BLACK DAVID L. HILL * MARTpf W. BERC0V1CX JOHN's. ELDRED CAROLE C. HARRIS MICHAEL F. MORRONS LARRY S. SOLOMON JOHN B. DUBECX CHRISTINE A. MEAGHER SHIRLEY S. PUJIMOTO PETER L. in la CRUZ* LAWRENCE P. HALPRLN DEBORAH SHOR TKINHB: C. DOUGLAS JARRETT EDWARD L.XORWEX ROBERT L. PLBSHNER JONATHAN P. LEVINE SHEILA A. MILLAR p PA a sy LAW omcBi Keller and Heckman uao IT* STREET, N-w. SUITE lOOO Washington, d. c. aooae September 8, 1981 TELEPHONE SOS -497-1100 CABLE ADDRESS "XIUCAS" WRITER'S DIRECT DIAL NUMBER (202) 457-1116 Mr. R.N. Wheeler, Jr. Union Carbide Corporation P.O. Box 8361 Building 3005 S. Charleston, West Virginia 25303 Re: Radian Report Dear Mr. Wheeler: Enclosed is a copy of the report you requested by the Radian Corporation entitled "Assessment of Control Technology for Reduction of Vinyl Chloride Monomer Emissions at Polyvinyl Chloride Plants." If I can be of any further assistance, please feel free to contact me. Cordially yours Enclosure UCC 026542 L,v -s*.i.y CORPORATION DCN 81-241-139-27-14 ASSESSMENT OF CONTROL TECHNOLOGY FOR REDUCTION OF VINYL CHLORIDE MONOMER EMISSIONS AT POLYVINYL CHLORIDE PLANTS Final Report January 1981 EPA Contract 68-01-4136, Task 27 Prepared for John R. Busik, Project Officer EPA - WSM Room 3202 401 M Street S.W. Washington, D.C. 20460 8501 Mo-Pac Blvd. / P.O. Box 9948 / Austin. Texas 78766 / (512)454-4797 UCC 026543 DISCLAIMER This report vas furnished co eh* U.S. Environmental Protection Agency by Radian Corporation* Austin, Texas in fulfillment of Contract #68-01-4136, Task Number 27. The contents represent the opinions, findings, and conclu sions of the authors and are not necessarily those of the Environmental Protection Agency. ii ucc 026544 CONTENTS Section Figures.......................................................................................................... Table*.......................................................................................................... 1. INTRODUCTION............................................................................... 1.1 Background......................................................................... 1.2 Objectives....................................................... ............ 1.3 Approach............................................................................. 2. SUMMARY.......................................................................................... 2.1 Relief Valve Emissions................................................. 2.1.1 Preventative Measure...................................... 2.1.2 Containment and/or Destruction................. 2.2 Reactor Opening Loss..................................................... 2.3 Fugitive Emission Control.......................................... 2.A Polymer Stripping........................................................... 3. PVC PROCESS DESCRIPTION......................................................... 3.1 Processes and Equipment.............................................. 3.1.1 Suspension Polymerisation Process........... 3.1.2 Reactor Cleaning.............................................. 3.1.3 Emulsion Polymerization................................ 3.2 Operation and Maintenance Procedures................... 3.3 Regulations on VCM Emission from PVC Plants... A. REACTOR RELIEF DISCHARGE EMISSIONS.................................. A.l Safety and Operability Considerations................. A.2 Discussion of Events..................................................... A.2.1 Causes and Effects of Relief Discharges A.2.2 Fault Tree Analysis........................................ ill Page 1 1 3 A 7 -7 8 9 11 11 12 13 13 1A 18 19 20 21 26 26 28 28 32 ucc 026545 CONTENTS (continued) Section Page 4.2.3 Operation and Maintenance..................................................... 39 4.3 Prevention of Dlachargee to Amosphere........................................ 41 4.3.1 Instrumentation and Automation.......................................... 42 4.3.1.1 Central Processor.................................................... 43 4.3.1.2 Processor for Single Reactor............................ 44 4.3.1.3 System Comparison..................................................... 47 4.3.2 Auxiliary Venting System....................................................... 49 4.3.2.1 Reactor and Venting Dynamics............................ 30 4.3.2.2 Design Baals............................................................... 36 4.3.2.3 Auxiliary Vent Capital and Operating Costs...................................................'.. 37 4.4 Containment of missions from Major Event Relief * Valve Discharges...................................................................................... 39 4.4.1 Gasholder Capital, Operating,and Energy Coses............ 61 4.4.1.1 Capital Requirements............................................ 63 4.4.1.2 Operating and Maintenance Costs....................... 63 4.4.1.3 Energy Requirements............................................... 66 4.4.1.4 Total Annualized Cost of Gasholder............... 66 4.4.2 Absorption System Capital, Operating, and Energy Coats................................................................................ 66 4.4.2.1 Capital Requirements............................................. 70 4.4.2.2 Operating, Maintenance, and Energy Costs............................................................. 70 4.4.3 Adsorption System Capital, Operating, and Energy Costs..................................*....................................... . 72 4.4.3.1 Capital Requirements............................................. 72 4.4.3.2 Operating, Maintenance, and Energy Costs............................................................. 76 5. REACTOR OPENING EMISSIONS.................................................................................. 3.1 Variables Affecting Emissions................................ 3.2 Problems Encountered.............................................................................. 3.3 Alternates for MeetingAllowable BOX............................................... 79 79 80 81 tv ucc 026546 CONTENTS (continued) Section page 6. FUGITIVE EMISSIONS............................................................................................ 84 6.1 Loading-Unloading Linas....................................................................... 84 6.2 Slip-Gauges................................................................................................ 35 6.3 Seals on Pumps, Compressors, and Agitators................................ 85 6.4 Relief Valve - Rupture Oise Systems.............................................. 36 6.4.1 General........................................................................................ 86 6.4.2 Premature Failure of Rupture Discs................................... 87 6.5 Manual Venting of Equipment and Equipment Opening................. 88 7. DEGASSING TECHNIQUES........................................................................................ 89 7.1 Process Description................................................................................ 89 7.2 Theory of Stripping Process.......................................................... gi 7.3 Stripping Equipment and Costs........................................................... 92 APPENDS A - BI2LI0GRAPEX............................................................................................... A-l APPENDS B - CALCULATION PROCEDURE AND COMPUTER PROGRAM FOR REACTOR AND VENTING DTNAMICS............................................................. B-l APPENDS C SAMPLE RUNS ON 10,000 GALLON AND 20,000 GALLON REACTORS......................................................................................................... C-l APPENDS D METRIC UNITS CONVERSION TABLE............................................................D-l v ucc 026547 FIGURES Number Page 1-1 3- 1 4- 1 4-2 4-3 4-4 4-5 4-6 4-7 4-8 4-9 4-10 4-11 4-12 7-1 7-2 Currant U.S. PVC capacity by plant size................................................. 2 Simplified flow diagram of PVC suspension polymerization process.............................................................................................................. 13 Polymerization reactor..................................................................................... 33 Overall diagraph of reactor system............................................................ 35 Temperature compensated flow control loop............................................. 36 Fault tree for flow control loop................................................................ 37 Diagram of central processor........................................................................ 45 Single reactor proceesor.,........................................................................... - 46 Auxiliary venting system.......................... 51 Flow diagram for the reactor and vent dynamics................................... 53 Schematic flow diagram of gasholder containment system for major event releases* Absorption system schematic flow diagram............................................... 69 Carbon adsorption system schematic flow diagram................................. 74 A four-bed vertical carbon adsorption tower......................................... 75 Dlffuslvity of VCM In PVC as a function of temperature.................. 93 B F Goodrich continuous slurry stripping system................................. 95 vi ucc 026548 TABLES Number Page 2- 1 3- 1 4- 1 4-2 4-3 4-4 4-5 4-4 4-7 4-8 4-9 4-10 4-11 4-12 4-11 7-1 7-2 Suamary of Capital and Operating Coat* for Alternate Systems to Prevent Reactor Relief Valve Emission* (December 1979 Dollars x 1Q~5)............................................................... Input Material for Polyvinyl Chloride Emulsion and Suspension Processes.................................................................................... Vapor Pressure and Density of VQt.............................................................. Data Heeded for Reporting of Venting of FVC Raactor........................ Comparative Costs of Local and Central Units for PVC Reactor Control.............................................................................................. Summary of Reactor Conditions and Relief Valve Flow Rat* Calculated by Simulation Program (10,000 gal Reactor)............... Summary of Reactor Conditions and Relief Valve Flow Rate Calculated by Simulation Program (20,000 gal Reactor)............... Estimated Capital Cost Factors and Costs for Auxiliary Vent with Condenser (December 1979 Dollars).................................... Annual Operating Cost Factors for Auxiliary Vent with Condenser (December 1979 Dollars)......................................................... Capital Cost Factors for Gasholder Containment System (December 1979 Dollars)............................................................................. Annual Operating Cost Factors for Gasholder Containment System (December 1979 Dollars)...................................... Capital Cose Factors for Solvent Absorption Containment System (December 1979 Dollars)...................................... Annual Operating Cost Factors for Solvent Absorber Containment System (December 1979 Dollars)...................................... Capital Cost Factors for Carbon Adsorber Containment Systn (December 1979 Dollars)..................... -............. Annual Operating Coat Factors for Carbon Adsorption Containment System (December 1979 Dollars)...................................... Suspension Resin Residual Monomer Control Cost Increases 68 MM KG/Tear Plant................................................................. Dispersion Resin Residual Monomer Control Cost Increases............. 10 16 29 40 48 84 54 58 60 64 67 71 73 77 78 96 96 vii UCC 026549 i.i 3ACEGEOUND SECTION 1 XNTHODUCTION Following the discovery that Vinyl Chloride (VCM) was carcinogenic, the National Emission Standards for Hazardous Air Pollutants containing allovabla amissions of VQi vara promulgated. This report reviews technology develop ments for control of suspension and emulsion process emissions at Polyvinyl" Chloride (PVC) plants to comply with the following regulations: 1. 40 CFE 61.64(a) and (e) prescribe limits on VCM emissions from reactor openings and limits on residual VOl in polymers following a stripping operation. 2. 40 CFE 61.63(a) prohibits discharges of VQt except for "emergencies". An ''emergency1' venting or relief discharge means a discharge which could not have been avoided by taking measures to prevent the discharge. 3. 40 cm 61.63(b) 1 through 6 prescribe either VCM emission limits or design specifications for use in certain equip ment for handling VQ1 liquids. The suspension and esulsion processes account for over 90Z of the PVC made in the United States. These are batch polymerization processes using stirred tank reactors. The capacity of United States PVC plants was about 3.49 x 10* T/yr (7.69 x 10* lb/yr) in 1979 from thirty-six plants whose capacities range from 23,000 T/yr (30 x 10* lb/yr) to 313,000 T/yr (700 x 10* lb/yr). Figure 1-1 shows the distributions of plant sizes and capacities. It can be seen that the three largest plants produce almost one-fourth and the sixteen largest plants (of the thirty-six total plants) produce over tvochlrds of the total capacity. The remaining twenty plants with one-third of ucc 026550 bcal CipMlsr * '.iii x LO* IS/yr ?aui Muofear ol ?lu :* 5*U trwm ^tukatts* Umrtur" - cU la, :980. ?igur 1-1. Caniat U.S. 77C eapaeicy by plane six*. ? ucc 026551 the capacity ara ac a graac disadvantage economically. Many of eha small planes ara abla co continue primarily by having capciva markets for chair produces. Tha oldar planes ganarally hava smaller raaceors which ara on eha order of 10 eo 20 m3 (2,000 eo 5,000 gallon) sizes with 20 co 50 such raaceors in eha plane. Never planes in eha Unicad Scacas hava 40 eo 100 m1 (10,000 eo rv 30,000 gallon) raaceors vieh 4 co 12 such raaceors. Huls in Germany reports development and use of 200 m3 (50,000 gallon) reactors in chair operations. Tha small reaceor systems require mora capital, more space, more util ities, more manpover, and additional operating, maintenance, and repair costs. Huls estimated the 200 m reactors, compared to 40 m reactors, would reduce capital by 23Z, space by 33S, utilities by 10Z, manpower by 50Z, and mainte nance by 25Z, for a 160,000 T/yr plane. Since the cose of meeting tha VQ1 emissions limits under the regulations is similarly affsetsd by rsaaeor sirs, a mors severs burden Is placed on the older smaller plants by these regulations This is caused by the greater number of pumps, agitators, reactor chargings and raaceor openings involved with small reactors. 1.2 OBJECTIVES A. Relief Valve Discharges A goal of this work is co provlda a comprehensive assessment of eachtology which can be used in controlling, preventing, containing and destroying VQ1 discharges. Another goal is eo dsiins a msthod for determining whether specific past and fueurs discharges ars "emergencies" or could have been avoided by taking measures eo prsvsnc the discharge. 3. Fugitive Emission Sources A comprehensive assessment of present and near ears fugitive emission control technology and tachnology to reduce reactor opening losses and res idual VCM in polymer and wastewater is the goal of this part of the work. 3 UCC 026552 1.3 APPROACH A Literature survey was nada o engineering developments and of basic physical-chemical daca for suspension and smulsion proeaaaaa in PVC plasca. A daacrlpcd.an vas prepared of dispersion asd suapaaalos PVC proeaaaaa using batch systems scarring vich the of raw nacarlala through chs finished PVC produce with example flowsheets, material balances, operating procaduraa, proeaaa control systems, equipment daaigs and cyplcal plane Lay- ouca. the chemistry of PVC reactor operation was reviewed including reaction rata vs. temperature and Initiator/inhibitor concentrations. 701 and PVC stability vs. temperature, 701 breakdown products, and reaction raeaa at nomal conditions. Tbs phyalcs of PVC reaction operation was reviewed in cluding 701 vapor preaaure vs. temperature, heat of raactlon, heat balancs on reactor, effaces of inarts and waear on reactor pressure, and effects of three phases, solid, liquid and vapor on heat transfer in the kettle and on handling of vented material. Plant tripe to PTC production facilities were tada to review technology in use for control of processes and 701 amissions. Surveys were aade of aenufacturess of equipment used in ?7C planes for consol of processes and prevention and/or containment of 701 emissions. Engineering design of rupture disc/relief valve and vent systems used In the chemical Industry for protection of equipment and control of emissions vers reviewed. "?rsmscare* failure of rupture discs vers discussed with manufacturers and users of such equipment to Identify design and operetlonaltalatansnce practices used for its prevention. External controls for relief valve dischargee ware evaluated including containment, ehersel destruction via flaring, incineration, a; in a boilar, catalytic destruction and other possible control technologies. 4 ucc 026553 The following were considered In these evaluations: 1. safety, 2. capital and oparaelng coses, 3. anargy requirements, and 4. enginaarlng and daalgn factors. Searring with an analysis of daca furaishad by E?A on ra'accor discharges In ?VC planes, a study of tha chemical, physical, operaelonal, anglnaarlng and conerol aspects of the equipment Involved was made. Vent system design, Inserumaneaelon, operation and maintenance practices used on reactors and other equipment from which relief valve discharges have occurred were reviewed, the causes of relief valve vents In reactor and liquid storage systems in cluding initiator excess, overcharging, heat exchange failure, inerts accumulation, contaminants accumulation, kettle charge mix error, controller failure, 701 quality, and external activities were established. A computer program was written to provide liquid and vapor discharge rates, reactor temperature and reactor pressure following a relief valve discharge at anygiven ?VC reaction rate and cooling jacket condition. Tha variables which affact reactor venting and chs techniques which are used to monitor these variables were reviewed. These variables included temperature, pressure, flow and reactor level. Appropriate control actions and operating procedures to prevent safety relief from all equipment In vinyl chloride service were evaluated. Designs and cost estimation for computer control of 701 reactors were developed. ?rom this information a procedure wee recommended to assess the tech nologies in use at the time of venting from a relief valve In a reactor area of a P7C plane so as to detsxmlns the conditions existing st the time of the venting to be a true "emergency1' or to be "controllable" with reasonable actions having been taken to prevent or control the discharge. 5 ucc 026554 A review was mad* of procaduras and equipment used in chemical planes to control fugitive amissions from loading--unloading lines, slip gauges, seals on pumps, compressors and agitators, relief valve rupture disc systems, manual venting of equipment, and opening of equipment. Dta on ode partition coefficient of 701 from polymers and water in literature end on tie effectiveness of stripping and drying operations vara collected and evaluated. Preliminary design parameters for equiaent to meet requirements were determined. 3ata an reactor opening 7Q1 emissions as a function of elms, tempera ture and pressure and when using eltier water or inert gas displacement were evaluated to establish a range of effectiveness for these procedures. Reactor cleaning technologies using solvent and high pressure washing wars reviewed. 5 UCC 02655S SECTION 2 SUMMABT Four aiu< of FVC production vhlch are potential sources of significant amountj of VQI emissions wsrs examined and an assessment mad* of technologies available for chair control. The major conclusions or observations of ehasa studias ara sumaarlzad In this saction and rafarancas mada co cha subsequent 3actions for datailad remarks. Tha araas assassad vara: Relief valva emissions, Enactor opening loss, Fugitive amission control, and Folymsr stripping. 2.1 BELIEF VALVE EMISSIONS Emissions of VCM from rupture disc/reliaf valva (RD/3.V) systams on polymerisation vassals can potentially account for tha largest volume of amissions from a PVC production unit whether a point or fugitive source. In tha worst case they can range up to Cha full contents of one or more reactors, i.a., 15,000 to 65,000 pounds. Tha releases may result from any number of cause* such as ths failure of equipment, instrumentation, power or ce ling supply, operator error, or inadequate maintenance. The NESHA? regulations prohibits cha discharge of VCM from manual vent valves [40 CFE ] 6I.64a(3)] and also from relief valves [S 61.63(a)} except for emergencies, i.a., a discharge which could not have bean avoided by caking measures co prevent the discharge, k study of existing facilities and new or 7\ ucc 026556 proposed designs indicates chat la 1: possible to essentially eliminate this souses of emissions, either '37 contaiaaent or destruction of the 701, or 97 implementation of effective preventative measures. 2.1.1 ?ravencattiva Measures through proper planning, daaiga, operation and maintenance procedures 7d emissions from eh* 3D/S.V (other chan choaa defined as emergency) say ba eliminated as discussed la. Section 4.3 and 4.6. Plant management is responsible for protecting the environment b7 ensuring: * Hew or existing facilities asm vail dasignad with adequate raaeeor cooling capacity, quick rasponaa control and monitoring systems for temperature, pressure, flow, ate., raduadanc isstrunieataeiotfc* utilities, and cooling vatas systems. * Qualified oparacora ara vail crainad and supervised, providad with standard oparaeing procaduraa, automatic control 373tans, and authority to taka corrective action to vane, retard or shortstop incipiant runaway enactions. * Maintenance is performed following vail daflnad procaduraa. * 411 paraotnal ara lnstillad with a concarn for preventing amissions. Fault Traa Analysis Cna naans of pradaearaining that a raaction systaa has baan dasignad and is balag operated vied tha minimum probability of a raliaf valve opaning to tha aeaosphere is to pnrforn a fault traa analysis (or similar axareisa) to ba sura chat all poaaibls points of failura ara covered by proper operating procaduraa, back up equipment or other redundant features. This technique is dsscribad in Section 4.2.2. 3 ucc 026557 Automatic Control Systsa Because of cha complexity of cha polymerization reaction procass and equipment, and cha unpredictability of temperature and pressure excursions, it is highly desirable to provide a well-designed, reliable, automated system co monitor cha reaction parameters, control cha cooling water, adjust cha release of gas or liquid co an auxiliary vent system, alert cha operating personnel, and trigger cha addition of retardants or snort-stops when neces sary. This is discussad in Section 4.3.1. The cost of these systems say be easily justified on the bases of increased productivity and safety. Auxiliary Vent and Recovery Svscam The reaction systam should hava adequata maans for relieving excess pressure by discharging inart gasas and/or controlled amounts of reactants to an auxiliary vent system as discussed in Section 4.3.2. The released material should be cooled, contained, and then recovered or destroyed. This vent system may be activated manually by the operator and/or automatically by a control system. 2.1.2 Containment and/or Destruction Although containment of relief valve emissions can be accomplished by means of a gasholder, a charcoal adsorber, or a solvent absorption system, coat studies, summarized in Table 2-1, indicate these methods are not cost effective for any commercial sized reactor. These containment techniques are discussed in detail in Section 4.4. Alao the destruction of VC1 in boilers or incinerators is not a viable alternative for economic reasons, and flaring of reactor emissions is not feasible for safety reasons as discussed in Section 4.1. 9 UCC 028558 ucc 026559 TAUI.K 2-1. SUMMARY Of CATITAI. AK1) Ol'EUATiNC COSTS fOU ALTERNATE SYSTEMS TO TKEVEHT HEACTOR REUEE VALVE EMISSIONS (Uucuwber 19IS Dulluru t 10 *) Cll|>lul OlKtU Kuock'oul Kt|ul|WHtnC Header Kitewtlun* tetiiliMiiUt Equt|Miiit Automatic Controla $- - Condenuatlon $ 1121 - 904 Cau Holder $ 821 600 1,020 Solvent Abaorptlun $ 021 600 665 TOTAL EljUmiENT engineering, Cuiuiructlou A Contingency $119 91 $im 914 $1,241 1,717 $2,OS6 1.175 TOTAL INVESTMENT $210 $2,619 $4,950 $1,261 Annual Operating Uuutu OEM Iuh. A Turca (22 uf liivuMtiwnl) Capital Chargea (202 uf invcttiwiiit) Credit fur Recovered VCH** $ 12 4 42 05) $ 01 51 510 (20) $ 94 100 1,000 (20) $ 00 66 660 (20) TOTAL ANN. Ol'TO. COST $ 41 $ 646 $1*124 $ 7S6 AAeaiimcu 1000 fuet header to containment ayatcm arua. "Auaimtaa 1 Major event re1euueu/year with automatic coot rot a having 152 UUCCiititi * Reference Tali leu; 4-1 4-6, 7 4-0, 9 4-10, 11 Carhon Adaurptinu $ 021 600 1,016 $3,217 2,061 $5,290 $ 74 106 1,060 (20) $1,220 4-12, n 2.2 3EACT0R OPENING LOSS The VCM amissions occurring when a reactor la vancad co tha atmosph ra (ochar chan an emergency relief discharge as dailnad in i 61.65(a)) ara referred co as raaceor opening loss (ROL). A wall ooaracad facility can raadily keep chasa emissions below 0.02g VCM/kg of PVC produce (dry solids basis), as required by 61.64(a)(2). The numerator, i.e., cha amount of 701 In cha gas phase just prior co opening, can be minimized by evacuation co a low absolute pressure for an adequate time period, by'displacement with water or inert gas, by steaming, or by a combination of chase. However, any residual polymer clinging to Che reactor walls continues co release unreacted 701, and hence an elevated jacket temperature for an extended time period is required to further reduce emissions. The divisor, i.e., the total PVC pro duction, may be increased by reducing the frequency of reactor openings. Several batches say be produced before It becomes necessary co open the reactor if special "closed reactor" techniques are used to clean the reeetor and/or if the vessel wells are creeted to minimise polymer buildup. The various options currently in practice or aveilable for license are discussed In detail in Section 5.4. 2.3 FUGITIVE EMISSION CONTROL Fugitive amissions of 7CM from process equipment in PVC plants ars regulated by 40 C7R 61.65(b), and included those from loading-unloading lines, slip-gauges, seals on pumps, compressors, and agitators, relisf valverupture disc systems, mamisl venting of equipment end equipment openings. A review of these regulations and tha mesas currently used or recommended for the control of fugitive emissions are discussed in detail in Section 6. U ucc 026560 2.4 POLE'S STSIPPISG emissions of residual 701 from cha process equipment downstream of cha scripper and from the finished resin, bacvaen cha cine it In shipped co the cine ie In converted to a consumer produce, ara dependant on cha effectiveness of eha polymar stripping procann. Tha release of unreactad 7d from the ?7C polymer In dapandanc on the time, temperature, and praanura (vacuum) of cha stripping oparacion, an vail an on cha parelcla siza distribution, and cha scrlppar dasign. Polymers mads by cha sunpannlan procann can ba aanily and economically scans scrippad in a continuous column so chac cha rasldual concancracion in lann chan cha 400 ppm allovad by I 61.64(L)(ii). Dispersion. type polymara nay ba scrippad bacchviza (at, aildar eaaparacuras co pravane chair dagradacion) co a residual 701 concancraeion lass chan cha 2000 pps allovad by ! 51.S4(1)(i). A daeailad discussion of cha problems and process variables is presented in Seccicn 7. U ucc 026561 SECTION 3 PVC PROCESS DESCRIPTION 3.1 PROCESSES AND EQUIPMENT Polyvinyl Chloride (PVC) is produced by polymerization of vinyl chloride monomers (VCM) in one of four processes in the United States. Three of these are batch processes: suspension polymerization which accounts for 78Z of capacity; dispersion or emulsion polymerization accounting for 13*; and bulk, polymerization which accounts for 6X. The fourth process, solution polymer ization, is a continuous process and accounts for only about 31 of the PVC-. rastn capacity. A brief process description follows. Vinyl chloride is generally received via rail in a tank car, or by pipeline from a Vd unit nearby or within the plant and is transferred to the Vd storage tank. The monomer may or may not contain an inhibiting agent, but if inhibited, the Vd is passed through a caustic decanter or fractionator to remove the inhibitor. Water, initiators, and suspending agents are first charged to the reactor. A measured amount of Vd is then fed to the reactor from the Vd storage tank and/or the monomer recovery system. The polymerization is then carried out at elevated temperatures and pressures. At approximately 33Z-90Z conversion, the bulk of the uareaetad monomer is vented to recovery and the slurry of polyvinyl chloride granules and water is transferred to the stripper to remove the remaining unreacted Vd. The stripping process is accomplished by the application of heat alone, a stripping gas, or a combination of heat and vacuum over a period of time. The unreacted monomer is driven off to the recovery system where it is accumulated in a surge tank and recycled to mono mer storage. The stripped slurry goes to a slurry blend tank with several 13 UCC 026562 ocher batches eo obtain a iota uniform produce, sicca any 7G1 remaining in chs polymsr if car stripping la ralaaaad cs cha atmosphere la ::.t subsequent oparaeions (i.a., drying, storage, and shipping) cha need far affaceive stripping la obvious. From cha bland cask cha slurry la pumped ca a cantrifuge far separation of water which la generally cranafarrad co a creaenanc araa bafara being disposed af or racyclad. The vac F7C cake from cha cancrliuga, containing about 30? aoiscura, la procaaaad through a hoc air dryer. The particle 3lea governs cha choica of drying cachniquas, which lacluda rscary drying, ilash- rotary drying, cwo acaga flaah drying, and spray drying. Tha allow- abla produce temperature la 33*C sines degradation oi cha polymar occurs above S5*C. Drying conclnuas until cha polymar noiscura concane la lowarad to 0,23 co 0,4 vt I. Iha drlad, solid ?7C parciclaa ara collaccad by cydonaa and/or bag collaccsra and chan sirad by scraana. Iha produce la conveyed co scoraga bins or silos, and oversinad parciclaa ara rejected. Iha aajaricy of cha flnlahad ?7C produce is shipped from cha plane In bulk rail-cars or crocks although soma Is packagsd in 30 pound bags. Iha suspension procsss will be described in norm detail below and da omulsion process will be described briefly In earns of les variation from ehs suspension process. I , 3.1.1 Suspension lolTaarlracion Process Suspension polynarlraclon Is by far cha nose common procsss used co manu facture FTC resins (73? of cha coeal 7.5. capacity). Figure 3-1 praaancj a simplified flow diagram. Iha raw macarlala required include vinyl chloride monomer, initiator, suspending agent, emulsifier, and deionised water (1). labia 3-1 shows the typical range by weight of cha input macarlala. 14 ucc 026563 ucc 026564 i figure 3-1. Simplified flow diagram of PVC suspension polymerization process. IA3L2 3-L. 3?W HAT5IAX. FOR FOLYVUttL CHLORIDE aflJLSIOM AOT STJSPSHSION PROCESSES Chamical Parra by Vaijhe Suapanaion 7iayl CHlorida Vacar Paroxida laisdacog Stabilirars LOO 130 - 330 0.1 - 0.3 0.01 - 1 Zauliioa 7layI Chlarlda Faery Sulionaea Fatry Alcohol Lauxyl Paroxida tfaear 40-60 0.4 - 0.6 0.4 - 0.6 0.4 - 0.3 100 *" SPA 600/2-77-023J. 16 ucc 026565 Initiators are compounds capabla of forming free radicals by charsal decomposition. Parent literature reports the use of many initiators. "Sus pension polymerization of VCM is initiated by organic peroxides in industrial practice, although azo compounds, boron derivatives, and redox systems can be used. Suspending agents are surface active compounds chat prevent agglomeration of PVC particles during polymerization of vinyl chloride. The suspending agent Influences partlcls slzs, porosity, and thus processing characteristics of the product. Deionized water used for suspension polymerization la deaerated, and free of organic matter and sulfur. Water serves three purposes; It provides beet transfer, it is a medium for the suspending agent which controls the- surface properties of the particles and it also moderates the bulk viscosity during processing. Processing of the final product is improved by the addition of small quantities of a secondary amulsifier to the systmn. Such emulsifiers include sulfonated oils or esters, ethylene oxide condensation produces with polyols, and other syntheelc surfactants. Vinyl chloride polymerization is carried out in stainless steel, glasslined carbon steel, or glass-lined stainless steel reactors, depending on raw materials used, corrosion resistance, and desired lifetime of reactors. Raaccor sizes vary between 10 a* (2,000 gals) and 200 a3 (50,000 gals); aach plant uses 4 to 50 such reactors (typically 12-13). Newer plants tend to have larger and fewer reactors. Each reactor la equipped with an agitator, baffles, and temperature controls. The procees involves the mixing of e weighed amount of vinyl chloride in a metered amount of water, initiator, and suspending agents which ars premixed in a clean reactor. A steam jet or vacuum pump is uisd to remove moae of the aoncondeneeble gas remaining after the reactor la charged. The amount of noneondensable gas left depends on ths absolute pressure after evacuation. The reactor Is jacketed to provide heating or cooling as necessary for startup and for controlling the reaction. The 17 ucc 026566 casperacura of cha reactor is raised co 53*C by passing steam through cha jacket. 3ecausa the polymerization reaction is exothermic, cooling water la circulated through eha jacket to keep cha eaaperacura constant, i.a., about 55*C during eha polymerization. Iha agitator, aithar top or bottom entering, uaaa wlciblade impellers to provide uniform agitation, which in important for both efficiency of haac transfer and control of polymer particle aita. Saaetion temperature la ona of cha primary control variables in suspanaion polymarizacion. Tamparatura lnfluaneaa molecular waight, molecular waight distribution, crystallinity of cha product, eha particla sica of cha polymar, and cha solubility and adsorptiricy of cha suspending agent. A master-slave cascade inscrtaiane syscam la usad for eaoparacura control. Scaaa, cold wacar, and rafrigaracad wacar or brlna ara circulacad through cha raaecor jacket as required. Tha polymarinacion eaoparacura can 'oa controlled with 30*C cooling vatar up to 702 conversion. Subsequently, cha raaccion raca incraasas norm rapidly dua to auto acceleration. Ac chin point, rafrig aracad wacar ae about 1S*C is required to affectively control cha camperacura. Polymerization cakas placa at a pressure of 317 k?a (73 psla) co 690 k?a (100 psia). Coaplaclon of cha raaccion is indicacad by a drop in pressura. Prolongation of cha cycla is harmful co rasin porosicy and color. Tha pol7oarlnation raaccion continues to 382 conversion which requires approxi mately six hours. Iha cycle is chan carminetad by transferring cha slurry to cha polymer bland cask or stripper. 3.1*1 Ssactor Cleaning After discharging tha bulk of cha product, between batches, cha reac tor is cleaned co move polymer buildup from cha previous polymerization cycla. Reactor cleanliness is extremely Important co product quality. 13 ucc 026567 Resin from cha previous batch and/or procacciva coaclng solution left in a reactor severely downgrade* the quality of the subsequent batch. This' cleaning process is dons either by high pressure water spray and/or solvents, by personnel who enter the vessel and chip away the buildup, or by a combi nation or these methods. The normal sequence is to (1) wash all the reactor surfaces with water and/or solvents, (2) apply a protective coating (which inhibits polymer buildup), (3) remove the protective coating solvents, and (4) wash with water again to remove excess protective coating. If the reactor must be opened to perform these operations, it is neces sary to first remove the vinyl chloride vapors remaining in the vessel from the previous batch by vacuum or by purging. These vapors are processed in Che monomer recovery system. Any noncondensable gases from chat system are vented after being routed through an absorber or adsorption system or incin erator. In some reactors, using eha newest technology, Che normal process of reactor preparation is performed without opening the reactor eo che atmo sphere. Lances with special nozzles project into the reactor for che washing and coating steps. Since there is no visual inspection for reactor cleanli ness, che washing and coating devices must function properly. 3.1.3 Emulsion Polymerization The equipment and process used in emulsion polymerization are basically similar to that used in che suspension process in chat liquid vinyl chloride dispersed in a water system is polymerized in a batch process. The difference is that more soap is initially added to che reactor co stabilize the dis persed monomer droplets and prevent cha formation of agglomerates. Many different soaps and surfactants may be used as emulsifiers, including natural and synthetic colloidal protective agents such as cellulose derivatives and polyvinyl alcohol. The emulsifier and initiator are dissolved in cold deionized water. A measured amount of vinyl chloride is added and agitated 19 ucc 026568 co form a raiativd7 stable aouision. ?olymaricaeion scarts vhen the raaccor coneanca art haacad. emulsion raaina can be pdymariead ac lower camperacursa (40-53*C) and ac fasear raeas chan suspension resins. The polTmedcaciau la carainacad ac 90S co 9SS monomer conversion. Polymerization raeas dacraaaa rapidly vhen a high canvaralon Laval is reached. A dacraaaa la pressure signifies compladon of cha raacclon. Toraactad viayL chiodde la recovered and racydad. Emulsion raalna arm mors sansidva co haae and shaar acraaaaa chan suapanaion raalna and 12 cara la aoc caitan, cha raaln pardda say ba changed In ways chae make Is unsuitable far use. The pardcla sizes abealnad by cha amulaion procaaa ara such analiar chan choaa obealnad by suapanaion. A sajor diffaranca In equipment of cha evo prscaaaaa la chae cha asulaion polymarizadon uaea a spray dryar co ansura cha salncananca of small pardcla slaa and. raduced casparacura and shaar scraaaaa during drying. 3.Z OPStASICM AND HAl3T3tANCS FSOCoDTOSS Tha produedon of ?7C cancara around cha bacch raaccors vhich hava a cycla cine ranging from 3 co LS hours duradon. Tha cyda s carta vlch cha charging and cendnuaa chrough a haae up period, a raacdon period, discharge of produce, and chan dean up of cha raaccor co prapara for cha cast bacch. tha oparaciona of raaceor charging and pdymerizaeion in oldar planca ara earrlad out sanually by an oparator vho change* valve poaidona, praparaa chemical addldvaa, and scare* and scop* pumps or compression systems, aec., as aaadad. Automatic controls ara used during varn-up and raacdon periods to ccnerel raaceor camparaeara, but oparaeor suparviaion la frequandy naadad co raaae control aceicn* and co prapara chemical additives, tha raaceor dean up is a manually controlled operation and often Involves a nan entering cha raaceor for hand daaning of cha raaccor valla. Never planes vlch sophis ticated on-line computer syscaaa hava auccmacad soma of cha raaccor charging scapa and hava also aucomacad cha daaning eparados using solvanc and costing craaenanca. ZQ UCC 026569 Most planes receive VCM u liquid in tank cars and manually control the transfer to in-plane storage. The recovery of 7CM from polymerisation`vessels and achar vanes is usually automated, compressing and condensing vapors from a gas holder and recycling the recovered liquid 7Q1. The polymer strippers and dryers are usually continuous operations processing feed from large polymer slurry holding tanks and conveying the product to bins. Bulk shipments and/or bagging operaelons are done periodically. Maintenance of reactors and the equipment associated with them is simpli fied by the batch operation. Repairs can be prescheduled and carried oue as part of the clean-up operation In preparation for the next charga. Maintenance of the major equipment in the more continuous 7Q1 recovery, slurry stripping, and polymer drying operations requires a scheduled "turnaround", as is normally done in continuous chemical plants. Small equipment such as pumps, compressors tanks, and heat exchangers usually have spares installed in parallel so that repairs can be made without loss of production. Redundancy of this cyp# is specially important for equipment uaed to control 701 amissions. As discussed in Section 4.3, the prevention of relief valve amissions, of 701 is very dependent on the performance of the operating and malntanance personnel and on the development and application of effactive standard proce dures . 3.3 REGULATIONS ON 701 HUSSION TftCZt FVC PLANTS The owner or operator of a polyvinyl chlorida plant is required to comply with the requirements of Sections 61.54 and 61.63 of Title 40 of the Code of raderal Regulations as discussed below. Reector and Other Process Equipment through Scrisping The concentration of vinyl chloride in exhaust gases discharged to the atmosphere from tech reactor is not to exceed 10 ppm as indicated in I 61.64(a) 21 UCC 026570 The exceptions eo ehis liaie are inargeac-/ veneing .(covered below) and * raactor opening loss ~jhi.cn la tot co exceed 0.02} vinyl ahlorida/kg (0.00002 lb vinyl chlorida/lb) of vinyl chloride product, with eba produce determined on a dry solids basis. Manual vane valva discharga: except for an emergency vane valva discharge, chart is so ba no discharga eo eba acnosphera from any i vane valva on a polyvinyl chlorlda raaceor in vinyl chloride service. An emergency nanual vane valva discharge naans a discharge zo the atmosphere which could not hava baan avoidad by caking measures co pravanc eba discharge. Viehin 10 days of any discharga co cha acaosphara from any nanual vane valva, eba owner or oparaeor of eba sourea from which eba discharga occurs shall submit eo eba Administrator a rapore in writing containing Information on eba sourea, natur* and causa of cha discharga, eba daea and eina of eba discharga, eba approxinaca total vinyl chlorlda loss during eba discharga, eba method usad for determining eba 7inyl chlorlda loss, eba action ebae was eakan to pravant eba discharga, and measures adoptad co pravant fucura discharges. In ! 61.64(b), (c), and (d), ie is stated that eba concentration of vinyl chlorlda In all exhause gasas discharged co eba acaosphara is toe eo exceed 10 ppn (axeapt as provided la Section 61.65a) for the following vinyl chloride process equipment: from each stripper, from nixing, weighing, and holding containers preceding eba serippar, and froa the nonoaar recovery system. Ibis requirement does not apply to equipment that has baan opened, is out of opera tion, and see eba raqulsesent in Section 61.65(b)(6)(1) before being opened. Zanioaaae Following eba Seriooar The following requirements sat forth In S 61.64(a) apply to saissions of vinyl chlorlda eo the acaosphara from eba combination of all sources following eha serippar in eba plane procasa flow including bue toe liaitad eo, etnerifugas, concentrators, bland tanks, filters, dryers, conveyor air discharges, baggars, storage containers, and in procasa wastavacar. ucc 026571 la polyvinyl chlorida planes using stripping technology to control vinyl chloride emissions, the weighted average residual vinyl chloride concentration in all grades of 77C resin processed through the stripping operation on each calender day, measured immediately after the stripping operation is completed, may not exceed: (i) ZOOO ppm for PVC dispersion (emulsion) resins, excluding latex resins; (11) 400 ppm for all ocher ?VC resins, including latex resins, averaged separately for each type of resin. the above mentioned emission standards (1 and 11) also apply to PVC plants controlling vinyl chloride emissions with technology other than stripping, or in addition to stripping. Relief Valve Discharge Section 61.62(a) states chat except for an emergency relief discharge, there is to he no discharge to the atmosphere from any relief valve on any equipment in vinyl chloride service. An emergency relief discharge aeane a discharge which could not have baen avoided by talcing aeaaures to prevent the discharge. Such a discharge necessitates a written report to the Administrator within 10 days containing all of the necessary information concerning the dis charge. Fugitive emission Sources Section 61.65(h) prescribe* how the fugitive emission from the following seven sources should be controlled. 1. Loading and unloading lines: After each loading or unloading operation and before opening e loading or unloading line to the atmosphere, the quantity of vinyl chloride in all parts of each loading or unloading line that are to be opened to the atmo sphere la to be reduced so that the parts combined contain no 23 UCC 026572 greater chan 0.0023 m3 (Q.13 ft3) of vinyl chloride at standard; temperature and pressure. Any vinyl chlorida removed from a loading Una la to ba ducsad through a control system from which cha concancraelon of vinyl chlorida in tha axhauac gases doaa not exceed 10 ppm (or equivalent aa provldad In Sacclon 51.56). 2. Slip gaugaa: During loading or unloading operations, tha vinyl chlorida amlaalons from aach slip gauga In vinyl chlorida sarvlca ara to ba slnlalaad by ducting any vinyl chlorida discharged from tha slip gauga through a control systam from which tha concentration of vinyl chlorida In tha exhaust gases does not exceed 10 ppm (or equivalent aa provldad in I 61.66). 3. Leakage from pump, compressor, and agitator seals: Vinyl chloride emissions are to ba minimized from equipment seals in vinyl chloride sarvlca by tha following provisions: (1) on all rotating pumps by installing sealless pumps 4? pumps with double mechanical seals; (11) on all reciprocating pumps by installing double outboard seals; (ill) on ell rotating compreaaors by installing compresaors with double mechanical seala; (iv) on reciprocating compressors by installing double outboard seals; (v) on agitators by installing agitaeors with double nechancal seals, (or equivalent equipment and/or procedures as provided in S 61.66). If double gal seals or double outboard seals are used, vinyl chloride emissions from the seels ere to be minimised by maintaining the pressure between the two seals so that any leak that occurs is lata the pump, compressor or agitated vessel; or by dueclng any vinyl chloride between the two seals through a control systam from which the concentration of vinyl chloride in the exhaust gases does not exceed 10 ppm (or equivalent as provided in ! 61.56). 4. Leakage from relief valves: Vinyl chloride emissions due to leakage from each relief valve on equipment in vinyl chloride service are to be minimized by a rupture dlac between tha equipment and cha relief valve, by connecting the relief valve discharge to a process tin* or recovery system (or equivalent as provided in I 61.66). 24 ucc 026573 5. Manual venting of gases: Escape for an emergency manual vane valve discharge, as discussed previously, all gases which are manually vented from equipment in vinyl chloride service are to be ducted through a control system from which the concentration of vinyl chloride in the exhaust gases does not exceed 10 ppm (or equivalent as provided in I 61.66). 6. Opening of equipment: Vinyl chloride emissions from opening of equipment (including loading or unloading lines chat are not opened co Che annosphera after each loading or unloading operation) are co be minimized as follows: (1) Before opening any equipment for any reason, the quantity of vinyl chloride is co be reduced so ehat cha equipment contains no more chan 2.0 percant by volume vinyl chloride or 0.0920 m1 (23 gal) of vinyl chloride, whichever is larger, at standard temperature and pressure; and (ii) Any vinyl chloride removed from Che equipment in accordance with paragraph (h)(6)(l) of this section is co be ducted chrough a control system from which the concentration of vinyl chlorida in the exhaust gases does not exceed 10 ppm (or equivalent as provided in I 61.66). "Equivalent Equipment" and Procedures Section 61.66 states chat upon writtsn application from an ovntr or operator, the Administrator may approve use of equipment or procedures which have been demonstrated to his satisfaction co be equivalent in terms of reducing vinyl chloride emissions co the atmosphere to chose prescribed for compliance with a specific paragraph of this subpart. For an existing source, any request for using an equivalant method as the initial maasure of control Is to be submitted to the Administrator within 30 days of the effective date. For a new source, any request for using an equivalant method is co be submit* ted to the Administrator with the application for approval of construction or modification required by S 61.07. 23 ucc 026574 SECTION 4 REACTOR RELIT? DISCHARGE EMISSIONS 4.1 SAJZTT AND OPERASILITT CONSIDERATIONS the rupturs disc/relief valve (3D/RV) system on F7C reactors is there to prevent over-pressuring of the reactor to the extent that the vessel ruptures. If this rupturing should occur, personnel in the area would be exposed to serious injury and other equipment nearby would be damaged. Since several reactors are generally near each other, one such rupture could esca late into a series of incidents. The effects are likely to be catastrophic. Existing regulations require safety relief devices on such vessels and strictly define the requirements for their installation and for both upstream and downstream connections. Both these legal requirements 3nri insurance company requirements for safety relief are strictly enforced. There is no likelihood that companies would accept the principle of connecting PVC reactor safety relief valves into headers which connect to gasholder and other collection or destruction systems. The discharge of large quantities of VQf vapor into the air is itself inherently unsafe. The flammability limits of VO! in air range from 4.0 percent to Z1.7 percent by volume. When the relief valve opens, a VCM vapor cloud of up to 130 m1 VQi/m* reactor volume (17 f?*/gal) may exit into the air and, under certain maceorologlcal conditions, ths VCM concentration in a cloud could remain at flammable levela for long distances. Although no cass of a 7Qf smiasios explosion Is known, similar flamablt materials have caused explosions with injury and damage from such clouds. This safety consideration, in addition to the known carcinogenic nature of VCM, justifies expenditures to minimize the frequency and amounts of relisf valve discharges to ths atmosphera. 26 ucc 026575 since oxidation of 7d produces a 3trass containing hydrochloric acid, chlorine and phosgene jasee, is will be necessary ca caustic scrub chs prod uce ju from ineinsracors, catalytic oxidation units and hollars. Catalytic chlorination reactors would require condanaar/abaorbar trains with collection of produce and craa&sne of vent streams to prevent further air pollution. Although haac raesvary from these oparaciona la possible, the low frequency and shore duration of eha occurrences indicacaa chat sort energy would ha expended for aquipoanc manufacture and aracclon chan could ha recovered in many years of operation. Such equipment sized for the large flows expected from reactor relief valves would not ha operabla for casas of minor events. Previous cose estimates have shown thae 7d destruction systems with heat recovery for high 7Q1 concentration require higher capital and operating coses than containment and/or recovery systems. The destruction systems lack, theadvantage of recovering cha 7CI as a useable material and cha haac recovered is not usually ae a useful level of energy, leaccor relief discharges are of very large magnitude over a shore period of tine and are accompanied by some unusual conditions if they axe truly "emergency" discharges, escape for a flare, the use of destruction systems, which involve a chemical reaction (oxidacion, addition or diaproporeionacion of cha 7d), requires instantaneous start-up of large complex pieces of equipment under upsee conditions which are demanding the attention of ell personnel in the plane to control the production equipment then in operation. "Larins in a chemical plane is always a last rasore approach. Its effects on the environment era about the seats order of magnitude as a 7d spill. In face, it may b versa than spills whan the high heat release, high noise level, and eexle ea well as noisome fuses produced ere considered. 27 ucc 026576 4.2 DISCUSSION OF EVENTS 4.2.1 Causes and Sffacts of Relief Discharges The two most frequent causes or relief discharges from PVC reactor are 1) too much liquid or the presence of aoncondensable gases in the reactor caused by errors in Instrumentation and improper charge operations, and 2) high temperature in the reactor because of inadequate cooling. Each of these results in high pressure in the reactor with substantial Vd emissions to the atmosphere when the relief valve opens. Since VQ1 liquid expands an unusual amount (up to 20 percent) when heated to reaction temperature, an overfilling of the reactor may not be evident when materials ars initially added. As tht reactor contents are heated toward reaction temperature, expansion of VQ1 liquid takas placs and the liquid level rises. When ths liquid reaches ths reactor top, hydraulic pressure will open the relief valve. Overfilling of the reactor can be caused by a water or Vd charge meter error, a liquid leaking into the reactor through a block valve, or wash wacsr not compltcsly drained before starting the charging operation. The presence of aoncondensable gases in the reactor will also cause high pressure to develop. Since the partial pressure of VQ1 and water vapor in the reactor cop will each reach chair vapor pressure, a multiplying effect occurs. Far example, if 50 percent of the vapor spaca is noucondansabl gas, than the total prassure will be twice the sum of VCM vapor pressure and water vapor pressure. Table 4-1 shows the density and vapor pressurs of liquid Vd at various cempsraeurss. Ths operating procedure Is to chargs water with additives of suspsnslon agents and initiator to about 30 percsnt of rsactor volume and then reduce reactor pressure to about 0.05 atmosphere using a vacuum pump. Some vaporization of ths wster occurs to sweep noncondsnsables out of the system. With the reactor blocked in under vacuum, ths liquid VQ1 is added to bring the total liquid level to about 30 percent of the reactor volume. As the reactants 23 Ucc 026577 lasts 4-1. 7AF0R PRESSURE AND OENSITT OF 7Qt lasporacur* *C *7 Vapor Praaaura ?sla -U.3 0 37.3 31.3 63.4 79.4 93.3 7.14 32 123 130 173 200 oo 14.7 23.1 33.3 119.3 163.0 223.2 293.4 Danaicy 3/nl 0.96 0.94 o.3a 0.33 0.32 0.73 0.76 29 ucc 026578 are heated to reaction temperature, liquid expansion raises che liquid level to about 90 percent of the reactor volume so chat the concentration of "noncondensables in the reactor at liquid VCM entry la increased as much as 5fold. Since the combined 701 and water vapor pressure at the normal operating temperature can reach about 10.2 Ad (ISO psla) and SO/3.7 systems are often sec ac about 13.2 Ad (195 psla), the presence of only 25 percent noncondensables in the vapor space say trigger a relief discharge. This would occur if chere were 5 percent noncondensables in the reactor vapor space at start of the liquid 701 charge. The source of noncondensables are 1) gases not removed by the evacuation, 2) gases dissolved or entrained in 701 liquid charge, and 3) leakage pest block valves into che reactor between vacuum treatment and heat-up completion. A failure to complete the purging of noncondensables is likely unless carried out thoroughly, foaming of che water during vacuum purging can carry additives out of che systems and cause problems with polymer quality. This makes it difficult to get a thorough purging without careful operation. The cemperaeure at which che sum of che vapor pressures of 7Q and vatar may reach reactor relief valve discharge pressure settings, even with no noncondensable gases present, is about 72"C or 17*C above che normal reactor initiation temperature of 55*C. The polymerization reaction is exothermic and cooling water-flowing through che reector jacket removes this heat. The polymer formed is insoluble in both monomer end water phases and appears as a solid parciela suspended in the vacar-VQi liquid mixture. As che reaction proceeds, che polymer tends to form e costing on the wells reducing che heat transfer effectiveness. Ac some point above the 50 percent conversion level an auco-acceleratlon of the reaction rate occurs- with Increased heat evolution. If an increase in temperature occurs ec any time, the reaction rate and heat evolution will increase. In normal operation cold waear is used in che reactor jacket to provide a larger temperature differencial between che reactor contents and the jacket as needed to control the reaction temperature. Heat transfer effectiveness depends on vigorous agitation and ample supplies of chilled water. Any unusual reactor fouling or loss of agitation or 30 UCC 026579 inadtquaclas la csol-lag wacar supplias will allow rapid haaciag of cha raaccor concancs and cha raliaf valva 317 opan from cha rasuidng arcassiva pressura in cha raaccor. Tha loss of agination is of nose conearo sinea haac cransfar is significantly raducad and supar-haacad 7d from iowar pares of cha raaccor will flash suddanly as ic is aovad slowly coward cha liquid surfaca by convacdon curranes. In chis casa a vary rapid risa in raaccor prassura can occur. Vhaa cha raliai valva firsc opaas on a raaccor, a rapid flow of vac 7Ci vapor, 7Cd liquid, and liquid wacar goas chrough cha valva. Tha oacarial orssane is oaa vapor phasa, cwo liquid phasas and possibly ona solid phasa, sonatinas vich raaceion procaadisg co produca aora solids and haac. Ac cha ouclac of cha valva, liquid 7G4 flashas as cha prassura Is radnead wlch cool ing of chs dsrura. da 7d boiling poiac ae aatospharle prassura is balow -L2*C (10*?) and uadar soma condicions wacar any ba frozan in cha liaas co maka anochar solid phasa. Ganarally, cha duradou of a major avanc is 10 co 13 aiaucas and cha flow raca of 7d vapor is asdnacad co ranga iron 2300 kg/ ds (a 5000 lb/da) co 50 kg/da (* 100 lb/da) ovar chis parlsd dapandiag on raaccor slza and how such aononar had alraady polymaricad bafsra cha raliaf valva opanad. In cha casa char cha raaccor is ovarfull, cha hydraulic prassura which spans cha valva is quickly rtiiavad by liquid and vapor flows and llccla or no polymar is prasaae. Tha valva ganarally rasaaes lcsalf wlch only a snail spill rasuldsgj howavar, if cha valva is of cha cypa which ranaias opan, a larga voltaa of maearlal condnuas co flow uadi raaccor cestparacura and prassura la raducad co a low laval and oparaeors can manually scop cha flow. Sidlarly, in cha casa of noneondansablaa in cha raaccor, chasa ara also quickly purgad, carnal prassura Is obtalnad, and only a raladvaly snail amission will rasulc If cha raliaf valva rasaaes lcsalf. Viih iaadaquaea haac roevsl, cha rising canparacura aggravacas cha sicuadon and a najor dlscharga ganarally rasulcs unlass cha raaceion is in 31 ucc 026580 the last stages, e.g., above 30 percent polymerized. Ac this high conversion level, most of the 7CM has been consumed and since the polymer density is higher (up to twice) chan the monomer density, the liquid level in the reactor is lower and hence there is lass entrainment of liquids and solids with the vapors. Under reacting conditions, essentially all of the remaining VC21 will be vaporized unless the reaction is stopped quickly. This can only be done with vigorous agitation and quick addition of proper chemicals. 4.2.2 Fault Tree Analysis It is desirable to foresee the potential causes for actuation of a reactor relief valve and to provide effective methods for reducing the prob ability of this type of occurrence. Several techniques have been developed and used within the chemical industry to describe and explain the events' which can cause a relief valve to lift. A common approach for analyzing complex systems, such as the batch reactor, uses logic models which are con cerned primarily with the logical (on, off) relationships between variables and events. Two well known and publicized techniques which utilize logic models are: 1) failure modes and sffacts analysis, and 2) fault tree analysis. A datalled discussion of these two types of analysis is beyond the scope of this report. However, an example of fault tree analysis appliad to a small portion of she reactor systme will illustrate soma of the features which may be applied to the entire process. A simplified schematic of a polymerization batch raactor in Figur 4-1 shows the individual reactant charging systems and the basic control instru mentation. The primary mode of controlling the reactor pressure and thereby prevent the relief valve from lifting is to control the total mass of material 32 UCC 020581 38S920 000 Figure 4-1. ViUyiuiirliutloti reuctoi'. charged to the reactor and :ha reactor tamperacure. Vinyl chloride monomer (Vd) and water containing dispersants, initiators-, and stabilizers are charged separately to the reactor. Reactor temperature is controlled by continuous stirring of the contents and regulating the flow of cooling water or steam to the vessel jacket. In the event the primary controls fall to function as designed, an automatically controlled valve may release excess pressure to an auxiliary venting system and/or a dump tank on signal from the controller. The first step In performing a fault tree analysis is to define cha system and then to define the faults or events to be investigated. For the system shown in Figure 4-1, the fault or top event to be Investigated Is the lifting of the relief valve in stream 1Q0. A. simplified diagram of some of the system interactions and control loops is presented la Figure 4-2-. The relief valve is actuacsd by vessel pressure, which is in turn affected by ~ 1) the mess of material charged, 2) the temperature in the reactor, and 3) operator action. As the logic progresses to the next level, the system and interactions became move complex. The object of fault tree analysis is co sec up these interactiona in a managable format suitable for analysis. The depth of analysis can and should be appropriate for the problem under consideration. Initial studies can be tailored to include only general items such as those shown in Figure 4-2. As more detail is needed, ch analy sis is expanded to include additional features. A level of analysis can quickly be reached which will be quite complex and will require considerable time and effort for manual development. To Illustrate this type of analysis, visualize only the control system for charging vinyl chloride monomer co the reactor as shown in Figure 4-3. This consists of a flow control loop which is camperature compensated. One possible fault tree for this loop la presented in Figure 4-4. This tree is not complete since items such as loss of elsctrlcal service, loss of instrument air, etc., are not yet included. The possible initiating faults 34 ucc 026583 'i UAUIUAI CUAIIOJe lOIttACIUH Lu CJ - Slllt AM HU fllOMHOUHE I e - mtsauttt M - MASS t - ItMl'tllAlUiU: figure 4-2. ftwctuJl tliugrwjili of* reactor uyuteM, M UU t ucc 026584 -- SIHEAM lOENIIFKAIKkN SAME AS SMEAM4 JttULtt t ucc 026585 Figure 4-3. Temperature compensated flow control loop. ucc 026586 figurt: 4-4. ' ' A= ut ItaulL. ictsti fur flou'coutfut fuoji. due co mechanical failures are easily identified in che lefc hand portion of chis figure. The right hand chain reflects potential errors in instrumenta tion setting or configurations which might be overlooked. This tree should be expanded co include all possible events that may occur in che VCM charg ing system. Similarly, chis approach should be applied co che water charging system, the reactor casperature control loop, the cooling water supply loop, che agitator, etc. Ifter the fault tree is defined, the next step is co develop a frequency of occurrence for each event. A valid occurrence rate can usually be found for equipment events in one of the many U.S. data bases for each of event. If data cannot be found then additional analysis can usually be undertaken to deduce realistic occurrence .rates. The interaction of che human operator with the system may well be much more difficult to quantify than equipment failures and may produce results which are misleading. Herein lies ons of che major objections co this type of analysis. It also is why, right or wrong, many operating systems are dssigned to minimize che human elements. Once che occurrence races have been established, then evaluation of che fault tree can proceed co che point where initiating events which would cause a relief valve to open, or other cop event, can be ordered by frequency of occurrence. Additional analysis can also define probable severity, l.e., the consequences of each occurrence, and then define which initiating events must be avoided, changed, or do not require alteration. Additionally, che impact of alcaraclone can be quickly evaluated. The fault, tree analysis can thus be utilised co highlight system weak nesses which might not otherwise be apparent. The rasules of the fault tree analysis can be used co prioritize che available effort and resources in che most effective manner to prevent che occurrence of the cop event through equipment and system design, operator and maintanance personnel training. 38 ucc 026587 redundancy, and development of airactive operating procedures. Tor a sore thorough discussion of fault tree analysis references in Section C in the bibliography, Appendix A, are suggested. 4.2.3 Operation and Maintenance Many reported ventings have been ascribed to operator error in charging the reactor and in inprnper adjusaient of controls during operation. Mainte nance, through failure to coordinate repair work with operators, nay cause ventings when operating equipment is opened. Z?A has indicated that nose operation is considered to be a "controllable" factor as related to venting .of reactors and other equipment In VC& service. To aid in assessing the cause of a reactor venting and to prevent similar occurrences in the future, it is suggested that the data listed in Table 4-2 be supplied by the plane_ management when reporting such an incidence. Adequate supervision of a production unit implies that each van involved in the operation is known to be trained in the work he is to do and is ready to do It properly when he reports to vork. Anytime a nan does not do his work properly, this supervision has failed by either giving the nan too nuch to do or by not having the nan properly equipped to do the job. Records of training need to be established for each man utilized in operations and periodic testing should be carried out to establish need for additional training. Evaluation of performance needs to be nade regularly on each nan. Supervision also needs to contact each man daily before he goee to vork to be sure he is in condition to carry out his dutiss properly. Eepeirs of equipment suet be thoroughly done as needed but only vhen the equipment is available for vork to be done on it. A checklist of action before dismantling the equipment should include confirmation by operations that the equipmsat is available and Is not in service. This type of coordi nation is standard practice In che chemical Industry. 39 occ 026588 TA3LZ 4-2. DATA. NEEDED FOR RETORTING OF VENTING OF FVC REACTOR 1. Personnel - Each operator, maintenance man and supervisor Involved a. Names, training history, work history (experience) b. Date and time reported for work - day of occurrence c. Condition at time reported for work - physical/mental d. Hours worked at time of occurrence a. Date and times start/end work for 7 previous days f. Duties g. Dates of other reactor vents involving them during the previous 12 months 2. Operating Data - Reactor involved a. Dace and time of occurrence b. Date and time charged - quantities of each material , c. Approximate Z polymerized at venting d. Length of time vent continued a. Reactor temperature and pressure at start of occurrence f. Copy of temperature chart, pressure chart, and log sheet g. Actions taken to prevent venting h. Deviations from standard procedure 1. Status of ocher reactors at start of occurrence j. External conditions - weather, utility supplies, ocher upsets k. Quantity of VCM vented 3. Cause of Venting Detailed chronological description with exact timing of each action in preparing, charging, starting up, and operating this charge to and after Che occurrence in the form of sworn statements from each of person nel listed in l.a. above. 40 ucc 026589 A.3 TSSTESTIQN OF DL3CHA2GZS TO AEfOSSHEtS An emergency relief valve discharge is defined is, 40 CF3. 61.55(4) as one which could aot have been avoided by caking measures co prevent cha dis charge. SI baa suggested chae a combination of proper instrumentation co dacacc upaae conditions, a gasholder and an automatic inhiblcor solution addition system can eliminate vinyl cblorlda lose fron chla source in enlacing planes. There axa, however, several addlelsnal operating and aaiacananca factors ebae should ba consldarad co anaura chae ehara ara oo relief valve dlachargaa as dlscuasad in cha following paragraphs. ^nmt syseass far addidou of retardant and short-stop solutions co cha reactor require avacuaelon of cha eharga manifold, naasuramane and siphoning of cha soluelon ineo cha manifold and chan opening cha nanlfald: co cha raaccor co allow cha soluelon Co drain ineo le. A considerable clan Is required co carry oue chase actions and in cha case of shore-scop addition, cha oparaeor may have co locaea and gee approval of a supervisor before pueelng cha soluelon ineo cha reactor. A procedure for adding cold water directly co cha reactor nay ba pare of an operator's function but cha beat content of water which can ba added provides only a short (3 10 minute) delay In cha raaccor temperature rise. All planes have redundant power supply systems either locally at cha reactors or general for cha entire plant. Ic Is imperative chat cha agita tors, cha cooling vatas supply, and cha inscmencacion continue co ba operable co prevent a major event release of 701 from reactors. Hany operating planes have computer systems co evaluate eransmlcrad signals from the reactors and alart operators of any deviation from normal conditions as they develop. Soma of chase cake aucomacic action co add reeardant and short-stop solution co the rsactsrs when high pressure, high casparaeura, or unusual viscosity conditions are indicated. Some plants also have vent lines with knock-out tanks connected co recovery 3yscams 41 ucc 026590 separata iron cha rupture disc/relief valve 37scams which procecc the reactor. These auxiliary vent lines mayhave relief valve settings below the rupture disc/relief valve settings or they say be automatically activated or signal from a controller. Some plants also have spars slurry hold tanka to which a reactor charge can be dumped before control of the reaction is completely lost. Such a dump can be automatically activated and the tank may have chilled water with short-stop solution in it. The literature indicates that at lease one plant maintains a stored volume of chilled (43*?) water for use in reactor jacket, cooling when either excess heat is generated in the reactor or an unusual fouling condition has developed which reduces heat transfer and the normal cooling water in the jacket can he replaced in less than S minutes by the chilled water. Literature also indicates technology development using multiple initiator systems which give a high initiation rate early in the cycle and a slower initiation race when auto acceleration normally occurs. Whether this tech nology is available for license was not determined. Its effect is to maintain near-constant reactor temperature and pressure. 4.3.1 Instrumentation and Automation Almost all plants have an automated cascade temperature control system for the ?7C reactors which adjusts jacket temperature to minimize reactor temperature rise. The reactor temperature Is measured by a sensor usually mounted In the reactor baffla. This sensor gives e response to changing temperature and is subject to giving low readings when polymer collects on it. Whan clean, the error can be near r2*P but under fouled conditions the error increases on the low side. As rtsctor ttmperaturs rlsss due to lowered heat cranefar to the reactor shell, this temperature measurement will lag considerably behind the actual reactor temperature due to the polymer buildup. When polymer is being formed in the reactor, the reactor pressure is a better indication of reactor temperature than is the temperature measurement. 42 uco 026591 Systems vara designed far instrumentation and automation of earcaia operations valid can prevent relief discharges cram reactors. Ida over charge casa and/or noucondanaabla caaa ara pravancad by comparing rsacrar pressure during heat up co the vapor pressure of VGi ac the casparacura indlcacad far the raaccor and vanelng of a small amount or gases co the 7G recovery ayscam or dumping slurry co a cank if prasaura is coo high. Ida inadequate cooling caaa is pravantad by obsarvlng cha raca o prasaura rlaa on cha raaccor and comparing this co a standard condition or cha scaga of raaeclon with addition of racardanc or short-scop aucomacically as naadad. Ida High vlseoslcy casa is pravancad by aonlcorlng agitator power and comparing chis co a standard vied addition of short-scop automatically baiora cha agitation and haac transfar caasas. For cha aulei-reaccor syscass usad in PTC production, a central control procaaaor and cha alternative of many locally souncad single-unit processors vara both evaluated. Coses far sensors, transmitters, control units and control equipment not already in place vers included in the astinatas. For the central processor, casts vers based on a commercially developed and competitive unit vhlch required little development work to apply it on the 77C reactor.control project. Cda coses of locally nouncad single unit processors vers based on known hardware co do the job but required sofevare development of sajor magnitude. Thera may be already developed controllers of this type for vhlch development costs would be such lass but the only known equipment of this cyps are proprietary with PVC manufacturers. Poten tially , they nay be obtained by license agreements. 1.3.1.1 Central Processor-- The central processor will use data stored in memory to decide whan or if modifications need to be made to the reactants. These data will represent not only measurements made on typical reaction cycles but also thermodynamic calculations of the reaction cycle. The central processor should be much 13 ucc 026592 mors responsive and accurata In assassins the reaction condition and in responding to any problems chan a human operator. ' A diagram of the central processor is shown in Figure 4-5. The central processor will be redundant such chat if one unit becomes inoperable the second one can be brought on line immediately, if not auto matically. The system will also be powered from a nonintarruptable power supply so chat in the event of a power failure the control will remain oper able. The historical data may be obtained by monitoring and storing reaction cycle parameters using che central processor. The central processor will be capable of acting as a data logger. It will also be able to Indicate, before caking action, any reactors expected co have problems so chat they may be watched more closely. The Teletype keyboard and prlatar wlll.be the input/output device for the procesaor. The keyboard will allow for requesting information, etc. The printer will be used by the computer to output data as well as any specific information requastad by the operator. The disc may be used for progrsm modification or data storage. 4,3.1.2 Processor for Single Reactor-- The processor for the single reactor will monitor the status of four input signals versus time. A diagram of the single reactor processor is shown in Figure 4-$. It will provide the proper control signals to valves Vi-Vj to maintain proper control over the reaction. The control parameters will be developed by monitoring the same signals as used by the controller during actual reactions. This Information will be uaed along with ehermodyuamic calculations co develop the guidelines used by the processor in its decision making procass. 44 uco 026593 At. At ucc 028594 A.C. Helui Chilled Utter * ucc 026595 I Figure 4-6 . Single reactor processor. the operator will still control she process so long as is stays In 3axa Units. the device will control she process only whan is gasa outside she proper bounds. The unis will provide switch cloauraa so activate lights as she oparsor'a station so iadicatt first a problem sicution la laaisasc and chan a second switch closure and light so indicate sha control actlvasad. These units will nos necessarily provide algnala suitable far daca logging. 4.3.1.3 Svstam Comparison-- The interesting ouccoms of sha coas analysis la chac sha individual reactor control system (wish aora chan 4 reactors) cases more chan sha cansral concral unle which has highar redundancy and nan? more faacures. The aujar factor in Shis high ease is sha rasaarch and davalopmanc cases. Table 4-3 shews comparative coses of csneral and lacal units. Although sha local unis is cansidarably lass complex Shan sha control unit, iss controlling function rust 'oa sha sans. "The safswara design is noc such easier for she remote unit than the central control unit. In fact, is is actually greater because the complete operating system rust be designed. The central unit data acquisition routines have already bean designed. The only hardware desi^ coaes in the central system will bar sha configuration of the option and checkout to be certain that shay function properly. So real hardware davalopmanc aust be dona as in sha case of sha local unit. The central system unit, because it already has daca acquisition and logging capabilities, say be brought on line as a daca logger. Than as sufficient daca are obtained, it nay be phased in as a controller. The local unit will require the use of a daca logger since it will not inherently have daca logging capability. This will be an extra expanse noc required by she cansral unit for development of controlling roucinee. ucc 026596 TABLE 4-3. COMPARATIVE COSTS* OF LOCAL AND CENTRAL UNITS FOB. PVC REACTOR CONTROL Source Local Unit Central Unit (2 with 1 on line) Development (Hardware) Software Development Installation TOTAL COST $35,000 $53,000 $5,000/Reactor $113,000 + $3,000/Reactor $10,500 $17,500 $ 95,000 + $3,000/Reactor $123,000 + $3,000/Reactor Maintenance (Routine) Instrument Technician Service Contract 1 hr/wit/unit $100/yr/unit 4 hrs/wit $6,000/yr *Deeeaber 1979 Dollars 43 ucc 026597 Tha wo fsaturas which could aaica eha local unie aors cose .sffaceiv* ara not ueilizad la am situation. Conduit and cabling esses ara aoe saved because aouintarruptabla povas must ba suppllad eo each uale and signals oust also ba sane bask co tha control station. Toluata production vfaich could rscQvsr davalopmant costa la alao not usad bacausa only a ralativaly few units will ba built for an individual plant. Tbs local units will 'cava ssvsral disadvantagaa. Tha units will not 'cava eba laharant said cast feature daaignad Into ebam. They will caad to ba pluggad Into a tasting unit to daearmise chat ebay ara functional. Tha cantral unit will have a salt ease roucina. which will ba run pariodically. Ths cantral unit will ba abla to taka Itaalf off lina or could ba manually r^itag off lias in caaa of problaaa. Tba oebar cantral unit will icaaadiatsly taka ovar control* Tba instr*.aaneacian Indudad doaa not cava a laval alarm on tba raactor so doaa net provida adequate procaction from ovarfilling. It doaa provlda for procaction from oebar cauaaa. If davalopmane of a rallabla laval alarm is obealnad eban eba ovsrsll instrumaataeion systas would provida tba naadad procaction. Such a laval inaerumane would probably coat 36,000 par raactor as installad* Ona inatrusane company iadicacad succass in this aaasuramanc using a radioactiva sourea dacactad by ion chaabar sanaing. 4.3.2 la-niiVenting System Under most conditions which can load eo repcura diac/raliai valva emis sions, a ralativaly --^ amount of sacarial raaovad from tha raactor will pravant eha ovarprassura davaloping. Tbasa ara tha casaa of raactor over charge-, toncondansaola gasas in eha raactor, or moderate unexpected raaceion rata incraasaa and haae eransfar raduceians. An auxiliary vane and racovary or daatruction systas which is saparaea from eha amarganc7 syscam is a practical way eo pravant raliaf valva amissions whara a crca amargancy is not involved. 49 ucc 026598 Ths system or systems would consist of reactor vent lines with pressure control valves, a header, a surge tank, a condenser with liquid crap, a vent line with back pressure control valves leading to an existing gasholder or incinerator, a chilled water storage tank, with chiller and circulation pumps and pumps for disposition of material collected in the surge tank. Figure 4-7 is a flow diagram of a system such as this. 4.3.2.1 Reactor and Venting Dynamics-- Pressure rise in the reactor is the result of temperature Increases as it Is heated to reaction temperature and as the reaction proceeds. Both liquid volumes and vapor pressures are increased by the temperature rls * The rate of pressure rise is relatively slow (< 2 psi/minute) during normal heat up to initial reaction testperature unless an overcharge condition or noncondensable gases exist in the reactor. These can cause a rapid (> S psi/ minute) rats of pressure rise as .the reaction temperature is approached* Similarly, after reaction is lnitiatad and stabilized with normal cooling water on the jacket, presaure rises are alow (< 1 pei/minute) because of the heat capacity of the materials in the reactor and the continuous heat removal by the jacket. However, when reduction of heat transfer and auto-acceleration of reaction rate conditions develop, the heat evolution increases and heat removal dacreases resulting in increases in the rate of presaure rise. A computer program was dsveloped to simulate ths changing conditions within ths rssctor and ths flow through ths rslisf valve. It la assumed that the mount of PVC present is small so that ths flow through ths rslisf valve is in three phases t. liquid water, liquid 7(21, and gas. Ths rssctor effluent flashes across ths rslisf valve and critical flow (Sonic) is usually obcainsd. Ths program caleulacss ths hast generated by the polymerization reaction and that removed via ths cooling jaekac with provision for varying water jacket testperature. The quantity of liquid entrained in Che effluent flow la initially equal to the liquid/gas volums ratio In ths rssctor and as mass 30 UCO 026599 ucc 026600 Piguru k~l. Auxiliary vault fig aybUau leave* the reactor, it la reduced linearly co 13 by volume in the total flow. The Bange-Kutta technique is used to integrate the dynastic material and heat balances over time. Figure 4-8 shows the flow chart for this program. The governing equations, program listing, and case result printouts are in the appendix. The relief valve discharge simulation program was run for 10,000 gal and 20,000 gal reactors. The results are summarized in Tables 4-4 and 4-5. Cases 3 and 4 are simulations of discharges due to reactor overfilling and they compare the effect of Introducing chilled water to the jacket with maintaining a constant (90*7) jacket temperature. In the five other cases, discharge is due to an axcessive reaction rate of 40Z/hs Initially.' In- _ cases 2, 6, and 8 chilled (48*7) water is introduced into the cooling jacket, while in cases 1, 5, and 7 it is assumed that the agitator failed and no cooling occurs. For the cases with 40Z/hr reaction race and no cooling (cases 1, 5, and 7) the pressure rises co a maximum of 3 pslg above the discharge pressure in approximately 30 sec. and then declines. When agitation la lost, higher pressures may occur in a shorter time due co sudden flashing of material broughe from the lower pert of the reactor by thermal circulation. Whan eha reactor is vented through a pressure control or relief valve, the Initial flow la a vapor/liquid mixture with some solids possibly present. Liquid VQf flashes in ch# valve and the inertia of the unfleshed material uses up the availabl* energy. In cases 1-4 ths initial flow is assumed to be 962 liquid by volume, while for the overfilling cases ths initial flow is entirely liquid. Although in normsl operation the liquid level in ehe reactor Is at the jacket level and entrainment may not be this large, it must b* considered in the dynamic analysis. In all cases chars was a linear reduction co a *nTM of 13 liquid entrainment as the amount of liquid 52 ucc 026601 LN (4 FIguru 4-tt Flow diugriui tor the readtur ami vent dyiunuicu. ucc 026602 bxtl* Urn* ll1 II 1* 1* 14 TABLE 4-4. SUMMARY OF REACTOR CONDITIONS AND RELIEF VALVE FLOW KATE CALCULATED BY SIMULATION FROCKAH (10,000 gal Reactor) ja u 1 (aallH iit4u4 i IuWbIb *f * ' uu >44.1 >44.1 44 44 1.4 1.4 Et-wlul I'aHJtl ItMIJI JhiM JAC lot iRlilal JhUUI Ual of *(* T*a> Tuaf *** *t lt> 141.4 - 1*4 141.4 MI-44 mm *4 *4 n> MI-44 HaiIbm PrvAbUfK MU*| VWA Ml Twf IlM *r 1* 144 in 4.1 144 14) 4.4 111 ll> 4.1 l> m 4.4 Maalau* Vbjwf fitH* i*i tim 14 n|Mb Ib >1.1 4.1 >4.1 4.1 11.4 1.4 11.1 1.4 Total MM Ui u14iuwdli 1.4* Ml 11.4 11.4 Talal VOI *** 14ualiul m*U 111 1*1 1** 1*4 * TABLE 4-5. SUHHAKY OF REACTOR CONDITIONS AND RELIEF VALVE FLOW RATE CALCULATED BY SIMULATION FROCKAH (20,000 gal Reactor) Lana MkiiIb liw im* CmIIm* JaiUI III Iib/in *r 1*101*1 MU MU I/hr ___ Bc-atmr CuoliLlBM l*lti*l 1*1Jaiiti lll Uit Haul fuaruu lewp luy *r 1lUalBiM fuaitua mJ tvmr )aw. T.r TIh Ml* i- bIb Maalaua Vaiwf IImi 14 4i* Mlt/aU fiat *1* fatal tfCtf II' M14 iMttaial TaUl VO* v*j 14milled mU > HI 4.4 44 m 144.> - m 114 4.4 114 4.* 1.4) 411 4W 4*1.1 44 m 144.4 ta-44 114 14* 4.1 144 U. 1.41 414 1 44 4.1 44 ii > 144.4 - 111 144.1 4.4 111 4.4 1.41 IU 4 1*1.1 ....................... 44 m ---1--4--4-.1----4 L *4-44 -- -J IIS 141.4 4.4 fr_ ----"---J HI* 4.4 1.44 111! -- -J - -- --- L*. J l ucc 026603 removed totaled to the volume of the raaecor heed. la ell cases, e period of up eo two minutes of venting was required ro achieve a significant VCi vaporisation rate in the reactor, depending upon che relief valve area, "or a nozzle area of 10 ial/10,Q00 gal (cases 1, 2, 3, and 6), che vapor race into che header of 30 to 33 lb aole/min per 10,000 gal was achieved in less chan one aiauce. If a higher auxiliary relief valve pressure setting is desired, a larger nozzle flow area, surge tank, and condenser must `o used in order to 'seep the pressure from rising above chsc of che safety relief vslve. Conversely, choice of a lover discharge pressure permits use of a smaller valve area and recovery system. The simulation program enables one to select a discharge pressure and flow area which are most suitable for a particular design. In addition, the program gives a time history of che conditions within che reactor which Is useful in determining when the relief valve should close. :_ The 7CH liquid entering the valve is flashed and goes to ths vase lines and headers wish ths gasss which ancarid ths valve. The calculated vapor race leaving the valve for the initial 961 liquid entrainment (first ninuce) is about half che vapor race for che IS liquid entrainment condition. This,indicates chat entrainment contributes to the stability of che vent system rather then che reverse. Sovsver, since entrainment ray not be severe depending on che level in the reactor, vent system dynamics rust be based on che maximum possible vapor flow leaving che valve at che inception of the venting. The vapor leaving the valve peseee through the vent line into the header and then into che surge tank. The volume of this tank seeds to be based on che time needed to actuate che chilled water flow to che condenser and to reach e stable operation. The simulation program output includes the quantities of 7Q liquid and vapor amltsad into ths recovery system at specified times, which are accessary for sizing the surge tank. 33 ucc 026604 4.3.2.2 Design 3asis--- The design of an auxiliary relief system can be based an results of the computer program which provides rate of pressure rise in the reactor and rats of venting from the reactor. Using the most adverse conditions of reaction rats and heat transfer, the pressure setting of the auxiliary relief valve which will prevent the rupture disc/relief valve from being actuated is determined. It should be noted that several minutes delay may occur after the auxiliary relief valve opens bsfors significant 701 vapor gsneraeion occurs inside the reactor. The auxiliary vent valves, lines, hesder, surge tank and condenser are sized based on the vent rate of liquid and vapor leaving the valve. The maximum vent flow usually devtlops after entrainment Is reduced by the lowering of reactor level which can cake as long as 2 minutes and depends on the valve size and initial reactor level. In order to ensure smooch operation of the auxiliary vent system, the pressure control valve on the vent lines may have to be slow opening. The pressure reduction section of the vent line may also have to be a special design transition piece of equipment such as a flaw nozzle. A motor operated ball valve which has a variable speed drive will probably provide a sufficient solution to the operating problem. The surge tank provided should be sized so that the pressure will reach 30 psig in the surge tank after more chan 1 minute when a venting starts with no entrainment and in about 2 minutes with worst case liquid entrainment. These times will be lengthened some by the condensation which should begin at about 40 psig. There should be adequate time allowed for the large pump to be started up and chilled water eo flow at the desired race into the condenser. When the resctor pressure is reduced, the auxiliary vent valve should dose. The vent system then should stabilize at about 25 psig. tfacer/polymer slurry should be pumped out to a slurry hold tank and liquid Vd can be either pumped to a recovery tank or allowed to vaporize slowly to the gasholder, the 36 ucc 026605 7d vapor recovery systems, or cha incinerator at a 3lav race as desired. The quantity of 7G and vatar co b expected can a a determined frost cda computer program. In a standby condition the equipment 3bould ba aaincained at 1 psig with a nitrogan or 7d vapor purging through cha small bypass on cha vans llna. Tha condansar and chiliad water tank ara maintained at cha 20*? eeaparacurs by cha slow vatar circulation through cha aquipmanc and co cha chiller. This circulation should ba dasignad co racovar cha chiliad vatar scoraga vithin 2d hours aicsr a pariod of vaneing has occurrad. Provision for pariodic or continuous caustic flushing of tha haadar nay ba naadad as a safacy factor and tha ''short-stop", naadad in tha surga tank, say require pariodic raplacaaanc. 4.3.2.3 Auxiliary 7nc Capital and Operating Costs -- Tha aquipmant shown in Flgnra 4-7 can ba sized using data from tha raactor and vane dynamics computer program. For capital tselaaclng purposes, all tha valves, lines and tanks handling 7d vara assumed co ba stain!ass staal materials. Tha vertical down flow exchanger vas assumed co ba carbon 3tael shall with staialasa tubas and heads. Tha vstar pumps, lines, tanks and chiller vara of carbon staal saterial. Table 4-d shows cha estimated capital costs par 1,000 gallon of reactor capacity and values indicated for a plant using 10,000 gallon reactors. Tha accuracy of chase estimates era =301. Operation of tha S7sc requires one hour daily far a nan to check tha flows, levels, and temperature of tha systn. It will, periodically, taka a full 24-hour shift position co return cha.unit to operational scarce after a significant eaisaion occurs, which nay ba as often as 3 co 20 times/year. Vlch the overtime requirement, about 1,000 nan hours/year vara estimated. 37 UCC 026606 TA3LE 4-6. ESTIMATED CAPITAL COST FACTORS AND COSTS FOR AUXILIARY TENT WITS CONDENSER (Dcafltbr 1979 Dollars) Caac Faacar* t/1000 gal 'Jain* tijfic 10,000 ial* Saaacara A Saaatar Xalaaaa and Callacclaa Syaeaa Ai Surga tuk A* Fua? aod Hacar Tsui laacallod tqulpaaac A| Flplot A* tsacrunaaca, Caacrol Valvaa aad laiacy At Suildlat aad Sica Sovalapnac Ac Tocai Fhytlaal Caac S 61,000 3,130 V.' 5 A| + At 7,030 V.*X 2,700 V***I 0.22 (A, * At) T ~ 419,300 13,300 * 433,100 224,300 63,200 93,700 L. IWiM9 3 Caadcaalaf Syaeaa 1| Caadaaaat Si SaMiwctla SCIC" Si Auxiliary Vaaaala (puapa, eadka, aacbaafart. aca.) $ 64,200 ' 12,600 V-' 26,600 * 1 332,000 63,000 106,700 Taeal laacallad Xaulpaaac s. F'-pln* (wear liaaa, vast Uaas, udllty) B* loacruaaacaciaa aad Salary s Sulldlnia aad Sica Oavalapaaac St Taeal nvyalcal Caat S Si It + Sf 39,300 * 11,100 ** 0.22 (B, St) 3 I tS, - 3. ^ s 301,700 236,900 34,700 3 110,400 } 903.700 C Cartload Syacau Taeal Fhyaloal Caac Q Eailaaarlaa aad Caucrueclea (33X3 A# + St .33 C *1,,726,200 369,000 s Caaeincawy aod Faa (20X1 Taeal Syacaa Caac .20 C CS*X 344,600 *2,1633,000 r Thouaaada ad (allaaa la aart caaccar; 1 Burtar at raaacara la plaac. *tf adacuaca stact can (1 day) and eonelauoua ciiiltutUiM (+ 40*7) aupply la avalladla trim aalaclaj -mica, ;hla usic will aac b saodad. 53 ucc 026607 Maintenance 0f the valves and pumps will b the major expense involved in keeping the ayscam operational. An inaeruaene technician for 2 hours/day and machinist 2 hours/veek will he needed, Maintenance materials Jill be about 310,000/yaar. The cose of supplying purge microgen and scearn is estimated ac $3,000/ year. The major energy requirement is the refrigeration needed. The \ operating coses are shorn in Table 4-7 for che 10,000 gallon reactor ease. 4.4 COSTAPMEST OF aOSSIOSS FROM MAJOR 27ZST 32X127 7A17E DISCHARGES One category of control chat is often proposed for eliminating 701 emissions resulting from major event relief valve discharges is containment. In this approach, che vapors released from the reactor are routed through a knock-out system to remove entrained polymer slurry and liquid 701 and then piped to either: 1) a gasholder, 2)- an absorption system, or 3) an adsorption system. Although all of these techniques are technically feasible and have essentially no impact on the environment, the capital, operating, and energy costs are significant as discussed in che following sections. The containment system should be sired for the worst case, l.e., to accommodate eh* entire 701 cherge to one reactor. In these discussions, che costs are developed for an example reactor of 10,000 gallon capacity, in a 200 x 10* Ib/yr plant with eight reactors. 39 ucc 026608 lean TABLE 4-7. ANNUAL OPERATING COST FACTORS FOR AUXILIARY VENT WITH CONDENSER (December 1979 Dollars) Investment $2,638,000 * I Engxg. Factor* $/yr/1000 gal Reactor Example Cost for 10,000 gal Reactor System Oneratin* and MaineBnance A Labor and Supervision 3 Supplies and Chemicals $ 12,700 V*1 1,100 V* $ 16,000 4,400 Utilities C Power (kWh <3 4c) D Steam S Cooling Water F Nitrogen G Total Utility 3 Total 0 & M 4,600 V 200 V 30 V 800 V ICC , D, E, F) I (A, 3, G) \ 46,000 2,000 300 3,000 62,300 82,700 J Insurance and Taxes (3 20Z of Investment) K Capital Charges (3 20Z of Investment) Total Annual Costs Credit for Recovered VQ1 Total Nee Operating Coses .02 I .2 I I <H, J, K) 2,000 V 52,800 527,600 663,100 (20,000) 9 643,100 *V * Reactor Volume expressed Is 1000 gallons. 60 UCC 026609 The knack-aut system raquired between the reactor and an7 containment system to trap entrained liquid 7CS and water would be ;ae same for each' of the thrae alternative containment systems discussed balow and would be similar co chat described in paragraph 4.3.2 above, but without the condenaing system equipment. Is would consist of a stainless scatl manifold con necting the individual reactor vent systaas and leading into a surge vessel of about 40,000 gallons capacity, wish a back pressure controller discharging to the inlet of the containment system. The installed cost of Just the knock-out systaa is estlmattd to be about $321,000 and is included in the capital estimatas for the three alternative containment schemes. The siring of the piping to and from the containment systaa is dependent on the available space and plant layout but is assumed to cost an additional $600,000 in these tramples. The accuracy of the cost estimates are o30S. 4.4.1 Gasholder Capital. Operating, and Saerav Costs The gasholdsr to be used far containment of 7G1 released from a reactor during a major event should be dedicated co that service unless it is shown that additional capacity is avallabia for "normal" recovery operations in axesss of that needed for containment of one reactor charge. A separate, smaller, gasholder is currently provided by many plants for the containment of 7Q1 amissions from normal operations. A proposed schmnacle flow diagram is shown In Figure 4-9 for incorpo rating the large gasholder and its auxiliary equipment into the plant. The piping and valving should be designed to be fail-safe and preclude the creation of an explosive mixture in the gasholder, the auxiliary equipment, or the piping* The actual flow scheme of the monomer recovery system is sot shown inasmuch as there are numerous configurations and etchniquas that may be used effectively. 61 ucc 026610 [ilitlaf kacter Irela Val luiltr Irun Mtur tew lari Ko>> (ilttlef Lethal tar M|H>ui (ulwlikr CmuIhciii ul linHi| Sftua ucc 026611 t Figure 4-9. Schematic (low diagram of gaaholdor containment ayatern fur major event releauea. Front che knock-cut ru*l a line goes directly to the monomer raeovery systaa far processing ai minor releases. dovevar, la the proposed schema, che vessel would also be provided with 4 back pressure valve sec far abaue 30 :o 60 psig chat would open to the large gasholder lalac manifold la the eveos ai a major release. The back pressure should be less ehaa one-half ai che setting on the polymeriescion vessel relief valve to ensure unrestricted flaw during major event releases. 4.4.1.1 Capital aecuirements--- The following are the normal specifications of a gasholder to contain che entire 4150 gallon Vd charge ca one 10,000 gallon reactor (i.e., assuming It is operated with a 1.4/1 Hz0/VCM ratio). Volume, cu it Diameter, it Haight, ft Material of Construction Type oi Seel dumber of stages 200,000 75 43 Carbon Steel Veter 1 The gasholder should be designed so that che guides and counterweights may be easily maintained to prevent "freezing" in one position during long periods oi nonuse. Xicrogen or other inert gae connections are required to purge che system, k procedure is needed ea periodically demonstrate the operability of the gasholder, auxiliary equipment, and piping. The capital caeca for a plant with a raactor sine between 3,000 and 40,000 gallons may be estimated using che cost factors showin in Table -4-3. The caeca for a system to accomodate a 10,000 gallon reaction are shown as an example* 63 UCC 026612 TABLE 4-8. CAPITAL COST -ACTORS FOR GASHOLDER CONTAINMENT SYSTEM (Doeembor 1979 Dollars) Coot Taetat* 1/1000 |al ituplt Coat Sot 10.000 tal laaeto* Sytct* A Cm Holder A tank M irmlM, fdn. $ 70,000 70.000 7*1 3 441,700 441,700 Tsui (A, * At) * 110,000 ?* 9 343,400 i loCOVOtT MttitMBC i CoMfVMM* * Motar it i* AceMMlotoo i Slat. Voooolo i* frlOM i? Sub Total lacovtrjr i lootaUttioo 4 Total UuniT MulM 4,340 V* 340 7>' 3,240 * 4,000 7** 4,000 * 1,700 7* Zei - it) 2 a It Clr * It) * 1 It 24.000 2,100 14.240 13,930 13,930 4.100 * 13,700 147,400 231.100 c Tatal tnittlloO lOOi, a Ottac B> Mpias Di loon. 4 Witr 9 luildlata 4 Sit* Oovwl. 3* Total Otkaf (At * It) 94,000 7*4 23,300 7*** 31,300 7*`* Zen,, a*. o) 1.134,300 312,200 70,400 232.900 443.300 t Total CoacatMOMt Sytta* Zee -a o.) 1,120,000 1 [ 1 l| rml'wi lytM It a Total Aqroiaal Coat Takla 4-4 130,000 IT*1 lex. it. ft) 121,000 400,000 3,241,000 it fttinaorltg t CoaotmatlaM it i Total IrotoN Coot 33X 0 202 0 I<C, It. It) 1,070,000 444,000 *4,934,000 ur *3.000,000 V liMUr Valuta ii|>uw4 La 1000 |alloao, H 1uMt MINIM loMtfc, 1000 faat. 64 UCC 026613 4.4,1.2 Operating and ^aincananca Costa-- The operating raqulrmanes of a gaaholdar 373cm are minimal, 79c series adherence so operating and maintenance procedures is necassar7 eo ensure the affective response of eha 379cm during an marganc7 release. Operating 3.aoulraaaacs--Ona parson should ba designated on aach shire co ba raaponaibla co saa chae eha gaaholdar is oparacional ae all tinea. Tasks eo ba parforaad would ba 1) log eha aceual Laval' of cha gaaholdar sank, 2) shack eha Uaa-up of valving eo and from eha holdar, 3) shack vaca? saal on gaaholdar, 4) shack Laval of overflow vacar sollacelon pie, and 3) periodl- sall7 salsa and lower eha cank eo dtmouacraca ics oparabilie7. Tina eo perform ehaaa duclaa la estimated eo avaraga ona hour par da7. Xlerogen is required for purging cha S7sra* and steam fer heaclng eha saal S7stam.ln winter soneha. ~ J* vtaingawaaea Requirements--To furehar assure eha operabiliC7 of eha 373cm, cha following rouelna maintenance would ba required: 1) Lubrleaca eha guides and rollers, i.a., all sovlng pares, eo prevane a mechanical "freaza-up" or locking of eha floating chamber. 2) Inspect, and repair as required, cha inscrumaneaclon and automatic soncrol devices 3) Parfors routine maintenance on pumps and compressors. 4) Parfors scheduled major lnspacslons of ancira 373tea on animal and/or blnannual baals. The time required co parfors ehaaa tasks is aaeimacad eo avaraga 300 ean-hours/yT. ifaincananea aacarlals required for eha pump and compressor includes spars pares, lubricants, seals, acc. S3 ucc 026614 4,4.1.3 Energy Requirements-- The energy coses for the gasholder concalanene system are negligible and are primarily for recovery of the VQi by compression and condensation of the vapors. If It is assumed that the gasholder is filled three times a year, the volume to be recovered over a total of 72 hours would be 600,000 cu ft of VOI vapor for a reactor of 10,000 gallon capacity. The compression would require about 2000 kWh and the condensation would consume about 120,000 gallons of cooling water. The rainwater runoff via the seal water systems adds about 200,000 gal/yr to the wastewater stripping operations. The incremental steam and cooling water requirements would therefore be about 4,200,000 lbs/yr, and 1,000,000 gal/yr, respectively. 4.4.1.4 Total Annualized Cost of Gasholder-- The approximate annualized cost for operating a gasholder to provide containment of VQ1 from a reactor of any capacity may be estimated using the engineering factors in Table 4-9. An example is given for a 10,000 gallon reactor case. The major expense of capital charges and the low expectation of VCH quantity recovered makes the containment of major discharges by a gasholder uneconomic and not cost effective. 4.4.2 Absorption System Capital. Operating, and Enemy Costs An absorption system can be used to effectively contain the reactor major.releases. The systma should be able to recover almost all of the VQ1 released and reduce the 701 concentration in the air emission stream to acceptable levels. 66 UCC 026615 TA3L2 4-9. AHOTAL OPERATING COST FACTORS FOR GASHOLDER COStAEMPI STST21 (Oacambar 1979 Dollars) Inrastaanc** $5,000,000 I Eagsg. Factor* S/yr/lOOO gal Raactor Ezaaplm Cose cor 10,000 gal Enactor Syscam Ooeraeiar & Maiacananea A Labor & Supervision 3 Supplies, Octal cals, Otllitia* C Power 3 Seua Cooling Water ? Mitragen Purge $ 23,000 7*1 5,630 7** 130 V 3,350 7 20 7 320 7 $ 31,300 22,500 1,300 33,300 200 3', 200* G Tocal Utilities I<C, 0, E, 7) 40,200. 5 Total O & M 2 (A, 3, G) 94,200 J Insurance & Taxas 2Z Z 100,000 : Capital Charge L Total Annual Coata 20Z I I (a. J, R) 1,000,000 1.194,200 Cradle for Recovered 7d S Total JTee Annual Operating Coat CL-H) (2,000 7) a-H) (20,000) $1,174,200 *V * Raactor Tolusw u;rui*d la 1000 gallons. **Froa leas I. Tabia 4-3. 67 UOC 026616 A schematic flow diagram for an absorption system using X, 2-0icXorothane as tha absorbing solvent is shown in Figure 4-10. . The piping and valving should be designed to be fall-safe and preclude the creation of an explosive mixture at any point in the system. The operation of the knock-out vessel ahead of the absorber is described in Section 4.3.2. The discharge from each knock-out vessel is piped directly to the absorption system manifold and also to the plant's normal Vd vapor recovery system during routine operations. The solvent supply tank should be elevated to provide a sufficient head to supply solvent to the absorption system in esse of a power failure. Controls on the solvent supply tank should be designed to permit operation during a power failure. Tha stripping column is designed to recover the lean solvent end send all VCM to recovery or disposal in a 24-hour periodT Absorber/3triooeg Type Number of Units Height, ft Diameter, ft Material of Construction Solvent Used Quantity of Solvent Needed, gal Rich Solvent Storage Tank Type Volume, cu ft Material of Construction Absorber Packed Tower 4 43 4.73 Carbon Steal 1,2-Dlehloroethane 43,000 Cylindrical 7,300 Carbon Steel Strioo r Tray Tower l 43 3.0 Carbon Steel S3 UCC 026617 Ot ucc 02661S Picture 4-1(1. aytaiew uclt^uuclc flou diagram. Laan Solvaat Storage Tank Type Volume, cu ft Elevation, ft Material of Construction Cylindrical 7,200 100 Carbon Seaal 4.4.2.1 Capital Eeouiraments-- Tha capital coats for an absorbar/strippar designed to handla tha entira diacharga from a reactor, In tba 3,000 to 40,000 gallon range, may ba esti mated using tha cost factors shown in Table 4-10. An example is given for a 10,000 gallon reactor case. 4.4.2.2 Operating. Maintenance, and Energy Costs-- Operating costs for tha absorption system are since tha system is normally not in use. An operator on each shift should ba responsible for keeping the system operational at all times. Tha absorption and stripping equipment should ba provided with a con tinuous purge of inert gas (such as nitrogen). Tha operability of tha pump, controls and instrumentation should ba demonstrated periodically. Energy costs for tha absorption stripping system are small. Tha main energy uses are pumping tha rich, VQI laden, solvent through the solvent stripper and into tha lean solvent storage tank; and tha steam and cooling water required to strip the solvent to VCU in tha stripper. Scheduled maintenance inspections and necessary routine maintenance on tha operating equipment should be performed. Inspection and rspair of instrumentation and control devices should also be performed on a regular basis. 70 ucc 02661Q Zk2LZ 4-10. CAPITAL COST FACTORS FOR SGL7HTT A3SCRFTICN CONIAEffiOT SYS72S (Daeambar 1979 Dollars) Cose Factor * S/1000 gal "rampla Cose Ter 10,000 3S1 Raaecor System Fquiymaac Ai Absorbars A i Serippar Aj Auxiliary 7asaals (Scoraga casks, pumps, comprassora) Ate local Ins tallad Squipaant S 43,900 7*7 20,300 7*7 23,300 7** 2*l. Ai, Aj) S 220,000 104,300 101,400 423,700 3 Piping 34,200 7** 136,200 C laserumsacaclos and Saiacy 23,400 7*1 32,00(1 0 3ii~t T.dings and Sica Davalapaane ** Total Coucaimanc Systam 23,400 7*1* (Ai > 3 C, 0) 71,400 663,300 Fi Esock-Out Syscaa 7: Saadax Sxcassian** S Tocal Physical Cose Tabla 4-4 130,000 L7-* 1(2. Fi. Fi) 321,000 600,000 2,086,300 Hi Eaginaaring and Construction Hi Coatingancy and Fa Hi Inicial EDO Charga 33Z G 202 O 6,920 7 I Total Syscaa Cost 2. Si. Hj, Ei) *7 * Saacsor 7oluaa axprasaad in 1000 gallons * Haadar- axcanaicn langrh, 1000 faae. 663,300 417,300 69,200 S3,261,300 Say -$3,300,000 ucc 026620 The annualised operating coses for an absorpelon systaa may b estimated as shown In labia 4-11. Tha major axpansa of capital chargas and eha low expectation of VQ1 quantity racovarad makes cha containaant of major discharges by absorpelon uneconomic and not cost affective. 4.4.3 Adsorotion Svstam Capital. Operating, and Energy Costs A carbon adsorption system can be used to contain reactor major releases. Tha system should be able to recover almost all of the VQ1 released and reduce the VCM concentration in eha gas emission stream to acceptable levels. A schematic flow diagram for a carbon adsorption system is shown in Figure 4-11. A typical four-bed vertical carbon adsorption unit Is depicted in Figure 4-12. The piping and valving should be designed to be fail-safe and precluded the creation of an explosive mixture at any point In the system. The operation of the knock-out vessel Is described in Section 4.3.2. The discharge from each knock-out vessel should be piped directly to the inlet manifold of the carbon adsorption system and also, to the plant's normal VQ1 vapor recovery system during routine operations. 4.4.3.1 Capital Requirements-- The carbon adsorption system should be designed to handle the entire discharge of VCH from the plant's largest reactor. Assuming an initial charge of 4130 gallons of Vd and 3820 gallons of HjO to a. 10,000 gallon reactor, cha specifications are: 72 ucc 026621 IA3L2 4-U. AXXUAL 0P23ATDIG COST FACTORS -OR 50L7KIT A3S0R3E3. COHTAITT^EMT 3TST21 (Daceobar 1379 Dollars) lavascsane** - $3,300,000 I less Oparaeiag 6 Maiatananca A Labor a Suparrlsion 3 Supplies 4 Chanlcala Uellieiss C Pwar 0 Seaam z Coolias Watar F Kieragaa Purge Sngrg. Factor* S/7T/1000 gal Raaceor $ 43,300 7* *1 3,330 V4-* 340 7 30 7 40 7 230 7 Example Cose for 10,000 gal Rsaccor Syscaa $ 37,700 13,300 3,400 300 400 2,300 G To cal tJellielas a tacal 0 & a ICC, D, 2, ?) I (A, 3, G) 9,100 * 30,100 j Insurance 4 Tax** 22 I 66,000 a Capital Charge L To cal Annual Coses a Cradle far Recycled 7Ci (6430 gal) a Total Hat Operating Cose 202 I I <H, J, K) 2,000 7 (MO 660,000 306,100 (20,000) $ 786,100Ire *7 Raacesr 7<jiua* la 1000 gals. **Fraa lea* t, Tail* A-1Q. 73 ucc 026622 *> Hit tew* Ur Figure 4-11. Carbon adsorption aya lea schematic flow diagram ucc 026623 10* H Figura 4-12. X four-'oad vartical carbon adsorpdon cowar. 75 UCC 026624 Typ Humber Height, ft Diameter, ft Bed area, sq ft 4 bed vertical absorber 3 33 10 314 The carbon adsorption system should be designed with an inert gas (such as nitrogen) purge system, A procedure is needed to periodically demonstrate the operability of the system. The capital costs may be estimated- using the engineering factors pre sented In Table 4-12. 4.4.3.2 Operating. Maintenance, and Energy Costs-- Operating costs for the carbon adsorption system are minimal since the system is normally not in use. An operator an each shift should be respon sible for keeping the system operational at all times. Energy requirements are mainly for cooling the carbon beds, supplying and condensing steam during regenaratlon, heating the drying nitrogen, and operating the N2 blower after regeneration. Scheduled maintenance inspections of cha carbon adsorption system should be performed. Maintenance and repair of all operating equipmant, instrumen tation, and control devices should also ha parformad on a regular basis. The operating costs ara estimated as shown in Tabls 4-13. Tha major expensa of capital charges and the low expectation of 7CM quantity recovered makes tha containment of major discharges by adsorption uneconomic and not cost effective. 76 ucc 026625 TABLE 4-12. CAPITAL COST FACTORS FOR CARBON ADSORBER CONTAINMENT SYSTEM (December 1979 Dollars) Cost Factor* $/LOOO gal Cost of System for 7-10 Equipment Ai Absorbers A2 Auxiliary Vessels (compressor, condensers, etc.) $ 126,180 V*7 100,400 V*s $ 632,200 400,000 Aj Total Installed Equipment _, (Ai -f A2) 1,032,200 B Piping (Vapor handling manifold, recovery, utility) 126,400 V*s 303,400 C Instrument and Safety 67,800 V*1 83,400 D Buildings & Site Development E Total Containment Equipment 77,700 V-4 (Aj, 3, C, D) 195,100 1,816,100 Pi Knock-Out System Fi Header Extension** G Total Physical Cost Table 4-6 130,000 LV*` I(S, Pi, Fz) 821,000 600,000 3,237,100 Hi Engineering and Construction (332) Ht Contingency and Fee (202) Hj Initial Carbon Charge I Total Systam Cost 332 G 202 G 33,800 7 1,073,000 _ 650,400 338,000 I(G, Hlt Hi, Hi) $5,298,300 Say $3,300,000 *7 - Reactor Volume in 1000 gallons. **L " Header extension length, 1000 feat. 77 UCC 026626 TABLE 4-13. ANNUAL 0PUPATING COST FACTORS FOR CARSON ADSORPTION CONTAINMENT SYSTEM (December 1979 Dollars) Investment ** - $3,300,000 I Item Engrg. Factor* $/yr/1000 gal Reactor Cost of System . for 7 - 10 Operating & Maintenance A Labor & Supervision B Supplies, Chemicals Utilities C Paver (37,300 kWh 3 4c) D Steam Cooling Veter F Nitrogen ? 8,300 V*1 13,100 7* 300 7 630 7 40 7 200 7 $ 10,300 32,100 3,000 6,300 400 2,000 G Total Utilities H Total 0 & M (C, D, E, F) Z (A, 8, G) 11,700 74,300 J Insurance and Taxes (8 22 of Investment) 22 I 106,000 K Capital Charges (8 202 of Investment) L Total Annual Costs M Credit for Recycled VGt (6,480 gals) N Total Net Annual Operating Cost 202 I Z <*. 2,000 7 (L-M) 1,060,000 1,240,300 (20,000) $l,220,300/yr *V * Reactor Volume in 1000 gallons. **From item 1, Table 4-12. 78 UCC 026627 SECTION 5 REACTOR OPENING EMISSIONS 3.1 VARIABLES AiTECTING EMISSIONS 40 CTR 61 ! 61.64(a)(2) provide* char eh* reactor opening loss (ROD from each reactor'opened is not to exceed 0.02 g VQf/Kg PVC produced. The reac tors are opened for maintenance and to remove degraded polymer which would otherwise contaminate product and interfere with heat transfer to cooling water In the reactor shell. At the end of each polymerization cycle, the reactor is vented to a gas holder and the polymer slurry is transferred from the reactor. Another bateh say then be started after flushing and treatment or the reactor oay be opened. The major variable affecting reector opening loss is the number of botches, run between openings. When a reactor is to be opened, hoc water is added, the Jachat is heated and the reactor is evacuated. The VCS vapor remaining in the reactor after venting to the gas holder and dumping of the slurry is quickly purged by the steam produced from the boiling water under evacuation conditions. The VQI trapped in the polymer particles, however, diffuses slowly into the water. Diffusion rate of the VQi out of the polymer depends on the temperature and the type of polymer involved (See Section 7.2). The temperature of the water and polymer In the reactor depends on the pressure (vacuum) and the jacket temperature. A very high jacket temperature may result in further degradation of the polymer making it more difficult to remove after the reactor is opened. Sufficient heating is needed to maintain a good boiling race so that the VQI is stripped from the water. 79 UCC 026628 Higher cemparaeures incraas* eh* diffusion rasa of 7CH into eh* vtuc but eh* amounc and eh* characteristics of eh* palmar adhering co eh* valla art both unpredictable. 1 low pressure vH allow bailing of eh* v*c*r ae law emp*racur* one results in alow diffusion of 7Q1 from eh* poiymar. Alesmataly, a reduced h*aeiag rac* viU produe* lied* stripping at asm and will allow Vd eo ramain in eh* vaear phase of eh* reactor unl*ss a very long elm* is spent ac eh* low boiling raca. Xh* boiling nusc b* continued until eh* 7d caneantt of eh* polymar and vacar is rtducad co eh* axrtne ehac vh*n eh* reactor is cooled down for entry, eh* 7d rattaining in eh* vapor space will b* below eh* allowabl* liaie. Th* rac* of diffusion of Vd froo polymer dspends so such on polymer charaeesriscios chat only field easting can establish eh* cia*-eettp*ratuz*?r*asur*-h*ac raca required eo achieve eh* allowable Hales on r*setor opens* ing aalssions. '.iany field easts at various eaoperacuras and base ratas are needed sine* eh* aaouae and charscrerlacica of polymer rattaining in eh* vassal varies from batch ea batch. X portable flan* ionisation dacacsor or ochar analyser nay b* inserted through a small aoszla or samples nay be taken eo daemraina eh* 7d concent of ehe vapor spaca in the reactor. These field * ceses should be sad* foe each formulation and repeated at least seasonably eo updata cha data. The regulations require periodic reports of ehe actual SOL emissions experienced in operaeion so the** measurements muse be nad*. 5.2 PSOBLdS STCCJUtfTStgP Typical problem* encountered are inability cc achieve eh* n*d*d heating of eh* vacar ia eh* reactor and failure eo achieve ehe needed evacuaeion pressure Fouling of heae exchanger* and reactor Jackee valla era eh* aajor causes of inadequate heating vhich reduces both ehe diffusion of 7G1 from eh* polymer and eh* stripping of 7G1 from eh* vatar. That* conditions rasulc from insuificiant redundancy and naineanance of h*at exchang* and vacuum equipmanc. 30 ucc 026629 Companies have reporead problems in maintaining efficient vacuum pump operations which ware solved in one instance when maintenance personnel received special training from manufacturers representatives. The VCM vent service for vacuum pumps is a particularly difficult one since a corrosion potential and polymer particles exist In this system; Adequate redundancy is necessary to permit the needed overhauls without affecting the vacuum available for the needed ciae-temperature-pressure-heat race required to achieve allowable SOL emissions. Seat exchanger fouling and or steam supply problsms are normal experi- \ ences in any chemical plant. There are usually predictable and corrective actions that can be taken to prevent this interference with operations by proper planning, maintenance, and operations scheduling. Saactor Jacket fouling does occur unexpectedly in soma cases but this effect is detectable and can be handled with alternate operating procedures to ensure the needed time-cemperature-pressure-heat rats doss occur In the reactor. 5.3 ALTERNATES TOR MEETING ALLOWABLE SOL Since a major variable Involved in computing SOL emissions is the amount of PVC made, a tachnique which allows several batches to be produced before the reactor is opened will minimize the amount of reactor purging required. "Closed Cleaning" technology such as high pressure sprays and solvsnt cleaning is used by some PVC producers. Othsr produesrs have developed special formu lations which give little or no wall deposits. Some manufacturers have developed reagents which condition the surfaces of the reactor walls so chat polymer does not adhere to the surfaces. Many patents cover special chemicals and nozzle designs for chess purposes and some of chess are avail able for license. Although, depending on the technique involved, these may be quite costly in terms of additional equipment needed as wall as license fees, they have ocher advantages which make them more valuable chan just aehieveing the allowable SOL. The turnaround time will undoubtedly be reduced giving additional production and the labor for manual cleaning operations will also ba lower. 31 ucc 026630 A procedure reported far suspension resin reactor cleaning used 400.0 co 5000 psi water in an 5RC watar jet cleaning syscam vich she water jec collar fitted directly into che reactor manway. This equipment allowed 22 co 30 bacches co be run between reactor openings instead of opening between each batch. An identical system for dispersion resin reactors allowed 3 co 13 bacches between openings. With some development expense a spray system of che type could be developed by any ??C producer. The 3SC technology was developed by Goodrich and is undoubtedly available far licensing. A solvent cleaning procaaa was dsveloped by Air Products and Chemicals, Inc. utilising Oi-mechylformamide COM?) as the solvent. The reactor is filled with solvent under an inert atmosphere and the reactor is heacad and stirred while a small continuous flow of solvent overflows chs raaccor cop. Aftar sufficient time elapses, che solvent is transferred co storage and the reactor la rinsed several times with water. The reactor Is then ready for. another polymerisation cycla. Solvent regeneration includes precipitation of solids, centrifuging co remove solids and distillation co purify che solvent. This process is patented and probably available for license. Ocher solvents are useable for cleaning che reactor. If che ?VC plant is associated with a TQf plant, dlchloroeehane would be an obvious choice since solvent recovery equipment would be already In place. If a spent solvent was useable as raw material for some ocher adjoining operation or had a ready aark.ec, che economics of purification could be affected favorably. A Shin-Saeu brochure indicates use of special techniques which prevent che accumlation of deposits on reactor walls, eliminating che need for sen to enter che resctor for cleaning. 3. ?. Goodrich Company also reports che use of a chemical solution which is sprayed on che reactor walls aftar water flushing the reactor. This creaaunc aftar each batch of polymer has allowed more chan 30 batches co be made before opening che reactor. 3och cha 5hinIstu and Goodrich processes appear to be available for license. 32 UCC 026631 The patent literature indicata* several special formulations consisting of dispersants, catalysts, and additives which minimize wall deposits during 77C reactor operation. The majority of these are based on relatively small scale tests so their applicability to commercial use may be questionable. The ultimate means of ensuring that the SQL Limitations are met is to analyze the vapor space for VQf and compute the results in terms of g VGi/Kg SVC. If the figure is higher chan the SOL allowabla, purging should be continued until the results show that tha raactor can ba legally opened. There should be relatively few cases (< 3Z) if the cima-cemperacure-pressureheat rate conditions are fulfilled. If excessive cumbers of cases requiring continuation of the purging occurs, a new sat of field tests should be carried out to reestablish the requirements for meeting the SOL allowables. 33 UCC 026632 SECTION 6 FUGITIVE EMISSIONS Sections I through 6 of 40 CIS. 61.65(b) are cha icons designated foe consideration in ehis pro1 act. These items cover fugitive emissions iron loading-unloading lines, slip-gauges, seals on pumps, compressors, and agitators, relief valve-rupture disc systems, manual venting of equipment and equipment openings. A review was made of the regulations themselves and of the material presented in Volumes 1 and 2 of the Standard Support and Environmental Impact Statements: Promulgated Emission Standard for.Vinyl Chloride and other literature. 6.1 LOADING-UNLOADING lines The regulations require that VCM content of lines to be opened will be reduced to less than .0038 m1 (0.13 ft3) at standard temperature and pressure and that the VCM removed by this operation be ducted through a control system from which the vent contains less than 10 ppm VOS or that use of equipment and/or procedures which have been demonstrated to be equivalent in eerms of reducing VCl emissions eo cha atmosphere be proposed in writing to the administrator and he approves the proposal. In tha usual eaaa of transferring VOl from tank cars to storage, at completiou tha tank car is evacuated to remove all tha VQt by vaporization. Under these conditions tha line will contain only VCM vapors. When liquid VCM 1s being transferred to tank cars or oeher storage vessels, cha lines are generally blocked at cha vassals and cha liquid present la allowed to vaporize into a gasholder. 34 UCO 026633 Sithar a wacar displacaaane or a vacuum 37scam can ba provided far cot loading-unloading lints. Vacuum pumps can provida adequately low pressure needed *0 achieve chs allowable Vd remaining la cha lints. The gases dlsplacad and chs vacuum pump discharge muse tncar a 7d recovery ayscam which achltvas cha < 10 ppm 7d concent o cha vane, and aperacing procedures muse specify cha uaa of vacuum oparaclon or wacsr flush ac each elms cha linas ara opanad. 6.2 SLIT-GAOCSS Thara ara no 'mown easas in which slip-gauges ara usad. Mast gaugss ara a ssalad cypa (ssgnaelc) and do noe hava any Vd leakage. This Is con- aidartd co ba a aaelsfaceory alearnaca co a csnnaeelon co a Vd racovary syscam, which muse ba usad vinh an7 sllp-gauga. Tha magsaeic gaugas ara ' consldarabl7 lass coscly chan vanelng ayacams. * 6.3 SSALS ON PTOP3, CCMP3ZS5CRS, AND AGITATORS tha rtgulaclans require chse Vd amissions from pumps, csmprtssors, and aglsacors ba alnlmiaad by Inscalling stal-ltss equipment, or by using daubla mschanleal seals wleh tichar a saal fluid, at prassura such chae cha laakaga will ba saal fluid ineo cha equipmanc, or by collacclng and duceiag any Vd 3aal laakaga chrougfa 4 conerol ayscam from which cha Vd in cha axhausc gas Is lass chan 10 ppm or equivalent, or by using damonscracad equipment and procsduras which ara approved by cha adminlstraeor. Tha mosc savara tarries for saals on roeaelng aquipmane is cha agicacor saals os ?VC raaceors. Sararsl planes indlcacad usa of a douhla saal wleh fluid, pressurized eo ansura saal fluid laakaga lneo cha vassal for agicacors. Soma planes also usa similar douhla saal sysesss on pumps and camprassors. A Continental Oil Company areicla indlcacad usa of eannad or magnseic drlva pumps. A Dow domical Company prasaneaeion indlcacad soma succass in usa of a saal-iass "Xoncro" pump in intermittent Vd sarrlca handling Vd. 35 ucc 026634 6.4 SELIET VALVE - RUPTURE DISC SYSTEMS Ic 13 standard practice for rupture discs to ba installed on all relief valves in 7d service as required by the regulations. Routine maintenance procedures are needed and a continuing program of studies of materials of . construction and supplier review are worthwhile. 6.4.1 General The primary purpose for installing a rupture disc Is to ensure that Che pressure relief valve Installed just downstream of It will function properly in case of an overpressurlaaclon. The rupture disc (3D) serves to Isolate the relief valve (SV) from the environment of the vessel and thareby prevent corrosion and fouling of the 37. * 3ecause vinyl chloride monomer (VCM) Is both toxic and flammable it is highly desirable that the flow of material from the relief system be stopped as quickly as possible after a safe working pressure has been attained following a release. This shut-off Is provided by the 3W. A significant potential problem is chat the 37 will not fully resaat because entrained solids or a piaca of the 3D may be lodged in the valv . This situation may be resolved In one or more ways. 1. Open a valve to a parallel 3D/37 and block In the malufnceionlng valve. 2. Pump out cha remaining vassal contents as quickly as posslbla to a holding tank. 3. Salaase vapor to cha normal vapor recovery system. 36 ucc 026635 6.4.2 Fraaacure Failure of Fuocura Ji3C3 Another potential problem, but small and easily resolved, la the pre mature failure of rupture discs. When ills occurs it dees aoc normally result In cha ralaasa of 7Ct if the 3.7 is vail seated. It is a matter of loss in production, if any, during cha else cha vassal is ouc of sarvlca for replace ment of cha 3D and cleaning and inspection of cha 37. Vhachar cha pranacurs failure of 3D'a is cha rasulc of corrosion or improper fabrication and casting procedures by cha manuiacturar is still open co question. In soma FTC plants chare is no known problem of prematura failure of 3D's due ca corrosion or unexplained rsasons whereas la other plants it has been a real problem end use of ceflon coated discs and/or special maintenance procedures have bean established co resolve is. ~ It is conceivable chat eha reason some FTC plants ere experiencing problems and others not is chat cha fabrication end/or inspection procedures are inadequate. Is would be reasonable for chess FTC producers co discuss this with chair 3D suppliers, and/or seek new suppliers in order co minimize maintenance coats. In one plant, after experiencing soma problems a faw years ego, they switched co ocher suppliers end now obtain ovar one year Ufa vich uncoacad, stainless steel 3D's. Khan Che 37 is pulled for its shop inspection, che 3D is cleaned and laspectad and then raturaad to sarvlca. They do noe experience any 3D failure with this approach. In some plants, the 3D's are replaced quarterly co minimize chances of premeeure failure, teflon coated disc are used in corrosive service, but it is noe known whether chls includes the reactor 3D's. this approach is accept able, but it might be more costly chan is raally necessary. 37 UCC 026636 6.5 MANUAL VETTING OF EQUIPMENT AND EQUIPMENT OPENING The regulations require manual venting of aquipmant wish Che VCM being ducted through a control aystam from which tha exhaust gas is lass than 10 ppm. It is also required that rasidual VCM vapor in tha aquipmant to ba opanad is lass chan 2.0 parcant by voluma at standard tamparatura and prassusa. Tha standard practica is daprassuring tha aquipmant through a VQ1 racovary system of adaquata parformsncs followad by usa of staam swaap to ramova remaining VOS vapors to tha racovary system before opening any vassal in VCM service other chan reactors. This procedure can meat all regulatory requirements. Reactor opening procedures are described in Section 5. 38 UCC 026637 SECTION 7 DEGASSING TECHNIQUES Whan a suspension or emulsion vinyl chloride polymerisation reaction reaches cha desired conversion, a water/polymer slurry containing between 52 and 252 unraactad 701 ramalna. Tha reactor la chan vancad co near aonoapherie pressure so thae tha liquid monomer volacizaa into a 701 racovary or destruction system. Tha remaining monomer constituting approximately 0.12 by weight of cha slurry or 1-32 of tha dewatered rasin. Is althar dis solved is Cha water phase of tha batch or trapped within tha polymer par ticles themselves. This residual monomar muse be captured for reuse or ~ destroyed in order co meat E?A regulations. If a polymer stripping process is used and residual 701 (2701) concents of 400 ppm in suspension rasin and 2000 ppm in dispersion rasin are achieved, only cha stripper vane muse be connected into tha 701 racovary or destruction system. If cha polymer is noe stripped Co these levels, regulations require all subsequent polymer handling vanes co be connected into this system. Suspension resin slurry is usually dumped co a hold tank for processing in a continuous stripper. Dispersion resin slurry is eieher vacuum stripped in the reactor or Cransferred to a special stripping vessel. After stripping, the P7C slurry muse be dewatered and dried for further processing. 7.1 PROCESS DESCRIPTION 7iayl chlorida monomer is usually removed from the reaction slurry by either vacuum stripping in che reactor or steam stripping in a separate stripping vessel. Suspension P7C resins are frequently processed in con tinuous operating steam stripping columns while emulsion (dispersion) resins 39 ucc 026638 nust usually be processed batchwlse under vacuum bacausa of :ha sensitivity of these resins to axcasslve heating. Inert-gas sparging can ba usad ia place of steam where dilution of the emulsion auae ba avoided, la addicion. degassing nay ba accomplished using proprietary scripping devices such as the agitated chin-film evaporator or the Parkaon stripper. These are dis similar short-residance-cima devices which are lacriasically adaptable to continuous procsssing, honomar recovered is compressed and condensed for reuse. Satchvisa flashing of a ?VC reaction slurry has three basic steps: (1} vent the 701 to the recovery system until Che reaction pressure is approximately atmospheric; (2) heat Che batch to 20 to 23*C above the polyaarization camperacuri; and (3) evacuate the reactor to an absolute pressure of approximately 400 nmHg. The reactor or stripping vessel is held sc tha*. temperature and reduced pressure for a specified time to achieve desired^ degasalng. The slurry may be sparged with steam or inert gas while beer is simultaneously applied by circulating hot water through the heating jacket. 3 7 Goodrich has developed a continuous slurry stripping syscaa which . is widsl7 used in the processing of suspension ?7C resins. This process utilizes a pressurized stripping column feed tank to relesse excess 701 and to form a transition from the batch reactor to eha continuous stripping caiuan. Tha hoe slurry is pimped from the feed tank to the stripping colum through a small vapor-liquid separator. Tha liquid slurry enters tha top of a couaear-currsne steam stripping column and tha 'vapor screams from the feed tank separator and column are sene to the 701 recovery system. isaoval at residual sonemar which is trapped within the polymer particles is a mass-transfer limiting process which becomes mere difficult wish in creasing viscosity. The wiped-film or agitated thin-film evaporator is a proprietary stripping device which reportedly exhibits diffusivities of of 1000 to 10,000 tlsas greater than those for simple molecular diffusion and can be used to process slurries for which the 'viscosity of the mixture 90 UCC 026639 ranges from L000 Co 100,000 cp. In chis unit, heat Is transferred through a metallic wall to a chin film of liquid. A mechanical agitator distributes the liquid evenly over the heat-transfer surface. Disadvantages of chis device are: design criteria limits heat transfer area of each unit, more maintenance is required Chan for a non-mechanical device, and foaming problems may occur. The patented Paritson device is a non-mechanical, place-type, dispersedflow contactor. The latex is dispersed into a controlled, high velocity scream of steam and the resulting two phase flow passes turbulently through a plate-type stripper. The stripped latex then discharges into a cyclone separator-usually operated under vecuum-where the latex is disengaged from the vepor. Multistage unite may be used to achieve desired residual* monomer level. Thin unit is applicable to foamy, heat-sensitive or viscous products. Its advantages are: complete absence of foam, lack of moving parts, lowholdup, lav resldsnce time, reduced surface fouling, and reducad coagulim formation. The main disadvantage is chat the plate design permits only a limited capacity range. Also, maximum design pressure cannot normally excaed 3500 mm&g. Typical production ratae range from 30 to 250 m3/hr and fluids with vlscosltlas as high as 50,000 cp can be processed. 7.2 THEORY OF STRIPPING PROCESS The unreacted vinyl chloride in PVC reaction slurry is present In three forms: (1) as a separate liquid VCM phuae, (2) dissolved In the water phase, and (3) trapped, within the PVC particles. The Immiscible liquid 701 vapor ises when the reactor is ventad to the recovery system at approximately atmospheric pressure. The monomer remaining in the water and in the polymer particles must be stripped from the slurry. Removal of the VCM which is dissolved in the water is e simple binary distillation problem. The water entering the tower is saturated with VQf, thus, the VCM concentration will ba In the range of 0.13X VCM at 50*C and 91 UCC 026640 atmospheric pressure eo 0.03* 7C1 at 30*C and LOO aeSg. This separation nay be accomplished with us* because the vapor pressure of 7C1 La auch greater chan ehac of water; eh* relative volatility or 701 ;o 2*0 La between 33 and LOO. In addician, these wo components fora a aiaiaua-boiliag ateoerop* which goes overhead with the vacar vapor and, thus, enhances eh* removal. The nouomer which La erapped within eh* polyaer parelclaa La such nor* difficult eo remove. Ihla ?roc*aa La 1Laitad 07 mass-transfer within eh* polymer which eakaa place *07 simple fickian diffusion plus rslanstioucontrollad swelling. 7G1 migration occurs by jumps between holes In eh* polymer acruceur* wlch a diffusivity of 2 s 10~12 cm2/s t SOX ae 30aC in both juapanaion and emulsion resins. Th* diffusivity La a strong function of temperature but La fairly insensitive eo eh* molecular v*ighc of eh* polymer. Ic variaa from 2 x 1Q~14 ca2/s at 90*C eo 1.3 * LO*12 cm2/s at 23*C (2aiar ea Figure 7-1). Th* race-controlling dinanalon La eh* ala* of eh* primary polyaax parxielas, rsch*r than eh* overall diameter. Thus, removal is Laprovad if eh* polymer grains ar* small and porous, but la raeardad by ch* prasac* of oon-porous, glaaay pareiclas. It higher temperatures eh* raaoval rata is improved rasarkably by eh* ona*c of "pseudo-boiling", or auclaacion. of a high Liquid/vapor interface. This occurs ac approximately 95*C under ac3osph*rlc conditions and ac 70*C in vacuus stripping with staaa. Very rapid raaoval of monomer can eaua* a marked inesaaa* in rasia porosity bacauaa eha expansion of 7Ct puts availing seres* on eh* polymer structure. 7.3 sracraG sociRfflir asd casts As discussed in eh* previous sections, 701 can b stripped from ?7C reaction slurry by a variety of different techniques Soma raalna ar* tore difficnle eo scrip chan others due eo low porosity and/or hast ssnaicivity. Special precautions ruse b taken in handling aoulaion resins because relative instability cauad by hac or work Inputs can form coagulum and foul equipment Lines, Smulsion raalna ar* usually .stripped within eh* reactor or in saparaea batch flash tanks whil* suspension resins nay be strippd continuously. 92 ucc 026641 t I t t id Kef; M-4 Figure 7-1 Diffuslvity uf VCH in PVC au a function of temperature. ucc 026642 Flash casks ars normally vertical vessels which ara ac laasc 303 larger chas chs reactor. This facilitates discharge of the viscous or 3lurry-cype reaction produces asd hslps raducs foaming at che vapor ouciac. Cua cask say ba asad for savaral reactor batches asd stainless steal construction is usually satisfactory. 1 vacuum system suitable for reals stripping in a 90 hM kg/yr plant, capable of pulllag 700 rmHg vacuum asd compressing to 4o00 aaofig, cas ba purchased for $230,000 to $313,000. Installed cost, includ ing condanaar will amount to approximately $1,030,000. The power and cooling water requirements for this unit ara 30 kwh/hr and 3 mJ/hr, respectively. Suspension resins can be stripped Is continuous, multi-stage, steam stripping columns. Siasy companies utilise a configuration developed by 3 ? Goodrich (See Figure 7-2). T*hen the polymerisation reaction Is complete, the batch la transferred to a praeeurlsad stripping column feed cask. The slurry Is then pumped continually through a small vapor-liquid separator and into the stripping column. The vapor leaving che cop of che column passes through a condenser into a second vapor-liquid separator. The liquid from the separator is returned to che coluam while che vapor is piped co cha ?G1 recovery or deotruetion system. This system reduces 3.VC1 in che TJZ slurry-, co a level so chat che dried finished product reels contains less chan I ppm 7C1 (dry resin basis) end can be designed co handle porous or aon-oorous slurry feed with VIOL concent ranging from 3,000 to 200,000 ppm. Table 7-1 and Table 7-2 show che percentage increase in plant capital required co achieve particular levels of residual monomer in che stripped slurry for suspension and dispersion resins, respectively. In addition, che percentage increases in product price required co maintain che pre-control return on inveeatenc is given for each caae. For suspension resin, an overall control efficiency of 933 cas be achieved in two ways. Case k involves stripping che reaction slurry eo -00 ppm VIOL, and reusing cha monomer, while Case 3 utilises collection and 94 ucc 026643 Recovered ucc Figure 7-2. - *- K- , Ref: g f Cuodricli coutiuuuue eiuVry utrippiug syutew. H-7 TA3L2 7-1. SUSPENSION USZi RESIDUAL MCilCMEl. CONTROL COST ZIC2Z1SZS S3 mm iG/Tna punt 2 tacreaae Case A Case 3 Plant Capital 19 27 Produce Price 3.3 21.9 Osase price: 24c/lb) Rei: A-l TA3LS 7-2. DISPERSION 3SH RESIDUAL MONOMER CONTROL COST INCREASES- Z Increase Ale 1 Ale 2-A Aie 2-* 14 MM kay-rr Plane Plane Capital 13. 21. 33. Produce Price U. 17. 52.9 45 MM ka/vr Plane Plane Capieal Produce Price Cbase price: 342/lb) 9. 6.2 14. 10.6 34. 40.3 Ref: A-I 96 ucc 026645 incineration of ch vent gases from the centrifuges, driers, etc. Typical new and existing suspension process FVC plants are judged able to afford Case A, but cot Case B. Two plant sizes were considered in assessment of control costs for dispersion resin production. For both a 14 MM kg/yr plant and a 45 MM kg/yr plant three alternatives were evaluated. Alternative 1 involves stripping che reaction resin to 30,000 ppm, at an overall control efficiency of 321. Case A and B for Alternative II correspond, respectively, to improved stripping to 2,000 ppm and incineration. From Table 7-2, it is Judged that Alternative 1 should not be a deterrent for new or existing dispersion resin plants end that Alternative 2-A should be realizable for plants with capacity greater than 45 MM kg/hr. Alternative 2-B was considered, to be a serious deterrent for all sizes of emulsion resin plants. Following stripping, polymer is blended, pumped to centrifuges for' partial dewatering and dried in either cocurrent rotary kiln driers or fluid bed driers. In most cases, by the completion of processing, or shortly thereafter, flexible 97C resins are essentially free of 7Q1 but monomer stripping of rigid or non-porous resins is far slower. However, it is now passible for ell manufacturers to reach 10 ppm residual 7Q1 In all finished resins end most ere doing so. One ppm residual is routine for soma grades produced by particular manufacturers. 97 ucc 026646 APPETDH A. Bibliography A-l ucc 026647 BIBLIOGRAPHY A. General 1 Standard Support and Environmantal Impact Statement: Emission Standard far Vinyl Chlorida. EPA-450/2-73-009 and 450/2-75-0Q9a, October 1975. 2 Enginaarlng Control Technology Assassaane for Cha Plastics and Basins Industry. NIOSH, March 1973. 3 National Emission Standards for Hazardous Air Pollutants. Inspaction Manual for Vinyl Chlorida, May 1978 NTI3. PB-239-778. 4 National Emission Standard for Vinyl Chlorida; Subpaxt F, 40 CFR Part 60, Revised as of July 1, 1979. 3 Khan, 2.S. and T.W. Hughes. Source Assassmanc: ZPA-600/2-78-004 i. May 1978. Polyvinyl Chloride.' 6 Tarry, Herbert and Nagy, S., System Analysis of Air Pollutant Emissions from the Chsmical/Plastics Industry, October 1974, PS-239-880. 3. Procsss Oescriptlon 1 Albright, Lyle F. Manufacture of Vinyl Chloride. Chemical Engineering. April 10, 1967, pp. 219-226. 2 Albright, L. F. Polymerization of Vinyl Chloride. Chemical Engineering, 74(10):131-138, 1967. 3 Albright, Lyle F. Vinyl Chloride Polymerization by Suspension Processes Yields Polyvinyl Chloride Resins. Chemical Engineering, June 3, 1967, pp. 143-132. 4 Back* A. L*. Solution Polymerization. Chemical Engineering, August 1, 1966, . pp. 63-73' 3 Bellamy, K* G. and V. A. Schwartz. Enginaarlng and Cost Study of Air Palludoa Control for the Pscrochamical Industry. Vol. 9: Polyvinyl Chloride Manufacture. EPAr450/3-73-006-i, July 1973. 6 Cameron, J. B., A. J. Lundeea and J. H. McCullsy, Jr. Trends in Suspension PVC Manufacture. Hydrocarbon Processing. March 198Q, pp. 39-30. A-2 ucc 026648 7 Church, Jam** M. Suspensicn Polymerization, Chemical. Engineering, August 1, 1966, ?p. 79-61. 3 Coda of Federal Hagulatioos. dole 4Q, Protection of Environment, Parts 5099, pp. 236-239. 9 Dude, Edward W. Emulsion Polymerization. Encyclopedia of Polymer Science and Technology. H. F. Mark, ed., New York, Wiley, 1966. 7ol. 5, pp. 301-339. 10 Eastman, G. C. Free-Sadical Polymerization. Encyclopedia of Polymer Science and Technology. 3. ?. Mark, ed., New Tork, Wiley 1367, 7ol. 7, pp. 361-431. U Father, Elliac. Suspension Polymericacion. Encyclopedia of Polymer Science and Technology. 3. F. Mark, ed., New Tork, Wiley, 1970. 7ol. 13, pp. 332-371. 12 Fawcett, 3. J. Polyvinyl Chloride: 4 Major Contribution of 3. ?. Goodrich to the Plastics and Organic Coatings Industry, ACS Div. Crg. Coans Plast. Chem., Preprints 36(1) 70-73 (1976). %j " 13 Gellner, Otto. Enulsion Polymericacion. Chemical Engineering, Augusts 1, 1966, pp. 74--73. 14 Goodrich to Nike Output of 'Ceon' P7C at Ohio Sica. Chemical Marketing Reporter, Dec. 17, 1979, pp. 7, 12. 13 Hatch, L. F. and S. Macar. Prom Hydrocarbons to Petrochemicals, Part 15Thezaaplastics 3yd. Proc., September 1979, pp. 173-137. 15 Industrial Process Profiles For Environmental Use. Ch. 10, Plastics and Haaina Industry. EP4-600/2-77-023 j, Feb. 1977. 17 Johnson, Gary 3. The Effect of a Modified Weber Number on Eesln Properties During 7Gi Suspension Polymerization. A.I.Ch.E., 71st Annual Meeting, Nov. 12-16, 1973, Paper NO. 124. 13 Eardoe, L. 4, Polyvinyl Chloride. Haport No. 13 (a private report by the Process-Economics Program), Stanford Hasearth Institute, Menlo Park, California,. June 1966. 224 pp. 19 Laacrte, Michael ?. National Enlsslon Standards for Hazardous iir Pollutants. Inspection Manual for Tlayl Chloride. N.T.I.3., P3-239 773, May 1973. 2Q Langsas, Michael. Polymerization of 7inyl Chloride in Presence of Sub stituted Olefins; Effects on Molecular Weight and Melt Hheology. Journal of Applied Polymer Science, 7ol. 23, 1979, pp. S67-576. 4-3 UCC 026649 21 McPherson, R. W., C. M. 5 carIts and G. J. Fryar. vinyl Chloride Monomer... What You Should Know. Hydrocarbon Processing, Mareh 1979, pp. 75-88. 22 Hears, C. L. What's Ahaad for PVC and VCM CEP, Oct. 79, pp. 13-18. 23 Haw Proeassas and Technology Alert. Chemical Engineering, Feb. 11, 1980, pp. 101-114. 24 PVC Chemical Profile. Chemical Marketing Reporter, 205 (2):9, 1974. 25 PVC Growth Plans Lead to Big VQt Expansions. Chemical Week, Feb. 13, 1980, pp. 26-27. 26 Protection of Environment. Code of Federal Regulations (SPA), Title 40, Parts 2.204 (pp. 27-29), 2.210-2.302 (pp.' 36-43), 61.60 - 61.70 (pp. 283-295), July 1, 1978. 27 Rules and Regulations. Federal Register, Vol. 41, HO. 205, Oct. 21, 1976, pp. 91, 94. 28 Schillaollar, C. M. Alloy Selection for VCM Plants. Hydrocarbon Processing March 1979, pp. 89-93. 29 Schlagel, Walter F. Polymer-Plant Engineering. Design and Scaleup of Polymerisation Reactors. Chmadeal Engineering, March 20, 1972, pp. 38--106. 30 Sorenson, Wayne R., Peter A. Schwab, Robert S. Allen, George Tillson, David J. Lorlne. Large Capacity External Cooled Vinyl Halide Poly merisation Reaetor. O.S. Patent Ho. 3,980, 628, Spec. 14, 1976. 31 Sorenson, Wayne R. PVC Today, SPE RETEC, Cherry Hill, HJ, March 1-2, 1977, pp. 5-6. 32 Standard Support and Environmental Impact Statement Volume 2: Promulgated Emission Standars for Vinyl Chloride. EPA-450/2-75-009b, Sept. 1976. 33 Suspension Polymerization. Ini Encyclopedia of Polymer Science and Tech nology! Volume 13: Plasties, Resins, Rubber, Fibers. John Wiley and Sons, the,. Hew York. Hew York, 197Q. pp. 552-571. 34 Terviesch 9. * Suspenslon-PVC in Large Reactors. Hydrocarbon Processing, * Hovember 1976, pp. 117-121. 35 Wahl, Martin H. Bulk Polymerisation. Chemical Engineering, August 1, 1966, pp. 60-64. A-4 ucc 026650 C. Saat7-Accidant Prevention 1 3arlow, 5.. Z., J. 3. Fussall, and X. 3. Siagpuxvalla. "Reliability and Fault Tree Analysis." Society far Industrial and Applied Mathematics. 1975. 2 3ixby, V. F. Corrosive Attack on Stainless Steel ?ol7 Vinyl Chloride Folymerinars, Vinyl Chloride Safety Assn., Oca. 30, 1975 Meg,, Houston, TZ. 3 Fussall, J. 0., 0. J. Powers, 3annets. "Fault Trias - A Seat*-cf-Tha-Arc Oisscussion." IaZ Trasssceians on 3aliabU.le7, 7ol. 1-3, Mo. 1* April 1974, pp. 51-35. 4 cussall, J. 3. Synchacie Traa Modal, A Formal Methodology for Fault Tria Construction, A2JCa-IQ98 (1973). 5 Hauptmanns, Ulrich. Fault Tria Analysis of a Froposad ithylaae Vaporization Unit. lad. lag. Chma. Fundam. 1930, 19, pp. 300-309. 3 Laroy, Alain. Safety Analysis Aids System Design, Oil & Gas J., Mare!* 3, 1980, pp. 32-34. * S- 7 Lass Frasaneasian, 7ol. 6 - Classical lasrgancy Program and Technical Manual, A.l.Ch.Z, Maw Torle, Ml, 1972. 3 File, 7. Faille Traa Analysis: How Useful? Hydrocarbon Processing, 59, Mo. 3, pp. 273-233 (1980). 9 Fowars, G. J. and ?. C. Tompkins, Jr. "Fault Traa Synthesis far Chemical Procassas." A.l.Ch.Z. Journal, 7ol. 20, Mo. 2 March 1974. pp. 373-387. 10 Fresh, 3. 7. "Application af cauls Traa Analysis." Chemical Hnginaarisg Frograss. July 1980. 3. Reaction Sinaelcs 1 Atkinson, 1. and J. 3. Flees, Jr. Hast Canscants far she reaction of 0(5?) acorns vich C3i-CHF, CHt*C3Cl, and CHj-CHBr over she Casparscure range 298-442*11 The Journal of Chemical Physics, Vol. 87, Mb. 6, Sapemoar 15, 1977, pp. 2488-2491. 2 Fitzpatrick, 3capban T. Particle Formation in Continuous Haulsion Polyaarixaeion of 7iayl Chloride. 34ch S?H Annual Technical Confarenea, Atlantia City, MJ, April 1976. Graaawieh, CT, 3F5, 1976, pp. 303-306. 3 Min, Sytsng 7., and Howard X. Gostin* Simulation of Saai-8aech HaulsIan Polymerization Reactors far Polyvinyl Chloride (?7C) Syseaa. American Chemical Society, 1979, pp. 272-278. A-5 ucc 026651 4 Stanaback, R. John. Halogenatad Hydrocarbons as Chain Transfar Agents In ?VC Polymerization. 3?E, 1977, pp. 262-253. 5 Sudo, Y., ac al. Tha Rata of Catalytic Reaction of Vinyl Chloride Monomer. Tokyo Kogyo Koto Semaon Gakko Eenkya Hokokusho, 10, 1978, pp. 71-74. 2. Reaction Control by Chemical Means 1 Eoyanagi, Shunichi, Naoetsu-shi, Hajima Hitaaum, Niigata-ken and Kinya Ogawa. Method for Polymerizing Vinyl Chloride. U.S. Patent # 3,790,542, Feb. 5, 1974. 2 Koyanagi, Shunichi, Hajime Kitamura, Kinya Ogawa and Toshihida Shimizu. A Method of Polymerizing Vinyl Chloride. The London Patent Office, #1312102. 3 Lewis, Roger H. and Ronald L. Friedman, tfovel Co-initiator Systems. U.S. Patent #3,763,128, Oct. 2, 1973. F. Computer Control 1 Conaldlaa, Douglas. M. Liquid Level Measurement Systems: Their Evaluation and Selection. 2 Gore, Fred. Computer-process interface checklist, tascrumants and Control Systems, Feb. 1977, p. 95. 3 Gran, 3., Andersen, J. A., 3. Kloster and M. J. Hessen. Application of. a Digital Computer in a PVC Manufacturing Plant. Economics and Math Systems, 93, 312-324, 1974. 4 Hanson, Robert S. Engineered Systems for the Control of Toxic Chemical Emissions. Air Pollution Control Association, June 24-29, 1979, pp. 3-15. 5 Lazenby, 3. Level Monitoring and Control, Cham. Engineering, Jan. 14, 1980, pp. 38-98. 3 Liptak, 3. G. Instrument Engineers Handbook, Volumes 1 and 2; Chilton 3ook Co. G. Adsorption 1 Hanson, R. E., and R. 0. Heffland. Control of Toxle Air Emissions in Chemical Manufacture. CEP, Feb. 1980, pp. 80-83. 2 Process for Removal of Chlorinated Hydrocarbons, Rohm & Haas Co., June 1977. A--6 Ucc 026652 Incineration 1 3artra, C. G. Miniating Emissions from 7iayl Chloride ?lanej, ES&f 11 (9), pp. 364-363 (1977). 2 Costa Sings Incineration Tread. Chemical Heek, Peb. 13, 1930, p. 42. 3 Haelman, 2. Ellsworth, III. Toxic Organic Chemicals. Destruction and Haste Treaoent. Scyea Data Corp., 1973, pp. 72-73, 133-139, 206-211, 231-243. 1 Slang, 7-H. Controlling 7Inyl Chloride Emissions. C2?, December 1976, ??. 37-41. 3 Lee, Sun-chiab, H. J. Jahnes, and D. C. MaCaUley. Thermal Oxidation Kinetics of Selected Organic Compounds, JAPCA, 29(7), pp. 749-731. 6 Santolerl, J. J. Thermal Oxidation: A Solution to the 7d Emissions Problem, ?roc. Ann. Ind. Air Pollue./Contam. Control Seminar 3, 1973. 7 Shih, C. C., J. S. Cotter, D. Dean, S. ?. Page, E. ?. Pulaski and C. T. Thorns. Cooperative Cost Analysis and Environmental Assessment for Disposal of Organechlorlne Hastes. EPA-600/2-73-190, August 197ff, pp. 1-47, 34--93. 1. Costs 1 Bellamy, 2. G., et al. Engineering and Cost Seudy of Air Pollution Control. 7ol. 9, Polyvinyl Chloride Manufacture, July 1973. PS-247 p. 703. ; 2 Carpenter, 3. 3. 71nyl Chloride - An Aseessaent of Emissions Control Techniques and Costs. EPA-630/2-74-097, tf. 5. Environmental Protection Agency, Heehington, DC, September 1974, p. 34. 3 Irikson, D. G. & 7. lalcevie. Emissions Control Options for the SCGH Eydroscienca Corp., SA Contract 63-02-2377, March 1979. 1 Guthrie, 2. M. Process Plant Estimating Evaluation and Control Craftsman 3ock Co. of America, Solano 3esch, CA, 1974. 3 Liptak, SeU'Or-'Safety Instruments and Control - 7alves Costs, Chemical EBStneerlng-a, Sov. 2, 1970, pp. 94-100. 6 Peters, Max S. and X* D. Tlaserheue. Plant Design and Economies for Chemical Engineers. A--7 ucc 026653 J. Reactor Opening Loss 1 Barr, John T. Solvent Cleaning of ?VC Reactors. Air Products and Chemicals Inc. 2 Cohn, Louis. Internally Coated Reaction Vessel for Use In Oleflnie Poly merizacion. United States Patent, #4,105,840, August 3, 1973. 3 Jensen, Bruce S. and Jimmie 6. Tolar. Solvent Cleaning and Recovery Process. United States Patent, #4,009,043, Feb. 22, 1977. 4 Krause, F. E. ''Prevention o PVC Reactor Fouling and VCM Stripping of PVC Resins" Symposium on Control Technology In Plastics and Resin Industry, Atlanta, GA, February 27-23, 1979. 5 Metal Surfaces Benefit from Ion Implantation. Chemical Engineering, Dec. 3, 1979, p. 60. 6 Oringsr, Kenneth "Polymer-plant Engineering: Current Practices in Polymer- Recovery Operations," ChE March 20, 1972. ^ 7 Preparing Emulsion Poly (Vinyl Chloride) while Avoiding Vinyl Chlorid* Emis sions. March 25, 1976, Chsmischs Werke Sills, AG, German Pac* 2442575, S Preventing Wall Deposits in Poly Vinyl Chloride Production, August 21, 1975, Chsmischs Werke Hula AG, German Pat. 2405973. 9 Prevention of Coating Deposits in ehe Production of Polymer and Copolymersof Vinyl Chloride by Suspension Polymerization, February 19, 1976, Chemisehe Werke Hula AG, German Pat. 2437044. 10 Taniyama, A. and Nakanishl, K. Production of Vinyl Chloride Polymers, (Scale prevention] Japan Patent Mo. 52(1977] 71534 asgd to Ryouichi K.K. 11 Settinerl, William J., Milton C. Tolly. Trtaasanc of Interior Surfaces of Polymerization Reactora to Retard Polymer Buildup. United States Patent, #4,105,341. August 3, 1973. 12 Weimar, Dean Raymond, Albert M. Durr, Jr. Reducing PVC Polymer Buildup in Polymerization Reactors with Dichioxamides and Alumina. United States Patent, #4,068,052, Jan. 10, 1973. K. Fugitive Emission Control - 1 Ashford, Nicholas. Protection: How? Chamtech, Get. 1979, pp. 608-611. 2 Carcinogens - Job Sealth Hazards Series U.S. Dept, of Labor, Jan. 1973, OSSA 2204. 3 Chsmtech, Oct. 1979, p. 610. A-3 UCC 026654 4 Evaluation of 7iayl Chloride Emissions la tie Lon; 3each Area, California. National 71 aid Investigations Centar - leaver. E?A/33Q/2-74/CQ2*, May 1974. 3 Evans, L., C. Elaedarj, 3. Vyatt, A. 3asola, V. Hamilton, and . 7atavuk. Standard Support - Environmental Impact Document. An lavescigacion of Health Effects aad Emission Reduction of 7iayl Chloride la the 71ayl Chloride Monomer aad Polyrlayl Chloride Industries. 7oluma II. Draft Copy of report. 0.3. Environmental Protection Agency, Research Tri angle Path, '.torch Carolina, March 1973. p. 430. 3 Filatova, 7. S., and 7. A. Antonyuzhanko. Dynamics of Hygienic working Conditions end Occupational Disease Incident Among Workers la Suspension Polyvinyl Chloride Production Over a Humber of Tears. HTIS (national Technical Information Service). July 1974. P3-233 S14T. 7 Sristar, Charles J. Safety Evaluation...Chemtech, Nov. 1979, pp. 663-472. 3 Mtikarji, Asu. Unloading end Storage Techniques for 71ayl Chloride Monomer, Chem. Engineer, Sept. 12, 1977, pp. 133-160. 9 Qelfka, E. 3., Jr. 7CM Exposures - Engineering Controls end Work Practices, s?S RETEC; 7GS-Tha Process Perspective, Hew York, NY, Oct. 31-Hov. 1, 1974, Greenwich, CT* SPS L974, pp. 13S-137. 10 Paneser, K. S. Choose the Right Seal, Hydrocarbon Processing 60, Ho. 1, pp. 107-110, 1980. 11 Rationale for Regulating 7iayl Chloride. SPA-450/2-75-009. 12 7ervalin, Charles, 3. Curtail 7iayl Chloride Exposure, 3yd. Proc., Pen. 1976, pp. 132-136. 13 7inyl Chloride aad Cancer - A Study in Prevention, Job 3afsty end Health, C. S. Oept. of Labor, QS3A, ?eb. 1977. 14 71nyl Chloride - Job Sealth Hazards Series, G. S. Dept, of Labor, June 1973, OSSA 2225. 15 Wheeler, R. H., Jr* Automated Monitoring of 71syl Chloride Operations, Chemical Engineering Progress 74, Ho. 6, pp. 56-63. 16 wheeler, R. H., Jr., and M. E. Sutherland. Control of Intranslt 701, Chemical Engineering Progress 71,, Ho. 9, pp. 43-33, 1975. A-9 UCC 026655 L. Pressurs Rslief Devicas 1 3oyla, W, J., Jr. Sizing Relief Area for Polymerization Reactors. Cham. Ingiaaaring Progress, Vol. 63, No. 3, 1967, op. 61-67. 2 Hanson, G. W. and H. A. Martin. Loss Prevention, Part VI, Pressure Vessels, 53a. Sizing Rupture Discs for Vessels Containing Monomers. American Institute of Chemical Engineers. Sixty-seventh National Meeting. Atlanta, Georgia, Feb. 15-13, 1970. 3 Huff, James R. Computes Simulation of Polymerlzer Pressure Relief with TvoPhase Flow in Relief Systems. Paper No. 59D, 65ch Annual A.I.Ch.E. Meeting, Nov. 27-30, 1972. 4 Isaacs, Marie. Pressure-Relief System, Chemical Engineers, Feb. 22, 1971, pp. 113-124. 5 Lipeak, Bela G. Instrument Engineers Handbook, Vol. I and II. 6 Lipeak, Bela G. Safety Instruments and Control-Valve Costs. Process Instruments Part 4. Chemical Engineering, Nov. 2, 1970, pp. 94-100. 7 Loss Prevention Guide No. 1, Pressure Relief. Imperial Chemical Industries Limited, Petrochem. Div., 3111Ingham Teesside, April 1973. 3 Myers, J. F. and L. S. Wood. Enhancing Accuracy of Rupture Discs. Chem. Engineering, Nov. 3, 1965, pp. 209-212. 9 Pressure Relief Devices. Special Hazards Bulletin, Amer. Insurance Assoc. Mareh 1973, No. Z-25. 10 Pressure Vessels. ASMS Coda, Section VXH, 1974, p. 66 (Div. 1). 11 Pressure Vessels Installation and Operation, Appendix M. ASMS Code, Section VIII - Div. 1, 1974, pp. 363-364. 12 Rearick, John S. How eo Design Pressure Relief Systmss. Part 2: Sizing Relief Systems and Disposal of Vented Material. Hydrocarbon Processing, Sept. 1969, pp. 161-166. 13 Raaziek, John S. How to Design Pressure Relief Systems. Part 1: Devices, Codes and Causes of Overpressure. Hydrocarbon Processing, August 1969, pp, 104-1081 14 Richter, 3. H. Size Relief Systems for Two-Phase Flow. Hydrocarbon Processing, July 1973, pp. 145-152. 15 Sefety Systems. Pressure Relief Devices. Allied Chemical Process Enginesring Manual, Juns 1973. A--10 ucc 026656 15 Vtllardson, David F. Relieving Devices - Rupture Disc vs. Relief Valve, national Peerolaum Rafiaers Assoc, (MPRA),- MC-77-12. 17 Vlasmlliar, X. L. Maw Relief Valve Gas Equations. Eydrocarbon Proceseing, May 1970, pp. 123-124. 13 Zoolt, Roy J. Ruptura Discs for Low-burse Pressures, Cham. Engineering. March l, 1976, ?p. 131-136. M. Polymer 3tripping 1 Albright, Lyle ?. Vinyl Chloride Polymerization by Suspension Processes Tields Polyvinyl Chloride Resins. Chemical Engineering, June 3, 1967, ?p. 149-130. 2 Bellamy, R. G., ee. al. Engineering Cose Study of Air Pollution Control for the Petrochemical Industry, Vol. 9: Polyvinyl Chloride Manufacture, E?A- /68-02-0235, July 1973, p. 79. 3 Serene, A. J. The Solubility of Vinyl Chloride in Poly (Vinyl Chloride). Polymer Preprints. American Chemical Society, Vol. 13, Ho, 2 (9& ~ ?p. 197- 203, 1974. 4. 4 3erans, A. R. The Diffusion of Vinyl Chloride In Paly (Vinyl Chlorid >. Polymer Preprints. American Chemical Society, Vol. 13, Mo. 2(9): pp. 203-203, 1974. 3 3erena-, A. E. and X- 3. Eopf enbarg. Removal of Solvent and Monomer Residuals from Glassy Polymers. Recent Developments in Separations Science, M. U., ad., Cleveland, 0B: C3C Press, 1976, Vol. 3, pp. 293-312. 6 Johnson, G. R* The Efface of a Modified Jeber Muaber on Resin Properties During VC1 Suspension Polymerisation, A.I.Ch.2. 71st Annual Meg., Mcv. 12-16, 1973, paper L2A, 33 pp. 7 Erause, ?. E., Vinyl Chloride Monomer Stripping of PVC Resins. Presented at Sympoaitm on Control Technology in the Plenties end Resin Industry, February 27, 23, 1979, Aclases, GA, pp. 1-3. 3 Lasasy, 1. 2. Analytical Chemistry of Vinyl Chlorlde-A Survey, American Laboratory 9(13), pp. 17-20, (1977). 9 Orlager, Xesaaeh*. Polymer-Plane Engineering: Current Practice In PolymerRecovery Operations, Chemical Engineering. March 20, 1972, p. 77. 10 Mastall, G. J. J. T. 3err, and R. X. S. Chaa. Stripping VQ1 from PVC Resin. Chemical Engineering Processing, 71(9): pp. 34-62, 1973. 11 Sorenson, 'Jayne R., (Continental 011 Company, Pcnca City, Oklahoma). PVC Today, SP2 RST3C, Cherry Bill, Mew Jersey, Marsh 1-2, 1977, pp. 3-6. A-LI ucc 026657 APPENDIX 3 Calculation Procedure and Computer Prograa Jor Reactor and Venting Dynatrl ca B-l UCC 026658 Calculation Proeedura: The governing equations are as follows: Orifice Flow Equations . so,c " Ai J MW, V c J Cl) where: i phase (liquid water, liquid VCM, or gas) Qj flow in lb mole/min * effective area for the flow of phase j c gravitational constant A? pressure drop across orifice density of phase j C orifice coefficient *0.61 tyj*1.0 for liquids expansion coefficient for phase j MW. - molecular weight of phase j Pi"1.0-0.35AP for sas J --B------- where: Heat Liberated across Orifice for Flash * t <H1 - t,ouc> (2) i - component (liquid water, liquid VCM, gaseous water, and gaseous VCM) * heat liberated to flash water and VCM in 3tu/min H., H. - enthalpy of component i at orifice inlet 1 1,ow and exit, respectively In addition, HRel " FV, HiO AHV, HiO + FV, VCM AHV, VCM (3) 3-2 ucc 026659 where: HjO* 701 " quancicy of Hi0 and 7d which flashes across valve, respectively. a27 H,a lSV vrv " enthalpy of vaporisation of HiQ 1 8lU' ' VQl and 701, respectively. and, since liquid 701 is immiscible with liquid water. Y7-p? ^ *5 (4) where: Y, ?,, - molar fractions of 701 and HjO in aas phase at the orifice outlet ?A, PA vapor pressures of 701 and 3*0, resoeccively,at the orifice outlet. This relationship holds true unless all of the liquid 701 leaving through the orifice flashes and the amount of vatar which flashes is very small compared to the 7CM. aquations (3) . and (4) may be solved for the flashed flow rates and compositions. Critical Pressure Picnic "0.53 ? (3) where: ?sonic * critical pressure ? * reactor pressure Pout pressure downstream of relief valve If Psooic is greater chan Pout then chare is a possibility that the flew through the orifice reaches sonic velocity. 3-3 ucc 026660 RADIAN e Critical Flow Sanation (6) where: V. , V molar average specific volume at inlet and _n ouc outlet of valve, respectively. If the sum of the flows calculated using equation (1) is greater than Qcr^c* Chen the flow is critical and equations (2) through (4) must be salved iteratively so that the sum f the liquid and gas phase flow rates do not emceed Qcr^c> Boiling Equation If the reactor pressure is less than the sum of the vapor pressures of the components in the reactor, liquid vaporizas. (7) where: Vt.oe,, - moles of gas which must vaoorize Q , Qttr, Qttj " flow mattes of gas, liquid VCM, and liquid u water leaving the reactor, respectively. a , Ojv, try * densities of gas, liquid VCM, and liquid * u u water within the reactor, respectively. Material Balances within the Reactor ^vc " ^v hs (3) LV - -2lV + "jTM 7,,c + at (9) 3-4 ucc 026661 3H" (10) (11) ^ m reaction rata constant " factor which may ba changed bv user to adjust reaction rata ^?VC ^L7' ^G* ^LW TM naasas or PVC, liquid 7CM, gaa. and liquid water in the reactor, respectively. ^V' fractions of VCM and water in the reactor vapor. *^ Heat Balance 1 where: and: Btu * total reactor heat content 3rsB * heat released by reaction 3j heat removed through cooling jacket. a___ a_____ ^vc rma --35- 3j OA. (Ta - Tj) Hjy where Hsst * heat of reaction in Btu/lh sola (I * overall-heat-transfar coafficientr A - area for heat transfer * reactor temperature 3-3 (13) ucc 028662 RADIAN / Tj " jacket temperature HTM. * Factor which may be changed by user to adjust heat * removal. The enthalpies of water and VCM are functions of tempera ture with a basis of liquid state at 157*F. Equation (13) is used to compute the initial heat content, the derivatives are calculated using equations (3) through (12), by the integration routine, then equation (13) is used to solve for the temperature by the Newton-Raphson root solving technique. The new temperature is then used to calculate enthalpies, vapor pressures, mole frac tions and densities. Additional water or VCM is either vaporized or condensed due to the enthalpy change of the reactor contents. Hc - ZXL <Ht - Hlf nw) <1 where: * heat released due to temperature change H, H. - enthalpy of component i before and after , i,ne temperature change, respectively. In addition, where: Hc -mgv. new AHV, VCM +flGW, new AHV, Ha0 (17) wV.new, M*--CW, ,new - mvaapssoersl2aodf | VCreMsapnedctwivaetelyr. which are The liquid and vapor masses are adjusted using equations (17) and (4) to establish a new vapor-liquid equilibrium for the beginning of the next time step. 3-4 ucc 026683 ucc 026664 COWOH AVION jIUH.M ,,trtWLh ( UH S UlU 1 -07/21/00- 11 i <*OI (IAIN I'Hit(,MAH MI1MAM uiiUli t 01 tf I 11 O0?(|OM HA1A1A1 00ll1i!| Ui-AfiK L:()nmit|<2) 0000011 cofu.au i.LOt-hr.: OOlll 000*1 OUllti LCltll |-AbU tbfOMI 11(11)011} 00000} 000012 IXIIMMAL KMfMItlUS |IUOtM( 11Alit ) 0000 000 1 ut ooiu 001) ooi? inn a 001 <4 00 } OUU 001 1 oo?o Oii? I (Hi?? oo;m 00?*t Ott?b 00.1. 00? / 00 ill I Ilf L lilt A|t i*mmi 2 ('(till f mu l iruiu ill *11 Ml .litltfllt .*SCIU mHAIIii auhu I w KlUMl iiitkJt in Ill'll*M i 1 st.lt 11 III lt?1 Il'ilul- } III'I Ov SlultAi.i A-.'. 11,HI it t'l tliUli .(<* 1 u't , Ml l ,11 I VI lin.llMl. HAIL | OOOI 0001 00011 0001 0 00*1*1 1 Ul U 1, i OOOt.Ml 01*70 II. 111| MM .*11 00 Oil on no 0001 0000 OOUli.i 0000)7 OOloVi 00 0.17? 1001 1*101 iy 2i;0| UOOl 0000 000] o* * uott/uo OiHU?7 OllUiK,} Ofimun lltIHOII 21 2061. 0001 00 flit (tool 0001 000/*1 0000^7 OOlu?/ 0016^2 121lh2 20L 207U 0000 0000 0000 0000 U II Oil lid Oil 0001 U0|2(U| iL OOIMI UUU/37 551.11 0001 00l7bi bl. 0001 O0U72 ML oooo 000115 Ab 0000 M 0Oil 1<| 5 Mb 0000 It 0001.(0 i.i<lai:i 0000 It 0001b2 C3 oor*o it 000152 Mi.y 0000 It 000155 HIVC 0000 u 000016 IIA noon it 000071 lib III 0000 t: 0001bH Ml VII oooo it 000121 HULL 0000 1.' 000015 3bII ooou It OOOOOii HIV 0000 It 00006b pit 00 Oft It 000007 I'VC OOilh i: 00000} Mb 0000 It 000 U|, HbW 00 Oft l( 000005 HU 0000 6 0011107 ItliOu ouuo It UUOUbl ML JF OOllO It 000100 [AO 0000 li U0003I II l*sii 0000 It 000107 n 0000 it 000100 V(. 0000 I* 000Q21 vu 0000 000.161 rv 0000 OOO'tbb 30fi| oooo 0007i| 5 30 0|> 0000 OOOlbl bOt 0000 000753 6?3|. oooo l> oooin ALV 0000 It 000137 IIJ 0000 M 000106 MTU 0000 It O0O0i| 0 M 0000 It 000131 OLV 0005 r UOOOOO Ml 0000 1. 000037 HLMIM 0000 [t 0001 i.O 116 UP ooou It 000072 IILVO 0000 1' 6000|7 IlltXIl Oil 00 It 000007 H6v 0000 H 0000j 4 ntvH 0000 It OQOO^b rot if 0000 It 60001,3 PVI OOUfi 0 6OU0O4 ur.i 0000 It 000123 ru. ui 000b l OUUOOu Ml-In) 0000 It 000054 HI 10) v IMIUU It 6 000i|*| It XI 0000 II 00010b 1 A1 0000 l< 000032 TJ 0000 1* 000 T? 0000 1 0UUQ76 VI V 0000 II 000121 WT 0000 h OO0OL.2 vv UOOQ U0U/U7 507U 6000 0001 0007*17 313|j 001777 bit 6000 unu/57 62 7M 0000 It U00U2 ALU 0000 It UflUlHl MLV 6000 It 000030 C 0000 K 000153 lllllltl 6000 M 00013b l)MG 0000 It 000110 r 6000 It 000067 IlfiVl OOOO It 00007b libit1) 6000 It 000070 IILUF 0000 1 000117 11 tit UO0U It uouoii MbVN 0QO0 It uoooOb MLM 6060 It 000120 PSONIC . 0000 It 000057 pu 6000 h UOOllb 06V 000 b It 000002 OLV 6000 h 0U011I( OTF on no It 000050 ItllOLU 6000 It 000124 fiVL oooo It 000046 ILMP 0000 It 000033 TJMlW oooo It 000026 V oooo 6 000077 VLW 6000 It UIIOQOO X 0000 00072u 3161* 0001 0000 001311 It 000572 52 F 0001 0U0712 71 OOOO It 000102 AO 0000 R 000112 HIM OOOO ft 000130 f 1 OOOO It 0001*14 PP1U OOOO It 0001^4 6HLV OOOO It 000036 IHThlN 0000 It 00013/ IIFVN 0000 It OOOO1b iur 0000 It 000136 Ml UN 0001 1 UOOOOO 1 f ML 0000 II uooolo MbU OOOO 1 UOOllb WF oooo It OUOQ6U ptoial OOOO It 0000*4 PU1 ooou It 0001^2 tit VF 0005 It 000005 0LVF 0000 H 000.115 PfONST 0000 It 000035 Fa 0000 K 0001^5 SVLF 0000 It 000023 TfHPF oooo It 000034 1Jlnln 0000 It 000101 VILMN 0000 It 0001)20 vv 0000 It 00012/ XFrttl oooo U0. 0000 0n. 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HE TURN i GO 10 <4ta.6.;itJS4 4 XA<Ot|l=X l)XAI JNt=UX X=XIUX*UT RETURN a UX A1 ON ISDX A I JN1 *2 *DX X=XA|JNI0X*0I RETURN t> OX A I JN 1 -i)X A ( JN 1 *2 t *UX X = XAUNJtOX*01 HEI URN 7 OXAIJN)=<UXAIJNItQXI/6, X = XA| JNI *UXA| JNWQI MLI URN EN0 8fOR.Nl HKNTh tPRNTF SUHHOUTlNt PRNTFIPRIFNR.NFAiB.C.0*E*F.G*0Pi0I C C THIS SUBROUTINE KEEPS IHACK OF THE NUMBER OF LINES ON EACH PAGE AND C DETERMINES WHLTilER TO PRINT C COMHON/CCINT/OT COMMON/CINf/Ti JS* JN.UXACXIOI tXAlSUQ) . 10.JS4 COHMON/CPH/NPM 026677 COMHUH/PAGt/LlNE NPH = 0 IF I IPHNt .LI .PHI I GO TO 4 IF H I .GL .INR-DT/2.1 . AND. 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Till: C0l. 001210 001213 001216 001251 001251 001251 001251 001251 001257 001257 001257 001257 001261 001302 001311 0013H 001317 001322 001325 001330 001333 001336 001336 001336 001336 001336 001336 001311 001312 001350 001353 001366 001370 001373 001101 001105 001125 001132 001137 001176 onisuu 001502 001503 uco 026674 I-1* COSI non lobub iOb<|b tilbiib iflbuO iftbi| 7 iftbbO uibbl ulbb2 ulbbi iftbb'i llbbb tlbbr. ftbbO lib;,f, UbbO llb`,0 ObbV ilbb 7 lib 60 ilbt,l ttboi tib|,1 llbob l|b60 llbi.7 Ob7(l Ob 71 Jb/2 Ub/3 Ub7b .lb7b ilb/b Jb7b Ob 7b ub/7 0600 00(11 Ob 62 UO(i 1 100*1 OOOf) ftoub llOftb 3b b 3b l. 3b/* 3b 0 * tb`j* 300* (01 t 302* 3o3* aO`i 3**b * lOi. * 307* '(06 * (O'.l* 3/U* 3/1 * 3/2* 3/3* (7(|* it b* 3/0* 377. 376* i 7 `J * 300 301 * 302 3*3* (Oh * (Ob* 301. * 37* lOO* ill'll yin * yjj 1 .(/2 3b 1* (bt, 1 (bb* ib(,4 IV c c c r. t c c lb 20 c c c c c t: |Nl|A|l'Y lb CAimiAlll Fl-UH LI* M,U lllL I| MATUOI fhAfl^l i l|LU|i=n.U(m3>l t l|6U| =l LU1 fOhl'l t t(UWt=f6V(Itr.l*7 1 iiiiu. =i Gui ltni't ) i*V-l<t*VITfMi*M pu^PuiifnPFi t'iorAi.=i'y it'u YV=i'V/eiriiAt yu=ivv III-A? 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IF 1/ ON. 11 .0. iniiF =0. ritu wapom-i.lotnii rnun iti<)ur is tmAituibuFn lu satisfy no hi. at IIAI^NFL 01 no Vl-bSl l.; Moy-m y*m u**i;-ri vn-ii/t. m*=, on mmm vn in V( -io yii Ml Mn=IO Mil M*U| -IlliUti HliU..=H(>tMt *" 1 UQlb03 unib03 unibtiA ftOlbOb Oft lbl*i 00lb23 0QLb32 UO1 b30 OOlbHO OOlbbO (lOibOU 0ftlb03 Oft 1 b03 001bO3 0(Ub63 001b03 001 bt>5 OftlbOb 001611 001L17 001022 00102*1 001031 001033 00103/ 0010*11 0010*1*1 0010*1 / 001Obi QOlObb OOlObb 00l6bb OOlObb OOlObb OlllOOl 001007 001071 001673 00167b 0011,77 0O17U1 001701 001701 (U-I) Co tlUbOS (Il)b05 tuibori flObOS 00 bob ll(Jb07 l)0b| 0 0 Ob 1 1 OOfe J 2 00b | 1 oob m OObl t| oobm oi)<>m OUblb OObjb 00b lb uOblb OObl 7 00b,?0 00b2l 0l)b?2 00023 Of. b?b 0l)b2b 00b27 00b27 00027 ;Uib(.7 UOb 70 00b7.l VJli* * 1(00* '|0l * 1(02 * 103* I. l*<l i.Ob* <|0ii + *|0 7* i|0u* t0`J* *iio* (.11* 4 12 413* 11 * * i(lb + 4 lb* (.17* lib* i(i`j* ((2u * iiil* (.22* ;.23* ii 2*i i(2S* 1. 2b * ..27* (i 2(, C r c ii c c c r. c c b b bl !i2 S3 imm vapoii I'jusstiur., vtv defsiiy. and kiachom hati coustani aiU cAi rui Airu i on mi M i. ltni'fkatuhi. m im mlachih; hiiiii v=t>i:tii_vmr>i*i i KKc7.7llbr>ribLX|'(0.03f`bort*li M'F I VtW=NLW/Hf>I.V V(-U=.3LU/|t||0LW vb=v-vrv-vlu c=iit.*|(Coiisi*irM|>/yG IM| ,U-.l'lOIAl- I'M'TOlAL ItLTijtffl TO orGlNhJNG 0| lilt LOOP FH THC NFxl TIM*- SlEOj go in i roulLIiminfl IS 1 STAlU ISnLL* IMO HOHt FtOW oul OF HI ACTOuI--SIOOl QUF=0. 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S. /. 1V, E 12.51 slop LOO i.t.i or uipi u ai k*n: no diacnkstu s. orccoro> coXO vi i 001701 OQ1701 001701 001701 001703 001713 001723 00172b 001731 00173*1 0017*11 0017N1 0017*11 0017*11 0017*1/ 0017H7 001 7*t 7 0017*17 001751 001751 001752 001753 001772 00177b 001777 001777 001777 0020U2 002002 002005 i i UfUH.NI INI 1 * INI I suimuuiiNt inti t c imis souiuiutine 10.010,1001 SETS UP TMC ORDINARY DIFFERENTIAL EQUATIONS c COMMON/C IN I / T i JStJM.DXAI3QQ) t XAISOOI 10,JS4 COHMON/CC INI/111 10=100 JN=0 GO 10 lb.tit I tl I i 10 b JS=2 GO 10 1 3 js=jsm lKJS.LO.il JS=1 If US.I U.2 I RETURN i ur=oio 1 10= III* OI 1 = 10 HLIUltN t OS4=JS*l * 1 IfUSH.LU.Sl JS4 = 1 If I JS4 .1-0.1 I GO TO 2 If US4.LU.il GO TO 4 111 IUMN 2 01=010/2. GO 10 i 4 10=01IU 01=2.*01 l = lu ML I UltN LNO UFOIt.NI INI INI SU0M0OI1NL INI (X.OX I c c OIIOINAIU Oil f LltLNT IAL LUNATION SOLVER rooS=r- c ! LOMMON/HNI /T JS JN.OXAdUQ) tXAlSQO) . 10,JSl ammiN/LtiNi/UT JN=JN*1 go io ly.ti'OtOitiQ y x=x+ux*or RETURN H GO 10 11*2 I'JS l OXAIJNIS0X x=x+nx*ui RETURN ? x=x+(ux-uxa<jnii*DT/2. HE rutIN . A GO 10 IHtStG*l||J&4 H XAIJNIsX OXAIJN|=UX X=X*t>X*Of RETURN 5 UXAtJNI=UXAIJNl*2.*UX XsXAl JNM0X*PI HE TUItN 6 OXAI JN|=PXAI JN1*2.*0X XsXAUNIPX*D1 HEIOWN 7 OXAI JNI=(OXAI JNI tpX 1/6. XsXA( JN1*UXA< JNUDT ML rUHN LNO Of Oft.Nl PRNTF .PHNTF SUBROUTINE HRMTHPHl .FNH.Nf .A.a.C.O.E.F.G.O.P.Ut C c mis subroutine kelps fhack or hie HuMora or limes on each page ano C DETERMINES WHETHER 10 PKIMT c COMMON/CCINT/DT COMHON/CJNI/I* JSiJNiOXAOOOJtXAlSOOl.10.Jsi COMHON/CPR/NPR COMPOM/PAGL/LINE ucc 026677 NPR=0 Ifl IPHNI .LI .pun GO TO * lFIM.Gt.FNR~OT/2.|*ANP.|(JS.EG.2I.GM.IJS<I.EQ.<m| GQ IQ b IF 111 *GL . 1PRN 1-01/2*1 .AND. | IJS.EU.2) .Oft * IJSH .EO.H) 11 GO TO 5 HLIUUN 1 NF = I S I PUN 1 c | PUN M Pit I t> PRINT lUGiAttttCtptEtf iGOiPiU * CMIIKMIIIIHMI 1UU I UHMAI (3*. llNL = l.lNltl CALI. SIllltLUtll NPUM ML 1 DIIN fc 1 = 11. IPHN!=lt. NF = 2 UU I U- I 1300 T K A ( J) =(t * GO II) U ENO HEOR.N1 PllNlE2iPI4NlF2 SUUHUUIJNt PHNJF2 C C fill 3 3UU1IUUI1NE PRINTS VARIABLES OH THE SECOND PACE C COHMON/t Pll INT/SI1Q.HQI .KOUNI POINT 1 1 IOKMAI4//ilbX'3(UHPKCFLASII.2X).317HFLASHED.3X1.1X,31SHTOTAL.SXI./. 1 l*X,2UHGAS|HXiailVtH LIQ. .2*.0IIH20 LIG. 1Xt,3HPVC *5X,7ttVCM GAS.3X 2 iUitVCM LIU,,/. 3 UX.lt It I I ME. GIGX,UtlELOwl,4X,01iPBOOUCE0.2|2X.UIIEHlSSIONf ,/, H UX,3HNIN.3X,t>IOHHOLE/HlN,2Xl. IX ,3 4 bllCOMOLf .AX I ./,SX. IQOII 'i----------------------------- ---------------------------------------------------------------------------------------------------------------- A - ---------------" "------ " * " ~ --- ,/1 DO 2 =l,KOUNI 2 PH [HI 3.S4T.II.S12,it.S43.II.SI <1,11,345.11.S4G.It.S47.It.S4a.lt * .si*. 11.stio. it 3 I OKHAII3X.1PE10.H tDLTU.HI KOUN7=0 hliukn l 111) OEOtl.Nl S fll|(t i S lOltt SUiiitOUHNE STORE4wt L C (Ills sOltitUUf INE STORES THE VARIAOEES FROM | ACM IIMESTEP TO OE PRINTED ON (tit slcund page Of iaoee COMMON/LSIORE/A1101 COHMON/LpItlNT/S 110*401 iROUNI ROIJN1-HOONIM DO T 1=1.N 1 SI t ,i<OUNI I = A | I I lit lUltH 1 MKJ rJr Mu> tNU ilFOH.Nl HfJt AHO.INLAK C C LINt-AH HLGHtSSlUN SUfJItQUT I NtC SU11HOUIINL LINEARUtViNtA'IU ))IMl NS I UN XtNt .UNWFIHt iUi 1 4 = I 14 1 FlllsU. FsO. DO 2 1=1N M1I=M1)*X1II*VI1I M?I=F12)XII> I lllFlAlfIII I MHI=MHltX(Il*Xm 2 P=I*U. .1=111 H-F U*l I Al/PI/iFtHI-f 121 *FI2I/P> A=FI4I/F'-U*F12/P HtIUHN LNO 026679 APPENDIX C Example Suns on 10,000 Gallon and 20,000 Gallon Saaeeors C-l UCC 026680 COUPONKnON DISCHARGE FROM A 1'VC BATCH REACTOR Caae I. High Reaction Kata - Zero Heat Removal RE AC i Alt PRESSURE AT UmE OF DISCHARGE = 194.79 PS1A PRESSURE DOWNSTREAM OF VA-VE : 64.70 PS1A lit AC|ult TI.MI* AT l|fE OF DISCHARGE = 161.BO F UA|E|t JACKET TEMP AT DISCHARGE* 90.00 F ufaciOr volume = 1337.000 fU FT IIErT OF REACTION - 4Sbl,*000 DlU/LUMOLL LIQUID VCM INITIALIV Ifi REACTOR = RAO.90 UihOLf EIQ IU0 INI1IALLY IN REACTOR = 24OS.7 LRhgLE VAPOR INITIALLY IN REACTOR = 1.M12 CflhOLE JACKET COEF TIHES AREA - 564.2 UTU/IUR- E DENSITY OF WATER irONSTAMTI = 3*4570 LURCH/CU FT INITIAL DENSITY 0*" VCH = .60593 LUMULE/Cu FT AREA OF RELIEF VALVE OrIFICE OPENING = .0694 SU FT ORIFICE FLOW COEFFICIENT - .610 MINIMUM LIQUID ENTRAINMENT = *0100 CIJ FT L1Q/CU FT GAS MINIMUM WAIEr JACKET TLMP = 40.00 F L1Q uOl WHEN MIN EnTAA|NMENT IS REACHED = 1219,4 CU FI TIME MIN JACKET TEMP IS REACNFO s 5.00 MIN IliAIlNG JACKET F#CtDI! 5 *00 REACTION RATE FAClOR = 2.00 TIME HlN RE ACTOR pressure PS1A Reactor temp DEGREE F water JACKET TEMP degree f HEACIOR HEAT EON1 ENT 111 U GAS LtFl IN rcaCtDR lumole VCH LlQ. left in reactur LflMOLC 1120 LlQ* lefi IN REACfOR LUHOLt REACTOR VCM EIQ. VOLUME CU FT REALTOR H2U LIQ. VOLUME CU FI .00 1.00-01 2,00-01 i.00-01 4.00-01 5 .'00-01 6 .'00-01 7.00-01 O'OO-Ol 9.00-01 1.00*00 1.10*00 1.20*00 1.30*00 1.40*00 1.50*00 1.60*00 1.70*00 1.00*00 1,95+02 l*9b*02 1,96402 1,97*02 1.97*02 1.90*02 1,96*02 1,90*02 1,97*02 1,95*02 1.94*02 1.92*n2 1.91*02 1,09*02 1.00*02 |,06*02 1.65*02 1.03*02 1.02*02 1.62*02 1.62*02 1.62*02 1.62*02 1.63*02 1.63*02 1.63*02 1.63*02 1.62*02 1.62*02 1.61*02 1.61*02 1.60*02 1.60*02 1.59*02 1,59*02 1.50*02 1,50*02 1.57*02 9,00*01 0,92*01 0,03*01 0.75*01 0,66*01 0,50*01 0,50*01 0.41*01 0,3.3*01 0,24*01 0,16*01 O.OfltOl 7.99*01 7.91*01 7.02*01 7.74*01 7,66*01 7,57*01 7.49+CI 2,04605 2.16*05 2.31*05 2.43*05 2.52*05 2.59*05 2.61*05 2.50*05 2,45*05 2,24*05 2.02*05 1.00*05 1,59*05 I.37*05 1,15*05 9,24*04 7,01*04 4.70*04 2.55*04 1.51*00 1.7**00 1.95*00 2.l6*Oo 2.36*00 2.54*00 2.70*00 2,03*00 2.90*00 2,91*00 2.92*0q 2,93*00 2,94 *0q 2.95*00 2.96*00 2.97*00 2,90*00 2.99+00 3,06*00 4.61*02 4,57*02 4,54+02 4,50+02 4,46+02 4,42*02 4,30+02 4,39+02 4,29*02 4.24+02 4,19*02 4,14*02 4,09*02 4,04+02 4,00+02 3,95+02 3.90*02 3,66*02 3.61*02 2.47+03 2.45+03 2.44+03 2.42+03 2.41+03 2*40+03 2.39*03 2.36*03 2*36+03 2.30+03 2.36+03 2.36+03 2.37*03 2.37*03 2.37*03 2.37*03 2.37+OJ 2.37+03 2.37+03 5.72*02 5.67+02 5,63*02 5.59+02 5,54+02 5.49*02 5.44+02 5.39+02 5,32*02 5.26*02 5.19*02 5.13*02 5,07*02 5.00*02 4.94*02 4.60*02 4,62*02 4.76+02 4,70+02 7,13+02 7.09*02 7,05+02 7.01+02 6,96+02 C.9H+0? 6.91*02 6.89*02 6.66*02 6.68+02 6,07*02 6,67+02 6,67+02 6,67+02 6.67+02 6.66+02 6.66+02 6.66*02 6*66*02 ucc COUPON ATIOM Tirtt hiN i*iu:flasii GAS flou nutt/Hih HhLFLASII VCM LIU, FLOW hle/hin IMU'l LASH 1120 LIU. Flow HULL/MIN ft ASHtii GAS FLOU hfll l/MN FLAStlLO ULM MO. FLOW hull/nIN FLASIlf 0 1120 LIO* FLOW holf/hih TOTAL total TOTAL Fyt- vc" gas vcn lio. |>l<OUUCLO Emission EHlSSlON L(i"OLt MIHOlE LUHOLf .00 1.00-01 2.60-01 3.HO-01 9.00-01 s.oo-ot L.00-01 7.00-01 (1.00-01 *J. 00*01 1.00*00 l.10+00 1'20*00 1.20*00 1.10*00 1.50+00 1.00*00 1.70*00 1,00*00 3.96.01 l.A7*QQ 3.66*OQ 5.99+60 0.96*00 1.31*01 1.91*01 2.01*01 1.66*01 9.59+fll 9.5S*6i 0.51*01 H.HO*ol 9.99+fll 1.00*1)1 0.37*01 0.33*01 0.29ol 0.25*01 2,99*01 2,90*01 2,79*01 2.65*01 2,96*01 2.21*01 1.05*01 1.29*01 3.97*00 1.30*00 1,36*00 1.39*00 1.33*00 1.31*00 1.29*00 1.20*00 1.26*00 1.29*00 1.23*00 1.99*02 1,90*02 1.35*02 1.2*1*02 1,20*02 1,00*02 9.07*01 6,39*01 1,73*01 6,99*00 6,93*00 6.93*00 6.92*00 6.92*00 6.91*00 6.90*00 6.90*00 6.09*00 6,60*00 2,63101 2,71*01 2.02*01 2.96*01 3,19*01 3,30*01 3,73*01 9.20*01 5.13*01 9,95*01 9.91*01 9.U7*01 9.62*01 9.70*01 9.79*01 9.70*01 9.66*01 9.62*01 9.57*01 9.26*0o 3.93*00 3.99*00 2.97*0n 2.39*00 1,59*00 9.90-01 ,00 ,00 .00 .00 ,00 .00 ,00 .00 .00 .00 .00 .00 1.99*02 1.39*02 1.39*02 1.20*02 1,19*02 1,06*02 9.05+01 6,21*01 1,50*01 9.70+00 9.73*00 9.75*00 9.77*00 9.00*00 9.62*00 9.09*00 9.66*00 9.00*00 9.90+00 .00 3*60-01 7.21-01 1,06+00 1.95+00 l.61*00 2.17+00 2,53+00 2.66*00 3.22*00 3.55+00 3*67+00 9*16*00 9*96+00 9.77+00 5*05+00 5.32+00 5*56+00 5.69+00 .00 2.66*00 5.92*00 0.2A + O0 1.13+01 1.95+01 1.60+01 2.16+01 2,62*01 3.06+01 3.59*01 9.06+01 9.95+01 9.90+01 5.39*01 5.76*01 6.22+01 6,65*01 7.06+01 .60 9.20-fli 7.92-01 1.12+00 1.30+00 1.50+00 1.60+00 1.69+00 1 .69 + 0(1 1.69+60 1.69+00 1,69+00 1.69+00 *.69+00 1.69+06 1 .69 + 00 1.69+00 1.69+00 1.69+00 ucc 026682 ^ ,y t t TIHL HfN UFACTOM pressure PSIA Hf ACTOP TEW1 OEGHEE F UAlEH JACKFT ILHP UtGiiEE F REACTOR HEAT CONTENT U1U GAS LtFl IN realtor EBnOEE VCH L1Q. LIFT IN REACTOR MMOLE H20 LIQ. LtFl IN REAtTOR Ml HOLE REACTOR LIO. volume 6U FT reactor 1120 L IQ. VOLUME CU FI 1.00too 1.00*02 1,56*02 7.00*01 3.00*05 3,01*00 3,77*02 2*37+03 *1 .LX+ 62 6,85+02 2*00+00 1.79*02 1,56*02 7.32*01 -1.90*00 3,02*00 3.72+02 2*37+05 X,56+02 6,65+02 2*10+00 1.77+02 1.55+02 7.20+01 -0.19+00 3,03*00 3.66+02 2*37+03 X.52+02 6.85+02 2.20*00 1.76+02 1.55+02 7.15+01 -6,00+00 3.00*00 3.63+02 2*37+05 X.X7+02 6.65+02 2 .'30*00 1*70+02 1*50+02 7.07+01 -6*70+00 3.05*00 3.59+02 2*37+05 X.XI + 02 6.8X+02 2.>1(1*00 1.75*02 1.50+02 6.96+01 -1.09+05 3.05*00 3,55+02 2.37+05 X.36+02 6.8X + 02 2.50*00 1.71*02 1.55+02 6.90+01 1.32+05 3,06*00 3.50+02 2*36+05 X,30*02 6.8X+02 2.00*00 1.70*02 1.52*02 6.02+01 -1,55*05 3.01*00 3.06+02 2*36+03 X ,25+02 6.8X + 02 2.70*00 1.66+02 1.52*02 6.73+01 -1.77+05 3,06*00 3.02+02 2*36+03 X,19 + 02 6.8X+02 2.00*00 1.67+02 1.51*02 6.65+01 -1.99+05 3,09*00 3.36+02 2.36+05 X.1X+02 6.83+02 2.00*00 1.65+02 1.51*02 6.56+01 -2.22+05 3.10*00 3.30+02 2.36+05 X,06+02 6,65+02 o 5.00*00 5.10*00 1.60+02 t,65*02 1.50+02 1.09*02 6.06+01 -2*00+05 6.00+01 -2.66+05 3,11*0q 3,11*00 3.30+02 3.26+02 2.36+05 2.36+03 X.03*02 3.96+02 6,83+02 6,83+02 5'20*00 1.61*02 1.09*02 6.31+01 -2,69+05 3,12*00 3.22+02 2*36+03 3,93*02 6,83+02 5.50*00 1.60*02 1.06*02 6.23*01 -3,11+05 3.13*00 3. 16 + 02 2*36+05 3.66+02 6.82+02 5.HQ*00 1.56*02 1.06+02 6.10+01 -3.33+05 3,10+00 3.10+02 2*36+03 3,63+02 6.82+02 5.50*00 5.00*00 1.57*02 1,50+02 1.07*02 1.06+02 6.06+01 -3.55+05 5,96*01 -3.77+05 3.10*00 3,15*00 3,10+02 3.07+02 2*36+03 2* <36i0^ 3,76+02 5.73+02 6,82+02 6,82+02 5.70*00 5.60*00 1.50+02 1,55+02 1,06+02 1.05+02 5.69+01 -3.99+05 5.61+01 -0*20+05 3.16*00 3.1I*Oq 3,03+02 2,99+02 2*36+05 2.35+03 3.66+02 5.63+02 6,81+02 6,61+02 5.90*00 1.52*02 1.05*02 5.72*01 -0.02*05 3,17+00 2.96+02 2*35+03 3.59+02 6,81+02 X,00 + 00 <*'10*00 1.50+02 1.09*02 1,00*02 1,05+02 5.60+01 -0,60+05 5,56+01 -0,65+05 3.16+00 3,19*00 2,92+02 2.06+02 2*35+03 2*35+03 3.5X+U2 3.50+02 6.81+02 6.81+02 0.20*00 1,06*02 1.05*02 5,07+01 -5,06+05 3,19*00 2,65+02 2*35+05 3.X5+02 6,aOt02 0.50*00 1.06*02 1.02*02 5,39+01 -5,27+05 3.26*00 2.61+02 2*35+03 3.XA+02 6.80+02 0.>10*00 l.05*f,2 1.02*02 5,30*01 -5,09+05 3,21*00 2,76*02 2.35+05 3.36+02 6,60+02 0.50*00 1.00*02 1.01*02 5.22*01 -5,70+05 3.21*00 2.70*02 2*35+05 3.32+02 6.80+02 O.bOtOO 1.05*02 1.00*02 5,10+01 -5,90+05 3,22*00 2.71+02 2.55+03 3.27+02 6,80+02 o;7o*oo 1.01+02 1,00*02 5,05+01 -6,11+05 3,23*00 2.66+02 2*35+03 3.23+02 6.79+02 0'60*00 0.90*00 5.00*00 1.00*02 1.59*02 1*50+02 1.39*02 1.39*02 1.36*02 0.97*01 0,66*01 0.60*01 -6,32+05 -.6,52 + 05 t* 12* 05 3.23+00 3,20*00 3.20*00 2.60+02 2.61*02 2.56+02 2*35+05 2.35+03 2*35+03 3.19+02 3.15*02 3.10+02 6,79+02 6.79+02 6.79+02 5.10*00 1.57*02 1.37*02 0,00*01 -6,92+05 3,25*00 2.55+02 2*35+05 3.06*02 6.79*02 ucc 026683 cmiiNMiimuN IlHt rtlN PltEl LAS|I bAS FLUM HOLE/MlM I'fttFLASli Vc LIO. Ft.OU HOLf/MlII CRFfLASM 1120 HO. Fiog note/hii4 FLASHLU FLASHED 6AS yen Liu. FLOW FLOW HOlE/MlN 'Ll/rtlN FLASHtD H20 LIU. FLOW HOLE/IN TOTAL TOTAL lUfAL l*U6 VC GAS ven LIU. pHO^UCLU EMISSION EMISSION LunoLt lumole luhole 1i90too 2.00400 2.10400 2.20400 2.10 400 2.10400 2.50+00 2..0400 2'70 400 2.00400 2/JO400 1'00400 1.10400 1.20400 1.10400 1.10400 3.50*00 1 *00 400 1.70400 1.00400 1.90400 1.00 400 1.10*00 1.211400 1.10*00 1.10400 1 .ii04Q0 1 .00400 1.70400 1.00*00 1.90*00 *1.0(1 (OU S'lO(00 1.22*01 1,1041)1 1 * 11 4(11 1.10*01 1.07401 1.01401 3.99401 1.9titnl 1,92401 1.00401 1,01401 1.01*01 1.7H01 1.7-1*01 l,7A*ol l.bfeitol 1.61*01 1.09*01 1,06 id 1 1.02*01 3.19+01 1.15*01 1.12+01 1.19401 1.154fll 1.12401 3.29*01 1.25*01 1,22*01 3.19*01 1.16tol 1.11*01 3.10+0* 1.21400 1,19400 1.10400 1,16400 1,11400 1.11*00 1.11*00 1,10400 1.00400 1.07*00 1.05400 1.01+00 1.02+00 1.00+00 9.90-01 9.75-01 9.60-01 9.16-01 9.31-01 9.17-.11 9.01-01 0.09-01 0.75-01 0.61-01 0.10-01 0.11-fll a.21-01 0.00-01 7.95-01 7.02-01 7,70-01 7.57-01 1.15-01 6.07+00 6,06+00 6,01+00 6,01+00 6.02+00 6.01+00 6.79*00 6,70400 6,76+00 6,71400 6,71+00 6.71400 6.69*00 6,60*00 6.66*00 6.61400 6.62400 6.60+QQ 6.50400 6.56400 6.51(00 6,52400 6.50+00 6.17+00 6.15(00 6,11(00 6.11(00 6,10+ 00 6.16(00 6.11(00 6.11*00 6.29+00 6,27tOO 1.51401 1,19+01 1,15+01 1.11401 1.16401 1.12401 1.26401 1.21*01 1,20(01 1,16*01 1.11*01 1.07*01 1.01401 3.99401 1.95*01 1.91*01 3.67*01 1.01401 1.79*01 3,76401 1.72*01 1.66*01 1.61*01 1.60401 3.57*01 3.51*01 1.19*01 3.16+01 3.12*01 1.39(01 1.15*01 3.12*01 3.26+01 .00 .00 .00 .00 .00 .00 .00 ,ou .00 .00 ,QQ .00 .00 ,00 ,00 .00 .00 .00 .00 .00 ,00 .00 .00 .00 - .00 .00 .00 .00 .00 .00 .00 .00 .00 1.92+00 1,91+00 1.96+00 1,97*00 1.99400 5.01+00 5,02*00 5,03 + OQ 5,05+00 5,06+00 5,07*00 5,00*00 5.09*00 5.10*00 5,11*00 5,12400 5,12*00 5,11*00 5,11400 5.11*00 5.15*00 5.15*00 5,15*00 5,16400 5.16*00 5,16400 5,16400 5, l6+0i| 5, l6+Oo 5.16*00 5.16400 5, 16 + 00 5,15*00 6*06400 6*12+00 6*55t00 6*77+00 6*96+00 7*19+06 7.19+oa 7*56+06 7*77+06 7*95+00 6*12*00 0*29*00 0*15*00 0*61*00 0*76400 0*90*00 1*01400 9*10400 9*11400 1. <|1400 1.56*00 1.67*00 1.79+00 1.10+00 1.00+01 1.01*01 1*02*61 1.01*01 1.01*01 1*05401 1*66(01 1*06+01 1.07*61 7.51+U1 7.11*01 6.15+61 6.76*61 9.10*61 9.50*61 9.99*61 1.01+62 1.00(62 1.12*62 1,16*62 1.19*U2 1.21(62 1.27*62 1,31*62 1.31*62 1.16*62 1,12+62 1.15+62 1.19+62 1.52+62 1.56+62 1.59(02 1.63*02 1.66+02 1.70(02 1.73+02 1.76+02 1.79(02 1.63 + 1(2 1.06+U2 1.09+62 1.92+62 1,69+00 1.69+00 1.69+00 1.69+06 1.69+00 1.69+00 1.69+00 1,69+00 1.69+00 1.69+00 1 ,69*00 1,69+00 1 ,69*00 1 .69+00 1.69+00 1.69+00 1.69+00 1.69+00 1.69+00 1.69+00 1.69+00 1,69+00 1.69(00 1.69+00 1.69+00 1,69*00 1.69+00 1.69+00 1.69(00 1.69+00 1.6*4+00 1 .69*00 1 ,69+00 ucc 026684 CONPMIITKM Tint HiM REACTOR PKESSUKf PSIA Hf ACT 0(( TEMP Of GIlCE F UMLll JACKIT TEMP OtGKEE F hi ACTOR lit AT CON I EM P1U GAS LLF1 IN |(t ALTON luhole yCH (.10* l.EFT IN REACTOR LU.M0LE 1120 LIU. LEFl IN realtor Utnoi.L H*-AC TOR t IQ. yOLUPE LU I T REALTOR 1120 | IQ, voLum: CU FI b,20*00 5.-30*00 5S10+QQ b.50*00 5.00*00 5V70+00 5.00*00 5.90*00 b.00*00 0.10*00 0.20*00 6.30*00 6.10*00 0.50*00 h.60*00 6.70*00 6.00*00 6.90*00 7.00*00 7.10*00 7.20*00 7'3U*00 7.10*00 7.50*00 7.b0*00 7.70*00 7.00*00 7.90*00 0.00*00 0.16*00 0.*20*00 0.30*00 0.90*00 1.36*02 1.31*02 1.33*02 1.32*02 1,31*02 1.30*02 1,29*02 1.20*02 1.27*02 1,26*02 1,25*02 1.21*02 1.23*02 1.22*02 1.21*02 1.20*02 1.19*02 1.19*02 1.10*02 1.17*02 1.16*02 1.15*02 1.11*02 1.11*02 1,13*02 1.12*02 1.11*02 1.10*02 1.10*02 1.09*02 t.06*02 1.07*02 1.07*02 1,37*02 1,36*02 1,36*02 1,35*02 1,35*02 1.34*02 1,33*02 1,33*02 1.32*02 1.32*02 1,31*02 1.31*02 1.30*02 1.30*02 1.29*02 1.29*02 1.20*02 1.20*02 1.27*02 1,27*02 1.26*02 1,26*02 1,25*02 1,25*02 1.24*02 1.24*02 1.23*02 1.23*02 1.22*02 1.22*02 1.21*02 1.21*02 1.20*02 4,00*01 1,60*01 1.00*01 1,00*01 1,00*01 1,00*01 1,00*01 1,00*01 1,00*01 1,00*01 1.00*01 1,00*01 1.00*01 1.00*01 1.00*01 1.00*01 1,U0*01 1.00*01 1.00*01 1.00*01 4.00*01 1.00*01 1.00*01 1.00*01 1.00*01 1.00*01 1.00*01 1.00*01 1.00*01 1,86*01 1.00*01 1.00*01 1.00*01 *7.12*05 >7,32405 .7,52*05 -7.72*05 .7.91*05 .0.10*05 -0.29*05 -0.10*05 -0,67+05 .0,06+05 -9,05+05 -9.23*05 .9,11+05 -9.59*06 -9.77*05 .9.95+05 -1,01+06 -1.03+06 -1,05+06 -1,06+06 .1,00+06 -1,10+06 -1,12+06 -1,13+06 -1.15+06 -1.16+06 -1.10+06 -1,20+06 .1.21+06 -1.23+06 -1.21+06 -1,26+06 -1,20+06 3,25+00 3,26+Oo 3,27+00 3.27+00 3.20+00 3,20+0Q 3.29+00 3.29*00 3,30+Oq 3,30+Oq 3.31+00 3.31+00 3.32+00 3,32+0(1 3.33+00 3,33+00 3.31+00 3,31+00 3,31+00 3,35+00 3.35+00 3,36+00 3,36*Oq 3,36*00 3.37+00 3.37+00 3.30+00 3,30+00 3,30+00 3,39+00 3,39*00 3,39*00 3.40*00 2,51+02 2,40*02 2,95+02 2,42*02 2,39+02 2,36+02 2,33+02 2,30+02 2.27+02 2,24+0? 2,21+0? 2.19*02 2,16+0? 2.13*0? 2,10+0? 2.07+02 2.05+02 2.02+02 1,99*02 1.97*02 1,91*02 1,92+02 1.09+02 1,07+02 1.01+02 1,02+02 1,79*02 1.77*02 1.71*02 1.72*02 1.70*02 1.67+02 1.65+02 2*35+03 2.31+03 2*31+03 2*31+03 2*31+03 2*31+03 2*31+03 2.31+03 2.31+03 2*31+03 2*31*03 2*31+03 2*31+03 2*34+03 2*34+03 2*34+03 2.33+03 2.33+03 2*33+03 2*33+03 2.33+03 2*33*03 2*33+03 2*33+03 2*33+03 2*33+03 2*33+03 2*33+03 2.33+03 2*33+03 2*33+03 2*33+03 2 33103 3,fl?+U2 2,90+02 2,94*02 2.90+02 2,07*02 2.03+02 2,79+02 2,75*02 2,71+02 2,60*02 2,64+02 2,61+02 2.57*02 2.54+02 2.50+02 2.47+02 2.43+02 2.40+02 2,37+02 2,34*02 2.30+02 2.27*02 2.24+02 2.21+02 2,10+02 2.15+02 2.12+02 2.09+02 2.06*02 2.03+02 2,00+02 1.97+02 1.94+02 6.78+02 6.70*02 6,70+02 6,76+02 6,70+02 6.77+02 6,77+02 6.77+02 6.77+02 6,77+02 6,76+0? 6,76+0? 6,76+02 6.76+0? 6.76+02 6,76+02 6,75+02 6.75+02 6,75+02 6.75+02 6,75+02 6,71+02 6.71+02 6,71+02 6,74+02 6,71+02 6,71+02 6,73+02 6,73+02 6.73+02 6,73+02 6.73+02 6.73*0? ucc 028685 COW^UUMIUH rmt niN I'lltfLAStt UA$ flow MOLL/ft1N 1*|(FFLAS1I VCH MO. flow HOLE/H1N 1`HEfLASIi 1120 LIQ. f*ou MOL/HIN tlASHtU (.AS flou MOI /HIN fLASIlUl VC*1 LlU. flow MULL/MIN FLASNtO 1120 LIO. Flow NOLL/MIN 101AL t*VL pitouuctu LnMOLk IOIAI VC* f,AS emission LUMOlL IUJAL vcn LI<J, miss ion LWHOLE 5.20+00 1.07*01 7,12.01 6,24*00 1.29(01 5.30+00 1.04*01 7,20.01 6.22*00 3.22*01 5,40*00 1.01*01 7,00-01 6,19*00 3.10*01 5,50*00 2.90*01 6,97.01 6,17*00 3.15+01 5.60+00 2.95+01 6.09.01 6.14*00 1.12*01 5.70*00 2.92*01 6.74-01 6,12*00 1.00*01 5.00*00 2.09*01 6.62-01 6.09*00 1,05*01 5.90*00 2.0to*ol 6.91.01 6.07*00 1,02*01 it.ObtOO 2.01*01 6.40.01 6.04*00 2,99*01 O.iotoo 2.81*Cl 6,29.01 6.01*00 2.96*01 0.20*00 2.70*01 6.10-01 9.99*00 2.93*01 0*1*# 6.30*30 6.40*00 to.bo too 2.75+nl 2.72*01 2.70*01 6.00-01 9.97-01 9.07-01 9.96*00 9.93*00 9.91*00 2.90*01 2,07*01 2.04+01 to.60 *00 2.07*01 9,76-01 9.00*00 2,01*01 to. 70*00 to.00*00 2.64*01 2.62*01 9.60-01 5\ 9.09*00 9.03*00 2.70+01 2.75+01 to. 90*00 7.0Qt00 2.99*01 2.97*01 9.47-01 9.37-01 9.00*00 9.77*00 2.73*01 2,70*01 7.10*00 2.94*01 9.27-01 9.75*00 2.67*01 7'20t00 2.92*01 9.10-01 9,72*00 2,64*01 7.10*00 2,49*01 9.09-01 9.69*00 2,62*01 7.40*00 2.47*01 4.99-01 9.67*00 2,59*01 7.50*00 2.4M01 4.90-01 9.64*00 2.56*01 / 'c.0 (00 2.42*01 4.02-01 `i.tol *00 2.j4*0I 7.70*00 2.40*01 4.73-01 9.50*00 2.51*01 7'00 * 00 2.10*01 4.64-01 5.56*00 2.49(01 7 .''*0 * 00 0.00*00 2,19* o1 2.11*01 4.96-01 4.47-01 5.53*00 5,50*00 2.46*01 2.44+01 0.10*00 2.11*01 4.19-01 5.47*00 2.41+01 U'20*00 0,10*00 0.00*00 2.29*fll 2 * 2*>t o 1 2.24*fll 4.11-01 4.23-01 4.15-01 5.44+00 5,42*00 5,39*00 2,19*01 2(56+01 2.14+01 .00 *00 .00 .00 .00 .00 ,00 .00 .on .00 .00 .00 .00 ,00 ,00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 *00 .00 .00 .00 ,00 .00 .00 .00 &15 tO 0 5,15+0q 5,14*0(1 5.14*00 5,13*0fl 5.12*00 5,12*00 5.11*00 5,10*00 5, 10*Qq 5.09*00 5.00*00 5.07*00 5,06*00 5.05*00 5.04*00 5,03*00 5.02*00 5,01*00 5,00*00 4.90*00 4,97*00 4,96*00 4.95*0(1 4.93*00 4.92*00 4,90*0(1 4.09*0(1 4.89t0(| 4,36*0(1 4,04+0(1 4,03+00 4,01+00 1.00(01 1*09+01 1.09*01 1*10*01 1*11*01 1,12*01 1.12*01 1.11*U1 1,11*01 1,14*01 1.14*01 1.15*01 1.15*01 1.16*01 1.16+01 1.17+01 1*17+01 1.10+01 1 10+01 1.19+01 1.19+01 1.19*01 1.20*01 1 .20(01 1.20(01 1 >21(01 1.21(01 1.21*01 1.22+01 1.22*01 1.22*01 1.21*01 1.23*01 1.95*2 1,90*02 2.01(02 2.04*02 2.07*02 2.10*02 2.13*02 2.16*02 2.19*02 2.22+02 2,25*02 2.27+02 2.30+02 2.33+02 2,36*02 2.30*02 2.41+02 2.44*02 2.46*02 2.49*02 2.51*02 2.54*02 2.56+02 2.59+02 2.61*02 2.64*02 2.66*02 2.60*02 2.71*02 2.73*02 2.75+02 2.70*02 2.60*02 1.69+00 1,69+00 1.69*00 1.69+00 1.69*00 1.69+00 1.69+00 1,69+00 1,69+00 1,69+00 1,69*00 1 .69*00 1.69*00 1.69+00 1.69+00 1.69+00 1.69+00 1.69+00 1.69+00 1,69+00 1.69+00 1.69+00 1,69+00 1.69(00 1.69+00 1.69*00 1.69+00 1.69+00 1,69*00 1,69*00 1,69*00 1.69*00 1.69*00 ucc 026686 TlttL MIN HrACTOR PRESSURE PSIA ' HrACTOll If HP ttEGREE F WAjEH JACKFT UMP OLGrEE F hCAClOh HEAI CCNlENl UlU GAS LtFl IN RLACfUH LtiMOt-E VCH liq. eeft IN REACTOR LONOLE tt20 LIO. eefi in REALTOR LunoLL REACTOR yen 1 iu. *QUr*E cu ft REACTOR H20 lU). VOLUME CU FI U'50 + 00 0X60*00 fl .'70*00 u;oo*oo u.9o+uo 9.00*00 9.10*00 9,20*00 9.50*00 9.90*00 J.50+00 9*60+00 9.70*00 9.00*00 9.90*00 1 '00*01 1.06*02 1,05*02 1.05*02 1.09*02 1,05*02 1,03*02 1.02*02 1.01*02 1.01*02 1.00*02 9,96*01 9,90*01 9,09*01 9.70*1)1 9,73*01 9.67*01 1.20*02 1.19*02 1,19*02 1.16*02 1,10*02 1.10*02 1.17*02 1.17*02 1.16*02 1.16*02 1.15*02 1.15*02 1.15*02 1.19*02 1.19*02 1.13*02 9,80*01 9,60*01 9.00*01 9.00*01 9.80*01 9.00*01 9,00*01 9.00401 9.00*01 9,00*01 9.00*01 9,00*01 9.00*01 9.00*01 9.00*01 9.00*01 .1.29*06 >1.31*06 >1.32*06 >1,39*06 >1,35*06 >1,36*06 >1.38*06 >1,39*06 >1,91*06 >1.92*06 > 1 ,93*06 >1,95*06 >1,96*06 > 1,90*06 >1.99*06 >1.50*06 5,90*00 3,ol*0o 3.91*00 3.Hl*00 3.92*00 3.92*00 3,92*00 3,93*00 3.95*00 3.93*00 3.93*00 3.99*00 3.99*00 3.99*00 5.95*00 3.95*00 1.63*02 1.61 * 02 1.58*02 1.56*02 1.59*02 1.52*02 1,50*02 1.90*02 1,96*02 1.93*02 1,91*02 1.39*02 1,37*02 1.35*02 1,33*02 1.31*02 2.32*03 2.32*03 2.32*05 2.32*03 2.32*05 2.32*03 2,32*03 2,32*03 2.32*03 2.32*03 2.32*05 2.32*03 2.32*05 2.32*03 2.32*05 2.32*03 1.92+V2 1.09*02 1.06*02 1.03*02 1.01*02 1.70*02 1.76*02 1.73*02 1,70*02 1,60*02 1.65*02 1.63*02 1.61*02 1.50*02 1.56*02 1.53*02 6.72*02 6.72+02 6.72*02 6,72*02 6,72*02 6.72*02 6.71*02 6,71+0? 6,71*02 6.71*02 6.71+02 6,71*02 6.71*02 6,70*02 6,70+02 6.70*02 ucc 026687 [- ! COUFOUJIVIOM UF IN I |Hfc rtlN PllFL*Sf GAS FLOW MOLl/Nlw FuLTtASII Vtt LIQ. FLOW NQLE/NIH i'ltf flash 1120 LIU, FLOW NULL/MIN Ft ASHt U ftASiiLI) FLASlif 1) CAS vcn LIU, 1120 L10, r LON FLOW FLOU NClL/MN null/Nin MOLE/NIN IOIAL t'UL piiomictu liinole IOIAL VCn f,AS EMISSION BUNDLE IOIAL ucn Liu. EN1SS10N LUNOLE 0.'50*00 <1.60400 0.70*00 u.00*00 0.90*00 9.00*00 9.10*00 9.20 *U0 9]SO *00 9**10*00 9*50*00 9.60*00 9.70*00 9 .*00*00 9.90*00 1.00*01 2,22*01 2.2Q*Tl 2, lo*f> 1 2.16*01 2.11*01 2.12*01 2,10*01 2.00*01 2,06*01 2.09*01 2.02*01 2.00*01 1.90*01 1.96*01 1.99*01 1.92*01 9.07-111 1.99-0* 1,91-01 1,09-01 1.76-01 1.69-01 1.62-01 1.55-01 1.90-01 1.91-01 1,19-01 1.20-01 1.21-01 1.15-01 1.00-01 1.02-01 5,16*00 5.11*00 9.10*00 5.20*00 5.25*00 5,22*00 5,19*00 5.16*00 5,11*00 5.11*00 5,00*00 5.05*00 5.02*00 9,99*00 9.96*00 9.94*00 2.12*01 2.29*01 2.27*01 2.25*01 2,21*01 2,20*01 2,16*01 2.16*01 2,19*01 2.12*01 2,10*01 2.07*01 2.05*01 2.01*01 2.01*01 1.99*01 .00 .00 .00 .00 .00 .00 .00 ,00 .00 ,00 .00 *00 .00 .00 .00 .00 9.00*00 9,70*00 9,76*00 9,75*00 9.71*00 9.71*00 9,70tOQ 9,60*00 9,66*00 9,69*00 9,62*00 9.60*00 9,56*00 9.57*00 9.55*00 9,54*00 1.21*01 1.21*01 1.29*01 1.29*01 1.29*01 1.29*01 1.29*01 1.25*01 1.25*01 1.25*01 1.25*01 1*25*01 1*26*01 1*26*01 1*26*01 1*26*01 2.02*02 2.09*02 2.07*02 2.09*02 2.91*02 2.91*02 2.96*02 2.97*02 2.99*02 1.01*02 1.01*02 1.05*02 1,07*02 1.09*02 1.11*02 1.11*U2 1 .69*00 1 ,6`J*U(1 1,69*00 1,69*00 1.69*00 1.69*00 1,69*00 1.69*00 1,69*00 1,69*00 1.69*00 1.69*00 1 ,69*00 1,69*00 1.69*00 1.69*00 ucc 026688 coapmimtoH DISCHARGE FROM A FVC HATCH REACTOR Case 2. IllgU Reaction Kate - Cold Hater on Jacket HC ACT OH PRESSURE AT UhC OF |11 SC HA|i Gtl = 194.79 PSIA PHESSUHE OOUnSTREAH OF VACWE = 64*70 PSIA HtAClOH H-rtP AT U|E Of DISCHARGE = 161.80 F uAlEH JACKET TE*U> AT UISC"ARGf= 90.00 F HFACTOH VOLUME s 1337,000 CU FT HEaT OF REACTION = 45516*000 blU/LUMOLt LIQUIU ven INITIALLY In REACTOR = 1160.90 LBhOLf LlQ 1120 INITlALEr IN REACTOR = 2465*7 LUMOLE VAPOR INITIALLY IN REACTOR = 1.M42 LUMOLE JACKET COKF TIMES AREA - 564.2~UTU/tUH F UENSllY OF HATER |CONSTANT = 3.4570 LUfOU/CU FT INITIAL DENSITY OF VCM = ,8Q*93 LUMUEE/CU FT AREA OF HtLIEF VALVE ORIFICE OPENING = .0694 SO FT OHiFlCE FLOW COEFFICIENT 5 ,61 MIN1HUH LIQUIU ENTRAINMENT b *0100 CU FT L10/CU FT GAS minimum hater jacket itnp = 46.00 f L1Q TOL WHEN HlN ElTKAjNMENT IS REACHED x 12J9.4 CU FI TIME MIN JACkEI Itnp is reached = 5,00 MlN Hf ATlNG JACKET FAClOlt s 1.00 REACTION RATE FACtOR s 2,0 C-10 TIME Mw|N REACTOR pressure PSIA HEACIOH IEMP DEGREE F water JACKET temp degree f REAL 10H HE A1 CONTENT R1U GAS LtFl IN RLAC|UR LimOLE VCM LIO. LEFT in REACTOR umotE 1120 LlQ. LtFl IN realtor LBOOLE REACTOR V^M LIU* volume CU FT REACTOR H20 LlQ. volume CU fT .00 1.00-01 2,00-01 3;00-01 4.00-01 5.00-01 6*00-01 7'00-01 U.00-01 9.00-01 i;oq+oo 1.10*00 1.20*00 1'40*00 1.40*00 1 .*56 *00 1.60*00 1.70*00 1.00*00 1.95*02 1.95*02 1,95*02 1.96*02 1.96*02 1.9G*o2 1.96*02 1,95*02 1.94*02 1,92*02 1.91*02 1.09*02 1.67*02 1.85*02 1.84*02 1.82*02 1.80*02 1.78*02 1.77+02 1.62*02 1.62+02 1,62+02 1.62+02 1,62+02 1.62*02 1,62+02 1.62+02 1.62*02 1.61*02 1.60*02 1.60*02 1,59*02 1,58*02 1,58*02 1.57*02 1,56*02 1,56*02 1,55*02 9,00+01 8,92+01 8.04+01 8,75+01 8,66+01 0.58401 8,50*01 8,41*01 8,34+01 0.24+01 0.16+01 0.08+01 7,99+01 7.91+01 7,02*01 7.74*01 7,66+01 7.57*01 7,49*01 2,04+05 2,14*05 2,23*05 2,40+05 2,35+05 2,37*05 2,35+05 2.27*05 2,08*05 1.83*05 1,57*05 1,31+05 1,05*05 7,83*04 5,20+04 2,56*04 -9,35+02 -2,75+04 -5,40*04 1,51+00 1,74+00 1,95+00 2,16*00 2,35*00 2,54*00 2,69*00 2,81+00 2,88+00 2.89+00 2.90+Oq 2.91+00 2.92+Og 2.94+00 2.94+Ofl 2,95+00 2,96+00 2.97+00 i 4.61*02 4,57*02 4,54+02 4.50*02 4.46+02 4,42+02 4,30+02 4.34*02 4,29+02 4.24+02 4,19+02 4.14+02 4,10+02 4,05*02 4,00+02 3,96+02 3,91+02 3,07+02 3,82+02 2*47+03 2*45+04 2*44+03 2*42+03 2*41+03 2*40+04 2*49+04 2*38*04 2*30*04 2*40+05 2*38+03 2*30+04 2.47+03 2*47+05 2*31+05 2*57+03 2*47+03 2.37+03 5.72+02 5.67+02 5.63+02 5.58+02 5,54*02 5,49+02 5,44+02 5,30+02 6,32+02 5.25+02 5,19*02 5,13*02 5.06+U2 5,00 + 02 4,94 +02 4.80*02 4,02+02 4,76+02 4,70+02 7,13+02 7.09+02 7,05+02 7,01+02 6.98+02 6,94+02 6,92*02 6,09+02 6,60+02 6,08+02 6,08+02 6.07+02 6,07+02 6,07+02 6.07+02 6.67+02 6,06+02 6,06+02 6,06+02 COUMUMWHIN UHL n%H PI)EFLAS|i GAS FEOU KOtE/HIh pheflash vch uu, FM>W MOLL/HIN PUFFLASH 1120 LIO. Fl OU MOLE/MIN i LASHLU FLASIILH FLASiltO GAS yen LIU, 1120 LIU* FLOW FLOW FLOW NO! L/hlN MOLt/MIFl HOLE/MIN 10IAL IOTAL 1UTAL PyL VCn Gas UCH LIU. (HOUUCtD EnISSION emission LliftOLk L-UMOLE LWHOLE .00 1.00-01 2.00-01 3.00-01 1.00-01 5.00-01 t..00-01 7*00-01 o.'uo-oi y.UU-Ol 1.00100 1.10100 1.20100 1.30100 1 >0100 1.bo*00 1.00100 1.70)00 1.00100 3.96-fll l.ODtoO 3.60+00 0,90+00 9,02*00 1.32101 1.9211)1 2 . Obl|) 1 9,01+0) 9,02+01 1.H7101 1.9 3*01 1.39*01 9.34l(tl 9.30*01 9.20*01 9.21*01 9. IV *1)1 9.12*01 2.99*01 2.09*01 2.70*01 2,09*01 2,90*01 2,19*01 1,03)01 1.20*01 2.70*1)0 1,36*00 1.39*00 1,32*00 1.31*00 1.29*00 1.27*00 1.20*00 1.29*00 1.22*00 1.20*00 1.99102 1,39*02 1.39*02 1.20*02 1,19*02 1,07*02 0,97*01 0,22*01 1,39*01 6,06*00 6,00*00 6,09*00 6,02*00 6.01*00 6.79*00 6,70*00 6.76)00 6.79*00 6.72*00 2.63*01 2.71*01 2.02*01 2,90*01 3,13*01 3,37*01 3,71*01 9.20*01 0.01*01 9.07*01 9,02*01 9.77*01 9,72*01 9.67*01 9.62*01 9.00*01 9.03*01 9,90*01 9 ,93*01 9.26*00 3,90*00 3,09*00 3,03)00 2.92*00 1,62*00 0,21.01 .00 ,00 ,00 ,00 .00 ,00 ,00 ,00 ,00 .00 ,00 .00 1.99*02 1,39*02 1.39*02 1.20*02 1.19*02 1.07*02 0,90*01 6,00*01 1,16*01 9 ,69*00 9,72*00 9,79*00 9,76*00 9.70*00 9,00*00 9.02*00 9.03*00 9,06*00 9,06*00 ,00 3.09-01 7*10-01 1 .00*00 1 ,93*00 1*79*00 2*19*00 2*99400 2.03*00 3*16*00 3*90*00 3*70*00 9*00*00 9.36*00 9*69*00 9*90*00 0*10*00 0*90*00 0.69)00 .00 2,60+00 0.92*00 0.26*00 1.13*01 l ,90*Ul I,79*l 2,10*01 2,62*01 3,07*01 3,52+01 3,97*01 9.92+01 9.05+01 5.29+01 5.72+01 6,19+01 6,07*01 6,90+Ul .00 9.21-01 7,90-01 1.13+00 1 ,90 + 00 1.60+00 1,71*00 1,72+00 1,72+00 1.72+00 1,72+00 1,72+00 1.72*00 1.72+00 1.72*00 1.72*00 1.72*00 1 ,72 + 00 1.72+00 ucc 026690 1 TlHt M|N Rt: AC I OH REACTOR PRESSURE II HP PSIA DEGREE F WAltR JACKET Tl HP OtGREC F hiACT OK lltAT C0N1EN1 R1U 6AS LIFT IN realtor LUHOLE vcn no. LEFT IN RtACTOR tnnoLE 1120 LIU* ItFl IN RtAt-TOR LunoLt REACTOR \ln l 10* VOLURE i;U FT REACTOR 1120 |_ 10* voluhe CU pi i.9u+oo 1.70+02 1.59+02 7,90+01 -6,06+09 2.99+00 3,76+02 2.37+03 9.65+62 6,66+02 2.00+00 1.73+02 1.59+02 7.32+01 -1,07+05 3.00+00 3,79+02 2.37+03 9.59+62 5.65+02 2''10+00 1.71+02 1.53+02 7,29+01 -1,39+05 3.01+00 3,69+02 2.37+03 9.53+02 6,65+02 2J26+Q0 1.70+02 1,52+02 7,15*01 1.60+05 3.01+00 3,65+02 2.37+03 9.96+02 5.65+02 2'30+00 1.60*02 1,52+02 7.07+01 -1.67+05 3,02+00 3,61+02 2.37*03 9.92+02 5,65+02 2 .'<10 + 00 1.66+02 1.51+02 6.9A+01 -2,13*05 3.03+00 3,57+02 2.37+03 9.37+02 5,65+02 2.50*00 1,65+{i2 1.5Q+02 6,90+01 -2.90+05 3.09+00 3.53+02 2.37*03 9.31+02 5,69*02 2.60+00 1.63+Q2 1,50+02 6.62+01 -2,66+05 3,05+00 3,99+02 2*36+03 9.26+02 5,69+02 2.70+00 1.61*02 1.99+02 6.73+01 -2.93+05 3.05+00 3,95+02 2.36+03 9.21+02 5,69+02 2 00+00 1.60+02 1.96+02 6,65+01 -3,19+05 3,06+00 3,91+02 2,36+03 9,16+02 5,69+02 2 '90+00 1.56+02 1.97+02 6,56+01 -3,95+05 3,07+00 3,37+02 2.36+03 9.11+02 5,63+02 ni 3.00*00 3*10+00 1.56*02 1,55+02 1.97+02 1.96+02 6,96+01 -3.71+05 6,90+01 -3,97*05 3,06+00 3,06+00 3,33+02 3,29+02 2*36+03 2*36+03 9.06+02 9.01+02 5,63+02 5,63+02 C 3'20+00 1.53+02 1.95+02 6.31+01 -9,23+05 3.09+00 3,26+02 2.36+03 3.96+02 5,63+02 3.30+00 1.52+02 1.95+02 6,23*01 -9.99+05 3.10 + 0(1 3,22+02 2.36+03 3,91+02 5.63+02 3.'4 0 + 00 1,50+02 1.99+02 6.19+01 -9,75+05 3.11+00 3,16+02 2.36+03 3.66+02 5,62+02 3.50+00 1.99*02 1.93+02 6,06+01 -5,00+05 3.11+00 3,15+02 2*36+03 3,62+02 5.82*02 3.60+00 1,97*02 1.93+02 5.96+01 -5.26+05 3.12+00 3,11+02 2.36+03 3.77+02 5,62+02 3.70*00 1.96+02 1.92+02 5,69+01 -5,51+05 3.13+Oq 3,06+02 2*36+03 3,72+02 5,62+02 3.00+00 1.99+02 1.91+02 5,61+01 -5,76+05 3.13+00 3,09+02 2.36+03 3.66+02 5,62+02 3.90*00 1.93+02 1.91+02 5,72+01 -6,02+05 3.19+00 3,01+02 2.36+03 3.63+02 5.61+02 H.'00*00 1.02+02 1.90+02 5,69+01 -6,27+05 3.15+00 2,96+02 2*36+03 3.59+02 5,81+02 0.10+00 1.90+02 1,39+02 5,56+01 -6.51+05 3*15+00 2.99+02 2*35+03 3.55+02 5,81+02 9.20*00 1.39+02 1.36+02 5.97+01 -6,76+ 05 3.16+00 2.91+02 2.35+03 3,50+02 5.61+02 9.30+00 1.37+02 1.36+02 5,39*01 -7,01+05 3,16+00 2.66+02 2.35+03 3.96+02 5,61+02 9 .*90 + 00 1,36+02 1.37+02 5,30+01 -7.25+05 3.17+00 2,69+02 2.35+03 3.92+02 5,60+02 9.00+00 1,35+02 1.36+02 5,22+01 -7.99+05 3. 17 + 00 2,61+02 2*35+03 3,36+02 5,00+02 9 .60*00 1.39*fl2 1.36+02 5,19*01 -7.73+05 3.16+00 2.76+02 2*35+03 3.39+02 5,60*02 9*70*00 1.32+Q2 1.35+02 5.05+01 -7.97+05 3.19+00 2,75+02 2*35+04 3,30*02 5.60+02 9.00*00 1.31+02 1,39+02 9,97+01 -6,21+05 3.19+00 2.72+02 2*35+03 3,26+02 5.60+02 9 .'90*00 1,30*02 1,39+02 9,60+01 -6,95+05 3,20+00 2.69+02 2*35+03 3,22+02 5,60+02 b.OO+QU 1.29+02 1.33+02 9,00*01 6,66+05 3.20+00 2,66+02 2*3b+03 A.16+02 5,79+ 02 O.'IU + OO 1.27*02 1.33+02 9,60+01 -6,91+05 3*21+00 2,63+02 2*35+03 3.19+02 5.7^*02 ucc 026691 llHI MlN pheh ash GAS FlOW nou/nis ivlflash wen UQ, F10U mou/hip wiei lash 1120 LIQ. F|OU holi/him h asiiuj flashed GAS VCn HO. FLOS FLOW f.gu/mn hull/hin FLASNLli 1120 L|0* FLOW HOLf/HHI TOlAL I'VL FHOUUCLl) MiOOLt total VC" GAS LfilStlON ^UflOlL lOfAL VCM LIU, EMISSION LHWiLE 1.40100 2,'OOtOO 2'lOtQO 2.20*00 2.10*00 2*40*00 2vaO*O0 2 *00*00 2.70*00 2.00*00 2*90*01) 3.00*00 3*10*00 1.20*00 3*30*00 3*40*00 3*60+00 3*00*00 3.70*00 3.60*00 3.90*00 <1.00*00 4. 10*00 4.20*00 4.10*00 *1 *40*00 4,60+00 4.60*00 *1.70*00 4*00*00 4.90*00 tt.OOtOU b.10*00 4.00*01 4.04*01 1*99*01 3.95+nl 1.91*01 3.07*01 3.02*01 3.70*01 3.74*01 1.70*01 1.660l 3.62*01 3.67*01 1.61*01 3.49*01 3.46*01 3.42*01 1.10*fll 1,34*61 1.10*01 1.26*01 1.21*01 1.19*01 1.IS*0l 1.12*01 1.00*01 1.06*01 3.01*01 2.90*01 2.94*01 2.91*01 2.07*01 2.04*01 1.16*00 1,17*00 1,16+00 1.13*00 1.11*00 1.10*00 1.06*00 1.06*00 1.06*00 1.03*00 1.02*00 1.00*00 9.06-01 9.70-01 9.64-01 9.39-01 9.24-01 9.16-Q1 0,96-01 a.oi-oi 0.66-01 0.62-01 6.30-01 6.26-01 a.U-ol 7,90-01 7.66-0) 7.71-61 7.69-Ql 7.46-01 7.33-01 7.21-01 7,09-01 6,70*00 6.66*00 6.66*00 6,64*00 6.61*00 6.69*00 6,67*00 6,64*00 6.62*00 6.49*00 6,47*00 6.44*00 6,41*00 6,39*00 6.36*00 6,33*00 6,30*00 6,27*00 6.24*00 6.21*00 6.16*00 6,16*00 6,12*00 6.09*00 6,06*00 6.03*00 6,00*00 6.96*00 6.93*00 6.90*00 6.67*00 6.63*00 6,00*00 4.30*01 4.33*01 4.26*01 4.24*01 4,19101 4.14*01 4.09*01 4.06*01 4.00101 3.96*01 3.91*01 3.06*01 3,02*01 3.77*01 3.73*01 3.60*01 3.64*01 3.00*01 3.66*01 3.61*01 3.47*01 3.43*01 3,39*01 3,36*01 3,31*01 3,27*01 3.23*01 3.19*01 3.16*01 3.11*01 3.00*01 3.04*01 3.00*01 .00 .00 .ou .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 ,00 .00 .00 .00 .00 .no .00 .00 ,Q0 .00 .00 ,00 .00 ,00 .00 ott .00 .00 ,00 ,00 4.06*00 4.69*00 4,91*00 4.92*00 4,93*00 4 .94*00 4.96*00 4.96*00 4,96*00 4,97*00 4.97*00 0.90*00 4,90*00 4.99*00 4,99*0fl 4.99*00 4,99*00 4,99+00 4,99*00 4,90*00 4,96*00 4,90*00 4,97*00 4,97*00 4,9fc*00 4.96*00 4,96*00 4.94*0(1 4,93 (Oil 4.92*00 4.91*00 4,90*00 4,09*00 6 66*00 6 00*00 6 29+00 6 60 + 00 6 69+00 6 00 + 00 7 06*00 7 24*00 7 40*00 7 66*00 7 72*00 7 07*00 0 01*00 0 16*00 6 29*00 6 91*00 e 64*00 6 66*00 6 77*00 0 00* GO a 99*00 9 09*00 9 19*00 9 20*00 9 37*00 9 96*00 9 66*00 9 63*00 9 71*00 9 70*00 9 06)00 9 93*00 1 00*01 7.90*01 7.00*01 0.2I+U1 0.61+01 9.00+UJ 9.90*01 9.70*01 1,02+02 1,06*02 1.09*02 1.13*02 1.17+02 1,20+02 1.24+02 1.27*02 1.31*02 1.39*02 1.30*02 1.41*02 1.44*02 1,40*02 1.61*02 1,64*02 1.67*02 1,11*02 1.64)02 1.67+02 1.70*02 1,73+02 1.71 t.02 1.79+02 1.02*02 1,06+02 1.72+00 1.72+00 1.72+00 1.72*00 1,72*00 1.72+00 1,72+00 1,72*00 1.72*00 1,72*00 1,72*00 1,72*00 1.72*00 1.72*00 1.72*00 1.72*00 1.72*00 1.72*00 1,72*00 1.72*00 1.72*00 1.72*00 1.72*00 1.72+00 1,72*00 1,72*00 1.72*00 1.72*00 1,72*00 1,72*00 1,72*00 1,72*00 1.72*00 "V COWM WfJON TiNF MIN REACIOK PHC&SUHr PSIA HfACTon TEMP urencc f UAlCIt JACKF1 UUP OLGnCC F HI AC 1 OK ML AI CCNlFNl M1U GAS UFI IN RtALfilR UiMOLC VCM HO. LIFT IN REACTOR LBttOLF 1120 l IQ. 1Lf * 1W HtALTOR Kin ole reactor vcn no. volume *:M H REALTOR H2U LlO volume tu FI 5.20+00 5.50+00 5>0 + 00 b.60+00 b.60+00 5.70+00 5.00+00 5.90*00 6 '00+00 6'tO+QQ 6v20+00 0.50+00 o.oo+oo 6.50+00 b'60 + 00 6.70*00 b'ao+oo 6.90+UU 7.00+UU 7.J0+OO 7.20+00 7.50+00 7.00+00 .7.50+00 7 *60+00 7.70+00 7'0u+00 7 *90 + 00 0.00+00 0.10+00 0.20+00 0.50+00 0.40+00 1.26+02 1.25+02 1.24+02 1.25+02 1.22+02 1.21+02 1.20+02 1.19+C2 1.16+02 1.17+02 1.16+02 l.lb+02 1.14+02 1.15+02 1.12+02 1.11*02 1.10*02 1,09+02 1.06+02 1.07+02 1.07+02 1.06+02 1.05+02 1,04+02 1.03+02 1.03+02 1.02*02 1.01+02 1.00+02 9,90+fll 9.91+01 9,04+nl 9,70+01 1.32+02 1.31*02 1.31+02 1,30*02 1.29+02 1.29+02 1.26+02 1.26+02 1.27+02 1.26+Q2 1,26+02 1.25*02 1.25+02 1,24+02 1.23+02 1.23+02 1.22+02 1,22+02 1,21+02 1,21+02 1,20+02 1.20+Q2 1.19+02 1,19+02 1.16+02 1.16+02 1.17+02 1,17+02 1.16+02 1,16+02 1,15+02 1.15+02 1.14+02 4.60+01 4,60+01 4,00+0) 4.60+01 4,60+01 4,80t0l 4,60+01 4,60+01 4,60+01 4.60+01 4.60+01 4,60+01 4,60+01 4,60+01 4.60+01 4,60+01 4.00+01 4.60+01 4,60+1)1 4,00+01 4,60+01 6.60+01 4.60+01 4,00+01 4.00+01 4.00+01 4.60+01 4.60+01 4.60+01 4.60+01 4.60+01 4.60+01 4,60 + 01 -9.14+05 -9.37+05 -9.60+05 -9.62+05 -1,00406 -1,03+06 .1,05+06 -1,07*06 -1,09+06 -1,11+06 .1,13+06 -1,15+06 -1,16+06 -) .20+06 -1,22+06 -1,24+06 -1,26+06 -1,26+06 -1,30+06 -1,31+06 -1.33*06 -1.35+06 .1,37+06 -1,39+06 -1.41+06 .1.43*06 .1,44+06 .1,46+06 .1 .46 + 06 . 1 .50 + 06 -1.51*06 -1,53+06 -1,55+06 3,21+0q 3.22+00 3.22*00 3.23+00 3.23*00 3.24*00 3.24*00 3,24+00 3.25+00 3*25+00 3.26*00 3.26*00 5.27*00 3.27*00 3.27*00 3.26*00 3.26*00 3.26*00 3.29*00 3.29*00 3.30*00 3.30*00 3.30+00 5.51*00 3,31+00 3.31+00 3.32*00 3.32*00 3.32*00 3,32*00 3.3,3*00 3.33*00 3,33*00 2,60*02 2.57*02 2.54*02 2.51+02 2,49+02 2,46*02 2.43*02 2,41+02 2,36+02 2.35+02 2.33+02 2,30+02 2,26+02 2,25*02 2.23*02 2.20*02 2,16*02 2.15*02 2,13*02 2,11*02 2,06*02 2,06*02 2,04*02 2,02+02 1,99+02 1.97+02 1,95*02 1.93*02 1,91*02 1,69+02 1.67+02 1.65+02 1,63+02 2 35+03 2 35 + 03 2 35 + 03 2 35*03 2 34 + 03 2 34 + 03 2 34*03 2 34 + 03 2 34*03 2 34*03 2 34*03 2 34*03 2 34*03 2 34*03 2 34*03 2 34*03 2 34 + 03 2 34+03 2 34 + 03 2 34 + 03 2 34 + 03 2 34*03 2 33*03 2 33*03 2 33*03 2 33103 2 33*03 2 33*03 2 33*03 2 33*03 2 33*03 2 33*03 2 33*03 3,n*U2 3.07*02 3.03+02 3,00+02 2,96+62 2,S3*U2 2,69*02 2.66+02 2,62+02 2,79+02 2.76+02 2.73+02 2.69+02 2.66+02 2.63+02 2,60*02 2.57+02 2.54+02 2.51+02 2,46+02 2.45+02 2,42*02 2.40+02 2.37*02 2.34*02 2.31*02 2,29*02 2.26+02 2,23+02 2,21+02 2.16+02 2.16+02 2,13+02 6,79*02 6.79+02 6,79+02 6,76+02 6,78*02 6.78+02 6,76*02 6,78*02 6,76*02 6,77+02 6,77*02 6,77*02 6,77+02 6,77+02 6,77*02 6,76*02 6,76*02 6,76+02 6,76+02 6,76*02 6,76*02 6.75+02 6.75+02 6,75*02 6,75*02 6.75+02 6,75+02 6.75+02 6,74+02 6,74+02 6,74+02 6,74*02 6,74+02 ucc 026693 OWfOM R1IUN niiL niN (`(tFlLASf CAS FLOW Hill F/H|(, (VFFLASII VCIt MQ. FLOW HfaU/HlN PMC| LAStl *120 L10. F| OU HOU /HIM f l ASll* U CAS FLOW Kt-L/PIN fLAS||t|) UCn L|U, flow H*H-1 /HIM FLASIItO U20 110. flow HOLC/HIN TOTAL TOTAt TOTAL FyL yen GAS VCH Ll<i. f'HOOuCLO Cm SSI ON FMSSIOH LtiHULt LtmOLl LUHOLf 5. 20*0(1 2.01*01 6.97-01 6,77*00 2.97*01 5.30*00 2.70*01 6.06-01 6.73*00 2,93*01 5.40*00 2.76*01 6.73-01 6.70*00 2.90*01 5 .`50 *00 2.71*01 6.62-01 6.67*00 2.06*01 5.60 + 0(1 2.60*01 6.61-01 5.63*00 2.03*01 5. 70*00 2.66*01 6.40-01 5.60*00 2.79*01 6.00*00 2.62*01 6.29-fll 5.66*00 2,76*01 6.00*00 269*01 6.16-01 6.63*00 2.73*01 C.0(1*00 2.66*(il 6.07-01 5.60*00 2,70*01 fa. 10*00 2,6Atftl 6.97-01 5.46*00 2.66*01 fa.20*00 2.61*F1 6.66-01 5.43*00 2.63*01 ni fa '30* 00 fa 'HO * 00 2.HO*ol 2.H6*0l 6.76-01 6.66-01 5.39*00 5.36*00 2,60*01 2.57*01 c: fa.60*00 2.42*01 6.66-01 5.33*00 2.54*01 fa.fab *uo 2.39*|}1 6.47-01 5.29*00 2.51*01 6.70*0(1 2.37*f.l 6,37-01 5.26*60 2.40*01 fa.U0*00 2.34*01 6,20-01 5.22*0(1 2.45*01 fa'90*U0 2.31*01 6.19-01 5,19*00 2.42*01 7. Oil * 00 2.2*7*01 6.09-01 5,16*00 2.40*01 /. 111*00 2.26*01 6.00-01 5.12*00 2.37*01 7.20*00 2.2H*fl 4.92-01 5,091 oO 2.34*01 7.* AO * 00 2.21*01 H.Oi-ol 5.05*00 2.31+01 7.4 0 i U 0 2.1*J Mil 4.74-01 5,02*00 2.29*01 7'60*00 2.16*01 4.66-01 4.99*00 2.26+01 7.60*00 2.14*01 4,60-01 4,95*00 2,23*01 7.70*00 2.12*01 4,60-01 4,92*00 2.21+01 7.'60*00 2.09*01 4.42-01 4,00*00 2.10+01 7.MO*OU 2,07*01 4,34-01 4.06*00 2,16*01 0.00*00 2.06*01 4.26-01 4,02*00 2.13+01 0.10*00 2.02*01 4.10-01 4.70*00 2.11*01 6.20 tOO 2.00*r1 4.11-ill 4.76*00 ;.00*01 0.AO*00 1.96*01 4.03-01 4.71*00 2,06+01 0. HO*00 1.96*01 3,96-01 4.1.0*00 2.03*01 .00 .00 .00 .00 ,00 ,00 ,00 ,ou ,00 .00 .00 ,00 .00 .OU .00 .00 ,00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .ou *oo .00 too .ou .flfu ,00 4,06+00 4.07+00 4,66*00 4,64*00 4,63*00 4.62+00 4,60*00 4,79*00 4.77*00 4.76*00 4,74*00 4.72*00 4.71*00 4.69*00 4.67+00 4,65*60 4.63*00 4,62*00 4.60*00 4.56+00 4.56+00 4,54*0fl 4.52*0(1 4,50+00 4.40*00 4.46+00 4,43*00 4,41+AO 4,39*00 4.37*00 4.34 *0(| 4,32*00 4,30tilo 1*01+01 1.01*01 1,02*01 1.02+01 1*03*01 1*04*01 1*04*01 1,05*01 1*05401 1,06*01 1*06+01 1.07+01 1.07+01 1*07*01 1,00+01 1.06+01 1*09+01 1*09+01 1.09+01 1 * 10*01 1.10+01 1.10*01 1 <11*01 1 .11*01 1.11*01 1.12*01 1,12*01 I .12+01 1,12+01 1*13 + 01 ' 1.13*01 1*13+01 1 * 13 + 01 1.67+02 1.90*02 1.93+02 1,96 *02 1.99*02 2.01+02 2.04+02 2.06*02 2.09+02 2,12*02 2.14*02 2.17+02 2.19+02 2,22+02 2.24+02 2.26+02 2.29+02 2.31*02 2.34*02 2.36+02 2.3A+02 2.40*02 2.43+02 2.46*02 2.47+02 2.49+02 2.51+02 2.63*02 2.66+02 2.67*02 2.69*02 2.61*02 2.63*02 1.72+00 1,72+00 1,72+00 1.72+00 1.72*00 1.72+00 1,72+00 1.72+00 1.72+00 1.72*00 1.72+00 1,72+00 1,72*00 1.72+00 1.72*00 1,72+00 1.72+00 1.72*00 1.72+00 1.72*00 1.72*00 1.72*00 1.72*00 1.72+00 1.72*00 1.72*00 1.72+00 1.72+00 1.72 + 00 1,72*00 1 . / 2 + 0 ( 1.72*00 1.72*00 ucc 026694 TiMIMlN Hf AC lull f'HESSUftf PSIA Hf AClOlt If HP DEGREE p HAlCi: JACKET TC HP UtGufC f HE ACTUK ML AT L0N1EN1 111 U GAs ctn ifj IttACjOK LUQLE VCH CIO. lift in HtACTOH LBMOLE 1120 LIU* LtF IN realtor LbOLt HL AC 1 (ill VLH 11Q. yuLMPL LU u REAtfOH H2U t>U. volume tu pi 0.SO too 6.6(1 + 00 U'70+00 6.60+00 ii. 90+oo <1.06 + 00 9.10+00 9.20+00 9.30+00 9'NO +00 9.GO TOO 9.60+00 9.70+00 9*60+00 9.90+00 1.00+01 9.71+fl 9,65+pl 9.50+pl 9.62+1)1 9,66+fll 9.60+01 9.36+01 9.20+01 9.22+01 9.17+01 9.u+ni 9.06+nl 9.01+01 6.95+01 6.90+01 6.66+01 1.16+02 1.13+02 1.13+02 1,12+02 1.12+02 1.11+02 1.11+02 1,11+02 1,10+02 1.10+02 1.09+02 1.09+02 1.06+02 1.06+02 1.06+02 1.07+02 6.00+01 6,60+01 6.60+01 6.60+01 6,60+01 6,60+01 6.60*01 6.60+01 6.60+01 6.60+01 6,60+01 6,60+01 6.60+01 6,60+01 6,60+01 6.66+01 -1.57+06 -1,56+06 -1.60+06 -1,61+06 -1,63+06 -1.65+06 -1,66+06 -1.66+06 -1.69+06 -1,71+06 -1,72+06 -1.76+06 -1,75 + 06 -1.77+06 -1.76+06 -1.60+06 3.36+00 3,36+00 3.36+00 3,36+00 3.35+00 3,35+00 3.35+00 3,36+Oq 3,36+00 3,36+00 3.36+00 3.37+UO 3.37+00 3.37+00 3.37+00 3.37+00 1.61+02 1.79+02 1,77+02 1.75+02 1.73+02 1,71+02 1.69+02 1,67*02 1.66+02 1.66+02 1.62+02 1,60+02 1,59+02 1,57+02 1.55+02 1.56+02 2.33+03 2*33+03 2*33+03 2.33+03 2*33+03 2.33+03 2.33+03 2,33+03 2*33+03 2.32+03 2.32*03 2.32+03 2.32+03 2.32+03 2*32+03 2*32+03 2.11+02 2.09+02 2.06*02 2,06+02 2.61*02 1.99+02 1.97+02 1.95*02 1.92+02 1.90+02 i.oe+02 1.66+02 1,66+02 1.62*02 1.60+02 1.76+02 6.76+02 6.76+02 6,73*02 6.73+02 6.73+02 6,73+02 6,73+02 6.73+02 6,73+02 6,72*02 6.72+02 6,72*02 6,72*02 6.72+02 6.72*02 6.72+02 COMIMMJIVIOM llHf niH I'lUTFLASll CAS Fl-OW *10L[/rt|fJ 1`nFFFASM VCH LIU, FLOU HOLF/MIN miLASli N20 110. F| OU WOI.J/HJM (lAMUU FlAStttO FLASIlFU FAS vcn UjU, H?.0 L16. 1L66 Ft-GW FLOW TiCU/MlN F|U|_t/niN nOUt/HIh lOlAL |*yC |>f<O"UCt0 MtnoFt IOTAL VCn CAS CflSSlON Mum t IOIAL vcn iiu, chission LtIMOLt u;oooo 1,01*01 3.00-01 4.64*00 2,01+01 0.00*00 1.01*01 1.02-01 4,61*00 1,90*01 U.70*00 1,00*01 1.75-01 4.60+00 1.96+01 0.00*00 1,07*01 1,60-01 4,64+00 1.94*01 0.00*00 O'100 *00 1,00*01 1,01*01 1,61-01 1,60-01 4,61+00 4,47*00 1.02*01 1.90*01 o'lo+ou 1,01*01 1,00-01 4.44*00 1,67+01 0.20*00 1,70*01 1.02-01 4.41+00 1.66+01 0.10*00 1,77*01 1.16-01 4.17+00 1.01+01 0'4 0+00 1.70+01 1,20-01 4,14*00 1.61*01 y `to*oo 1.71*01 1,21-01 4,10*00 1.79*01 IMO*t* y.00*00 0.70*00 yToo*00 1.71+01 1.60+01 1,67 Ml I 1.17-01 1.11-01 1,06-01 4.27+00 4,24+00 4.20*00 1.77*01 1.76+01 1.71*01 0.00*00 1,66*01 2.09-01 4.17*00 1.71*01 1.00*01 1,61+01 2.00-01 4.11*00 1.69*01 ,00 ,00 *00 *00 .00 .00 .00 .00 .00 ,00 0(1 ,ou *ao ,00 .00 *00 4.27*00 4,26+00 4.21+00 4.20+00 4,16+00 4,15+00 4,11*00 4.10+00 4,06+00 4,05*00 4.01*00 4,00*00 1.96*00 1,95+00 1,91+00 1,90+00 1.14+01 1.14+01 1*14+01 1.14*01 1*14+01 1.15*01 1*16+01 1*16+01 1*16+01 1*16+01 1*16+01 1*16+01 1*16+01 1.16+01 1.16*01 1.16+01 2,66+02 2.1.7 + 02 2.69*02 2.71+02 2,73+02 2.76+02 2,77*02 2,76+02 2.60+02 2.02*02 2,04+02 2.00 + 02 2.67+02 2,60+02 2,01+02 2.S?*U2 1.72+00 1.72*00 1,72*00 1.72*00 1,72*00 1,72*00 1,72*00 1,72*00 1,72*00 1,72*00 1,72*00 1.72*00 1,72*00 1,72*00 1,72*00 1.72*00 JFlM ft699 O CMPmmioN DISCIIAKCL FUUII A I'VC HATCH HKACTOR Cuse 3. Overfilling - CuntOmt Temperature KIACtOH PRESSURE Al Ilf.E tlf nlSCHAliOL = |<) AC I OK ItNC AI Tlftf 0| DISCHARGE = Iti:AClOH VOLUME = 1327.000 CU Ff 191. Vi PS 1A 12*4.00 F PltrSSUHL OOMNSTltfAh OF WAM/E = 64*70 PSIA UATdt JACKLI TEMP AT UISCAit(.F = 90.00 F IIEaT OF INACTION = 45516^000 UlU/LUMOLL LIQUID VCM INITIAI.IV IN REACTOR = lOf.OO LGMOLf LI(1 1120 1N11IAILY IN HEAC * OR = 2603.0 LBMOU VAPOR 1NII1AI.lv Hi REACTOR = .0317 LRNOLE JACKET COLF TIMES AREA = 564.3 HTU/M-F Ut NS11V OF HAILH U ONSlAhfl = 3.9*>70 LDPOLI/CU FI INITIAL DENSITY OF VCM = .033/7 LOMOLE/Cu FT AULA Of HLLIIF VALVE OrIFICE OPENING = .0191 SO Fl ORlFICf FLOW COEFFICIENT = .10 MINIMUM L Kill 111 CNT|jAlNf.LNT s .0100 Cll IT LlN/CU FT GAS MINIMUM WATER JACKET Tt-MP = 90.00 F LIU uOL UtltN Mill frritAlNMLNI IS REACHED s- 1219,9 CU FI TIME MIN JACKET TLmP IS ItEACPI 0 = 5.00 MIN IHATING JACKLT FACT00 = 1,00 reaction rate facior = .10 1 I ML niN RLACTGH PHESSUItF PSIA ( ACTOR irMi UEGllEC F water JALKf T TLMP degree f REAC|DU HEAT LffllENl PI J GAS LLFI IN rlaltur CUMOLE VCM LlQ* left in Rt AC IOH lrmole ll20 LIU. LEFl IN REACTOR ermole R+rAClPH VCM l IQ. VOLUME CU ft REACjqH 1(20 L IQ. VOLUME CU FI c -ia UCC 028697 .00 1.00-01 2 .*00-01 3'0G-01 9.00-01 5.00-01 6.00-01 7.00-01 tl.GO-lii 9.00-01 1.00too 1.10+00 1.20+00 1.30+00 1.90+UII 1.50+00 1.60tOO 1.70+00 1.110 + OU l.95 + ||2 1,32+02 1,32+02 1,32 + 1*2 1.31+02 1.31 +f*2 1.31+02 1*31*02 t .30+1.2 1.3.12 1,30+02 1.29+02 i.?9+(>2 1.20+f2 1.26+12 1.27+02 1,26+02 l.?5*r? 1.29 *f.2 1,35102 1,30+02 1.35+02 1.35+C2 1.35+02 1,35+02 1.39+0? 1.39+02 l ,39*r2 1,39*0? 1,39102 1,39 + 02 1.33 + 02 1,33+02 1,33+02 1.32+02 1.32+02 1.31+0? 1.31*02 9.00+01 9.00+01 9.00+01 9,00+01 9,00+01 9,00+01 9.(10*01 9.00+01 9,00+01 9.00+41 9.00*01 9.00+01 9.00+01 9,00+01 9.U0+H1 9,00+0] 9.00+01 9.00+01 9.00+01 >1.09 + 06 -1.09+06 -1,09+06 -1.03+06 -1.03+06 -1.03+06 -1.03+06 -1.03 + 06 -1,03+06 -1.09+06 -1.09+06 -1,05 + 06 -1.05+66 -1.06+06 -1.07+06 1,00+06 -1.10+06 1,12+06 -1.19+06 3.47-0? 1.53-01 2.60-Oj 3,t|5-0i 5.17-01 b,96-01 7.72-01 0.99-Oj 1.01+00 1.13+00 1.29*00 1.39+00 1.99+00 1.53+00 1.61*00 1.60+00 1.79+00 M?*00 1.7,9 + 00 9.06*02 9.03+02 9,00+02 9.77+02 9.75+02 9.72+02 9,69+02 9.66+0? 9.63+02 9,61+02 9,56+02 9.55+0? 9.52+62 9.99+0? 9.95+0? 9,9? + 02 9,39+02 9,35+02 9,43+02 2*60+03 2*59+03 2*50+03 2*56+03 2*55+03 2.59+03 2.53+04 2*52+04 2*51+04 2*50+04 2*99+04 2*90+04 2.97+04 2*96+04 2.95+03 2.99+03 2*99+03 2.99*03 2*93+03 5.P3+U2 5.79+02 5.76+02 5.72+02 5,69+02 5,66*02 5,62+02 5,59+02 5.55+02 5.5P+02 5.90+02 5.99+02 5.91+02 5.37+02 5.33*02 5,20*02 5.29+02 5.20+02 5,16*02 / .53 + 0? 7.99+02 7,95+02 7.92+02 7,30+02 7.35+02 7,31+02 7.20*02 7.25*02 7.22+02 7.19+02 7.16+02 7.19*02 7,11+0? 7,09+0? 7.0/+0? 7,05*0? 7,09*0? 7,09*0? couponMMM II Hi Hit* riU 1 l. AS|* GAS FLO** H*tU/rt||| Thl FLASH Vt 1 10. flow Hi LI /Hill **KF| l. A till 1120 Lit*. Ft OU iioli /mu t | ASM U 6A S ILOU 7.01 L/MN FLASllM) 1ucn L 1*1, flow HOll/HIH FLASIlFU 1120 Lio. flou H0LL/H1I+ TOl Al. TOIAL IUIAI. l*Wk 1l*C GAS VCM |_l. I'lioMlCtli Lnissioh LHISSION LllHOLL MlM*Ll LUHOLt .00 l'ou-oi 2'00-01 4voo-ui 9.UU-01 U.00-61 6.00-01 7.00-01 o.'Oo-di 9.00-01 i .uo+ou 1.10*00 1.20*00 I '40*00 i ;<io*oo 1 . 50 *00 1 't>0*0O 1.70*00 i.uu*na 1.02-1)2 5.51-ftl 1.00-* ltd 1 .iil-fltO 2.41*00 4.04*00 l.OHtOO 9.76*00 s.aotro 7.00*00 0.4*1*00 l.00*ul 1.20*01 1.04*01 1.72*01 2.0*1*01 2.56*01 2.66*01 2.70*01 4.57*01 2.54*01 2.50*01 2,06*01 2,01*01 2.46*01 2.41*01 2.20*01 2.17*01 2,09*01 2,00*01 i.y*oi 1.76*01 1,61*01 1.04*01 1.20*61 9.00*00 0.70*00 1.42*0*1 1.7510? 1.2*1*02 1,24*02 1,21*02 1.19102 1.16*02 1.10*6? 1.11*02 1.00*0? 1,00*02 9,94+01 9,92*01 0.01+01 0,00+01 7.19+01 6.07*01 0.62+01 2.05*01 6,02*00 2.17*01 1.60*01 1.64+01 1.67*01 1.71*01 1.76*01 1,00*01 1,66+01 1.94+01 2.01*01 2,10*01 2.20*01 2.44*01 2,09*01 2.60*01 2.94*01 4.26*01 4,11*01 2.94*01 l.<|2t0l 1.00*01 9.o7*Oo 9.60*00 9.07*00 9.20*00 0.90*00 U.60*00 0,45*00 7*96+00 7.52+00 f .00*00 6.49+00 5,65+00 0.70*00 4,61*00 2.10+00 4.44-01 .no 1.75*02. 1,20*02 1,22*02 1,21*02 1.10+02 1.16*02 1.10*02 1.11*02 1.07+02 1.00*02 9,92+01 9.01*01 a,00+01 6.07+01 7,16+01 6.06+01 0,62*01 2.0&+01 6.16+00 .00 6*70-04 1.45-02 2.02-02 2.60-02 4.44-02 4.90-02 0.62-02 5.26-02 5*07-02 6.09-02 7.09-02 7.69-02 0.20-02 fl.05-02 9.02-02 9.97-02 1.05-01 1.10-01 .00 l .Ol+UQ 4,02*00 5.0|.+ 00 6,74+00 0,90*00 1.02+01 1.20*01 1,49*01 1.50*01 1.79*01 2.00+01 2.22*01 2,06*01 2./1+01 2.99*01 4.40*01 4,61*01 4.90*01 .00 1,17*00 2.17*00 4,16*00 0.11*00 5,00*00 5,95*00 6,60+00 7,69+00 0,50*00 9,26*00 1.00*01 1.07+01 1.14+01 1.16*01 1.22+01 1.25*01 1.26*01 1.26+01 ucc 026698 i cocapom jitkim nm rtiN REACTOR PHCSSUMl PSIA l(| ACT OH imp (If COLE | WAltH JACKET Tl I P UCGfttr r of ac urn MEAT COM 1 EM rnu GAS LtM 1U lit ACTOK ctmnLE vcn lio. LEFT IN IU. ACTOK LflHOLE ||2(J LIU. lef* in RLALTOIt LlinOLt RbACTOK y^n ii6. WOLimt by i t REACTOR II2U L IQ yotunf CU FI 1 .90+00 2.00100 2.10 *00 2,20*00 2.50 *00 2.*10*00 2.00*00 2.00*00 2,70*00 2.00*00 2.90*00 5.00*00 5.10*00 5.20*00 5'50 * 00 5.00*00 5.00*00 3.60+110 5.70*00 5.00*00 5.90*00 I.OUIOO 9 .'10*00 1x20+ 00 H'iUKIO H .1(0*00 1.5(1 HIU 1 *(j0*00 1.70*00 1 '(10*00 1.90*00 5 *00 *00 b'lotoo 1.25*02 1.22*02 1.21*02 1.20*02 1.19*02 1.19*02 1.10*02 1.17*02 1.16*02 1 li*02 1.10+02 1.10*02 1.15*02 1.12*02 1.11*02 1.10*02 1.10*02 1,09*02 1,0(1 *0 2 1.00*02 1.07*02 1.06 + 1)2 1.06*02 1.05*02 l.CO+o? 1,00*02 I . 5*r, 2 1.02*f,2 1,02*02 1.01*02 1.01*02 1.00(02 1,95*01 1,50*02 1.50*02 1.29*02 1.29+02 1.20*02 1.20+n? 1.27*02 1.27*02 1,26*02 1.26*02 1,25+02 1.25+02 1,21+02 1.21+02 1,25*02 1,25+02 1.22tfl2 1.2?+o2 1.21+02 1.21 + q2 1.20+02 1.20*02 1.20+02 1.19+02 1,19+02 1.10+02 1. 1U + 0? 1.17 + .-.2 1.17*02 1.17*02 1.16*02 1.16*02 1.15(02 9,00*01 9,00*01 9,06+01 9,00+01 9.00*01 9,00+01 9.00*01 9,00+01 9.00+01 9,00*01 9.00+01 9,00+01 9,00*01 9.00+01 9,00+01 9.00+01 9.00*01 9.00+01 9,00+01 9.00+01 9.00*01 9.00+01 9.00+01 9.00*01 9,0 0 * u 1 9.00+01 9,00+01 9,60*01 9,06*01 y.OOHil 9.00*01 9.60*01 9.nr+ot -117 + 06 *1.19+06 -1.21+06 -1.25+06 -1.25+06 -- 1,26+ 06 -1,50+06 -1.52+06 -1,51*06 -- 1,56* 06 -1,56+06 -1,10+06 -1,12 + Ott -1,11*06 -1,16*06 -1,10+06 -1,50*06 -1.52+06 -1,55+06 -1.55+06 -1,57+06 -1.59+06 -1.61+06 -1.62+06 - 1,61 * ltd - 1,66 + 06 -1.61- *06 -1.69*06 -1.71+06 -.! . /5 + 06 -1.71 + 06 -1.76+06 -1.77+06 .79*00 .00+00 .00*00 .01+00 .01+00 02+00 ,02+00 .02+00 .05*00 .05*00 09+00 .01+00 .01*0(1 .05 + 0(1 .l)5+0(l 06 + 0 {( .flb+00 .Ob+ 0(j .07*00 07+00 .07*00 .ftU+Oo .00+00 .09*0o .89 + 0(1 .09+00 .90*00 .90 + Co 90+on J 91 + 0 0 .91 + 0(1 ,91+00 .91*00 1,50 + 02 9,27+02 9.29+02 9.22+02 9,19*02 9,16+112 9.19+02 9,11+02 9,00+02 9,06+02 9,05*02 9,01+02 3.90*0? 5,96*02 5,95+02 3,91+02 3,09+02 3,06+0? 3,09+02 3.01+02 3,79*02 3.77+02 3,75+0? 3,72+02 3.70+0* 3.60+0? 3,66 + 11? 3.69*02 3.61*0? 3,59*0? 3.57*02 3,55+02 3,53*0? 2 13*03 2 15403 2 15 + 03 2 95+05 2 13 + 05 2 15+05 2 15 + 05 2 13 + 05 2 13 + 03 2 13*03 2 13 + 03 2 13+03 2 15 + 05 2 13 + 03 2 15 + 05 2 13+05 2 13 + 03 2 12*05 2 12+05 2 12 + 03 2 12 + 03 2 12 + 03 2 12+03 2 12+05 2 12 + 05 2 12 + 05 2 12 + 03 2 12 + 05 2 12 + 03 2 12 + 05 2 12 + 05 2 12 + 05 2 92 + 03 5.12+02 5,09+62 5,05+02 5,01+02 9,90+02 9,99+02 9,91+02 9,00+02 9,09+02 9.01+02 9.70+02 9.79 +02 9.71+02 9.60+02 9.1.5*02 9.62+02 9,59+02 9.55+02 9,62*02 9.99*02 9.96*02 9.99+02 9.91+02 9.30+02 9.35+02 9,32+02 9.29+02 9.27+02 9.29+02 9.21+02 9.10*02 9.16+02 9.13*02 7,09+0? 7,09+0? 7,09+02 7,03+02 7,05+02 7,03+0? 7.03+0? 7,03+02 7,03*02 7,03*02 7,02+0? 7,02+02 7,02+02 7,02+02 7,02+C? 7,02+02 7,02+02 7,01*02 7,01+0? 7,01+0? 7,01+02 7,01+02 7.01+02 7,01+0? 7,01*0? 7,00+p? 7,00+0? 7,00*0? 7.00+0? 7,00+0? 7,00+02 7,00*02 6,99*02 ucc 026699 I I HI rliN |)HlfLAS|i GAS ri nu Moi.L/mr. D| I M ASM V(rt LID. FLOW rt| I f/him IMifl 1-ASM 1120 MO. Ft OU HOLf/fUM 1 I A SHI li I t AStltU PLASMID GAS VCrt HU. M20 LIO. Mow MOW FLOW Ml i/MN MOM /tt | M hOLt/MIN 101 AL |*yL fHOWUCLU lmoll TMAt VC" GAS EMISSION LUHOlt ioial VCrt MU. EMISSION LtmOLf J .`JOtoo 2.00400 2.10400 2.20400 2.30400 2.90*00 2.50*0*1 2.00*00 2.70*00 2.00*00 2'`JO * 00 A.OUlUO 3.10400 A.20*00 A. ill 400 A >0 4 00 A. !iO * 00 A.'00400 A.70400 A.00400 A.*JO 4 00 9 . Oti * 00 t` lotiia 1,20400 i. AO 4 00 *1 > 0 t il<l 9 . 1*0 4 00 9 .(.0 i 00 <,. 7o *00 I .00*00 `I .`JO * 00 j . Oil l (111 5. Ill too 2.72401 + 2 o`J 4 o I 2.674(11 2. <`1*01 2.02401 2594 q1 2.57*01 2.59*0) 2.02401 2.9 9 * 01 2.**7*r l 2.99*01 2.12401 2.10*01 2.30*01 2. At.*01 2.AA*01 2.31*01 2.2***1 1 2.27*01 2.20401 2.23401 2.21*01 2.19*01 2.17*1,1 ?.IS if 1 2 131 o 1 2.11 * 01 2,09*01 2.07401 2, 09* o 1 2.0 111 1 2.01401 9,12-ni 9.01-01 0.91-01 0.00-01 0.70-01 0.60-01 0.50-01 0.10-01 0.AO-Ot 0.20-01 0.11-01 0.01-01 7,92-01 7.03-01 7.71-01 7.OS-01 7. Si.-01 7.17-01 7.3(i-ol 7.30-01 7.21-01 7.13-f.l 7.OS-01 G.9G-II1 g, no-ni r. ,00-111 6.72-0l G.69-01 G.57-01 G.19-01 6.12-01 G.31-01 6.27-01 1,71*00 1.71*00 1.69400 1, lib 400 1,61400 1.62*00 1.S9400 1.S7400 1,SH 4 00 1.S2400 1,19*00 1.17*00 1.IS 400 9.124 06 1,10400 1.37400 1.3S400 1.33400 1.30400 1.26400 9,251 00 1.23400 1,21400 1,164 00 1.1G400 9.11*00 9.1I4Q0 9,09400 9.07*60 9.01400 1.02400 1.00*00 3,90400 2.00401 2.OS* 01 2.b2*01 2.79*01 2.77*01 2.71*01 2.71*01 2.60*01 2.66401 2.63401 2,61*01 2.90101 2,99401 2.93401 2.90401 2.10101 2.96*01 2.13*01 2.11*01 2.39401 2.36401 2.31*01 2,32*01 2.30401 2.27*01 :,29*01 2.23*01 2.21*01 2.19*01 2.17*01 2.19*01 2.13401 2.11401 .00 . l)0 .00 *00 .00 .00 .00 .00 ou .no .0(1 .00 .00 .00 .no .00 .00 .no . no .00 .00 .00 .no .00 .00 .00 *00 .00 .00 .nu .oil .00 .00 1.05*00 1.01400 1.03*00 9.02400 9.01(00 9,00*00 3,99*00 3.90*00 3,97*00 3,96*00 3.95*00 3,99*00 3.93*00 3.92+06 3.91*00 3.90*00 3.09*00 3.00400 3,06*00 3,05*00 3,09*00 3.03*00 3,01*00 3,00*00 3.79*00 3,7 7 * ft 0 3.76*00 3.75*00 3./3*0n 3.72100 3.71*00 3,69*00 3,60*00 .15-01 *20-01 .25-01 .30-01 39-01 .39-01 .93-01 .97-01 .51-01 .55-01 .59-01 .63-01 .67-01 .70-01 .79-01 .77-01 .01-01 .09-01 .07-01 .90-01 .93-01 .96-01 .99-01 2 .02-01 2 .05-01 00-01 2 .10-01 2 .13-01 2 .16-01 2 .10-01 2 .21-01 2 *23-01 2 *25-01 9,10+ul 9.96+01 9.73*01 5.00*01 5.27*01 5.53*01 5.00*01 6,05*01 6,31*01 6.57*01 6.02*01 7.07*01 7.32*01 7.96*01 7.01*01 0.09*01 0.29*01 0.92*01 0.76*01 0,99+01 9.22*01 9.95+01 9.67+01 9,90+01 1.01*02 1.03*02 1.06+02 1,00+02 1.1 Of02 1.12+02 1.19*02 1.16*02 1.10*02 1.26*01 1.26*01 1.26+01 1.26+01 1.26*01 1.26+01 1.26+01 1.26*01 1.26*01 1.26+01 1.26*01 1.26*01 1,26*01 1.26*01 1.26+01 1.26+01 1 .26+01 1.26*01 1.26+01 1.26+01 1.26*01 1.26+01 1.26*01 1.26*01 1.26*01 >.26+01 1.26*01 1 .26*01 1 .26*01 1.26*01 1.26(01 1 .26*01 1 .26*01 COMPOSJmOM nm niN HEACTON I'lUSSUKl l*i>U K| AC Toil TEMP U| cutt r UAlLH JACKri T| HP Of GlEf r Id AC I Oil nt at C CMEN1 Mill UAS llft im hlaltuii CUMOLE ucn liq. LIFT IN 111 AC TON MtMOEE 1120 HQ. LlFt IN me amok LllNOLt MLAC106 yLM iio. WOLl'Pt hu 11 REALTOM 1120 EIQ VOLUME CU FT 0.20100 4,40101 1.15102 9.00*01 -1,79*06 1.92+00 3,51+02 2 42+03 4,11+02 6,99+02 0.3U*00 4.04101 1.15*02 9,00*01 -1,01*06 1.92+Oft 3.49*02 2 42+05 4,66+02 6,99*02 5.40+00 4.74101 1.14*02 9,00*01 -1,02*06 1.92 + Of) 3.47*02 2 42+03 4.05*02 6.99+112 0.SO 100 9.74101 1.14*02 9.00*01 >1.64*06 1,93+00 3.45*02 2 42 + 03 4,03+02 6.99*02 5.60+00 0.70100 9* OOtf) 1 4,65101 1.14*02 1,13*02 9,00*61 -1,05*06 9.00*01 >1.67*06 1,95+00 1,95*00 3,43+02 3.41+02 2 42 + 03 2 42 + 05 4,00+02 3.90*02 6.99+02 6.99*0? 0.00100 9.50*01 1.13*02 9,00*01 >1,66*06 1.95+On 3,39+02 2 42 + 03 3,95+02 6,99+02 5 .`90*00 9.55*01 1.12*02 9,00*01 >1,90*06 1.94+flo 3.37+02 2 41 + 03 3.93*02 6,99+02 fj 'OOtOO 6.10100 9.40*01 9,43101 1,12*02 1.12*02 9,00*01 >1,91*06 9.00*01 >1.93*06 1.94+00 1.94 100 3.35+02 3.33+02 2 41+05 2 41 + 03 3,91+02 3,00*02 6,96+02 6,96+02 6.20100 9.39*01 1.11*02 9,00*01 >1.94*06 1.95+00 3.32+02 2 41*03 3,06+02 6,96+02 t 6.00100 9.34101 1,11*02 9,00*01 >1,95*06 1,95+00 3,30+02 2 41*03 5,04+02 6,96+02 M +>.40*00 9.29*01 1.11*02 9,00*01 >1,97*06 1.95+00 3.26+02 2 41*03 5.01*02 6.96*02 6.50100 9.25101 1.10*02 9.00*61 >1.96*06 1.95+fifl 3.26*02 2 41 + 03 3.79+02 6,90+02 6.60100 9.20*01 1.10*02 9.00*01 >2.00*06 1,96+00 3.24+02 2 41 + 03 3.77*02 6.96+02 6 *70+0 9.16ml 1.10*02 9.00*0] >2.01*06 1.96*On 3,22+02 2 41+03 3.75+02 6,96*02 6.00100 9.11*01 1,09*02 9,00*01 >2,02*06 1,96+00 3.21+02 2 41+03 3.72*02 6,96+02 6.40100 9.07*01 1.09*02 9.00*61 >2.64*06 1,46+00 3.19+02 2 41+03 3.70*02 6.97+02 7.00100 9,04*01 1.09*02 9,00*01 >2.05*06 1.97*00 3.17*02 2 41 + 05 3.66*02 6.97*02 7.10100 0.99101 1.00*02 9,00*01 >2.06*06 1.9/+00 3.15+02 2 41 + 05 3,66*02 6.97+0? 7.20100 7.30100 0.95*01 0.90*01 1.00*02 1.00*02 9.00*01 >2.06*06 9,00*01 >2,09*06 1.97*On 1.97*0q 3,14*02 3.12*02 2 41+05 2 41 + 03 3. (,4 + 02 3.62+02 6.97+02 6.97+02 7.40+00 0.06*01 1.07*02 9,00*01 -2.10*06 1.97+Oft 3.10+02 2 41 + 03 3.59+02 6.97+02 / '50100 7[60100 0.1*3*0 l 0,79 mi 1,07*02 1.07*02 9.00*61 - , 1 HO*. 9.00*01 >2,13+06 1.96*60 1.96+00 3.09+02 3.07*02 2 `ll *05 2 41+03 3.67+02 3.55+02 6.97*02 6.97* 02 7.76100 ft.75*01 1.06*02 9.00*01 -2.14+06 1.96+00 3, ilb + 02 2 41 + 03 3.53+02 6,97*02 oC a--j o o o 7.00*00 7.40*00 u.ooioo 0.10100 o.7imi 0.67*01 *.6411.1 ft.60101 1.06*02 1.06*02 1.06*02 1.05 m2 9.06*61 9,00*01 9.00*01 9,00*01 15+06 -2.16+06 2.17 + Ou >2,19*0+, 1.96*0ft 1,99+00 1.99+00 1.99*00 3.04+62 3,02+02 3.01 * 02 2.99+02 2 41*03 2 41 + 03 2 41*03 2 41*03 3.51*02 3.49*02 3.47+02 3.45*02 6,9*.* 02 6,96+02 6,96*02 6,96+0? 0.20100 0.57 mi 1.05*02 9.00*01 -2.20+06 1.99*00 2.90*02 2 41*03 3,44+02 6,96* 0? o.30*06 0.53m 1 1.05*1:2 9,00*01 >2.21*06 1.99+00 2.96+02 2 41 + 03 3.42* 02 6,96+ 02 0.00100 ft.50 t 01 1.04*02 9,00*01 22*06 2.00+00 2,94*02 2 41*03 3,40*02 6,96+02 couponMMftM i im. mri |>6t FLAS|* 6AS FLOW MOLf/HI h Vt 61*1. FLOW H..U /HIM FIlLl LAS|| 1120 Lid. F| OU tun i /nut f l A bill 6 6 AS (1.01 MU i/MN F6ASHLIJ yen Lid, FLO hi H^LL/fl If* FLASIIf 0 1120 LEO* Flow MOLL/HIM TOTAL I'yL 1`MOUUCLU Lunnt.L totm. yen gas epissioi* MH16LL total yen lio. chission LUHOLl 5.20*00 a'30+00 5.40+00 5.5L+0G 5.60*00 5.76*UO 5.00*00 5.90*00 0.00*00 0. 10*00 u.20+00 u.30**10 0.40+00 0.5U+0U t.'00*06 0'7O+0O ,,'uu+au i,.'9MtUll 7.00*00 !. lutiiu /. <*11*1111 1. io+oo 7.4u*uo 1 .50*00 7.00+00 7. 7(I*I)U 7.00*00 / *9(110b 11.00 *00 it'10* Oil O.20 *00 t>.30*0U c .Jiii * ml 2.00*01 1,90101 1.96+pl 1 . `>0 1 |> 1 i.93*pi 1.91*01 1.09*01 1.07*01 1.06*01 1.04*01 1.02*01 l.01*1 1.79*01 1.70*01 1.76*01 1.74*0 1 1,73*01 1.11*01 1 . 7*l**.l 1 .1.6*01 1 .1.7 MU 1 .fcitrl 1.64*01 I .*.2*01 1.61 * 01 1.09*01 1.6it*f1 l .1*7*01 1,ft6*fl 1.94 *01 1.92*01 1.61*01 1.60*01 6,20-01 6.12-01 6.06-01 6.90-01 5.91-01 5,05-al 3.70-01 6.71-01 6.64-01 5.5U-01 6.61-01 5.46-01 5.39-01 5.32-01 5.26-01 5.20-01 5.14-01 6.00-01 5.02-11 4.96-01 4.911-01 4.06-01 4.79-01 4.7 3 - * 1 4.60-01 4.62-01 4.67-01 4.51-01 4.46-01 4.41-01 4.36-01 4.30-01 4.25-01 3.95*00 3.93*00 3,91*00 3.00*00 3,06*00 3.04*00 3.02*00 3.79*00 3.77*00 3.75*00 3.73*00 3,70*00 3,60*00 3,66*00 3,64* Uli 3,61*60 3,59*00 3.57* on 3.66* or 3.53*00 3,60*00 3.46*00 3,46*00 3.44*06 3,41*06 3,39*00 3.37*00 3.35*00 3.33*00 3.3)*60 3,20*00 3,26*00 3.24*00 2.09*01 2.67101 2,06*01 2.63*01 2.01+01 1,99+01 1.97+01 1.95+01 1.94+01 1.92+01 1,90*01 1.00+01 1,07+01 1.65+01 1,03+01 1.01+01 1.50+01 1 ,/fc + oi 1.76*01 1.76+01 1.73+01 1.72+01 1.70+01 1.66+01 1 .*.7+01 1.66+01 I.64+01 1,62+01 1.61+01 1.69*01 1.60+01 1 .66*01 1,66+01 ,00 .OU .1)0 .00 .00 .00 .00 .00 ,00 ,110 ,U0 ,00 .00 .00 .00 .00 .00 .00 .l)U .00 .00 .00 .00 .00 .00 .00 .00 .00 . 00 - 00 .00 .0U .00 3,66+00 3,65*00 3,63+00 3,62+00 3.60+00 3.69*00 3.67+0U 3,56+00 3,54+00 3,53+00 3.51 + 0*1 3,50+Ofl 3.40+00 3.46+00 3,45+00 3,43+00 3.42+00 3,40*00 3.30+00 3.37*00 3,36+ 00 3,33*00 3.32*00 3.30*00 3.20*00 3.27+00 3,25*00 3.23+00 3.22*00 3.20*00 3.10*00 3.16*00 3.15+00 2 20-01 2 30-01 2 32-01 2 34-01 2 36-01 4>b 30-01 2 41-01 2 43-01 2 44-01 2 46-01 2 40-01 2 60-01 2 52-01 2 64-01 2 55-01 2 57-01 2 59-01 2 61-U1 2 62-01 2 64-01 2 66-01 2 67-01 2 60-01 2 70-01 2 71-01 2 73-01 2 74-01 2'i 76-01 77-01 70-01 2 00-01 2 01 - U l 2 02-01 1,20+02 1.22+02 1.24*02 1.26+62 1.2P+U2 1.30*02 1.32*02 1.34+62 1.36+U2 1.30+U2 1.40+U2 1.42+U2 1.43+02 1.46+U2 1,47*62 1.+19+02 1.51*U2 1.62*02 1.64+02 1.66*02 1.67*02 1.69+02 1.61+02 1 .62*2 1,64*02 1.6F+U2 1.67+U2 1.I9+U2 1.71*02 1.72*02 1.74*02 1.76*02 1.77*02 1.26+01 1.26+01 1,26+01 1.26+0J 1.26+0J 1.26+01 1.26+01 1.26+01 1.26+01 1.26*01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26*01 1,26*01 1.26+01 1.26+01 1.26+01 1.26+fll 1.26+0] 1.26+01 1.26*01 1.26*01 1.26+01 1.26+01 1.26+01 1.26+0] 1,26+ftl ucc 026702 cmpMunoM 11 Ml MlN lit AC TOM Pb r SSUB f I'SJA M| ACT OH nnc Of 6(tf f I UAJ IK JACK! T Tl hi* ill 6,iff F FEAUOli Ml AT com urn HAS Ll-Fl 1U lit- At: fOll LHhflLE VCH 616. 11FT IN R1ACI0H L Of,OLE *|20 LIU. 1.1 F* IN iuaMoh MJHOLL iu-acioo yLli 1 IU. volume irU fT realtor 1120 LIU. VOLUME CU FI tt'bOtOO A. 96+01 1,01*02 9.00*01 3+06 2.00*00 2.93+02 2*11+03 3.30*62 6.96+02 6.60+00 11.93*01 1.09*02 9.00*01 -2.21+06 2.00+00 2.91+02 2*10+03 3.36+02 6,96+02 8.70+00 A.39*0l 1.01*02 9.00*01 -2.25+06 2.00+00 2.90*02 2*10+03 3.39+02 6,96+02 U.00+00 0.3b tfl 1 1.03*02 9.00*01 -2,26+06 2,00 + 00 2.30+02 2*10+03 3.32+02 6.95+0? 6.90*00 0.33*01 1.03*02 9,00*01 -2,20+06 2.01+00 2.07*02 2*10+03 3.31+02 6,95*02 9.00*U0 030* 01 1.03*02 9.00*01 -2.29+06 2.01+00 2,06*02 2*10+03 3.29+02 6,95+0? 9'iotoo 0,27*01 1.03*02 9.00*01 -2.30+06 2,01+00 2.01+02 2.00+03 3.27+02 6.95+0? 9.20+00 0.21*01 1.02*02 9.00*01 -2.31+06 2.01+00 2.03+02 2.10+03 3.29+02 6.95* 02 9.30*00 0.21*01 1.02*02 9.00*01 , 32 + 06 2.01+00 2.01+02 2*10+03 3.29+02 6.95+02 9.90*00 o.iotri 1.02*02 9.00*01 -2,33+06 2.01+00 2.00*02 2*10+03 3.22+02 6.95+02 9.50+00 o.lb*ni 1.02*02 9.00*01 -2,39+06 2.02*00 2.70*02 2*10+03 3.20*02 6.95+02 n i 9.6(1*00 0.12*ol 1.01*02 9.00+01 -2,36+06 2.02+00 2,77+02 2*10+03 3.1P+U2 6,95+02 9.70*00 0.09*01 1.01+02 9.00+01 3f* * Q6 2.02+00 2.76*02 2*10+03 3,17+02 6.95+02 9.00*00 0.0b*0l 1.01+02 9.00+01 -2,37+06 2*02+00 2,71*02 2*90+03 3.15+02 6,95+02 9'90*00 0,03*01 1.01*02 9.00+01 -2.30*06 2,02+00 2.73+02 2*90+03 3.19+02 6.99+02 1 .'OOtOi 0.01*ol 1.00*02 9.00*01 -2,39*06 2.03+oq 2,72+02 2*90+03 3.12+02 6.99*02 fov> Sr CD O CO 1 * COUI>IM*rlOH Tlrtl mn i`tki:ri. AS|( I.AS ri-og nout /nn PlifFLASU w<n nn. FLtiu MOLl/ftin |>|< till ASM II*u t in. Ft uij non /nin f L A 5111 U ftAbllMi FLASH!U 6A5 vcn Liu, 1120 Lin* CLOU FLOW Flow 6.0U/M1N HULL/tt in noLF/nin TUf At. 1*1/6 pltUUUCLI) LllWOLt toial li/cn ii/.s nISSION MIMOLl iutal yen Liu. Lnlssion LIlMOtt 0.56*00 0.60+UU 6.70**10 O.UlllOU -,.90*00 9.0(1*00 9. lil+00 9.20*00 9.30*00 9.90*0 9.50+UO 9.6Q+00 9.76+00 9.00*00 9.90+00 l.OO+Ol 1,90+01 1.97+fll 1 .HI.* til 1.99 +Hi 1.93+01 1.92 + Ol i.hO+oi 1.59+ni 1.311*01 I,37 + m 1,35+ni 1.39+rt 1,33+1*1 1.3**01 1.30*01 1,29+01 9,2(1-01 9,15-01 9,10-01 H.oo-ni 0.Ol-ol 3,96-01 3.91-01 3.06-01 3.02-01 3.77-01 3.73-01 3.66-01 3,09-01 3.59-01 3,55-01 3,51-01 3.22*00 3.20*00 3.16*00 3.15*00 3,13*00 3.11*00 3.09*00 3.07*60 3.05*60 3,02* tlO 3.00*00 2,90*00 2,96*00 2,99*00 2,92*00 2,90*0U 1.53+01 1.52*01 1,51*01 1.99+01 1.96*01 1,96*01 1.95*01 1 .99*01 1,92+01 1.91+01 1,90*01 1.30+01 1,37+01 1.36*01 1.39*01 1.33+01 .00 .00 .00 *1*0 ,00 .00 .00 .00 .00 .00 .00 ,00 .00 .00 .00 .00 3.13*00 3,11+00 3,09+00 3,00+00 3.06+00 3.09+00 3.02+60 3,00+00 2.99+00 2,97*00 2,95+00 2.93*00 2.91*00 2.09+00 2.60*00 2,06+00 2*63-01 2*05-01 2*06-01 2*07-01 2*00-01 2.09f01 2*91-01 2,92-01 2*93-01 2*99-01 2*95-01 2*96-01 2*97-01 2*90-01 2*99-01 3*00-01 1.70*02 1.00+02 1.01*02 1.03*02 1.69*02 1.06+02 1.07*u2 1.00+02 1.90+02 1.91*02 1.93+02 1.99*02 1.96*02 1.97+62 1.90+02 1.99+02 1.26+01 1,26+0) 1.26+01 1.26+01 1 .26*01 1.26+01 1.26+0) 1.26*01 1.26+0) 1.26+0) 1.26+ft) 1.26*0) 1.26+01 1.26+01 1.26+01 1.26+01 it in ucc 026704 ( DISCHARGE FROM A FVC UA'CCU REACTOR Cuae 4. Overfilling - Cold Water on Jackut IUALtOK PRESSURE Al Hrl- QF OlSCtlARGI = 194.70 PS|A PRESSURL DGUrjSTK|T*M OF UACWL = 64. 70 PSIA 111 AC. OH ItMP AT Tlr-C Op disc HARGL = 135. 00 F UAfEN JACKET Ttrt( AT OISCRAR(.r = 90.00 F r<IAC,0| VOLUME = 1447. 000 CU FI LIOU(! VCM !!!!! I Ati I(. REAL jijji = VAPOR INITIALLY IN HLA( TOR = lhhole .0417 LNMOLi: MEAT OF ItCACfltlN - 45516*000 lilU/LUMQLt Lid !*20 INITIALLY IN HEAC'OR = 2604,0 LRMOLE JACKET COEF Tints AULA = 564.3 UTU/M-F ULNSiFY OF UATLK (CQNSiANT 1 = 3.4570 LllpOlt/CU ft ANITA OF ItLLILF VALvF OtilFlCL OpENIfiG = .0194 SO FT MINIMUM LlOUfO EI(|pAIMf-ENT = .0100 CU FT Llfj/CU FT GAS LIO "OL WHEN HIW tMTMAiNfitNT IS HEaCMEU c 1219.4 CU FI tlldb JACKET FACTOR1 = 1.00 INITIAL DENSITY OF VCM = .0447/ LHHOLE/Cll FT ORIFICE FLOW COEFFICIENT = .610 MINIMUM WATER JACKET TEMP = 40.00 F TIME MIN JACKET TEMP IS REACHED = 5.00 MIN reactiun rate FAC 1OR = .*0 01 oro c o-->j <O> o TIME MU1 HLACTUR PRESSURE PS1A Rl ACTOR TEMP UpGREE r UAlEK JACKET TTMP ULGrEE f REACTOR HEAT COM ENT Itl J GAS LEFT IN rlactdr LHMoLE VCM Lid. LEFT IN REACTOH LHMoLE 1(20 Lid. LLF1 IN REACTUR Ll)M0Lt rcactor VCM LIU* volume Ml FT reactor 1120 Lid. VOLUME CU FI .00 1.00-01 2 '00-01 4.00-01 4.00-01 S.Oti-ul u.Oli-Ol 7.00-01 U.00-01 9.00-01 1.00100 l'lll 100 1.20100 l.30*0U 1.40*00 l.bUlOO 1.60100 1.70100 1 '60 + 00 1.96+02 1.42102 1.42102 l.421fl2 1.4H02 1.41102 1.41102 1.31102 1.30102 1.40+02 1.40102 1.29+02 1.29102 1.2610.2 1,27ip2 1.271(2 1.26+02 1.25u>2 1.24 m2 1.35+02 1.35+02 1.35+02 1.35+02 1.35(02 1.35+02 1.34+02 1.44(02 1,34+02 1.34+02 1.3t|t02 1.33+02 1.33+02 1.33+02 1.33+02 1.32+02 1.32(02 1.31(02 1.31(0? 9.00101 6.92101 6.63101 8.76101 8.66101 6.56101 6.50101 6.41101 6.34101 6.24101 6.16101 8.06+01 7.99+01 7.9U01 7,62101 7.74+01 7.66+01 7.57+01 7.49+01 -1,04 + 06 -1.04 + 06 -1,04+06 >1,03+06 -1,03+06 -1.03+06 -1.03+06 -1.04+06 -1.04106 -1.04106 -1,04106 -1.05+06 -1,05+06 -1.06+06 -1.00+06 -1.09+06 -1.11106 - 1 .14 + 06 -1.15+06 3,47-02 1.54-01 2.60-01 4.1)5-01 5.1 /-Dl 6.i(6-0] 7.71-01 0.94-01 1.01 + 00 l.li+Qo 1.24+00 1.34*00 1*44+00 1.54+00 1.61 + 0(1 1.60+00 1*74+00 1.77+00 1.70+00 4,66*02 4,03+02 4,00+02 4.77+02 4.75*02 4.72*02 4,69+02 4,66+02 4,63+02 4,61*02 4,50+02 4,55+02 4,52*02 4.49*02 4.45+02 4,42+02 4,39+02 4,35+02 4.33+02 2*60+03 2.59+03 2*56+03 2*56+03 2*55+03 2*54+03 2.53+04 2*52+04 2*51+04 2*50+04 2*49+04 2*40+04 2.47*04 2.46+03 2*45+04 2.44+03 2*44+04 2.44*04 2*43+04 5.03+02 5.79+02 b.76+02 5.72+02 5.69+02 5,66+02 5.62+02 5,59+02 5.55+02 5.52+02 5.40+02 5.44+02 5.40+02 5.37+02 5.33+02 5.20+02 5,24+02 5.20*02 5.16+02 7.54+02 7.49*02 7,45+02 7.42+02 /,30 + 02 7.35*02 7,31+02 7.20+02 7.25+02 7.22+02 /,19*02 7.16+02 7,14+02 /.11*02 1,09*02 Z.07+02 7.05+02 7.04+02 7.04+02 COHeOKWHU* 1 (HI |N PUllLASil GAS TLOiJ mu /hit, miLAStl Wf?1 LK+. FLOW iM/ if. I'ltF.f |. ASH 1120 LIII, Flow HOLI /MW 11 ASid |i GAS ILCW Mit/HJN fLASHtO VC Ll, f LOW hull/WIN flashfu 1120 LIO* FLOW mgu/hih TOTAL pVL puouuct-u LIIOOLF total VCl 0AS Cf+ i .SSI lift MWOL TOf AL VCh LIO. CHiSsiuw LliHOLt .'00 1.110-01 2.00-01 i.VlI-ul 4.00-01 !. 00-01 u%06-61 7.00-01 O.00-01 9.00-01 1 'OOfrOU i ;io*imi 1*20+00 1 .MO too | >0*00 1.SO*00 1.00*00 l.70*00 1.00+00 1.02-02 5.51-01 1,00+00 1.66+00 2 , -41 tfltt 1.04*|i0 nfttifo 4.76+00 S.oo+ro 7.00+1.0 (1,40*00 1.00*01 1.20+01 1.44*01 1.72+01 2.U9 + M 2.55io1 2.65 + ftl 2.741 111 4.57+01 2,64+Ql 2,00+01 2,46+01 2,41+01 2.46+01 2.41*01 2,24+01 2,17+01 2.09*01 2,00+01 l.A`i+01 1.70*01 1.61*01 1 .42+01 1.20+01 9.01+00 4.74+OU 1.29+00 1.75+02 1.24+02 1,24+02 1.21+02 1,19+02 l,16 + 02 1,14*02 1.11*02 1.07*02 1.04+02 9,94+01 9,41+01 (1.00+01 0.07+01 7,17+01 6,05*01 4.59+01 2,44+01 6.05+00 2.17+01 1,60+01 1.64*01 1.67*01 1,71*01 1.75+01 1 .00+01 1.06+01 1,94+01 2,00*01 2.09+01 2.20+01 2,44+01 2.49+01 2.60*01 2.94+01 4.26+01 4.10+01 2.92+01 1.42(01 1.00+01 9,07+00 9.60+00 9,47+00 9.24+00 0.90+00 0,69+00 0,49*00 7.97+00 7.S4+00 7,01+00 6.49+OQ 6.69*00 4.7*++ 00 4,61+00 2,14+00 4,2+t-0l .0+) 1.75+02 1.24+02 1,22+02 1.21+02 1.10+02 1,16+02 1.14*02 1.11+02 1.07*02 1.04*02 9.92+01 9.40 + 01 0.79*01 a.o6+oi 7.17*01 6,05+01 4,50*01 2,42*01 6,01+00 .00 6*70-04 1.45-02 2.02-02 2.60-02 4,44-02 4*911-02 4*62-02 5*25-02 5.07-02 6*40-02 7.09-02 7.60-02 0.27-02 0.04-02 (j. 4 0-02 9*95-02 1.05-01 1.10-01 .00 i.ot+oo 4.42+00 5,06+00 6,73+00 0.44 + 00 1 .02+01 1.20+01 1.39*01 1.50*01 1.79+01 2.60+01 if.22 + 01 2.46+01 2.71*01 2.99+01 4.29+01 1.61+U1 4.90*01 .00 1,17+00 2.17+00 4.15+00 4.11+00 5,04+00 5,95*00 6,04 tOO 7.69+00 0.51+00 9,20+00 *.00+01 1.0/*01 1.14+01 1.10+01 1.22*01 1.25+01 1.26+01 1.26+01 026706 ooc t I 01 oa oC So TINT fllN FCACTOR PRESSURE (*SIA tt( ACTOR TfP degree r WATER JAtKFT Ti HP DEGorr ( REAM OR HEAT IPlilEM mu CAS UF1 IN RE AC jliR euooee yen LIU. lift in REACTOR EimOLE ((20 LIU. Ltf I IN ML AM OK ERNOEE REACTOR v*-n l IU* y.iiLUHE ib'u r t reactor 1120 L 10. VOLUME CU FI 1.`JO too 2.0Q+OO 2.'lOtttO 2'20tOO 2.30100 2.10tUO 2.60100 2>0tQ0 2.70tOU 2.00100 2.VOi00 3'OotUO 3.10100 3.20100 3.30100 3.10100 3.60100 3.60+00 3.70100 3.00100 3.VU100 1.00100 1.10100 1.20100 1.30100 1.10100 1.50100 1 .*>0*00 1*70100 1.00100 i. yotoo s.ooioo 5.10100 1.23 + 1(2 1,^2102 1,21102 l,20ir.2 1.19*02 1.10*02 1,17i(i2 1.10102 1.15*02 1.15*02 1.11if 2 1.13102 1.12*|>2 1.11*02 1.10*02 1.10102 1.09+02 l.OAU`2 1.0/102 1.07102 1.00102 1,06102 1.05io2 1.01(02 1.03102 1.02102 l.02*r2 1.01*u2 1.00102 *1.99+1.1 `1.9?*l)l i.attoi 9.00+01 1.30102 1.2V102 1.29102 1.20102 1.2A102 1.27102 1.27102 1.20i2 1.2CI02 1.25io2 1.25102 1.21102 1.2H02 1.23102 1.23102 1.22102 1.22*02 1.2U02 1.2li02 1.20102 1.20102 1.19(02 1.19(02 1,10+02 1.10(02 1.17102 1.17(02 1.17*02 1.10102 1.16*22 1.15(02 1.15(02 1,11(02 7,10101 7.32101 7,21101 7.16101 7.07101 6,96+01 6.90101 6.02*01 6.73*01 6.66*01 6,56*01 6,10*01 6.10*01 6.31*01 6,23*01 6.11*01 6.06101 5.90*01 5,09*01 5.01*01 5.72*01 `5,61*01 5.56(0] 5.17*01 5.39(01 5.30101 5.22*01 5,11(01 5,05ml 1,97ml 1 .of ml 1.0ft till 1,00*01 .1,17*06 -1.20*06 -1,22*06 -1.21*06 -1.27*06 -1,29*06 -1,31*06 -1.33*06 -1,35*06 -1,30*06 -1.10*06 -1,12*06 -1,11*06 -1.16*06 -1,10*06 -1.50*06. -1.52*06 -1,51*06 -1.56*06 -1.50*06 -1,60*06 -1,62*06 -1,61*06 -1.66*06 -1,60*06 -1.70*06 -1.72*06 -1.71*06 -1.76*06 -1,/7*06 -1.79(06 -1.0K06 -1.63*06 1.79*00 1.79*00 1.00*00 1.00*Oft 1.OltOft l.nitoo 1.02*00 1.02*00 1.03*00 1,03(00 1.03(00 l.QHOO 1.01*0(1 1.05*0q l,ftb*0(| l.Q5*Oo 1.06*00 1,06*00 I.O61O0 1.07(00 l.O/iOQ 1.80+0(1 1*00*00 l.oftion 1*09+00 1*09(00 1.09(00 1.09(00 *90+00 l,4U(0n 1,9U + 0(t 1.91100 1.91*00 1,30*02 1.27*02 1.21*02 1.22+0? 1,19*02 1.16*02 1,11+02 1.11+02 1.00+02 1.06+02 1.03+02 1.01+02 3,90+02 3,96+02 3,91*02 3,91+02 3,09*02 3.06+02 3,01*02 3.02*02 3,00+02 3.77+02 3.75*02 3,73*0? 3,71+02 3.69+02 3.66+02 3.61+02 3,62*02 3 , *>0 + 02 3.50*02 3.56+02 4.51*02 2 13 + 03 2 13*03 2 13+03 2 13+03 2 13+03 2 13 + 03 2 93+03 2 13 + 03 2 13(03 2 13103 2 9 3 + 03 2 13(03 2 13(03 2 (3*03 2 13*03 2 93*03 2 13*03 2 92(03 2 92(03 2 92(03 2 92(03 2 92(03 2 92+03 2 92 + 03 2 92 + 03 2 92 + 03 2 92 + 03 2 92+03 2 92 + 03 2 92 + G3 2 92 + 03 2 92 + 03 2 92 + 03 5.12+02 5.P9+02 5,05102 6,01+02 1,90+02 9,91*02 1.91*02 1.66+02 1.01*02 1.01+U2 1,70*02 1.79*02 1.71+02 1.60+02 1.65+02 1.62+02 9,59*02 9.5E+02 9,52(02 9.50+U2 9,47*02 4.44+02 4,41*02 4.30+02 4.35+02 4.3? *02 4.30+02 4.27*02 4.24+02 4.21+02 4.19*02 9.16(02 9.14(02 7.09+02 7.09+0? 7,09+02 7.03*02 7,03*02 7.03*02 7.03*02 7,03*02 7,03*0? 7.03*02 7,02(02 7.02(02 7,02*02 7,02*02 7,02*02 7.02*02 7,02*02 7,01*02 7.01+02 7,01+02 7,01+02 7.01(02 7,01+02 7,01+02 7,01+02 7,00+02 7,00102 7,00+02 7,00+02 7.00+02 7.00+0? 7.00+02 7,00+02 COMMON AVION O) O *xj CD CD ! lril liirt Htm.AS|l 6 AS FI OU MOLf /F.ir 1*1+1 CLASH v+rt no. FLOu Hr.il/niu IH+fTLASh 1120 110. fl<ih nou/niii t l A5iiiU HA5HU1 FLASH! n GAS VCn LJU. 1120 L(C. (LOU FLOW FLOW MiLt/hlN HULl/HIh HOLt/MN 101AL I*Vl |*HOUUCLU LitHOLL TUIAL WC" GAS t+ilSSION MirtOlt (OfAL UCfl LIU. OilSSION LUMOLt 1 .90+00 2.00*00 2.10*00 2.20*00 2.40*00 2.00*00 2.50*00 2.00*00 2'70+00 2 '00*00 2.90+00 1 4.*00+00 M) 4.10+00 S .201 00 4.40+00 3.40*00 4.'50 +00 4.00+00 4.70+00 4.00+00 4.90+OU H .'Oil *00 1.1 0 Ml 0 <+.20*00 4 .'40 + 00 1 .Hu Mill I .50*00 4.1.0 1 Oil H.70*00 H*00*00 H .`JO *00 5.00*00 5.10*00 2.71+01 2.09+01 2.00+01 2.0i*nl 2.00 + 1*1 2.50*01 2.55+01 2.54+01 2.50+01 2.46+M 2.<*:**r. 1 2.43*01 2.H0+0 1 ?.. 40 * 0 1 2.45+ol 2. 14+ f, | 2.41+0t 2.29+01 2 2*>+01 2.2* + f 1 2.22+01 2.20+01 2.17*01 2,15+01 2.14*f;l i.ll + .il 2.09*01 2,0/ *01 =*.05 + 01 2.04*01 2.00*01 1.90+01 1.90*01 9,10.01 0.99-01 0,00-01 0.77-01 0.07-01 0.50-01 0.46-01 0.40-fll 0.20-01 0,10-01 0,00-01 7.90-01 7.00-01 7.77-Sl 7.07-01 7.50-01 7.49-01 7.90-01 /.il-ol 7.22-01 7.14-ftl 7.0H-01 6.9h-ll 0.07-01 0,10-01 o i ii--s i (..02-III 6,54-it 1 +..H5-01 0.47-01 *.. 4ll-0 1 0.22-01 0, lH-01 4.73*0(1 4.70*00 4.07+00 4.05*0(1 4.02*00 4.00 + 0(1 4.57+00 4,54*00 4.52+00 4.49+00 4,40*00 4,44+00 4.41+00 4.39+00 4,30+00 4,43*00 4.31 +0(1 4.20*00 4,20 +Oil 4,24+00 4.211*00 4.10+00 4,15+00 4.12*00 4,10+00 4.07*00 4.04100 4.02*1*0 3.9*1+00 3.*J7 Mill 3.94 * 01* 3.91 *11(1 3.04+00 2.07+01 2.04+01 2,01+01 2.70+01 2.75+01 2.72+01 2.70+01 2.67+01 2.64+01 2,61+01 2.50+01 2.56+01 2.53+01 ,*.50trtl 2.46+01 2.45+01 2,43+01 2.40*01 2.30+01 2.35+01 2.33+01 2,30101 2.20+01 2.26*01 2.22+01 2.21+01 2.19+01 2.16*01 2.14*01 2.12*01 2.10*01 2.07*01 2.05+01 .00 .00 .00 .00 .00 .00 .00 .00 .00 ,00 .00 .00 .00 .00 .no .00 .Oil .00 .00 .00 ,00 .00 .00 .oo .00 .00 .00 .00 .00 .ou .00 .no .00 4.04 *00 4.03+QO 4,02+00 4.01+00 4.00+00 3,99+00 3.90+00 3,97+00 3,96+0(1 3,95+00 3,94*00 3,93+00 3.91+00 3.90+0(1 3.09*00 3.07+00 3.06+00 3.05+00 3,03*0(1 3,02+00 3,01+00 3,79 + 0(1 3,70+00 3.76+00 3,75+Oft 3.73*00 3.71+00 3,70+00 3.00+00 3.07+00 3.05 * 0 0 3,o3+rto * OQ 1.15-01 1.20-01 1.25-01 1.29-01 1*34-01 1*30-01 1.43-01 1.47-01 1.51-01 1.55-01 1.59-0l 1.62-01 1.66-U1 1.09-01 1.73-01 1*76-01 1*00-01 1.03-01 1.00-01 1.09-01 1.92-01 1.95-01 1.90-01 2.01-01 2.03-01 2.00-01 2.09-01 2.11-01 2.14-01 , 2.16-01 2.10-01 2.21-01 2.23-01 4.10+01 4.4S+UI 4,72+01 4,99*01 5,26+01 5.52+01 5.76+01 6.04+01 6.30+01 6.55+01 6,eo+oi 7.05+01 7.30+01 7.54+01 i.ir*oi 6.02*01 0.26+01 0.49*01 0 72 + 01 0.95+01 9.10+01 9,40+01 9.62*01 9.OH + 01 1.01+02 1.03+02 1.05+02 1.07+02 1.09*02 I.11+02 1.13*02 1.15+02 1.17*02 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1,26+01 1,26+01 *.26*01 1,26+01 1.26+01 1.26+01 1,26*01 1.26+01 1.26+01 1,26+01 1.26*01 1.26+01 1.26+01 1,26+01 1,26+01 1.26+01 1,26+01 1.26+01 1.26*01 1,26*01 1,26+01 1.26+01 COHPOH MION TiM (1|N HEALTON PHI'S SUftf ('61A Itl AC 1 OR TtW* 111 GHEE r UAlf.lt JAiKF1 li ns* lltG+El F KfAC ton lit. AI LOti 1 -61 mo gas Ltn in jU.At|uii UmoLE VCM Lltt. ELFI IN H6ACJ0H LBftOLE ||2() LIU. LtFl IN lit AM <Ht LO"OLE n+rAcion nEAMo< l/6n 1 III. II2U LIO. woluhe 6U f i volune CU pi 5. 20*00 5.30+00 5.90 + 00 S.'bO + OO 5'6OtO0 5.70*00 5.00*00 5.90*00 f,'00 + 00 b'10+00 0.20*00 i>.30 + 00 0,*10*00 0.50*00 b.bU+00 0.70*00 0.00*00 o.yo+oo 7.00*00 7'IG*00 7.20*00 7.30*00 7.10*00 7.50*00 7.00*00 7 *70 + 00 7.00*00 7.90*110 0.00*00 0.10*00 0.20+00 0.30*00 0.90*00 9.79 + f'l 9.60*01 9.62+01 9.57*01 9.51+pl 9.96+01 9.90+01 9.5b*rl 9.29tpl 9.29*01 9.19+01 9,19+01 9.09*01 9.09 +(ll 9.00*01 0,95 + r.l 0.90+01 0.06+01 O.01+01 3.77*01 0.72tpl 0.60*01 0.69+01 0.60+01 U.b6+nl 0,52+fll O.lu+pl fl.99*nl 0.90 + 01 ii.lo* pi n,3?tni H. 29* ll 0,25+f.l 1.19+02 1.19+02 1.13+02 1.13+02 1.12+02 1.12*32 1.11+02 1.11+02 1.11+32 1.10+02 1.10*02 1.10+02 1.09+02 1.09+02 1.00+02 1.00+02 1.00+02 1.07+02 1.07*02 1.07+02 1.06+02 1.06+02 1.06+02 1.05+02 1.05*02 1.05+02 1.09 + 02 1.09+02 1.09*112 1.03+.",2 1.03+02 l .0 3+02 1,02+02 9.00+01 9.00+01 9.00+01 9,00+01 i.eo+oi 9.00+01 9,00+01 9.00+01 9 (lit + 01 9.00+01 9,00+01 9.00*01 9,00+01 9 .00 + 01 9,00*01 9,00+01 9 .0(1 + 01 9,00+01 9.00*01 9.00+01 9.1*0 + 01 9.00+01 9.60+01 9.00+01 9.00+01 9.00*01 9.0C+P1 9.60+01 9.00*01 9 . <11 *01 9.00*01 9,00+01 9.00+tl -1.05+06 >1.06+06 >1.00+06' >1.90+06. -1.92+06 -1,93+06 -1.95+06 -1.97+06 -1,96+06 -2.00+06 -2.01+06 >2.03+06 >2.05+06 -2.06+06 -2.06*06 >2.09*06 -2.11*06 -2,12*06 >2,19*06 -2,15*06 -2,17+06 >2.16+06 -2,19*06 -2,21+06 -2.22*06 -2.29+06 -2.25+06 -2,26+06 -2,26+06 -2.29+06 -2,30*06 -2.32+06 >2,33*06 1,91+00 1 92+0(1 1,92+Ofl 1 * 92 + 00 1.9^+Oq 1.93+00 1.93+0n 1.93*00 1.93*Oft 1.99+00 1,99+00 1,99+00 1.99+00 1.95+00 1.95+00 1.95+Oft l*95+0ft 1,96+Oft 1 96+ Oft 1,96+Oft 1.96*00 1.97*00 1.9/+00 1,97*00 1.91+00 1.97+00 1.90+Qo 1*90+00 J.yft+oo 1*96+Oft 1,90+00 1.99+00 1.99*00 3.52*02 3,50*02 3,90*02 3.96*02 3,99+02 3.92+02 3,90+02 3,39+02 3.37+02 3,35+02 3,33+02 3.31+02 3,30+02 3,26+02 3,26+02 3,29+02 3.23+02 3.21+02 3.19+02 3,16+02 3.16+02 3,15+02 3,13+02 3.11+02 3.10+02 3.00+02 3.07+02 3.05+02 3.09+02 3.62+02 3.01+02 2.99+02 2.90+02 2*92+03 2.92+03 2.92+03 2*92+03 2.92+03 2*92+03 2.92+03 2.92+03 2.91+03 2.91+03 2.91+03 2*91+03 2.91+03 2*91+03 2*91+03 2*91+03 2.91+03 2.91*03 2.91*03 2.91+03 2.91+03 2.91+03 2.91+03 2.91+03 2.91+03 2*91+03 2.91+03 2.91+03 2*91+03 2.91*03 2*91+03 2*91+03 2*91+03 9.11+U2 9,09+02 9.06+02 9,09+02 9.01+02 3.99+02 3,96+02 3,99+02 3.92+02 3,(19+02 3,07+02 3.05+02 3,03+02 3.00+02 3,70+02 3.76+02 3.79+02 3.72+02 3.70+02 3.60+02 3.66+02 3,69+02 3,62+02 3.60+02 3.50+02 3,5fc-tU2 3.59*02 3.52+02 3,50*02 3.90*02 3.96+02 3.95+02 3.93+02 6,99+02 6,99*02 6,99+02 6,99+02 6,99+02 6,99+02 6,99+02 6,99*02 6,99+02 6,90+02 6,90+02 6.90+02 6,90+02 6.90*02 6,90*02 6.90+02 6.90*02 6.90+02 6,97*02 6.97*02 6.97+02 6,91+02 6,97+02 6,97+02 6,97*02 6,91+02 6.91+02 6.91*02 6,96+02 6.96 + 02 6,96+02 6,96+02 6.96*02 ucc 026709 Tim h|N l>KLTl AS| CAS MUM mgli /m*i IVt'ftA.Sli VCH LIU. rL*H* rtl U/MIll I'llEl l ash 1120 l IQ. Fl iiii hQl.f /MIN I l A Sill l* FLASHtl) I LASIltO ii AS yen F|U. 1120 LIU. MOW FLOW f i QU r.CI t/HIN HULL /flIN MOLL/HIN TOT At. I'yL FliOUiiCtU LllMOLL TOTAl wen gas LRISSIUH t-IJHOLE 1UTAL yen Liu. FHlSSlUN LUMOLC 5.20+00 1.94+01 6,06-01 3.06*00 2.03+01 5 '30*00 5J40+00 i.92+ni l.`Jl*0l b.99-01 b, 91-01 3.03*00 3,01*00 2.01+01 1.99*01 t> .to*o 5.60* 00 1.09+nl t,07*ol b. 01-1)1 5.76-01 3.70*00 3,76*00 1,97*01 1.96*01 t'70*00 1 .lift* 111 S.69-01 3,73*00 1.93+01 5 00*00 1.113*01 b,62-tll 3,70*00 1,91+01 5 `JO *00 ^,00*00 1.01*01 1.7`JtOl 5.55-ftl 5.40-01 3.60*00 3.66*00 1.09+01 1,07+01 0.10*00 1.77*01 5. 11-01 3.62*00 1.05+01 6 v20* 00 l,7G*ol S.3H-Q1 3.60*00 1.03+01 u*ni-* 0^30*00 6.'in too l, 74 + itl 1.72*01 b,27-01 b.21-01 3,57*00 3.54*00 1 .01+01 1.79+01 0.bO *00 1.70*01 b.iti-nl 3.52*00 1.77+01 t! *00*00 1.69*01 b. 00-01 3.4`>*00 1.75+01 o.70+00 i,G7*r*i b.01-ftl 3.47*00 1.73*01 6.00*00 O.90+U0 1.65+01 1.64*01 4.95-01 t.Urt-oi 3.44+00 3,41+00 1.72*01 1.70*01 7.00100 1.62*01 *1.02-01 3.39*00 1.66101 7.10*00 1.60*01 `1.76-111 3.36*011 1.66+01 7 .'20*00 l,ti`J*0l 1.70-01 3.34+00 1,64+01 7'50*00 1. !>/*(! 4.64-01 3.31*00 1.63+01 7.00*00 1.SO 01 l.bO-Ol 3.29+00 1 .61*01 7.SO*00 1 . U'l * (* 1 4 b2-o 1 3.26*00 1,69+01 7'oi *00 1 . l>2* fi 1 1.46-01 3.23*00 1.67+01 7.70*00 1 ,50+01 4.40-01 3.21+011 1.56+01 7.00*00 1,49 + |l 4.3b-01 3. lltt 00 1.64*01 7.`Ju Mill It,00*00 1.0 / ti l 1 .`16*01 4.29-1:1 4.23-01 3. ll.i l 0 3, 13 MlO 1.1-2*01 l .61 + 01 it. 10 *00 l, 4 *1 * 0 1 4.10-.U 5.1H0U 1.49*01 .1.20*00 1.05*01 4.12-ill 5.00+60 1 ill.*01 0.50*011 l .11 Mil 4.07-01 3.06+00 1,46*01 Jt.`10 tou l .10tfl 4.02-nl 3.(13 tdU 1,44*01 .00 .00 .00 .00 .00 .00 .00 .00 .00 .QU .00 .00 .00 .00 .00 .00 .00 ,00 .00 .00 .00 .00 .00 ,0U .40 .00 . 11" ,00 .00 .00 .oil .00 .110 3,60+00 3.50+00 3,56+00 3,54+00 3.53+00 3,51+00 3.49+00 3.47+00 3,45+00 3.43+00 3,42+00 3.40+00 3,30+00 3,36+00 3.34+00 3,32+00 3.30+00 3,20+00 5.26+00 5.24+00 3,22+00 3.20+00 3.10+00 3.16+00 3.14+00 3.12+00 5.10 + 0(1 3,06*00 3.05*00 3,03+00 3.01+00 2.99+On 2,97+04 2 25-01 2 27-01 2 30-01 2 32-01 2 34-01 2 36-01 2 30-01 2 39-01 2 41-01 2 43-01 2 45-01 2 47-01 2 40-01 2 5U-01 2 52-01 2 53-01 2 65-01 2 57-01 2 50-01 2 60-01 2 61-01 2 63-01 2 64-01 2 66-01 2 67-01 2 60-01 2 *>9-01 2 71-01 2 72-01 2 73-01 2 76-01 2 76-01 2 77-01 1.19+02 1,21+02 1.23+02 1.26+02 1,27+02 1.29+02 1.31*02 1.33+02 1,34+02 1.36+02 1,30+02 1 .40 + 02 1 .42+02 1.43+02 1.45*02 1,47+02 1 .49 + 02 1.60+02 1.62+02 1.53+02 1,56+02 1,67+02 1.60+02 1.60+02 1.61+02 1.63+U2 1.64+02 1,1.6*02 1 .67+1*2 V.69 + 02 1.70+1*2 1.72+02 1 .73 + 02 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1,26+01 1,26+01 1.26+01 1,26+01 1.26+01 1.26+01 1.26+01 1.26+01 1.26+01 1,26+01 1,26+01 1,26+01 1.26*01 1.26+01 1.26+01 1.26*01 1.26+01 1 .26 + 01 1.26+01 1.26+01 1.24+01 1.24+01 1 .26+01 l.26+01 1.26+01 1.26+01 1,26+01 ucc 026710 llL HlN ItlTACUiM isiitSSU|{j' I'SIA l<| ACT fill TEMP UFGMEE r (Mint JAlKFT Tt nr DLGM f f |.f ACIUh lit Al t Crtl LM VU) GAS ttn IN |<t Atyuti tnnocE vtn lid* ItFT IN RLACTOK LIWOLE ||20 LIU. LLF* IN fiLAWUtt LiinoLt |(t ACTOI+ Vtn i iq. VOLUME tu FT KEACTOK ||2U lIQ, VU^UME CU FI 0.50*00 0.60+00 0.70*00 0.00*00 0.90 + 1)0 4.00*00 4.10*00 9.20*00 9.00*00 4.90*00 9.50+00 9.00*00 9.70*00 9.00*00 9.90*00 1.00*01 0.21*01 O.lU+ftl 0.19*01 A. 11*1)1 o.ootol a.09*oi A.01*1)1 7.90*01 7.9 b till 7.92*01 7.00*01 7.05+0I 7.02*01 7.00*01 7.77*01 7.79*01 1.02*1)2 1,02*02 1.01*02 1.01*02 l.oi m2 1.01*02 1.00*02 1.00*02 9.90*01 9.96*01 9.92*01 9.90*01 9.07*01 9.09*01 9.02*Q1 9.79*01 9,1)0*01 9.00*01 9.00*01 9.00*01 9.60*01 9.00*01 9.00*01 9.00*01 9.00*01 9,00*01 9.00*01 9,00*01 9,00*01 9.00*01 9.00*01 9,00*01 -2,59*06 -2.26*06 -2.37106 -2.30*06 -2,39*06 -2.90*06 -2.92*06 -2.93*06 -2.99406 -2,96*06 -2.96+06 -2,1)7 + 06 -2.99+06 -2.60+06 -2.61+06 -2.52+06 1.99*01) 1.99*00 1.99*00 1.99*00 2.00*00 2.00*00 2.00*00 2.00*00 2.00*00 2.00*00 2.01*00 2.01*00 2.01*00 2,01*00 2.01*00 2.01*00 2,96*02 2.95*02 2.99*02 2.92+02 2,91+02 2,90+02 2,06+02 2.67+02 2,06+02 2.09*02 2.63*02 2.62+02 2,61+02 2.79+02 2.76*02 2.77+02 2.91*05 2*91+03 2*91+03 2.91+05 2.90+03 2.90+03 2*90+03 2*90+03 2*90+03 2.90+03 2.90+U5 2*90+05 2*90+05 2.90+03 2*90+03 2.90+03 3.91+02 3,39+02 3,30+02 3.36*02 3,39*02 3.33+02 3.31+02 3.29*02 6,20+02 3,26+02 3.25+02 3.23+02 i.21+02 3.20+02 3.10*02 3.17 *02 6.96*02 6,96*02 6.96*02 6.96+02 6.96+02 6,96*02 6,95+02 6,95+02 6.95*02 6,95+02 6.95+02 6.96*02 6.96+02 6.96*02 b.96+02 6.95+02 ucc 026711 i 11 HI HiN porflash 6 AS FLOW WLI /lllr I'l-t FLASH U(H LIU. FI U fU U /MIN 1*1111 LASH 1120 1 1U. Fl OH HOl.| /fill* 1 l ASillU FLASH! 0 FLASH!H las vrn LIU. 1120 LIU. ILOi. FLOU FLOU hOLi/MN HUL1/H1N HOLF/MIH TUI AL TOTAL IUTA1 l`W(- 'UC GAS UCH LIU. (U10MU1LU EMISSION CHISSION LltMOLt 1-liNOl f. LtJHOLL U.90+00 U.60+00 6.7U+00 b.uo+OO 3.9U+93 9.00*1)0 9.10*00 9.20+QO 9;io+oo 9.90*00 9.90+00 9.00*00 9.70+00 9.00*00 9 .*90 *00 l.OO+Ol 1 . 3fi*|,l WlllBl |,35 + ftl 1.itlM 1.32+fl 1.3i*nl l.29*m 1.2Hml 1.2/till 1.29*01 1.29*01 1.22t|l 1.21 *ltl 1.20(111 1.10*01 1.17 * 01 3.96-01 3.91-01 3.66-01 3.01-01 3.76-fl 3,70-01 3.1.6-al 3.61-01 3.96-(I 1 3.01-01 3,96-01 3.91-01 3.37-01 3.32-01 3.27-01 3.23-pl 3.00*00 2,90*00 2,99*00 2.93*00 2,90*0(1 2.00*00 2.09*00 2.02*00 2,00(00 2,77*01* 2.79*00 2.72*00 2.70*00 2.67*00 2,69*00 2, u2* ft 0 1 .<*3*01 1.91+01 1.90*01 1.30*01 1,36*01 1.39*01 1.33*01 1,32*01 1.30*01 1.29*01 1.27*01 l.26*01 1,29*01 1.23*01 1.22*01 1.20*01 ,00 ,00 .00 .00 .00 ,00 .00 .00 ,ou .00 ,ou .00 - .00 .00 .00 2.92-03 2,99*0(1 2.93*00 2,91*00 2.00*00 2.U6*0(i 2,09*00 2.62*00 2,00*00 2.77*00 2,79*00 2,73*00 2,71*00 2,66*00 2,66*00 2.69*00 2.62*00 2.70-01 2.79-01 2*00-01 2*02-01 2*03-01 2*09-01 2*09-01 2*06-01 2*67-01 2*00-01 2*09-01 2.90-01 2.91-01 2*92-01 2*93-01 2*99-01 1.79*02 1.76*02 1,77*02 1.79*02 1.6(1*02 1 .02+02 1.63*02 1.09+02 t.69+02 1.07+02 1.06*02 1,09*02 1.91+02 1.92*02 1.93+02 1.99*02 1.26*0| 1,26+01 1.26+01 1 .26+01 1 .26 + 61 1.26+01 1.20+01 1.26+01 1.26*61 1.26+01 1.26*01 1 .26*01 1.26+01 1.26+01 1.26+01 1.26+01 m in ucc 026712 t U1SCUAKGE FUUM A TVC HATCH REACTOR Case 5. Uiglt Reactor Rate - Zero Heat Reuoval tUAClUlt I'HLSSUKE M FlfE OF hlSCHAitOr = 214.79 PS|A. HI ACiOl( (Enp A1 TIM F DISCHARGE = ' 1 f ft ,50 1 PH| SSUKE UOUiifltlfAh OF VALVE = 64.70 PSIA UAlEC JACKET TEMp AT DISCiAHCf = 90,00 f HT AC fOK VOLUME = 2674,000 ( U F I HEAT OF KCACiION = 45516*000 UlU/LOHuLC LIQUID WCM INITIALLY If) REACTOR = 9?l.t0 LFMOLE LKl 1120 INI HALLY IN KCACIfllt = 4929,6 LflHOLE VAPIHt IN 111 ALLY IN lit At (Oil - 2,969' LlfiDLt JACKET COLF IIHf-S AHtA = 095.6 UTU/M-F UENSilY Of UAliH t( ONSfANT) = 3.4570 IDfOLf/CU FI INITIAL OLNSITY F VCH = ,79912 UlMILE/CU FT AFC A 0| DLL ILF VALVE. OkIFICF OpENIhG = SU F) OH if ICE FLOW COEFFICIENT = .ftlU niNlnUn Lloillll tMTHAlNrttNI s *0100 CU FI L1IJ/CU FI GAS minimum watch jacket temp = 40.00 f LJQ VOL UHEN rtlN EnTHAiIWFHT IS MEaCMEo = 2430.0 CU FT TlpE hill JACKET tenp is heacueu = 5,00 MIN ItlAIING JACKET FAC I OH ? .QO KtACTlOh HA1E FAClOH = 1.3(1 Time MIN HEACTON PHESSLIIU PS1A Hf AC Kilt if Hr Ut'GRFE F WATCH JACKFT TEMP OEGitEF F HEAC(06 MEAT LENIENT I)1J GAS LCFl IN rlaltdr lmmole VCM tlQ. left IN HE AC roii LHHOLL ||20 EIO* eefi in HEaLTOII uiole ItLACIOH vln ein* volume Lli f| RE ACJ oh H2U LlQ. volume cu ft 0 011 .00 2.15+02 1,60+02 9,00+01 9,66+05 2.99+Ofl 9,21+02 4*93+03 1.15+03 1.43+03 * 1.00-01 2.Ift+fl2 1,69+02 0,92+01 9.09+05 3,40iQo 9.14+0? 4*90+03 1.14+03 1,42+03 2.00-01 2.16+02 1.69+02 0,03+bl 1.01+06 3.90+Q(| 9.06+02 4*07+03 1.13+03 1 .41+03 3*00-01 2,17+02 1.69+02 0,75+01 1.03+06 4,46+flo 0.90+02 4*04+03 1.13+03 1.40+03 4.00-01 2,17*02 1.69*02 A.66 + 01 1.04+06 4.91+00 8.90+02 4*02+03 1.12+03 1.39+03 b.00-01 2*16+02 1,69+02 0.50+01 1.05+06 5.33+00 8,02 + 02 4*79+03 1.11+03 1,39+03 0.00-01 2, 10+02 1.70+02 0,50+01 1,05+06 5.70+00 8,71+02 4*77+03 1.10+03 1.30+03 7.00-01 2.10+02 1.69+02 8,41+01 1,05+06 6.00+00 0.65+02 4*76+03 1.00+03 1.30+03 6*00-01 2.17+02 1.69+02 A.33+01 1,02+06 6.19+00 8,55+02 4.74+03 1,07+03 1,37+03 9.00-01 2.1b+n2 1.69+02 8.24*01 9,60+05 6.23+00 8,45+02 4.74+03 1.06+03 1.37+03 1 .'Ob tUO 2.13 + 02 1.60+02 O.lf +01 9.15+05 6.26+0(1 0,34+02 4* 74 + 03 1.04+03 1,37+03 1 '10 + 00 2.11 +02 1.67+02 0.00+01 ft.62+05 6,20 + 0(1 0.23+02 4*74+03 1.03+03 1.37*03 1 '20 + 00 2,09 + 1:2 1.67+0? 7.99+01 * ,09+05 6,31+00 8.13*02 4*74+03 1.01+03 1.37+03 1.30+00 2.07+02 1.66+02 7.91+01 7.56*05 6* 33*00 0.02+02 4*74+03 1.00+03 1.37*03 1.40+00 2,05+02 1.65+02 7.0?+01 7.02+05 6.35+00 7.92+02 4*73+03 9.07+02 1.37+03 1.50+00 2.03+02 1,65+02 7.74+01 6,49+05 6,30+00 7.02*02 4*73+03 9.74+02 1.37+03 1.60+00 2.01+02 1,64+02 7.66+01 5.96+05 6*40+00 7.72+02 4*73+03 9.60+02 1,37+03 1.70+00 1,99*02 1.63+02 7.57+01 5,42+05 6,42+00 7.62+02 4.73+03 9.47+02 1,37+03 l.oo+oo 1.97 + ('2 1.63+02 7.49+01 4.09*05 6,44+00 7.52+0? 4.73 + 03 9.34+02 1.37+03 ucc 026713 co*moi AVION nut M|N natLASl bAS FLO* nou/Hfr IVEFLASII Wert lm*. FlOU miu /Miri l*Hl-l LASH ti2t) tio. F| IIM HUL| /MIN 1 l /.MlllJ bAS FLOW mi e/hin 1LASuLU VC" lIU, FLOW FI Asiltl) It2 LIII. FLOW hole/min 101 Al l`yb (`HolHlFLll L|jMOLL TOTAi VC" GAS EMISSION i-imniE IU1AL VCM LIU. EMISSION LllhOLE s00 1. 00-01 2.00-01 i]00-01 9.00-01 5.00-01 b'tiO-Ql 7'll0-01 it. 00-ill y'oo-dl 1 '00*0*1 1.lu100 1.20*00 1.40*00 1. 00 *00 | 'bt'i *Oii 1 ,bO*0U I .70*00 1 '(10*00 7.65-01 4.02*00 7.99*0*1 1.21*01 1.02*01 2.69*01 4 . 69 * 0 1 5.95*01 0.60*01 1.01*02 1.00*02 <1.99+01 y. o*i*r.i y. 7`j+oi 9.65*01 9.56*01 'l.H* *111 t. 47* M 9.2 710 1 G,24*01 6,03*01 b.HlOl 5.5?tfll 5.15*01 11,66*01 3.09*01 2.95*01 1.31*01 2.95*00 2.91*00 2.07*00 2.03*00 2.79*00 2.75*00 2.71*00 2.67*00 2.64*00 2.59*00 2.90*02 2.90*02 2.GO* U2 2.67*02 2.50*02 2.27*02 1.90*02 1.95*02 6,90*01 1.90*01 1.90*01 1.90*01 1.90*01 1.90*01 1.90*01 1.97*1.1 1.97*01 1.97**11 1 . 17 t !i 1 5.03*01 6.00*01 6.22*01 6.95*01 6.09*01 7.29*01 0.03*01 0.09*01 1.09*02 1.10*02 1 .09*02 1.07*02 1.66*02 1.05*02 1.09*02 1.03*02 1.02*02 1,01*02 1 ..10*02 5.20*00 9.64*0(1 3.09*01) 2.91*00 1.02*00 9,54-01 .00 .00 .00 .00 *00 .00 .00 .00 .00 .00 .00 .00 . t)0 2.90*02 2.09*0? 2.79*0? 2.66*02 2.99*02 2.26*02 1.06*02 1.90*02 5.95*01 9.97+OU 9.54*00 9.60*00 9.66*00 9.72*00 9.70*00 9.9 ton 9.09*00 J.yb*flfl 1.00*01 .00 6.90-01 1,90*00 2. 10*00 2.00*00 3.50*00 9.20*00 9,09*00 5.57*00 6* 23* OU 6.06*00 7*97*00 Q.06*0U 0.63*00 9*10*00 y.70*00 1.02*01 1.07*01 1.12*0* .00 5,95+00 1.20+01 1.03*01 2.90*01 3.10*01 4.91*01 9.69+01 5.50*01 6.59*01 7.60*01 0.60+01 9.59+01 1.06*02 1.15*02 1.25*02 1.35*02 1.99*02 1.53*U2 .00 5,07-01 9,32-0* 1.27*00 1.51+00 1.64*00 1.64+00 1 .64 + 00 1.64*00 1.64+flO 1.64*U0 1.64*00 1,64*00 1.64*00 1.64*00 1.64*00 1.64 + 00 1.64 + (to 1.64+00 ucc 026714 I coopohmion 1 iHL hiN (tl AC (OH i'ufssimr psia Kl ACT01* irMp uruncr r WAlLIt JAf Kf T Tl ni* Ul Ui ff f FF ALll'It ML Al lltllLM ItlU CAS LIU lh llt-AijUX MlftOCL vcn tie. LtFl IN HI AC IOil LftMOLC 1(20 LIU. LEF* IN hiA^ruH LIjnoLL HEACIOH v*-ri i |q. itlLOMl EU M HLAL I Olt HUH I.IQ VOLUME CU FI T.90+00 2.00+UU 2.10+00 2.2U+00 2.40*00 2.90+00 2.00*00 2.60+00 2.70+00 2.00+U0 2.90+00 i.Ou+OO 3. 10 + 00 1 .'20+00 .1.40+00 4.90+00 4 >0 + 00 4.00+00 4.70+00 4'00+00 J '90 + 00 H. OlM'ilO H 'tO + OO 4.20+00 4.30*00 4.40*00 H *00 + 00 <1.00*00 1 .'70 + 00 *(.00 + 00 4 .90*00 u.ou+uu 5.10+00 i.ys+oa 1,93+02 1,91+02 1.90+02 1,9Q + ri2 l.'U.+fl? 1.44+02 1.02+02 1.00+02 1.70+02 1.77+02 1.70+02 1.73+02 1.71+02 1.70 + o2 i.r.o+o2 1.66+02 1.09+02 l.c.4*02 1 .ol + p2 1.00+02 1.90(02 1. ti/*(i2 1 .Lit + ()2 1.94+02 1.92*02 1.91 tr.2 1.4 9 + 02 1,44*02 1 ,`l6+o2 l,4n*02 1.44+02 1.42+02 1.62+02 1.61*1)2 1.61+02 1,60*02 1.59+02 1,59+02 1.50*02 1.57+02 1.56*02 1,56+02 1,55+02 1,54 + r<2 1.54*02 1,53*02 1.5?+u2 1.52+02 1.51+02 1.50+02 1,50+02 1.49*02 1.40*02 1.47+02 1,47+2 1.46 + 02 1.49*02 1.49*02 1.44+0? 1,44*02 1.43*02 1.42*02 1.41*02 1.41+02 1.40+02 7.40 + 01 7,32+01 7.24+01 7.15+01 7.07+01 6.90+01 6,90+01 6.1)2 + 01 6,73+01 6,69+01 6,56*0) 6,40+01 6.40+01 6,31+01 6,23+01 6,14+01 6,06(01 5.90+01 5,09+01 5,01+01 5.72+01 5.04 + 11) 5,56+01 5.47(1/1 5,39+01 5.30+01 9,22+01 5.14*01 9.09*01 4.97+01 4,00 + 0) 4.0fi(0l 4,00+01 4.45+05 4.02+05 4.20+05 2,75+05 2,22+05 1,69*05 1.17+05 6.40+04 1,16+04 >4.05+04 >4,24+04 -1,44+05 -1.95+05 -2.46+05 -2.97+05 -+.40*05 >4.90+05 >4.40+05 -4.97+05 -5.46+05 -5.95+05 -(..44 + 05 -6.92+05 -7.40+05 -7.07*05 -tl. 44 + 05 - * . 01 * 05 -9.27+05 -9./4i05 > | ,02 + 06 -1,66+06 >1.11+06 -1,15+06 6.4 7 *0(1 6*49+00 6.51*00 6.53+0|) 6,59+00 6.57+Qo 6.59+Qo 6.61+00 6.63+Oq 6,69+00 6.67 + 0(1 6,60 +(Jo 6.70+On 6.72 + 0(1 6.74(00 6,75*00 6.77+Oq 6.79*Oo 6.00+60 6.02+00 6.03+00 6.05+0(1 6,46 + 0(| 64O0 0 6.09*00 6.91 + 0(1 6,(2(110 6.-|3tOo 6,95+00 6.,96* 0(1 6.97*00 6.99+0(1 7.00+00 7.42+02 7.43+02 7.23+02 7.14+02 7.04*02 6.95+02 6,06+02 6,77+02 6.60+02 6,60+02 6,51+02 6,42+02 6.34*02 6.26+02 6.17*02 6,09+02 6.01*02 5,93+02 5,05+02 5.70+02 5.70+02 5.62+0? 5,55+0? 9,47*02 5.40+0? 5.43+02 5,26+02 5.19+02 5,12*0? 5,05*02 4.90+02 4.91+0? 4.04*0? 4*72+03 4*72+03 4*72+03 4*72+03 4.72+03 4.72*03 4*71+03 4*71+03 4*71+03 4*71+03 4*71+03 4*71+03 4*71+03 4*70+03 4*70+03 4.70+04 4*70*03 4*70+03 4*70+03 4*69+03 4*69+04 4*69+04 4*69+04 4*69+04 4*69+04 4*69+04 4*60+04 4.60MJ4 4*60+04 4*60+04 4.60*04 4*60+04 4*67+04 9.21+02 9,00+02 0.96+02 0.04+02 0.71+02 0.59*02 0.47+02 0,45+02 0.24+02 0.12+02 0.01+02 7.90+02 7.79+02 7.60*02 7.57+02 7.46+02 7.46+02 7.25+02 7.15+02 7.05*02 6.95+02 6.05+02 6.75*02 6.66 * 02 6,56+02 6.47+02 6.40*0? 6.29*02 6.20+02 6.11*02 6.02+02 5.94+02 5.05+02 1.47+04 1.47+04 1.37+03 1.37+ni 1.36+04 1,36*03 1.36+03 1.36+03 1.46*04 1.46*04 1.36*03 1.36*03 1.36+03 1.46*03 1.36*04 1.46*04 1.46+03 1.46*03 1,46+04 1,36+03 1.36*03 1,36*04 1.36+03 1 ,46*03 1.46+04 1.46+04 1.35+04 1.35+04 1.45+04 1.45+04 1,35+04 1,45+03 1,35+03 SU9Z0 oon llM) (1|N TltLILASl1 l.AJi Ft.UU HilLL/NIl- ri m ash vcm i. in. IK>VJ Hill f/MIII 1`KCl)./ $11 1120 110, F| mi MOI-E/HU. ^ LAS.Ill* (.AS fL3L MILL/MIN flashed WC Liu, flow mull/MIN n ashed 1120 L10. F| OU MOLt/MIU lOlAL Tvl (IIOUHCLU L|)M)l.t 7(If AL I/CM 6A6 EMISSION Limoi t. iotal OCH LI4*. EMISSION Lmmole 1 .90*00 2*00*1)0 2.10*00 2.20+UU 2. 30*00 '<1U * 41 It 2.50*OU 2.60*00 2'70+UU 2'ill* 400 2'90*oo 3'uotou .1.10*00 i.2uh*o 3.30*0*1 3.4tl*0U 3.50*66 1.1.414(111 3.70*00 3.00*00 i.`>0 4 00 4.0o*UU 4.10*06 '(.20 400 *| . 3l) (1(11 *1.1(0 11(0 I 'till 41(1) `(.(OHIO 4. /OHIO *4 .Oll + UO *1 .`>0 4 00 01| IK 0 `t.1040(1 0.10401 `>.00*1)4 n.`>`J40i A.09*04 n.ootni 0.7)4(14 o.ltl 41(1 t . ;;* 4 it 4 0. *14401 0,34 till 0.25+1' 1 o.iutni *1.07 401 7.99*1,1 7.`X* *0 4 7.01101 7.7 i* III 7.64*01 7 , ill.( III 7.0 010 l 7.00*nl 7.1?4()1 /.24*(i l 7,10 4(1 1 /. 00 4 lit ( .00 4,1 It . 93 4 (1 1 6. Oi* 4 (. 1 6.7o*ri 6, /l t01 6.63tf|l t.. ill.11 1 ... *l`l 4(1 1 2,56*00 2. *42400 2.10400 2.41*00 2,10400 2,17400 2,11401) 2,29400 2.26*00 2.22400 2.19400 2,lb4 OO 2.12400 2,00il,0 2.05400 2,01400 4.90400 1.90400 1.91400 1.0(1 too 1.05400 1.02*00 1.79*1,0 1,76*00 1,71*00 I , 7 |i i |)<i 1.67(00 1,6*| *00 1.61400 1 .bO| (111 1 .55*00 1.b260 1.1)0 100 1.46101 1.464U1 1.46401 1.45*01 1,45*01 1,15401 1.44*01 1.44*01 1.44 *01 1.4-1*01 t ,41*61 1.1241)1 1.42(01 l .41 41*1 1.41*01 1.41401 1.40*01 1.40*01 1.19*il| 1.19401 1,-10401 1.10*01 1.17*61 1.17*01 1. It, 41(1 1,14. * 0 1 1.15*01 1.15*01 l ,14 16 1 1.11(01 1.11*01 1.12*01 1.12*01 9,09*01 >, 70*01 9.60*01 9,57*01 9,47*01 9.16*01 9.26U1 9,16*01 9.05*01 0,95*01 0.65*01 0.75401 it. 654 01 it, 56* U l 0.46401 I., 16* III 0.27401 0.16401 6.00401 7.99*01 7.90401 7.01*01 /.72+01 7.61401 7.55*01 7.46*01 7.10401 7.29*01 7.21*01 7.11*01 7.65*01 ...97 *01 6.19*01 ,00 .00 .00 ,00 *00 .00 ,ou ,06 .00 .00 .00 .00 .00 .0(1 .00 .00 .00 .00 .00 .00 .00 .00 ,1)0 .00 .00 .110 ,00 .00 .00 *00 .nil *i|U .00 1,01*01 1.0)401 1.01401 1.02401 1.02+01 1,01*01 i.ai+oi l,01*01 1 ,1)4*01 1.04+01 1.04*01 1.05401 1.05401 i.n5*n 1.05401 1.06*01 1.06*01 1.06401 1,06*01 1.06401 1 ,06401 1,07401 1.07*01 1.07*01 1,67*01 1.07*01 1.07*01 1.07*01 1 ,07*0| 1,07*01 1,07*01 1.0/401 1,07*01 1.16401 1*20401 1.25401 1*29401 1*32401 1.36401 1*40401 1.43*01 1.46401 1*50401 1.53*01 1.55*01 1.50401 1.61*01 1*63401 1.66*01 1.60*61 1.71*61 1.73*01 1.75*01 1.77+01 1.79*01 1.01*01 1.03*01 1.04*01 1 .06*01 1.00*01 1.09*01 1.91*01 1*92*61 1.93*01 1 .95*01 1.96*01 1,63*62 1.72*02 1.01*02 1.90*62 1.99*02 2,00*62 2.16*02 2.25*02 2,33+02 2.42*02 2.50*02 2,50*62 2.66*62 2.74*62 2.02*02 2.90+U2 2.90*02 3,06*02 3,14*02 3,21*02 3.24+02 3.36+02 3.43*02 3.50*02 3.50+02 J, 65*02 3.72+02 3.79402 1.05+02 3.92+02 3.99*02 4.06*02 4.12+02 L.63*00 1.63+00 1,63+00 1.63+00 1.63+00 1.63+00 1.63+00 1.63400 1.63400 1, bit00 1.63400 1.63400 1.63400 1.63400 1.63400 1.63400 1.63*00 1.63400 1.63400 1.63+00 1.63+00 1,3*00 1.63*00 1.63*00 1.63+00 1,63 + 110 1.63+00 1.63*00 1.63*00 1.63+00 1.63*00 1.63*00 1.63*00 ucc 026716 CMMHMTHM ll Ml. MIN IlfACTOIt PHtSSUHr PS IA It* AC 10H If HP maun f HAUII JACKI T Tl HP iHf.UU | I f At 1OK ill. AT t Oil 1 ihi 11 J 6A S 1.6F1 IN NL ACT DJI LUMOLt WCM Ll* LIFT IN KLACTOIt LUMOLL ||?0 LIU. |Lf 1 IN lit A1-T UK LllMOLL H^ACIOK tf^M Liu* VOLUML Ml FT lUACTOll 1120 LIU, VULUhf tu FT 5'20*00 5.30+00 5.40*00 b'60*OU 5.t>0 + Q0 tj;/o*iio 5. 00*00 b.90*00 6 '00 *U0 6.111*00 .,.20*00 o.30*00 u.40 + 00 6.5)1*00 0.00*00 0 *70*00 o'uo*oo u ''JO *00 7.00*00 7.10*00 7.20*00 7.30*00 7.00*00 7.bO*00 7.00*00 7.70*00 7.00*00 /.`JO *00 0.Oft* 00 o.io*oo 0.20*00 (1.30*00 a. 00*00 l. <11*02 l.40*02 1.30*02 1.37*02 1,36+02 1.3b*2 1.34*02 1.3?+02 1.31*1-2 1.30*02 l.2y*o2 1,2*r2 1.27*02 l.20*r2 1.25+02 1.24*02 1.23*02 1.22*02 l,21*f2 1,20*f.2 1.19*02 1.10*02 l.17*02 1.10*02 1 15 + (i2 1.14*02 1.13*0? 1.13*02 1 *l?*f2 1.11*02 1.10*0? 1.IPMP2 1.07*02 1.40*02 1,39*02 1.30*02 1.30*02 1,37*02 1,36 + 0? 1.36*02 1,30*02 1.3b*02 1.34*02 1,33*02 1.33*02 1,32*02 1,32*02 1.31*02 1.30*02 1.30* 42 1,29+02 1.29*02 1,2fl * fl2 1.2A*Q2 1.27*02 1.27*02 1.26*02 1,20*1)2 1,2b*p2 1,2b*02 1.24*02 1.23*02 1.23*02 1,22*02 1,22*0? 1.2|*02 4.00*01 4,30*01 4.00*01 4,00*01 4.00*01 4,00*01 4.00*01 4.00*01 4.00*01 4,00*01 4.00*01 4.00*01 4,00*01 4.00*01 4,00*01 4.00*01 4.00*1)1 4,00*01 4.00*01 4.00*01 4.00*01 4,00*01 4.00*01 4,00*01 4,00*01 4.00*01 4.00*01 4.00*01 4 , liO + 01 4.00*01 4.00*01 4.00*01 4.00)01 >1.20*06 -1.24*06 >1.20*06 .1.33406 >1.37*06 >1,41*06 .1.40*06 .1,49*06 -1.63*06 -1,60*06 -1.62*06 -1,66*06 -1,69*06 -1.73*06 -1,77*06 >1.01*06 -1,0b*06 >1.09*06 -1,92*06 -1.96*06 -2.00*06 >2.03*06 -2.07*06 >2.10*06 -2.14*06 -2.17*06 21*06 -2.24*06 -2.20*06 T2,31*06 -2.34*06 > ->.37*0u .41*06 7.01*00 7.02*00 7.03*00 7.Ob*Qo 7,06*00 7.07*00 700+00 7,09+00 7.10+00 7.11+00 7.12 + QQ 7.13+On 7.14+00 7.Ib+fln 7,16+00 7*17+00 7.|0+00 7.19+00 7.20+Oq 7.21+Ofl 7.22+00 7.23*0(| 7.24+00 7.24+Oft 7 .,?b + 00 7.26 + 0(1 - 7.27 + 0,1 7.20*0(1 t7?3 + "fl 7v5i9ton 7. jO + Otl /, Utllf) 7.31+00 4,70*02 4.71*02 4.65*02 4.50*02 4,52*02 4,46*412 4,39*02 4,33*0? 4.27*02 4,21*02 4,15+02 4,10+02 4,04+0? 3,90+02 3.92*02 3.07*02 3,01+0? 3.76+0? 3.70+02 3.65+02 3.60+02 3.54+0? 3,49+02 3.44+02 3,39+0? 3,34*0? 3,29+02 3,24+02 3.19+02 3,14+0? 3,09+0? 3,05+0? 3,00+0? 4 .67*03 4 67+03 4 .67*03 4 .67+03 4 .67+03 4 .67+03 4 .66+03 4 .66+03 4 .66+03 4 .66+03 4 .66+03 4 .66+03 4 .66+03 4 .66+03 4 .65+03 4 65+03 4 .65+03 4 .65+03 4 .65+03 4 .65+03 4 .65+03 4 .65+03 4 .64+03 4 .64+03 4 *64+03 4 .64+03 4 .64*03 4 .64+03 4 64+03 4 .64+03 4 .63+03 4 .63+03 4 .63+03 5.76+u2 5.60*02 b,60 + 02 b.bl+02 5,43*02 5.35+U2 5.26*02 5,20+02 5.12*02 5.05+02 4,97+02 4.90*02 4.62+02 4.75+02 4.66+02 4.61+02 4.54*02 4.47*02 4.41+02 4,34*02 4,27+02 4,21+02 4,14*02 4.06+02 4,02*2 3.95+02 3.69+02 3.f 3 + 02 3.77*02 3.71*02 3.65*02 3.59*02 1.54*02 1.35+03 1.35+03 1,35+03 1.35+03 1,15+03 1,15+03 1,35+03 1.35+03 1.35*03 1.15+03 1.35*03 1.35+03 1.35+03 1,35*03 1,35*03 1.35+03 1,35* 03 1,35 + 63 1.34+03 1.34+03 1.34+03 1,34+03 1.34+03 1.34+03 1.34*03 1,34+03 1.34+03 1,34+03 1.34+03 1,34*03 1.34*03 1.34+03 4,34+03 ucc 026717 C4WHOU*IUM4 i im tt|0 I'M (I LAS|I 6AH IIOH HOLl/fU/l 1'liUTI-ASH wen lio, Ftuu HUM /njri I'llKlLAiili u2 i.io. Ft OU nOL| /Mil I l Ai>til L> H-AfcHM) ILASlltf) GA6 ven L|. H20 L10. I LOW FLOW FLOW f.G) L/Mli m**ll/hin moll/niu \ Tltl At. TO At (OfAL |*UL yen (iAS WCn LIU. |>IH)UlH:tU LftlSSION frniSSlON Liinm.L LIIMOU LUMOl.f 6.2u*uu 6.12*01 1.97*00 1.11*01 it, 01*01 6'30*l>0 6.16*01 1.99*00 1.11*01 6.79*01 i;*tu*ou 6.29*01 1.92+00 1.30*01 6.66*01 6.60*00 6.22*01 1.19*00 1.10*01 6.69*01 6. toll* Oil 6.16*01 1.17*00 1,29*01 6.61*01 6.70*0U 6.09*01 1.19*00 1.20*01 6,99*01 ti.iinttm 6.02*01 1.12+00 1.20*111 6.37*01 6.911 tilO 6.9n*fll 1.29*00 1.27*01 f,,A0*01 t., u to on 6.90 *|l 1 1.27*60 1.27*01 6,21*01 totou `i.Oltfll 1.26*00 1,26101 6,16*01 6.20*00 6.7/*0l 1.22+00 1.26*01 6.09*01 nI to.36|0U t.71*0l 1.20* 00 1.26101 6.01*01 L.HAmn `t. 66* II1 1.16*00 1.P91CI 9.96*01 b.biuno ri.69*0l 1.16+00 1.29*01 `i,90*01 1*. 6Q *110 :*.!>.!* Ill 1.11*00 1.21*01 6.01*01 it. TO *0(1 6.10*01 1,11 *00 1.21*01 6.77*01 it .00 *00 6.12*1)1 1.U9M10 1.22*01 6.71*01 to'JUMIO 6. 16* 111 1.07+00 1.21*01 6.69*01 7.011*00 6.31 M* 1 1. Ob+tlO 1.21 mi 6,60*01 7.10100 6.26*6 1 l.OllflO 1.20*01 6,62*01 /'Soioo 6.20 *(il 1.01+oO 1.20*01 6.96*01 /.Mil toll 6. lb* 1*1 9.00-01 1.19*01 6.90*61 /.<10*00 6.09*01 9.60.01 1 .1(1*01 6, Aft* 01 7.'union 7.00100 6.09 *(' 1 `1.99*1 1 9.99.1* 1 J. 111.). 1 1 . Ito*01 1.17*01 6.29*01 t, ;-.i* in 7.70*00 9,91 + 1*1 9.12-1*1 1.17*01 6.10+01 /.00*00 `1 . *19*|> 1 0.90-01 1.16*01 6.12*01 7.'JO t 00 0.'00too 9.09*1*1 9.79 If. 1 0.76-01 0.67-ill 1.16*01 1.16*01 6.07*01 i> .61*01 it, lot 00 9. 79 * 1* 1 0.90-111 1,19*0) 9.96*01 0.20 Hill 9.69+01 It. 2 A-ill 1 .19 Ml1 9.911Ul to.in*00 9,1.6 * ft 1 0.06-91 1. 1 A till 9,06+01 to.10*00 *i. *t(i + oi 7.09-01 1.12*01 `1 i* 1 + 01 .00 .00 .no .00 ,00 .00 .00 .00 .00 .00 .00.00 .00 .0(1 .00 .00 .00 .uo .00 .00 .00 .00 .00 ,00 . lilt .00 .00 .00 .1)0 .00 ,1)0 .00 .00 1.07+01 1.07+01 1.07+01 1.07+01 1.06+01 1,06+01 1.06+01 1.06+01 1,06*0| 1,06+01 1,06+01 1,06+m 1,0b*01 1,06+01 1.06+01 1,06+01 1.09 + 111 1.09+01 1.09+01 1.09*01 l,Ql0| 1,01*0) 1.03*01 1.01*01 1,02*0i 1 .l)2 + 0| 1.02 + 01 1,01+01 1.01+01 l .Ul Mil 1.00*11 + 1.00 +111 9,90100 1 97*01 1 90 + 01 1 99+01 2 01 + 01 2 02 + 01 2 01 + 01 2 09 + 01 2 06 + 01 2 06*01 2 flfa + 01 2 07+01 2 00 + 01 2 09 + 01 2 09*01 2 10*01 2 11*01 2 12*01 2 12*01 2 11 + 01 2 11 + 01 2 19+01 2 16 + 01 2 16 + 01 2 16*01 2 16*01 2 17 + 01 2 17 + 01 2 10 + 01 2 10 + 01 2 10*01 2 19+01 2 19 + 01 2 20* U1 9,19* u2 9,26*02 9.31*U2 9.30*02 9.99 +02 9.60+02 9.66+02 9.62+02 9.60*02 9.79*02 9.00*02 9.06*02 9.91*02 9.97*02 6.02*02 6,flfl* 02 6.13*02 6,19* U2 6.29*02 6.30*02 6.36*02 6.90*02 6.96*02 6.60*02 6.66*02 6.60*02 6.66*02 6.70*02 6.76*02 6.00*02 6.09*02 6.09+02 6.99*U2 1.61+00 1.64*00 1.61+00 A. 61*00 1.63+00 1.63+00 1.63+ 00 1.63*00 1.63*00 1.63*00 1.63*00 1.63*00 l.t>3*00 1.63+00 1 .63*00 1.63*00 1.63*00 1.63*00 1.63*00 1.63+00 1.63+flo 1.63*00 1.63+00 1.63*00 1 . *t3* 00 1.63* 00 1.63*00 1.63*00 1,63*00 1.63*09 1.63*00 1.63*00 1.63*00 ucc 026718 CORROMATION 1 |HL tun ill AC TOM MltCSSUHl MSI A H| AC lO|t IFHP U| GHCC r uAtlm JAC Kf T If HI* otGnrr F III AC 1 oil ML AT cm I EMI 619 GAS Ltd IN Iff-AC fUH mruji-C VCM LlO. I.LFT IN 111 ACTOK UIMGCF 1(20 (IN, Lf.Ft IN ItCACTOM LltnOLL Hj; AC I DM 1. IN* yoi.uHi. Ml FT UFACtoK H211 Litl. wunjMt: tu FI U.50+00 6.60<00 o;7o+oo u >0*00 M.90+00 y'uumu 9.10*00 9'20 *00 9.30*00 9.'dO*no 9'S0+U0 '1.00*00 9.70*00 9'00*00 9"90*00 1.00*01 l.00+02 1.07+02 1.06+02 1.06*02 l.9*fl? 1.0*1+02 1.01+0? 1.03*02 1.02*02 1,02+(i2 1.01+02 1,00*02 9,97*01 9.91+01 9.09+01 9.79+01 1 .21 + 02 1.21+02 1.20+02 1.20+02 1.19+02 1.19+02 1.10+02 1.10+02 1.17+02 1.17+02 1.16+02 1.16+02 1.16+02 1.15+02 1.15+02 1.11+02 1.00*01 1,00+01 1.00+01 1.00+01 1.00+01 1.00*01 1.50+01 1.00+01 i.un+oi 1.00+01 1.00+01 1.00+01 1.0A+G1 1.00+01 1.00+01 1.00*01 -2.11+06 -2.17+06 -2.50+06 -2,53+06 -2.56+06 -2.59+06 -262+06 -2,65+06 ^ +? # tb tOb -2,71+06 -2.71+06 -2,77+06 -2,00*06 -2.03+06 -2.05*06 -2.60+06 7.32.00 7.33+00 /.31+00 7.31 + 0j| 7.35+On 7.36+00 7.36+00 7.37+00 7.30+00 7.30+00 7. 39+ Ofl 7.39+Ofl 7*10 + 0(1 7*91+00 7*11+Ofl 7.12+00 2.95+02 2,91+02 2,06+02 2.02+02 2.77+02 2.75+02 2.69+02 2.61+02 2.60+02 2.56+02 2.52+02 2.17+02 2.13+02 2.39+02 2,35+02 2.31+02 9*63+03 9 *63+03 9*63+03 9*63+03 9*63+03 9 62 +(13 9 *62 + 03 9*62+03 9*62+03 9*62+03 9*62+03 9*62+03 9*62+03 9*62+03 9*61+03 9*61+03 3.90+02 3.92+02 3.37 + 02 3.31+02 3,26+02 3.21+02 3,15+02 3.10+02 3.05+02 3,00+02 2,95*02 2,90+02 2.65+02 2,60+02 2.75+02 2.70+02 1.39+03 1,39+03 1.39+03 1.39+03 1,31*03 1.31+03 1,31+03 1.31+03 1,31+03 1.31+03 1,39+03 1.31+03 1,31+03 1,39*03 1.33+03 1,33*03 ucc 026719 i ucc 026720 o In rut mu ria.i i a;,ii t.A-S I I Oh tiOKt /nin 1*1(1 1 LASH vi: liq. ll.OU rioM /him I*IU-| LASH M2 1 11). n uu rtULf/MIN 1 1 At,ill l, liAb 1 t-Oh r 0| i/MN FUAOtllll \tC Ll`1. fl-OU MULl/hlN n Asuf n 1120 1 |0. FLOW hou:/nih Till AL |*yt (liDUllltl) i amiLt HUAI l/C" tiAS truss ion Mtrinu: lTAL \k/cn uio. fMISSlOh ldholi: a.'titittio It. Ml Mill U./UtilO U.'OlimO It. 90* ><1* 9.00*00 J. IblOO vi.2otuo VI. 40*1)0 9.411*00 M.50+UU vi.oiimo >.7umo vi.aomo *>.`in mo 1 'llllllll * .55+01 4.51ml 4.46+01 4.42ml 1. 47 *M *1. 33ml `1.2*1*01 *i ,25 ml 4.211ml 4. 1 fit pi *1. 12*II1 4.00*01 4.04 mi H.nomi 4,9bmi j.wtm 7,71-ll 7.57-01 7.*11-01 7.25-01 7.10-111 6.94-ni (>, 7*1-01 0.00-01 n.oo-ni 6,36-0l 0.22-01 o.uo-ni 5,95-l 5.01-ci `i.6A-fll 5.55-nl 1.12*01 1,11*01 1.11*01 1,10*01 1.09*01 1.0`ltfll l.oilllil 1,00*01 1.07*01 1.001 01 i.or.mi 1. nr>*oi 1.04*01 1,04*01 1,0.1*01 1,03*01 4.75 +oi 4.70401 4,00*01 4.01*01 4.5b* 0| 4.01*01 4.40*01 4.42*01 4.37*01 4.33*01 4.20*01 4.24*01 4,1V) * 01 4 .lt>*01 4.11*01 4.00*01 .00 .00 .00 .00 .1)0 .no .00 .00 .00 .00 .00 .no .no .00 ,00 ,00 9.94*00 9,91*00 9.07*00 9.04*00 9.1*0*00 9.77*00 9.73*00 9.1.9*00 9.65*00 9.61*00 9.57*00 9.53*00 9.49*00 9,45*00 9.41*00 9. 17*00 2.20*01 2.20*01 2 * 21tOl ?.21*01 2.21*01 2.22*01 2.22*01 2.22*01 2.23*01 2.23*01 2*24*01 2.24*01 2.24*01 2*24*01 2.24*01 2.24 *01 5 .VIA* u2 6.03*02 6,07*02 6.12*02 6.16*02 6.21*02 6.25*02 6,29+02 6.33+02 6.40*02 6,42+02 6.46+02 6.50*02 6.54*02 6.50*02 6.62*02 1.64*00 1.64+00 1.63+00 1,63*00 1.64*00 1.64+00 1.64 + 00 1,64*00 1 .64*00 1.64*00 1.64*00 1.64+00 1.64+00 1.64+00 1.64+00 1.64+00 COWtHMIlOM MSCItAttUE WUM A 1*VC BATCH KFACTOR Case 6. High Reactor Rata - Cold Water in Jacket HI AC 1 OH PRISSHRC Af U** OF |iIECt*A| Gt = 214.74 PSIA HFACIUH IENP AT Tiff Of DISCHARGE = 1(6.50 F Kt AClOH VOuinC = 267i.00a CO FT liouiu vcn i.4)i i ah y in hi act oh = 421. to cuhocc VAPOR I til I f ACL.1 IN RtAcTDR = ?.( ?4 CRhOCI UNSiTY 01 WATCH IfOWSlAHIl = 1.4570 CPP6I I /CO FT ARC A OT RCCILF VACVC ORIFICE OPENING = .HAS SU F | minimum ciuum cnteainnefit = *oiuo cu it li/co ft gas CIO wOl whim MIN Et'THA]NHFNT IS RCaC|IC() = 2410.0 CO FT IlLAllNG JACKiT FACTOR = 1.00 PRESSURE HOWhSTRFrtM of VALVE = 64.7fl PSIA WATER JACHL1 IIMP AT lUSCAR6r = 00*00 F IICAT OF REACTION = 45516*000 UlU/CUMoEL CIO 1120 IMTIAECY IN HE AC I OH =. 492?.& UOUHL JACKIT COIF TINES AHLA s 045.6 BTU/M-F INI 11 AC 111 NS I nr of VCN = .70012 l flNOLE/CU FI ORIFICE FI OH COITFICICNT = .610 Mill IRON WAUr JACKET ltHP = 4**.00 F TIME UN JACKET TEW* IS REACHED = b,00 MIR REACTION RAIt: FACTOR = 1.50 um MlN REACTOR PRESSURE PS 1A Reactor TEMP DEGREE r WATER JACKET Tl Nil DEGREE E HfAC IUR lit A1 CDNIEN1 E1U GAS LCF1 IN RtAl TUN UihfR-L VCN CIO. ceft in RtACTOR CDF,UCC D2o cm* CCFI IN REACTUR cunocc RL ACT (lit VCN 110. yocnpt cu I T REACTOR ||2*l CIO. VOLUME CU El .ou l.Oil-Ill 2.00-01 A. 00-01 4.00-01 b'OO-Ul b.'OO-Ol 7.00-01 o'ao-ai y.00-01 l.uu+oo 1 .10*00 1.26+00 1.311 + 11H 1.40100 1.bo too 1.60*00 1.70*00 l .lietun 2.15+02 2.lb*f2 2.lb+f2 2. lb*C.2 2 lt+ 02 :.i6*n2 2.10+02 2.16+62 2. I4tf? 2.12 *|.2 2.10*02 2,00 + |2 2.0bt|>? ? . 01 + 02 2.01*02 1 ,y`j*o? 1 . `t 7 * 0 2 1 . *74*02 1.42* (.2 1 .GO102 1.GIH02 1.69+02 1,64+02 1.64*02 1.64+02 1.64*02 1.64* ,12 1.60*02 1.60*02 1.67*02 1.66*02 l .6!>*r2 1 *65+1)2 1 .64*02 1.61*ft2 1.62*02 1.62*02 1.6| *f>2 y.ooi01 0.42*01 0.01*01 0,7b*Cl 0.66*01 0.50*01 fl.50+01 0.41*01 0.11*01 0.24+01 0,16+01 0.00+01 7,44+01 7.4)*01 7.02+01 7.74*01 7.66*01 7.57 + 01 7.44*01 0.66+ Ob 4.62*05 0.47*05 1.01 + 06 1.01+06 1.02+06 1.01*06 0.42*Ob 4.56*Ob 6.47*05 0.17*05 7.77*05 7.16+05 6.56* Ob 5.45+05 5.15*06 4.74+05 4*14*05 i. 6*1 + 05 2.44100 1.4U*00 1.47*00 4.45*00 4.41*00 5.12*00 5.60+00 5.47*00 6. 16 + Ofl 6. 14*00 6.22+00 6.24*00 6.2 7 1 0(1 6*24+00 6.11*00 6,14*Oc 6. 16*00 6,110 + 00 6.40 + 0(1 4.21+02 4.14+02 4,06+02 0.40+02 0.41*02 0,02+02 0.74+02 0,65+02 0.56+02 0,45+02 0.14+02 0.24 *02 0.11*0? 0.01+0? 7.41+02 7. (Jl* ft? 7.71*02 7.64+0? 7.54+0? 4*41+01 4*40+01 4.07+01 4*04+01 4.02+01 4*74+01 4*77+01 4 * 76 + 0l 4.75+01 4.74+01 4*74*01 4*74+01 4.74+01 4*74+01 4.71 + 01 4.71+01 4*71+01 4.71+01 4.71*01 1.15+ui 1.14+01 1.13+01 1.12+01 l.11 + 01 1.10 + 01 1.04+01 1 .Ofl + Oj 1.07+01 1.06+01 1.04+01 1.01+01 1.01+01 1.00+01 6.07+02 6.71*02 4.60+02 6.47*02 4. *6*U2 1.45* 01 1.4ii + 01 1.4 1+01 1,40+01 1.14+01 1,34*01 1.30 + 01 1.10*01 1.17+03 1.37*03 1.17*01 1.17+01 1.37+03 1.17*01 1,37+01 1.37*01 1.37+03 1.17+03 1.17*03 ucc 026721 COMIHMIAflOM * 1 HI 11 iN i t AS|> bAS I t *iU m-M /Mf 1*1.1 f'LAStl tier* Mu. I:i0u hivt.l /Mil |>HE| l ASM HifO 1.1(1. F| 7)1* il | /Mil 1 | AMU 1* flashmi FI. ASHA 1) IAS vtn i iu. i2`> i io* 1 UH+ 1 low H.nu tot L/HH Ituu /MU MOL 1-/MU TOTAL 1*0*. |'00O(|Ltl LltMOLL TUTAI UC fiAS EMISSION t-ltmiLL 1UTAL ucn i i<t. emission LUftOU .00 l.lib-01 2.00-01 1. oo-o l 9.uo-ui s.oo-ul b.00-01 7.on-01 o'oo-oi 9. On-ul 1,0(1*00 1.10*00 1.2o***o 1.10*00 1 ,9b*UO l . fill * .*0 1 ,1.0*00 1.70**10 1.00*00 1 .7*5-01 1.0*1 * lib /. Sit ill! i.22*r*i 1 .til till .00*1*1 i.72+ri 5.51 till *1.71*01 9.99 Ml) 1. lilt *1*1 '>.70*0 l (.*.7*1*1 i.iiotni 9.95 + f.l i. V-Mj.l 9,?9 + <ll 1.11* III 9.051 7*1 0.21*1*1 0.01*1)1 5.00+01 ti.hltiil 5. lltol 9 .01*1)1 1,05+01 2,09*01 1.21*1)1 2.92*00 2.00*00 2.0(1*00 .>.110*1)0 2.75 + 00 2.71*00 2.07*00 2.01*00 2.59*00 2.55*710 2.90*02 2.09*02 2,79*12 2, Of.* 02 2.9***02 2.25*02 1.00*02 1.*12*02 7., 00 till 1.*17*01 1 .07*01 l.9b*01 1 .*11.* it) 1.9b*01 1,95+01 1 ,<l* *tl l, 9 5 + fl 1 l .99*01 l . 9 9 10 i f.01*01 5,99*01 0.21*01 I .97**11 t. til *U1 7,20*01 0.01*01 0.07*01 1, lib* 02 1.00* 02 1.07*02 1.00*02 1.09*1*2 1.01*02 1.02*02 1 ,t)l *rtc 9,91**01 *. *19 * 01 9. 72*01 S.20*0a *1 .b/*0f| 1,92*00 1,01*00 1 91* * 0 0 b.10-01 .00 .1)0 .00 .00 .00 .00 .00 .00 .1)0 .00 .00 .0*1 .00 2.90*02 2.09*02 2.79*02 2,1*5* 02 2.90*02 2,25*02 1.09*02 1.10*0? 5.90+01 9 .*((. +0(1 9.53*00 9.59+00 9.bb*0n 9.70*00 9,75*00 9.01*00 9.00*00 9.90* 0i| 9.95+00 00 b*97-01 1 .19*00 2.09+00 2*70*01) 1.97+00 9.15*00 9.01+00 5.99*00 b.11+00 b.79 + 00 7.11+00 7.09*00 (1.91*00 0*95*00 9.95*00 9.91*00 1 .09*01 1.00+01 .00 5.95+u0 1,20*01 1.02*01 2,90*ul 1.17+01 1.90*01 9 .bit* 01 5.57+01 fc.fo+oi 7.57+01 0.5b+01 9.51+01 1 .05 + 02 1,15 + 2 1.29*02 1.11*1*2 1 .92+02 1.52+02 .00 S. 09-01 9.90-01 1.29+011 1.59*00 1.7.7 + 00 1.60+00 1 .bU+OO 1 .fcU + 00 1 .7.0 + 00 1 .b*t +0(1 1.bO+00 1 .1.0 + 00 1 .bO + 00 1 .7.0 + 00 1 .bO+Oft 1 .b+Oft 1 .7.0+00 1.7,0 + 00 ucc 026722 11 Ml M|N |Vf Af 11*1* UKFSSUOI I'SlA Hf AC1Oh rrm* nu.ntt r WAltl. JACKf1 i( w l)LG|iLE 1 irACin6 lit. HI (-(III fill mu 6 AS UM IN lit AC jO|< UiMOLE yen lIQ* LEFT IN he ac rim LUrtOLE ||2U LIU* let* IN REA6TUH Liinoit H^ACIDli VLH LIU* VOLUME tu f T |(E AC f OK 1120 (.10, VOLUME CU FI 1.90+00 2.00 + 01) 2.10+00 2.2u + u0 2.40+00 2.40+00 2 '50tu0 2.60+OU 2'70*00 2 . Ul) tUO a.mo*oo 3.0(|t30 i.io+oo 4. 20too 4.40+00 4.40+00 3.50+00 3 '60+00 4.`7o+oo 3.00*00 3.90+00 4 , Oil tOU 4. IOMIO *4 '20*00 4.4iitou 1 .*4 0 Mill *4 .bO * OH *i .b(i * 00 *4.70*00 *4.410 toll *1 . 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Ft OU ilOLI /HII* UAOiU'U H-A6I0U FI Atiilt 1* c.hS vtn U'i. 1120 Lie. | LQE 1 LOW FLOW hFLc./MM HULL/MW HALF/MU* lot At- TIlfAl lOlAL I*y6 yc 6AS VC |. |U. |>M(lOucUi Fn15SiO(* FUlSSlOt* LIUIOLt - *-IW10|L LOMOt-l 0.50100 U.uUMMl a. 7itoo ll'OO + OO .tJ9uiOO >. 0u *00 i'lotoa *V2U 1 Uli y. 10 + 00 9.9U*tttl 9.50*00 >.60*00 y *'/o*oo y. no too y.yotoo l.00 toi 't.ofctrl t.o't *ii i.9*7*<>i 1.95*01 1.06+6 1 i.Oiitl*! 1.77*01 .1.71*01 -1.6*7*01 1. fait *01 1.61*01 i.hitri 1.51*01 1.0*71(11 1.95t(,l 7.56-01 7.411-01 7.27-01 7.12-01 6. *70-01 6,0*1-01 6.71-01 6,57-01 6,99-01 6,11-11 6, Ul-.ll 6.06-01 6. `71-01 5.01-01 5.69-01 6.57-01 0.97*00 0.09*00 9.0?*00 9,75*00 9,61**00 9.61*00 9.5*1*00 9.97*60 9.90*00 9,11*00 9,26*00 9,19*00 9. 12*00 9.05*00 0,90*00 0.91*00 9.25*01 9.20*01 9.15*01 9.10*01 9.05*01 9,01*01 1.96+01 1,91*01 1,07+01 1,92+01 1.10*01 1,71*01 1,69*01 1,65*01 1.61+01 1.5J> + 01 .00 .00 .00 ,ou .OU ,nu .OU .OU ,00 ,ou .00 *00 .00 .OU .00 .OU 9.07+00 9,02+00 a.97+00 o,yi+o 0.00*00 0, Jtl* 00 0,70*00 0.71+00 0,60+00 0.61*00 0.50*00 a.51+00 0,90+00 0.91+00 u.i7ton 0.12*00 2*06*01 2*06+01 2*07+01 2*07+01 2*07*01 2*00+01 2.00*01 2.00+01 2*00+01 2.09+01 2*09+01 2*09+01 2*09+01 2*10*01 2*10+01 ?. 10*01 6.*9*U2 5,71+02 5.77*02 5.01*02 5.05*02 5.09+02 5.91+02 5.97+02 6,01+02 6.09 + 112 6.00*02 6,12*02 6.15*02 6.19*02 6.22*02 6.2(,*U2 1.6U+U0 1.7,0* 00 1.60 + 00 1.60*00 1.60*00 1.60*00 1,60*00 1.60*00 1.60*00 1 .60* liu 1.60*00 1.60*00 1.60*00 1.60*00 1.60*00 1 .60*00 +J:liJ ucc 026728 i CMIHMIITKHI R1SCI1AKDE FROM A l'VC HATCH REACTOR Case 7. lligli Reactor Rate - Zero Heat Removal HIACtUII PRESSURE AT I IpE OF DISCHARGE = 219.79 PSIA PRESSURE DOWNSTREAM OF VALVE = 69*70 RSI A ttf ACfOK TErtP AT TIpE Of DISCHARGE = 160.60 F WAlER JACKET TEMP AT DISCHARGES ?0.00 F RfACtOR VOLUME = 2675.000 CU F I IIEaT OF REACTION = 96616*000 UIU/EOMQLE LIQUlO VCM INITIALLY IN RtAClOR = 921.60 LRMOLE tlU 1120 INITIALLY IN REAC>OR = 9929.6 EDMOEE VAtHtit 1NIIIAILY IN REAcfOH = 2.9699 LRHOLE DENSITY OF WATER (CONSTANT 1 s 5.9670 LRMCi f./CU FT JACKET COKE TIMES AKEA " 895.6 HTU/MIN E INITIAL DINSITY OF VCM = .7991*! EUMOEE/CU FT area or relief valve orifice opening = ,2776 so ft MINIMUM LIQUID ENTRAINMENT S .0100 CU FT Eio/cu FT GAS ORIFICE FLOW COEFFICIENT = .610 MINIMUM WATER JACREI ltMP'* 90.00 F LIU uOL WHEN min ENTRAINMENT IS REACHED = 2950.0 CU FI TIME MIN JACkFT TEMP IS REACHED = 6.00 MIN HEATING JACKET FACTOR s *00 REACTION RAfC FAC I DR = i.au TiML H|N REACTOR PRESSURE PSIA HfACTOR TEMP oesrce f WATER JACKET TEMP degree f REACTOR HEAT E0N1ENT DIU GAS CLFI IN RLACtOR LUMOEE VCM L)0. LEFT IN REACTOR LHMOLE ||20 110. EEFI IN HEaLTOK ERMOEE RLAC1DR Vj;M LIU. volume LU FT REACTOR H2U ElO. volume LU FI Uoo1 i .00 1'00-01 2'00-01 2.16+02 2.16+82 2.15*02 1.68*02 1.68*02 1.68*02 9,00*01 8.92*01 8.83*01 9.66+06 9,79+05 9.80+05 2.99*00 3,99*00 9,87+00 9,21402 9,07+02 0,92+02 8*93+03 9,87+03 9*02+03 1.15+03 1.13*03 1,12+03 1.05+03 1,01+03 1.39+03 i'00-01 2.19+02 1.68*02 8.75+01 9,59+06 5.66+00 0,76+02 9*77+03 1.10+03 1.38+03 9.00-01 2,12+02 1.68*02 8.66+01 8,96+05 6,19 + 00 0,59+02 9.79+03 1.07+03 1.37+03 6.00-01 2.07+02 1.66*02 8.68+01 7.66+06 6.22+00 0,30+02 9*79+03 1,05+03 1,37+03 6.00-01 2.02+02 1.69*02 8.60+01 6,57+05 6,26+00 0,10+02 8,79+03 1.02+03 1,37+03 7.00-01 1.90+02 1.63*02 8.91+01 5.09+05 6.31+00 7,99+02 9*73+03 9.93+02 1,37+03 8.00-01 1,93*02 1,61*02 8.33+01 3.83+05 6,35+00 7.00+02 9*73+03 9.67+02 1,37+03 9.00-01 1.09*02 1.60*02 8.20+01 2,59+05 6.39+Oc 7,61402 9*73+03 9.82+02 1,37+03 1 '00+00 1.86*02 1.68*02 8.16+01 1,38+05 6,95+00 7.93+02 9*72+03 9.10+02 1,37+03 1.10+00 1.81*02 1,57402 8.08+01 1,89+09 6.07+00 7,26402 9*72+03 0,95+02 1.37+03 1 .2u + 00 1.77*1 2 1,66*C2 7.99*01 -9.80409 6.51+00 7.09+02 9*72+03 0.72+02 1.36+0 3 1.50 + 00 1,75*02 1,69482 7.91*01 -2.13+05 6,65*00 6.92+02 9*71+03 0.60+02 1.36t03 1.90+00 1.69*02 1,52402 7.82+01 -3.25*05 6,50400 6.76+02 9*71+03 8.20+02 1.36403 1.60+00 1.65*02 1,51*02 7.79+01 -9.35*05 6.61+00 6,60+02 9*71+03 8.07*02 1.36+03 1.60+00 1,62*02 1.99*02 7,66*01 -5.93+05 6,69+00 6,99+0? 9*70+03 7,86+02 1.36+03 1.70100 1.69*02 1.90*82 7,67+01 -6.99+05 6.60400 6,29+02 8*70+03 7,67+02 1.36+03 1.80+00 1,66*(i2 1,96*02 7,99*01 -7,53+05 6,71400 6,19+02 8*70+03 7,87+02 1.36+03 t ucc 026729 cm f i nt H1N |`|>tFLASn 6AS ruw nOLf/MlN I*(<ULAS|| urn uq. FIOU nm/nirj t'Htl ASH 1120 MU. Finn MOLf/MIN f l ASIIl b rt-ASlttO FLASH* 0 r.AS vcn mu. H20 LIU. H-OU FLOW FLOW Ml E/HIN Hurt/nin HOLE/HIH 10IAL l*VL pMOUUCtO LUnOLt rurAL VC" OAS EMISSION huno* e lOJAt vcn MO, cnisstON LUHOLE ;oo 1.00-01 2.00-0* a.oo-oi 1.00-01 0.00-01 0.00-01 7 *00-01 0.00-01 J.00-01 t'ou+oo 1.10*00 1.20*00 i ,ao*uo 1^10*00 1,5otoo 1.00*00 1.70*00 1.00*00 i.satno 1.19 + oi 3,56* a1 7. li*ill 1.01*02 1,95+02 1 . MO * |i2 1.00*02 1.01*02 1.77*02 1.74*02 1.09*02 1.6t>*o2 1.01*02 l.57*02 1.0*1*02 ,50+n2 1,17+02 1.11+02 1,25*02 1.10*02 1,03*02 7.02*01 3.01*01 5.72*00 5.55+00 5,30*00 5,22+00 5.00+00 1.90+00 1.75+00 1.60+00 1,10+00 1.32*00 1.10*00 1.05*00 3.92*00 3,79+00 5,97*02 5,50+02 1.90*02 3,01*02 1,50*02 2.90*01 2.00*01 2.07*01 2.05t 01 2.03+01 2.01*01 2.79*01 2.77+01 2.71+01 2,72*01 2,70*01 2.00*01 2.00+01 2.03*01 1.17+02 1,21+02 1.35*02 1.50+02 2,02+02 2,11+02 2,00402 2.00+02 1.90*02 1.91+02 1.00+02 1,02*02 1.77*02 1.73+02 1,09+02 1.05+02 1.01+02 1.57*02 1.53+02 l.OI+Oi 0.11+00 1,55+00 ,00 00 ,00 .00 ,00 ,ou .00 00 .00 ,00 .00 ,00 .00 ,00 ,00 .00 5,96+02 5.57*02 1.97+02 3.73*02 1,10+02 1,90 *0| 1.92*01 1.91*01 1.96*01 1.97*01 1.99+01 2.00*01 2,01*01 2,02*01 2.03*01 2,01+01 2,01+01 2.05+01 2,05+01 *00 6.91-01 1.30*00 2*05+00 2*70+00 3*31*00 3*07+00 1*30+00 1*05*00 5*20+00 5*60+00 +,*05+00 6*30+00 6*69+00 6*90+00 7*21+00 7*10+00 7*71+00 7*91+00 ,00 1.21+U1 2.10+01 3.09+01 5.53+01 7.50+01 9.13+01 1.13+02 1.32+02 1.50 + 02' 1.67*02 1,01+02 2.01+02 2,10+02 2.31+02 2.19+02 2.65+02 2.79+02 2.91+02 .00 9,61-01 1.61+00 1.01*00 1.01*00 1.01+00 1.01+00 1,01+00 1.01+00 1.01+00 1,01+00 1.01+00 1.01+00 1.01+00 1,01+00 1,01 + 00 1.01*00 1.01 + 00 1.01+00 ucc 026730 TlHE H|N REACTOR PRESSURf PSIA HfACTOH TEHP UfGHEE r WATER JACKET T| HP DEGREE f (if AC 10ft HtAl CPNllNT P1U GAs LEFT IN (It ALT DR ttirtOLt VCM LlQ. (EFT IN REACTOR ERHOEE Il20 LIU, UH IN realtor ERfiOtt REACTOR Lib* VOLUPt !ru ft REALTOR 1120 LlO. VOLUHE LU FI 1.90+00 2.00+00 2;io+oo 2 20+00 2.40+00 2.40+00 2.>0 + 00 2'60*00 2 '70+00 2.00+00 2.90+00 4.00+00 4.10+00 4.20+00 4.40+00 4.40+00 4.50+00 4.60+00 4.70+00 4.'00 + 0Q 4.90*00 <1,00 + 00 4X10 + 00 4.20+00 4.40+00 *1 '40*00 tl.50 + 00 4.60 + 00 4.70+00 4.00+00 4.90+00 5.00+00 5.10+00 1,52+02 1.49+02 1.46*02 1.44+02 1.41+02 1.40*02 1.46+Q2 1,44+02 1.31+02 1.29+02 1.27+02 1.25+02 1.24+02 1.21+02 1.19*02 1.17+02 1.15+02 1.14+02 1.12+02 1.10+02 1.09*02 1.07*02 1,06+02 1.04+02 1,03+02 1.02*02 1,00+02 9,92+01 9.60+01 9,66+01 9.57+01 9,47*01 9.46+01 1,45+02 1.44+02 1,42+02 1.41*02 1,40+02 1,46+02 1.47+02 1.46+02 1,45+02 1,34+02 1.32+02 1.31+02 1,30+02 1,29*02 1,26+02 1.27+02 1,25+02 1.24+02 1.23+02 1.22+02 1.21+02 1.21+02 1.20+Q2 1,19+02 1,16+02 1,17+02 1.16+02 1,15+02 1.14+02 1.14+02 1.13+02 1,12+02 1.11+02 7.40+01 7.32+01 7,24*01 7.15+01 7.07+01 6.96+01 6,90+01 6,62+01 6,74+01 6,65+01 6.56+01 6,46+01 6,40+01 6,41*01 6.23*01 6.14+01 6.06+01 5.96+01 5.69+01 5.61+01 5.72+01 5.64+01 5,56+01 5.47+01 5.39*01 5,30+01 5.22+01 5.14+01 5.05+01 4.97+01 4,66+01 4,60+01 4.60+01 *6.54+05 *9,54+05 *1,05+06 *1.15+06 *1,24+06 *1,33+06 *1,42+06 *1.51+06 *1,59+06 *1.66+06 *1,76+06 *1.64+06 *1,92+06 *1.99+06 *2,07+06 *2.14+06 *2.22+06 *2,29+06 2.36+06 *2,42+06 *2,49+06 *<,55+06 .2,62+06 *2.60+06 *2.74+06 *2,60+06 *2.06+06 *2.92+06 -2,97*06 *3.03+06 *3,00+06 *3.13+06 -3,19+06 6.73+00 6.76+00 6,79+0q 6.01+00 6.64+00 6,06+00 6,09+00 6,91+Oq 6.93+00 6,95+00 6,97+00 6,99*00 7,01+00 7,03+00 7.05+00 7.06+00 7.06+00 7.10+Ofl 7. H + Oq 7.13+Ofl 7.14+00 7,16+00 7.17+00 7,19*00 7.26+00 7.21*00 7.22*00 7.24*00 7,25+00 7.26+00 7.27+60 7.26+00 7.29+00 6.00+0? 5,05+0? 5.72+02 5,56+02 5,45+02 5,32+02 5,19+02 5,07+02 4,95+02 4,63+02 4,71*02 4,60+02 4,49*02 4.36+02 4,27+02 4.17+02 4.07+0? 3.97+02 3.67+02 3,77+02 3,60+02 3,59*02 3,50+02 3.41*02 3,32+02 3.24+02 3.15*02 3,07+02 2.99+02 2.91*02 2,03+02 2.76*02 2,69*02 4 09+03 4 69+03 4 .69+03 4 .69+03 4 66+03 4 66+03 4 .60+03 4 .66+03 4 67+03 4 .67+03 4 .67+03 4 ,67+03 4 .66+03 4 66+03 4 66+03 4 .66+03 4 65+03 4 65+03 4 .65+03 4 ,65*03 4 .64+03 4 *04+03 4 64+03 4 .04+03 4 .03+03 4 ,03+03 4 .03+03 4 .03+03 4 03+03 4 .02+03 4 .02+03 4 .02+03 4 .62+03 7.26+2 7.10+02 6.92+02 6.74+02 6.67+02 6,40+02 6,24+02 6,0e+U2 5.93+02 5,76+02 5.63+02 5.49*02 5,35+02 5.21+02 5,06+02 4.96*02 4.62+02 4.69+02 4,57+02 *1,45+02 4,34+02 4,22+02 9,11*02 4,00*02 3,90+02 3,79+02 3.09+02 3,59+02 3.49+02 3.40+02 3,31+02 3.21+02 3.13*02 1.36*03 1,36+03 1,36*03 1,36+03 1,35+03 1,35+03 1,35+03 1.35+03 1,35+03 1,35+03 1,35*03 1,35+03 1,35+03 1.35+03 1.35+03 1,35+03 1.35+03 1,35+03 1,34+03 1,34*03 1,34+03 1,34 + 03 1,34+03 1,34+03 1,34+03 1.34+03 1,34+03 1,34+03 1,34+03 1.34*03 1,34+03 1,34+03 1,34*03 ucc 026731 CWIMW MWM nm min n+LFLAS|| GAS FLOU HOLf/nilt I'ltFFLASII Vf.H LIO. FLOU HQLi/niFl Pltff LASli 1120 LIO. F| OU HOLI/MIN f LAMltb FLASMtO FLASIILO GAS VCn MU. ||20 (.IQ* FLOU FlOM FLOU U/MN HUtf/rtIN MOLf/MIN lOlAL IQT/i 1UTAL PV*- VC" UAS UCM LIU, pitOt+UCLU ^MISSION FttlSSlOM Ll)MOLt MIMOI L MiMOLF 1.90 too a .'oo too 2.10*00 2.20*00 2'30t0O 2.10*00 2.50*00 2 >0100 2,/atao 2.00*00 2'911*00 3.00*00 A. 10*00 1.20*00 4.30*00 4.90*00 4.but00 4.00*00 4.70*00 4.00*00 4.90*00 9.00*00 9.'10 *00 9.20*00 9.40*00 9 *90*00 9.50*00 9.00*00 9.70*00 9 *00*00 9 *90*00 9.00*00 *1 *1 0 * 00 1.90*02 1.37*02 1.19*02 1.31*02 1.20*02 .1,20*02 1.23*02 1.20*02 1.10*02 I*l5tp2 1.13*02 1.11*02 1.00*02 1.06*02 1.09*02 1.02*02 9.97*01 9.77*01 9,57*0) 9.30*01 9.20*01 9,02*01 9,09*fll 0,07*1)1 0,50*0) 6.33*01 0.17*01 0.01*01 7,05*0) 1.70*01 7.55*01 7.9 l {. 1 7.2(>*(> 1 3.07*00 3,55+00 3,99*00 3.32*00 3,21*00 3.11*00 3.0j*oO 2.91*00 2,01*00 2.71*00 2.02*00 2.53*00 2.95*00 2.30*00 2,20*00 2.20*00 2.13*00 2.05*00 1.90*00 1.91*00 1.09*00 1.70*00 1.71*00 1.05*00 1,59*00 1.53*00 1.90*00 1.92*00 1,37*00 1.32*00 1.27*00 1.22* 00 1.17*00 2,01(01 2.59*01 2,57*01 2,59*01 2.52*01 2,50*01 2.97*01 2,95*01 2.93*0) 2,90*01 2.30*0) 2.30*01 2,33*01 2.31*01 2.29*01 2,20*01 2.29*01 2,22*01 2,19*01 2.17*01 2.15*01 2.12(01 2,10*01 2.00*01 2.05*01 2.03*01 2.01*01 1,90*01 1.90*01 1.99*01 1.91*01 1.09401 1.07*01 1.50*02 1.90*02 1,93*02 1,90*02 1,30*02 1.33*02 1.40*02 1,27*02 1,25*02 1.22*02 1.19*02 1,17*02 1.19*02 1.12*02 1.09*02 1,07*02 1.05*02 1 ,02*02 1.00*02 9.02*01 9.02*01 9.92+0I 9.24+01 9.09*01 0.05*01 0,07*01 0.50*01 6.43+01 0,10*01 7.99*01 7.63*01 7.07*01 7,52*01 .00 .00 ,00 ,00 .00 .00 ,00 ,00 *00 .00 ,00 .00 ,00 ,00 .00 .00 .00 .00 .00 .00 .00 .00 .00 .00 ,00 .00 ,00 ,00 *00 .00 *00 ,00 .00 2.05+01 2,05*01 2,0b*01 2,05+01 2,05*0i 2,09+01 2,09+01 2,03*01 2,03+01 2,02*01 2.Q1+Q1 2,01*01 2,00+01 l,99*0l 1.9A+01 1,97+01 1,9G + 01 1,95+01 1,94*01 1.92*01 1.91+01 1,90*01 1,00+01 1.07*01 1,05+01 1.09+01 1,03+01 1,01*01 1,79*01 1,70+01 1,70*01 1,75*01 1,73+01 0 11 + 00 0 20 + 00 0 95 + 00 6 60 + 00 0 79 + 00 a 07 + 00 A 99*00 9 11 + 00 9 21+00 9 31 + 00 9 90*00 9 99+00 9 57*00 9 65*00 9 71*00 9 70 + 00 9 09 + 00 9 90 + 00 9 95+00 1 00*01 1 01 + 01 1 01+01 1 01 + 01 1 02 + 01 1 02+01 1 02*01 1 04+01 1 04+01 1 04 + 01 1 09 + 01 1 09 + 01 1 09 + 01 1 09 + 01 4.00+02 4.22+02 3.36*02 3,99+02 3.62*02 3.75*02 3,60+02 9.00+02 9,12+02 9.29+02 9.35+02 9.96*02 9,57+02 9.60*02 9,79*02 9.69+02 9.99+02 5.09*02 6.19*02 5.20*02 5.36*02 5.97+02 5.56+02 5.65*02 5.73*02 5.62+02 5.90*02 5,90*02 6.06*02 6.19+02 6.22+02 6.29+02 6.36*02 1,61+00 1,01*00 1.01+00 1.01*00 1.01+00 1,01+00 1,01 + 00 1.01 + 00 1,01+00 1,61*00 1.01+00 1 ,01*00 1,01+00 1.01+00 1.01+00 1,01*00 1,01+00 1.01*00 1,01*00 1 .01*00 1 .01 + 00 1.61*00 1.01+00 1.01*00 1.01+00 1.01+00 1,01*00 1 .01 + 00 1.01+00 1.01+00 1.01+00 1.01+00 1.01 + 00 ucc 026732 CWIPMATMMI Time fllN reactor PRESSURE PSIA Hf ACTOli TEMP OfGHEE p UAyEH JACKET TIMP DEGREE F iiEAClOK MEAT com EMI III J GAS EEFI IN KtACjUK EUMUEE VCM LlO. left IN REACTOR congee 1120 LIU. IEFI IN REACTOR lrmole H*: ACT PH Vcm i)Q. VOLUME CU FT reactor H20 i_IQ volume CU FI 5. 20*00 9.26+01 1.10+02 9.60+01 - 3.29 + 06 7.30+00 2,61*02 9 62+03 3.09+02 1.39+03 5.30+00 9.16+01 1.10+02 9.60+01 -3.29+06 7.31+00 2.59+02 9 .61+03 2,95+02 1.33+03 5 >0*06 9.07+01 1,09*02 9.80+01 -3.33*06 7,32+Oq 2,97+02 9 .61*03 2.67+02 1,33+03 5.50+00 6.9A+Q1 1.06+02 9.60+01 -3.36+06 7.33+00 2,90+02 9 61*03 2.79+U2 1,33+03 5'6QtOO 6.09+fll 1.06+02 9.60+01 -3.93+06 7,39+Qo 2.39+02 9 .61*03 2.71+02 1.33+03 5.70+QO A.OO+ol 1.07+02 9,6(1 + 01 -3.97+06 7,35+00 2,27+02 9 61*03 2.63+U2 1,35+03 bv60+00 A.72+01 1.06+02 9,60+01 -3.52+06 7.36+0o 2,21+02 9 .60*03 2,55+02 1,33+03 5>o+uo U.bH+Ol 1,06+02 9,60+01 -3,56+06 7,37+00 2.19+02 9 .60+03 2,00+02 1.33+03 6.00*00 a.ii6 + ()l 1*05+02 9.60+01 -3,60+06 7,37 + Oq 2.06+02 9 *60+03 2,00*02 1,33+03 6'10+00 a.oo+ol 1.09+02 9,60+01 -3,65+06 7,36+00 2.02+02 9 ,60+03 2,33+02 1.33+03 6'20+00 6,9 1 + pl 1,09+02 9,60+01 -369 + 06 7,39+00 1.96+02 9 60+03 2,26+02 1.33+03 L01M 6'30 + 00 b >0 + 00 6,39+01 6.27+01 1.03+02 1.03+02 9.60+01 -3,73+06 9.60+01 -3,77+06 7,90+00 7.90+00 1.90+02 1.05+02 9 ,60*03 9 *59+03 2.19+02 2,13+02 1,33+03 1,33+03 b.50+00 a.20+rl 1.02+Q2 9,60+01 -3,01+06 7,91*00 1.79*02 9 .59+03 2.06+02 1.33+03 b.60+00 6.13+fll 1.01+Q2 9,60+01 -3,09+06 7*92+00 1.79*02 9 .59+03 2.00+02 1,33+03 6.70+00 A, 0 7 + it 1 1.01+02 9,60+01 -3.66+06 7,95+00 1,60+02 9 .59+03 1.93402 1.33+03 6.00+00 a.oi+oi 1.00+02 9.60+01 -3,92+06 7,93+00 1.63+02 9 *59+03 1.67+02 1.35+03 6'90*00 7,95+01 9.96*01 9,00+01 -3,95+06 7,99+00 1.56+02 9 .59+03 1.61+02 1,33*03 7,00+00 7,69+01 9,93+01 9,60+01 -3,99*06 7,99+00 1.53+02 9 .59+03 1.75+02 1,33+03 /.'10+00 7.69+nl 9.66+01 9,60+01 -9,02 + 06 7.95+00 1.90+02 9 .50+03 1.69+U2 1,33+03 7.20*00 7.76+pl 9,63+01 9.UQ+01 -<t. 05+06 7 96 + 0q 1,93+02 <1 .56+03 1.69+02 1,33+03 7.30+00 7.73+01 9,76+01 9,60+01 -<1.08 + 06 7.96+00 1.36+02 9 .56*03 1,56+02 1,33+03 7>0+00 7.66+01 9,79+01 9,00+01 -9.12+06 7.97*0(1 1,39+02 9 .56+03 1,53+02 1,32+03 7 '50*00 7.63+01 9,69+01 9,00+01 -9.15+06 7.9 7 + Of) 1.29+02 9 .5A+03 1.90+02 1.32+03 7.00+00 7.56+01 9,65+01 9.60+01 -9.16+06 7.90+ Ofl 1 .25 + 02 9 .56+03 1,93*02 1,32+03 7.70*00 7.53+01 9.60+01 9,60+01 -9.21+06 7.90+00 1.21*02 9 .50+03 1.36+02 1 ,32 + 03 7.1*0+00 7.99+f1 9.56*0l 9,00+01 -9,23*06 7.9^+00 1.16+02 1 .57+03 1.33+02 l ,32+03 7.90+00 7,99+01 9,52+01 9,60+01 -9,26+06 7.99+00 1.12*02 9 .57+03 1,26+02 1,32+03 (1.00+00 7,90+01 9,96+fll 9,60+01 -9,29+06 7,50+Ofl 1.00+02 9 .57+03 1,23+02 1,32+03 6.10+00 7,36+ol 9.99+01 9,00+01 -9,32+06 7.50+00 1,09+02 9 .57+05 1,19+02 1,32*03 6.20+00 7.32+01 9,90+01 9,60+01 -9.39*06 7.1+00 1.00+02 9 .57+03 1,19+02 1,52+03 6.30+00 7.26 + f.l 9.37*01 9.60+01 -9,37*06 7.51+00 9.67+01 9 .57+03 1,10+02 1,32+03 6.00+00 7.29+01 9.33+01 9,60+01 -9,39+06 7,52+00 9,30+01 9 57+03 1.06+U2 1,32+03 tu rn ooo tum'oiimiuH IlHI MjN l*(lHAS|t 6 AS FLOW MOlF/MI|. Pill flash urn liq. FLOU MflLl/MIN poefeash 1120 LIU, Ft OU noLi/niN HA bill l> fl-AbhUI liAS VCn L|*l. FLOW FLOW U/MN mule/nIN FI ASIIl 0 t(0. FLOW MOLE/h 111 IGIAL TUTAI 10JAL Py6 WCn GAS VCM LIU, FMOUULLO EMISSION EMISSION tunoLt MiMOl l LUMOLE 5,20tQO 5.30*00 5.40*00 5.56*00 5.66*00 5.70*00 5.00*00 5.90*00 6.00*00 6*10*00 6.20*00 .;au*oo 6>0*00 6 '50*00 6*60*00 6.70*00 6.Uo * 00 6.90*00 7.06*00 7.10*00 7.20*00 /.aooo 7 . HO * 00 7.50 *0U 7.60*00 7.76*00 7.00*00 7.90*00 a'outou U.10*00 0.20*00 (1.50*00 (I. HO * 00 7.12*(ll 6,99*01 6.05*01 6.72*01 6.59*(il 6,H6*0l 6.55*01 6,21*01 6,09*01 5.97*01 5.05*01 5.71*01 5.62*01 5.51*01 5.39*01 5,20*01 5.10*pl 5.07*01 H.96*01 H.06 * o1 H.76*01 H . 6*> * 0 1 H. 56*01 H.H6*0l H.iu*Ol H.26*01 H . 17 * 01 H.07 Mil 3.90*01 3.09*01 3.00*01 3.7U *0 1 3.61 * 01 1,12*00 1,00*00 i.u*i too 9.95-01 9.55-01 9,16-fll 0.70-01 O.Hl-ol 0,05-01 7.71-01 7.36-01 7.06-01 6.75-01 6.HH-01 6.15-01 5.07-01 5.6Q-01 5.34-01 5.09-01 H.OH-fll H.61-01 H.30-01 H.16-01 3.95-01 3.75-01 3.55-01 3.37-01 3.19-01 3.0|-ol 2.05-01 2.69-01 2,53-01 2.39-01 1,OH * 01 1.02*01 1.60*01 1.70*01 1.75*01 1.73*01 1.71*01 1.60*01 1.66*01 1,6H*01 1,61*01 1.59*01 1.57*01 1.5H401 1,52*01 1,50*01 1,H7*0l 1,H5t01 l.H 3* 01 1,H0*0l 1.30*01 1.36*01 1.33*01 1.31*01 1.29*01 1.26*01 1,2H*tll 1,22*61 1.19*01 1 . 1 7 G1 1.15*01 1.12*01 1,10*01 7.37*01 7.22*01 7.07*01 6,93*01 6,79*01 6,65*01 6.52*01 6.39*01 6.26*01 6.13*01 6.00*01 5.60*01 5.76*01 5.6H *01 !i. 52*01 5.H1 * 01 5.29*01 5,10*01 5,07*01 4.96*01 H.05*01 4.75*01 4.64*01 4.54*01 H , 4 H * 01 4,33*01 4,23*01 4.14*01 4.04*01 3,94*01 3.05*01 3', 75*01 3.66*01 ,00 ,00 ,00 .00 ,00 ,00 .00 *00 .00 ,00 .00 .00 .00 .00 .00 .00 .00 .00 ,00 ,00 .00 .00 .00 .00 .00 .00 .QO ,.iu .00 ,00 66 .oil .00 1,71*01 1.70*01 1.60*01 1.66*01 1.64*01 1.63*01 1.61*01 1.59*01 1.57*01 1.55*01 1,53*01 1.51*01 1.49*01 1.47*01 1.45*01 1.43*01 1.42*01 1.39*01 1,37*01 1,35*01 1,33*01 1,31*01 1.29*01 1,27*01 1.25*01 1.23*01 1,21*01 1.19*01 1.17*01 1,14*01 1.12*01 1.10*01 1.00*01 1.05*01 1.05*01 1.05*01 1*05*01 1.05*01 1.06*01 1.06*01 1*06*01 1.06*01 1.06t0l 1*06*01 1*06*01 1,07*01 1 .07*01 1.07*01 1,07*01 1*07*01 1.07*01 1 .07*01 1*07*01 1*07*01 1 .07*01 1*07*01 1*07*01 1.00*01 1.00*01 1.00*01 |.00 to 1 1*00*01 1.06*01 1.00*01 1.00*01 1.06*01 6.44*02 6.51*02 6.50*02 6.65*02 6.71*02 6,70*02 6,04*02 6,90*02 6,97*02 7,03*02 7.09*02 7.14*02 7,20*02 7.26*02 7.31*02 7.36*02 7,42+02 7.47*02 7,52*02 7.57*02 7,61*02 7.66+02 7.71*02 7.75*02 7.00+02 7.04*02 7.FP+U2 7.92*02 7.96*02 0.00*42 0.04+02 0.00*02 0.11*02 1,01*00 1,01*00 1.01*00 1,01*00 1.01*00 1.01*00 1.01*00 l.altoo 1.01*00 1,01*00 1.01*00 1 .01*00 1.61*00 1.61*00 1.01*00 1 ,61*00 1.01*00 1.01*00 1 .01*00 1.01*00 1.01*00 1.01*00 1 .01*00 1.01*06 i.ai*oo 1.61*00 1.Ul+00 1.01*00 1.01*00 1.01*00 1.01400 1 .01*00 1.01*00 ucc 026734 coapottiinoM I |ML niN Hi AC 1011 PHCSSilHf HSIA H| AC I OH u:w ihghee r UAlClt JACKET urn* degree f hi AC ICO HIA1 U-m EM hid UAS Ltn in RLACjUit umoLE VCM CIO. UF1 IN KCACIhH LBMOtE tl20 LIU. lef* in REAlTOR LQnoLt REACTOR vh 1 1U. vuluhl 6U IT REACTOR 1120 LlO. volume CU FI 0.50+00 6'60*OO 0.70400 0.00*00 U. 90400 9*00*00 9.10400 9*20400 9.10400 9.10*00 9.50*00 9.00400 9.*70400 9.00400 9.90400 1.00401 7.20f(il 7.17*01 7.13*pl 7.10401 7.07*01 7.09*01 7.01*01 0.90*01 6.95401 6.92*01 6.90*01 6.07401 6.05*01 6.02*01 6.00*01 6.70*01 9.29*01 9.26*01 9,23*01 9,19*01 9.16*01 9,13*01 9,10*01 9.07*01 9,04*01 9.02*01 6.99101 0.96*01 6,99*01 6.92401 6.69401 6.67*01 9.60*01 9.60*01 9.60*01 9.00*01 9.00*01 9.00*01 9.00*01 9,00*01 9.60*01 9,60401 9.60*01 9.80401 9,60*01 9.60*01 9.60*01 9.60401 <-9.92*06 >9.99*06 .9.96*06 .9.96*06 >9.51*06 .9,53*06 .9,55*06 .9,57*06 >9.59*06 >9.61* 06 >9,62*06 >9.69406 >9,66*06 >9.67406 >9.69406 >9.71*06 7.52*00 7.52*00 7 * Ofl 7.55*0q 7.59*00 7.59*00 7.59*00 7,55+00 7.55+00 7,55+00 7,56*00 7.56+00 7.56+00 7,56+00 7.57*00 7.57*00 0,99+01 0.60+01 6,26*01 7,93*01 7.61*01 7.29*01 6,99401 6,69+01 6.91*01 6,13+01 5.06+01 5.59*01 5,39*01 5,09+01 9.05+01 9,62+01 9*57+03 9*56+03 9.56 + 03 9*56+03 9*56+03 9.56*03 9.56+03 9.56+03 9*56+03 9.56*03 9*56*03 9.56403 9.55*03 9.55403 9*55*03 9.55*03 1.02+62 9.77*01 9.36*01 9,00*01 6,63*01 6.26*01 7,93*01 7,59*01 7,26*01 6.99*01 6,63*01 6.33tUl 6,09*01 5.76*01 3.99*01 5.23401 1.32 + 03 1.32+03 1,32+03 1,32*03 1,32*03 1,32+03 1 ,32+03 1,32*03 1.32403 1,32*03 1.32*03 1.32*03 1.32*03 1.32+03 1.32+03 1.32+03 UCC 026735 ! COM PUN AVION II Ml .1|N |`ULFLAS| 6AS FLUU mill/nit I'mILLasii WfM Lin. Fi ou MftU/MlU pun LASH 1120 LIU, Ft Ok! non /niN 11 ASllf 0 FLASHLO FLASIIFU (.AS yen LIU. II2U LIU. FLOW Ft OH Flow MU L/MN HULL/ttIN HQLt/hIN IOIAL I'yL PHOOUCLU t ||MOLL TUfAl UCP UAS EMISSION LimOLl- IUJAL yen Liu. emission LUMOLL 6. Silt 00 O.uUtOQ U.70*00 O.'&O + OO o.U0*00 y'ootoo 9*10*0" `J.20 *00 9.30 + 00 9'HC+00 9.50*00 9.00*00 9s10*00 9.00*00 9.90*00 1.00*01 3.53*61 3, HH t(l 1 3.35+01 3.26*01 3,ia*r>i i. 09*1.1 1.01+pl 2.92* III 2,00*1)1 2.76*01 2.67*fll 2.S9*ol 2.51*01 2.H3*oi 2.iS* Pi 2.27*01 2,20-01 2.11-01 1.90-01 1.06-01 1.70-01 1.63-pt 1.53-01 1.02-01 1.33-01 1.20-01 1.15-01 1.07-01 9.09-02 9,16-02 0.06-02 7.00-02 1.00*01 1,05*01 1.03*01 1,01*01 9,00*00 9,60*00 9,36*00 9,13*00 0.09*00 0,66*00 0,02*00 a.ia*oo 7,95*00 7,71*00 7,07*00 7,23*00 3.57*01 3,00*01 3.39*01 3.30*01 3.21*01 3.12*01 3.00*01 2,95*01 2,06*01 2.70*01 2,70*01 2.61101 2,53*01 2,05*01 2.37*01 2.2*0l .00 .00 .00 .00 .00 ,00 .00 .00 .00 .00 .00 ,00 .00 *00 .00 ,00 1.06*01 1.03*01 1.01*01 9,90*00 9,60*00 9,H6*00 9,23*00 9,01* 00 0,70*00 0,55*00 0,32*00 0,10*00 7.07*00 7.6H* on 7.H1400 7.17*00 1.00*01 1.00*01 1.00*01 1.00*01 i ,oe*oi 1.00*01 1.00*01 1.00*01 1.00*01 1,00*01 1.00*01 1,00*01 1 .60*01 1,06*01 1.00*01 1.00*01 0,15+62 0, 19*02 0.22*02 0.25*02 0,20*02 0.32*02 0.35*02 0.37*02 0.H6+U2 0.*13*02 6.*16 + 02 0.H6+02 6.51*02 6.53*02 0.56+02 0.50+02 1,01*00 1,01*00 1,01*00 1.01*00 1.01*00 1.01*00 1.01*00 1,01*00 1,01*00 1,01*00 1,01+00 1,01*00 1.61+00 1.61*00 1.61*00 1 .61*00 II IN ucc 026736 I DISCHARGE FROM A tVC BATCH REACTOR Caae 11. Iligli Reactor Rate - Cold Uater oa Jacket heacioh pressure ai nut of discharge = 2111.79 psia PRESSURE POWmSTHLAM OF VAhVC = 69. IQ PSIA HI AC I OH |EM|> A1 TIpE OF DISCHARGE = It ft. SO I WAlEll JACKET TEMP AT UISCOAKGf = 90.00 F REACTOR VOtUMt = 2673.000 CD FI IIEaT OF REACTION = 95516*000 UIU/Ltm(iLE L1UUIO VCrt ItUIIALlY IN REACTOR = 921.50 UIMOLE LlQ 1120 INITIALLY IN HE AC Mill = 9929.6 LBMOLE VAFUit INITIALLY IN BLACfOK = 2.9099 LUHOLf DENSITY OF WATCH (fONSfANll = 3.9570 LltmC/CU FT JACKET CURE TIMES AREA - 895.6 UTU/MIH F INITIAL OENSlTY OF VCM = .79912 LRMULE/CU FT AREA Or HINIhUM L10 UOL IlNG HLLIEF VALyC OrIFICE LlOUIIl ENYrAINhENT = WHEN MIN ENTRAINMENT jacket factor s 1.00 OPENING s .27/0 SO FT .0100 CO FT LIP/CU FT GAS IS REACHED s 2930.0 CU FT ORIFICE FLOW COEFFICIENT = .610 MINIMUM WATER JACMT lt-MP = 90.00 1I*E MIN JACKET TEMP IS REACHED = REACTION rate FACTOR s 1 .50 F 5.00 M Time hiN HEACTOR PRESSURE PSIA reactor TEMP degree f water jacket tlmp UE6REr F REACTOR HEAT CONI ENT IUU GAS LEFT IN REACfOH LUMOEE VCM LIQ. left in REACTOR U1M0EE ||20 LIO. left IN AEaETOH lrmole REACTOR tfEM lio. VOLUME EU FT REACTOR 1120 i_10. volume CU FI .00 2.15+C2 1,60*02 9.00*01 9,66*05 2 * 99+0() 9,21*02 9.93*03 1.15+03 1.93+03 ni 1.00*01 2.19*02 1,60*02 0.92*01 9.72*05 3,01*00 9,07*02 9*07+03 1.13+03 1,91+03 2.00*01 2.19*02 1.60*02 0.03*01 9,66*05 9.73*00 0.92*02 9*02+03 1.12*03 1.39*03 3.00*01 2.13*02 1,60*02 0,75*01 9,30*05 5,51*00 0.76*02 9*77+03 1.10+03 1,30+03 9.00-01 2.11*02 1.67*02 0.66*01 0,67*05 5,99+00 0.59*02 9*79*03 1.07+03 1,37+03 5.00-01 2.06*02 1.66*02 0.50*01 7.31*05 6.06+00 0.39*02 9*79+03 1.05+03 1,37+03 6.00-01 2.01*02 1.69*02 0.50*01 5,99*05 6.11+00 0.19+0? 9*79+03 1.02+03 1.37+03 7.00*01 1,96*02 1.62*02 0.91*01 9.60*05 6.16+00 7,99*02 9*73+03 9.93*02 1,37*03 0.00-01 1,91*02 1.61*02 0.33*01 3.29*05 6.20*00 7,01+02 9*73+03 9,67+02 1,37+03 9.00*01 1.07*02 1.59*02 0,29*01 2.00*05 6.29+0(1 7.62+0? 9*73+03 9.93+02 1,37+03 1 `00*00 1.02*02 1.57*02 0,16*01 7.29*09 6.20*00 7,95*02 9*72+03 9,19+02 1,37+03 1.10*00 1.70*02 1,56*02 0.00*01 .5.16*09 6.32 + Oq 7.27*02 9*72+03 0,95*02 1,37+03 1.20*00 1.79*02 1.59*02 7.99*01 .1.79*05 6,39+00 7.10+02 9*72+03 0.73+02 1.36+03 1.30*00 1.70*02 1,53*02 7.91*01 -2,93*05 6.39+00 6.99+02 9*71+03 0.51+02 1,36+03 1.90*00 1,66*02 ).51*02 7,02*01 -9.10*05 6,92+00 6.70+02 9*71+03 0,30+02 1.36+03 1.56*00 1.63*02 1.9`J + p2 7.79+01 -5,25*05 6.95+00 6,62+02 9*71+03 0.09+02 1,36+03 1.60*00 1,59*02 1,90*02 7,66*01 -6,37*05 6.9^*00 6,97+02 9*70+03 7.09+02 1,36*03 1.70*00 1,56*02 1.96*02 7.57*01 -7,97*05 6.52+Ofl 6,32*02 9*70+03 7.69*02 1,36+03 1 >0*00 1.53*i,2 1.95*02 7,99*01 -0,55*05 6+59400 6,17+02 9*70+03 7.50*02 1.36*03 ucc 026737 COMPOIUTIOM 1 iW NtN I'lUFLASj. GAS FLOU MOLL/HI l> 1*1)1.FLASH \lcn L-IO. FLOg H(|LE/HItJ l*Hf| l ASH 1120 LIU. Fl OU MOL| /MIN llASHLU FLASHED FLASHED GAS Vtn LIU, H20 LfO. FLOU FLOU FLOU NOt L/M1N MULL/MIN MOLL/MIN 101AL IOIA1 lUfAL lyt yen GAS ycM |_JU. pOOUuCLO EMISSION EMISSION LUMQLL LHMOLL LUMQLE .06 1.00*01 2.00*01 3.00-01 4. 00-01 S.00-01 0,00-01 7.00-01 0.00-01 9.00-01 1.00100 1.10*00 1.20*00 1.30*00 1,00*00 1.50*00 1.00*00 1 '70*00 1.60*00 1.63*00 l.Stttltl 7.13ml 1.62*02 1.94*02 1.0*0*02 1.0*4*02 1.00*02 1,76*02 1.71*02 1.67*02 1.63*02 1.69*02 1.66*02 1.61*n2 1.07*02 1.49*02 1.41+f2 1.26*02 1.16*02 1.03*02 7.60*01 2.99*01 6.70*00 6.62*00 6.36*00 6.16*00 6.02*00 4.66*00 4,71*00 4,66*00 4.41*00 4.27*00 4.13*00 4.00*00 3.67*00 3.74*00 5,97*02 5.56*02 4.96*02 3.60*02 1,46*02 2.69*01 2.67*01 2,05*01 2,03*01 2,00*01 2.76*01 2.76*01 2.73*01 2,71*01 2,69*01 2,66*01 2.64*01 2,61*01 2.69161 1.17*02 1.24*02 1,35*02 1,57*02 2.02*02 2.09*02 2.04*02 1,99*02 1.93*02 1.69*02 1.64*02 1.79*02 1.74*02 1.70*02 1.66*02 1.62*02 1.56*02 1,54*02 1,60*62 1.04*0i 0.22*00 4.70*00 ,00 ,00 ,00 ,00 ,00 .00 .OU .00 .00 ,oo .00 .00 .00 .00 .00 ,00 5.96*02 5.57*02 4.97*02 3,72*02 1,36*02 1,90*01 1,92*01 1.94*01 1,95*0| 1.97*01 1,96*01 1,99*01 2,00*fli 2,01*01 2.02*01 2.02*6| 2.03*01 2.03*01 2.03*01 00 6.93-01 1.36*00 2.05*0U 2.69*00 3.29*00 3.63*00 4.33* OU 4*79+00 5.21+00 5.60*00 5*95+00 6.26+00 6*56+00 6.65*00 7.11*00 7.34*00 7.55*00 7*75*00 .00 1.21*01 2.46*01 3.66*01 6.52*01 7.49+01 9.40*01 1,13+02 1.31*02 1.49+02 1.66+02 1.63+02 2.00+02 2.16+02 2.32+02 2.47*02 2.62*02 2.77+02 2.91*02 .00 9,66-01 1,62*00 1.64+00 1,04*00 1.64*00 1.04+00 I.U4+00 1.04+00 1.64+00 1.64+00 1,04+00 1.64+00 1.64+00 1.64+00 1,64+00 1.04+00 1.64+00 1.64100 ucc 026738 1 TlML riiN HLACTOIt PMESSUltf MSI A Hf.ACIOIt irnp Ot GMEE F wAjrn JACKET imp OEGhLT F l\E AC)tIH llt-Al (OIllENl DlU GAS LkFI IN MLAt jOR LUMOLE UCN LIQ. left in HEACTOK LWHOLE H20 LIU* LEFI IN HEALTUK LWHOLE KMCTOK v^n iiq* VOLUME Mi Fi HEALtou H2U L10, volume LU FI 1.90*00 1.19*02 1.11*02 7.10*01 >9,61*05 6.57+On 6,03+0? 1 *70+03 7.31*02 1.36+03 2 "0(1*00 1.10*02 1.12*02 7.32+01 >1,06+06 6.60+Oq 5,89+Og 1 *69+03 7,13*02 1.36+03 2.10*00 1.13tfl2 1.11+02 7.21+01 >1.16+06 6.62+Qo 5,76+02 1 .69+03 6,96*02 1,36+03 2.20*00 1.11*02 1,39*02 7.15+01 >1,26+06 6.65+00 5,63+02 1 .69+03 6.79*02 1,36+03 2.30*00 1.30*02 1.30+02 7.07*01 >1,36+06 6*67+00 5,50+02 1 .60*03 6.(2 + 02 1.36+03 2. *10 *00 1.35*02 1.37+02 6.90+01 >1.16+06 6.7O+O0 5.37+02 1 .60*03 6.16+02 1,35+03 2.50*00 1.33*02 1,35+02 6.90+01 >1,55+06 6,72+00 5,25+02 1 .60*03 6.30+02 1.35+03 2.GO*00 1.30*02 1.31+Q2 6.02+01 >1.61+06 6,71+00 5.13+02 1 .60+03 6.11+02 1,35*03 2.70*00 l,2o*o2 1.33+02 6,73+61 >1,73+06 6,76+00 5,01*02 1 .67*03 5,99*02 1,35+03 2.00*00 t,2fc+|i2 1.32+02 6,65+01 >1.61+06 6,76+Qg 1,09* 02 1 .67*03 5.05+02 1,35+03 2.90*00 1.21*02 1,30+02 6,56*01 >1.90+06 6,00+00 1.70*02 1 .67*03 5.70+02 1,35*03 0o1> o 3'0fl*00 i.'IiWOO 3.20*00 1,21 *f,2 1.19*02 1.10*02 1.29+02 1,20+02 1.27+02 6,10*01 6,10 + 01 6.31+01 >1,90+06 >2,06+06 -2.11*06 * 6,02 + 0q 6,01*00 6.65+00 1.67*02 1.56*02 1,16*02 1 .67*03 1 . 6b* 0 3 1 .66*03 5,56+02 5.13*02 5.29+02 1.35*03 +.35+03 1,35 + 03 A'30*00 1.16*02 1.26+02 6.23+01 >2.22*06 6,A/+00 1,36*02 1 .66*03 5.16+02 1,35+03 3 10*00 1.11*02 1.25+02 6.11+01 >2,30+06 6, l|9+00 1,26+02 1 .66*03 5.01+02 1.35+03 3'50*00 1.12*02 1.21+02 6.06+01 >2.37+06 6,90+00 1.16+02 1 .65*03 1.91+02 1,35+03 3.00*00 1,10*02 1,23+02 S.9A+01 >2.15+06 6.92+00 1,06+0? 1 .65*03 1.79+02 1,35+03 j'70+00 1.09*02 1.22+02 5,09+01 >2.52+06 6,93+Qo 3.97*02 1 .65*03 1,60+02 1,35+03 3 .'00*00 1.07*02 1.21+02 5,01+01 >2.59+06 6,95+00 3.07*02 1 65*03 1.56+02 1,31+03 3.90*00 1,06*02 1,20+02 5.72*01 >2.66+06 6,96+00 3.70*0? 1 .65*03 1.15+02 1.31+03 1.00*00 1,01*02 1.19+02 5.61+01 >2.73*06 6.90+00 3,69*0? 1 .61*03 1.31+02 1.31+03 1.10*00 1.03*02 1.10+02 5,56+01 -2.79+06 6.99+Ofl 3,61*02 1 *61*03 1.23*02 1.31+03 1.20*00 1.01*02 1.17+02 5.17+01 >2.06+06 7.00*00 3,52*02 1 .61*03 1.13+02 1.31+03 1.30*00 1.00*02 1,16 + 02 5,39+01 >2.92+06 7.01*00 3,11*0? 1 .61*03 1.03 + 02 1.31+03 1."10 too 9.07*01 1.15+02 5,30*01 >2.96+06 7.03*00 3.36*02 1 .61*03 3.93+02 1.31+03 1.50*00 9,75*01 1,11+02 5.22*01 >3,05*06 7.01+00 3,20*02 1 ,63+03 3.03+02 1,31*03 1'Go*00 1.70*00 9.63*f. 1 9.51*rl 1,13+02 1.12+02 5,11+ol >3,10+06 5.05+01 >3,16+06 7.05+00 7,06+00 3,20+0? 3,12*02 1 .63*03 1 ,63*03 3.73*02 3.61+02 1,31+03 1.31+03 1.00*00 9.10*01 1.11+02 1,97+01 >3,22+06 7.07+00 3,05+0? 1 ,63*03 3.55+02 1,31*03 *.'96*00 *i.00*00 9.29*01 9.19+01 1.11*02 1.10+02 1 . OF l* 1 -3.20+06 1.00+01 >3,33*06 7.0U+0fi 7.09+00 2.90+0? 2,91+02 1 .63*03 1 .62*03 3.16*02 3.30+02 1.31+C3 1.31+03 t*' 1U * Q 0 9,00*0l 1,09+02 1,00+01 -3,39*06 7.10*00 2,01+0? 1 .62*03 3,29+02 1.31+03 ucc 026739 COliMMWWM T'lHt niN PHEFLASp GAS FLOW ttOLf/rtlr PllCELASH wen tio. FLOW HoLF/ftlll PUFFLASH 1120 LIO. Fl OU HOLf/ttJN li Abut u flashed FtASIlFD GAS ven Liu. 1120 LIU, Ft06 FLOW FLOW hOLf/HIN HULt/niN HOLf/MN T01AL IOTAL 101AL PUL yCn GAS VCrt LIU. pHOUUCtU EMISSION EMISSION LattOLE MIMOEE LUnOLE l .90 mo 2.00*00 2.10 *00 2.20*00 2 *3(1*00 2'90*00 2.00*00 2.66 *00 2.70*00 2.00*00 2.90*00 3.00*00 3.10*00 3.20+00 3.30+00 3.40*00 >v50 tOO 3.60*00 3.70*00 3 .'00 *00 3.90+00 t'OO*00 4.10+00 4.20+00 4.3o * 00 4.40*00 4 '50*00 4.60*00 4.70*00 4.00+00 4.90 *00 5.06*00 5. 10*00 1.37+02 1.34+02 1.31*02 1.20*02 1.2f*o2 l.22*n2 1.20+02 1.17+02 1.14*02 1.12*02 1.09*02 1.07*02 1.00*02 1.02*02 1.00*02 9.02*01 i.<1*61 9.41*01 9.21+01 9.02*ul d.flitdl d.6b 101 0.47*01 0.29*01 0.12*01 7,9b+0l 7.79ol 7.63*nl 7.47*nl 7.32tl 7.17 l (t 1 7.02*01 6.07*01 3.62+00 3.50*00 3.39*00 3.20*00 3.17*00 3.06*00 2.96+00 2.06+00 2.77+00 2.67*00 2.50+00 2.49*00 2.41+00 2,33+00 2,25*00 2.17+00 2.09*00 2.02+00 1.95*00 1.00*00 1.02*00 1.75*00 1.69*00 l, 6 3* fO 1,57*60 1.51*00 1.46*00 1.40*00 1.35*00 1.30*00 1.25*00 1.21tuO 1.16*00 2.56*01 2,54*01 2,51*01 2.49*01 2,46*01 2.44+01 2.41+01 2.39*01 2.36+01 2.34+61 2.31+01 2.29+01 2.26+01 2.24*01 2.21+01 2,19*01 2.16+61 2.14+01 2,11*01 2.09*01 2,06*01 2,03*01 2,01+01 1.90*01 1.96*01 1,93*01 1.91*01 1.00*01 1.06*01 1,03*01 1.01*01 1.70+01 1,76+01 1,46402 1,43+02 1,39*02 1,36+02 1.33+02 1,30+02 1.27+02 1,24+02 1,21+02 1.10*02 1,15+02 1.13+02 1.10+02 1,00*02 1.05*02 1.03*02 1,61*02 9.06+01 9.64+01 9,43*0) 9.22*01 9,02*01 0,03+01 0,64+01 0,45+01 0,27*01 0.09*01 7,92*01 7,75*01 7,50*01 7.42*01 7.26*fl| 7,10*01 .00 ,00 QU .00 .uo ,0" ,00 .00 .00 .00 .00 ,00 ,00 .00 ,00 .00 .00 .00 .00 .01) .00 .00 .00 .00 .00 .00 .00 .00. .00 .00 .ou ,00 2,03+01 2.03+01 2,02+01 2,02+01 2.02+01 2,01+01 2,01+01 2.00+0} 1.99+01 1.90+0) 1.97*01 1,96*0i 1,95+01 1.94+01 1.93+01 1.92+0* 1.90+01 1.09+01 1.00*01 1.66*61 l.U5+l 1.03*01 1.02*01 1.00+01 1.79*01 1.77*01 1.75+01 1.73+01 1.72+01 1.70+01 1.60*01 1.66*01 1,64*01 7 94 + 00 0 11+00 0 26+00 0 41+00 0 54+00 0 67 + 00 0 70 + 00 0 09*00 0 99+00 9 09*00 9 17+00 9 25+00 9 33*00 9 40 + 00 9 47+00 5 53t 00 9 59*00 9 64+00 9 69 + 00 9 74+60 9 79*00 9 03*00 9 07 + 00 9 91*00 9 94 *00 9 90+00 1 00 + 01 1 00*01 1 01+01 1 0) *01 1 01 +01 1 01+01 1 02*01 3.05+02 3.19+02 3.32*02 3.45*02 3.52*02 3.T0+U2 3,02+02 3.94*02 4,06+02 4.17+02 4.29*02 4.39*02 4.50+02 4.61+02 4.71*02 4 .21+02 4.91+02 5.00+02 5.1C*02 5.19*02 5.20+02 5,3f *02 5.45+02 5.54*02 5.62*02 5.70+02 5.70+02 5.06*02 5.93+02 6.01*02 6.02*02 6.15*02 6.22+02 1.04+00 1.04*00 1.04*00 1.04+00 1,04*00 1,04+00 1,04*00 1.04*00 1 ,04*00 1,04*00 1.04*00 1.04*00 1.04*00 1.04*00 1.04*00 1 .04*00 1.04*00 1 .04*00 1.04*00 1.04*00 1.04*00 1.04*00 1,64*00 1.04*00 1.04*00 1,04*00 1.04*00 1.04*00 1.04*00 1.04*00 1,04*00 1.04*00 i.04*00 ucc 026740 CONPMJUUM T |H| M|N Rf AC TOIl PHESSUItl I*SIA RfACTOR tchp OfOHEE p UAlLH JACKET TEMP UE lilt EC F l-.i ACTOR IILA1 C0M1EN1 mu GAS LEFT IN lit ACT OH canoeE yen cm. LEFT IN REACTOR CHMOLE 1(20 LIU. LtFl IN REACTOR Lfinocc reactor vLn i io. 90LHPE cu FI REACTOR H20 1. jo uoLunf cu FI 5 . ? 11 + 00 ii'30+00 5.90+00 5.50*00 5.00*00 5.70*00 5.00*00 5.90*00 6 *00*00 6.^10 + 00 b .'20*00 b'30+00 0.90*00 0.50*00 0.00*00 0.70*00 0.00*00 0.90*00 7.00*00 7M0 + 00 7.20*00 7.30*00 /.'9 0 *00 7 '50*00 7.00*00 7.70*00 7 'U0*00 7.90*00 6.00*00 6.10*00 6.20*00 6.30*00 6*90*00 0.9ft* ft 1 6.09*61 6.60*03 6.71+ot A.b2|>l 0.59+01 6.95*01 6.36*01 6.30*fll 6.23*01 6.15*fll 6.09*01 6.02*01 7.95*01 7.69*01 7.63*01 7.77*01 7,71*01 7.66*01 7.60*01 7.55*01 7.50*01 7,95+fll 7.91*01 7,36*01 7.32*01 7.27*01 7.23*01 7.19*nl 7.15*01 7.12*01 7.06*fll 7.09*01 1,06*02 1.06*02 1.07*02 1.06*02 1.05*02 1.05*02 1.09*02 1,03*02 1.03*02 1.02*02 1.02*o2 1.01*02 1.00*02 9.96*01 9.93*01 9.07*01 9.02*01 9.77*01 9.72*01 9.67*01 9.62*01 9.5A*A1 9,53*01 9.99*01 9,99*61 9.90*01 9.36*01 9.32*01 9.26*01 9,29*01 9.21*01 9.17*01 9.19+fll 9,60+01 9,60+01 9,00*01 9.60*01 9.60*01 9,60*01 9.60*01 9,66*01 9.60*01 9.60*01 9.60*01 9,60*01 9,60*01 9.60401 9.60*01 9,60*01 9,60*01 9,60*01 9.60*01 9,60*01 9.60*01 9.60*01 9,60*01 9,60*01 9.60+01 9,00*01 9.60+01 9.60+01 9,60+01 9,60*01 9.60*01 9,60*01 9.60+01 -3,99+06 -3,95+06 -3.59+06 -3.55*06 -3.69+06 -3,69+0b -3,73+06 -3,76+06 -3,62+06 -3,67*06 -3,91+06 -3,95+06 -3.99*06 -9.03+06 -9.07+06 -9.11+06 -9.15+06 -9.16*06 -9.22+06 -9.25+06 -9,29+06 -9.32+06 -9.35+06 -9.30+06 -9.92+06 -9.95*06 -9.97*06 f>0 i 0& -9.53+06 -9,56*06 -9.56+06 -9.61*06 -9,69 * Qb 7*11+00 7*12+00 7.13+00 7.19+00 7.15*00 7,15+Qo 7.lb+OQ 7,17+00 7,16+00 7,16+00 7,19+00 7,26+00 7*26+00 7,21*00 7.22+00 7.22+00 7.23+00 7,29+00 7.29+00 7.25+00 7.25+00 7.26+Oq 7.26*00 7,27+00 7.27*00 7*26+00 7,26+00 7.26+00 7.29+00 7.29+00 7.36+00 7.30+00 7.30*00 2.77*02 2.70*02 2.63*02 2,57*02 2.51+02 2.99+02 2,36+02 2,33+02 2.27*02 2,21*02 2,16+02 2,10+02 2.05+02 2.00+02 1,95+02 1,90+02 1.65+02 1.60+02 1.76+02 1.71+02 1,67*02 1,63+02 1,56+02 1.59+02 1.50*02 1,96 + 02 1,93+02 1.39+02 1,36+02 1,32+02 1.29+02 1,25+02 1,22*02 9 62+03 9 .62+03 9 .62+03 9 .61+03 9 *61+03 9 *61+03 9 >61+03 9 ,61*03 9 *61+03 9 60+03 9 *60+03 ** .60+03 9 66+03 9 .60+03 9 .60+03 9 *60+03 9 .59+03 9 .59+03 9 59+03 9 .59+03 9 .59+03 9 59+03 9 *59+03 9 .59*03 9 .56+03 9 .56+03 9 .56+03 9 56+63 9 .56+03 9 .58+03 9 .58+63 9 .56+03 9 *56+63 3.21*02 3.13+02 3,05+02 2.97+62 2.90+62 2.02+62 2.75*02 2.66*02 2,61*62 2.59+62 2.96+02 2,91+02 2.35+02 2.29+02 2.23+62 2.17+62 2,12+62 2,06+02 2.01+02 1.96+02 1.90+62 1.05+62 1.01+62 1.76+02 1.71+62 1.67+02 1.62+02 1,50+02 1,59+62 1.50+62 1.96+02 1.92+02 1.39+02 1,39+03 1.39+03 1,39+03 1.33+03 1.33+03 1.33+03 1.33+03 1,33+03 1.33+03 1.33+03 1.33+03 1.33+03 1.33+03 1.33+03 l,33+03 1.33+03 1.33+03 1,33+03 1,33+03 1.33+03 1,33+03 1.33+03 1.33+03 1.33*03 1.33+03 1.33+03 1,33+03 1,33+03 1.32+03 1.32+03 1.32+03 1.32+03 1.32+03 ucc 026741 urn rt'.N f>|tn l.AS|i GAS FMM miLF/nu PMTUASit Vcft no. FM1M rUM-t/Hiri plttf LASH 1120 LIQ. F|.OU HOLf/MIN i lASiltU KtASlltO FEASIIEO GAS wen MU, 1120 LIO. FLOW FLOW FtOW notE/niN HUM /H|N MOLE/HIM TolAE TOTAI IOJAF Pve wen GAS ven no, l>i(uouctu EMISSION Crtission EtiriOLE eunoi E LUH06E 5.'20400 6.71*01 1.12*00 1.71*01 6.96*01 6.10*00 6.69*01 1,07*00 1.71*01 6.00*01 s.'notoo 6.06*01 l.o$*oo 1,60*01 6.66*01 6.60*00 6,11*01 9.91.01 1,66*01 6,61*01 6.60*00 6.10*1)1 9.62.01 1.61*01 6.16*01 5'70+00 6.0St|i 1 9.10-01 1.61*01 6,22*01 6.00*00 6,92*01 0.70-01 1,60*01 6,09*01 6.^0400 6.00*01 0.93-01 1.66*01 6.96*01 b.`00*00 6.67*01 0.09-01 1.61*01 6,02*01 bs|0*00 6.66*01 7.76-01 1,61*01 6,69*01 6 .20*00 5.93+01 7.00-01 1,00*01 6,66*01 0 1 6*30*00 6.00*00 b.60400 3.1l*0l 6,19 Ml 1 6.00MI1 7.11-01 6,01-01 6.60-01 1,06*01 1,01*01 1,01*01 6,99*01 6,11*01 6,19*01 6 >0*00 4,96*01 6.26-111 1.10*01 6.07*01 6.70*00 *1.06*01 6.99-01 1.36*01 9.96*01 6.00*00 H. 7H*q1 6.71-01 1.11*01 9.09*01 b.WO+OO *1.61*01 6.00-01 1,11*01 9.72+01 7.00*00 H.62*01 6.20-01 1.20*01 9.61*01 7.10*00 H.H1*01 6.01-01 1,26*01 H,60*01 7*20*00 0.11*01 0.70-01 1,21*01 9.19*01 7.10*00 0.20*01 0.66-01 1.21*01 9.20*01 7*00*00 O.lUtfll 0.16-01 1.10*01 9.17+01 7,60*00 0.00*01 0.16-01 1.16*01 9.06*01 7.60*00 1.0`J*ol 1,96-01 1.11*01 1,96*01 7 .*70*00 1.79*01 1.77-01 1,11*01 1.06+01 7.00*00 1.69*01 1.69-01 1.00*01 1.76*01 7.*0*40 l,69*fil 1.02-01 1.06*01 5,66*01 a. oq*oo 1,60*01 1.26-01 1,01*01 1,69*01 0.10*00 1.00*01 1.09-fll 1.01*01 1,99*01 u.2u*00 1. lilt 01 2.93-61 9,00*0(1 1.19*01 0.10*00 1.21*01 2.70-01 9,66*00 1;?6+U1 0.HO * 00 1.11 * 01 2.60-01 9,29*00 1.16*01 .00 .00 .00 .00 .00 ,o .00 .00 .00 .00 .00 .00 .au .00 .00 .00 .00 00 .00 .00 .00 .00 .00 .00 .00 .00 *00 .00 ,00 .1)0 .QU .00 1.62*01 1.61+01 1.69+01 1,57*01 1.55*01 1,51*01 1.51*01 1.99*01 1.96*01 1.99*01 1,92*01 1 .90+01 1.10*01 1.16+01 1.19+01 1.11*01 1.29+01 1.27+01 1.25+01 1.21+01 1.20+01 1.10 + 01 1.16+01 1.11+01 1,11+01 1,09+01 1,06+01 1.09*01 1,02+0} 9.S2+0U 9,60*00 9,99*00 9,19*00 1.02*01 1*02401 1.02*01 1.02*01 1.01*01 1.01+01 1.01*01 1.01*01 1.01*01 1.01*01 1.01*01 1.09*01 1.09+01 1.09*01 1.09*01 1.09*01 1*09*01 1 ,09*01 1.09+01 1*09+01 1.09*01 1.05*01 1.05+01 1.05+01 1*06+01 1,05+01 1*05+01 1.06*01 1.06+01 1.05*01 1.06+01 1.05*01 1.06+01 6,29*02 6.36+02 6,92+92 6.90+92 6,66+02 6,61+92 6,67+92 6.73+02 6,70+02 6,09 + 92 6,90+02 6.95*02 7.00+02 7,06+02 7.10+02 7,16+92 1.20+02 7.26+02 7.29+92 7.39+92 7.30*02 7.9 3*02 7,97*02 7.51*02 7,55*02 7,69*02 7.62*02 7.66*02 7.69*02 7.73*02 7.76*02 7.79*02 7.03*02 1.09*00 1,09+00 1,09+00 1,OH* 00 1,09*00 1,09*00 1.09*00 1.09*00 1.09*00 1,09+00 1.09*00 1,09*00 1.09*00 1,09*00 1,09*00 1.09*00 1.09*00 1,09*00 1.09*00 1.09*00 1 . OH * 00 1.09*00 1,09*00 1.09*00 1,09*00 1,09*00 1,OH * 00 1,OH * 00 1,09*00 1 .OH*00 1,09*00 1.09*00 1.09*00 ucc 026742 CMPOMJmOM iim niN HL AC TOR pressurf P6IA ttfACTOR ?EHP DEGREE r UAl LR JACKET temp l)tG|iEE F Rf AC I oft lit AT COMEM filU GAS ILM IN lit AC I UR MMOLE UCH U0, left IN REACTfiK LtMOEE 1120 LIU. LtF* IN REALTOR LurtOEL 1(6 AC TOR VLfl l Id* volume cu FT REACTOR H20 L10. volume tu FI a'to*oo 0.60*00 0.70*00 0.00*00 0.90*00 9'00*00 9.10*00 9.20*00 9'3Q+00 9 '40 *00 9.50*00 9 *60 + 00 9'70*00 9.'00 *00 9.90*00 1.00*01 7.01*01 6.90*01 6.95*01 6.92*01 6.09*01 6.06*01 6.U3+01 6.00*01 6.70*01 6.75*01 6.73*01 6.71*01 6.69*01 6.67*01 6.65*01 6.63*01 9.10*01 9,07*01 9.04*01 9,01*01 0.90*01 0.95*01 0,92*01 0,90*01 0.07*01 0.05*01 0.02*01 0.00*01 0.76*01 0,76*01 0,74*01 0.72*01 4 ,00*01 4.00*01 4,00*01 4,00*01 4.00*01 4.00*01 4.00*01 4.00*01 4,00*01 4.00*01 4.00*01 4.60*01 4,00*01 4,00*01 4,00*01 4,00*01 *^o 6b t Ob -4.60*06 -4,71*06 -4.73*06 -4.75*06 -4.77*06 -4.79+06 -4.61*06 -4.63*06 >4.05*06 -4.07*06 -4,00+06 -4,90*06 -4.92+06 -4.93*06 -4,95*06 7.31*00 7.31*00 7.31*00 7,32*00 7.32*00 7.32*00 7.33*00 7.33*00 7.33*00 7,33*0o 7.34+00 7.34+00 7.34*00 7,34*00 7.34*00 7,35*00 1.19*02 1.16*02 1.13*02 1.11*02 1.00*02 1.05*02 1.03*02 1.00*02 9.00*01 9,50*0) 9,37*01 9,16*01 0,97+01 0,70*01 0,60+01 6,44+0] 457+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*57+03 4*56+03 4*56+03 4*56+03 1.35+u2 1.32+02 1.20+62 1.25*02 1.22+62 1,19+62 1.16+62 1.14+62 1.11+62 1,00+62 1.06*62 1.04+U2 1.01+62 9,92+01 9,72+61 9.52+61 1.32+03 1.32+03 1.32+03 1.32+03 1,32+03 1.32+03 1,32+03 1,32+03 1.32+03 1,32 + 03 1,32*03 1,32+03 1,32+03 1,32+03 1.32+03 1.32+03 ucc 026743 1 CUNI'UHliriUN *i In IlHl h|N cum.asm 6AS Fl-OW MOU/HlM I'ixCFLASH W| H L IQ, FLOW Nrl-f/HIM PUCI LAStl 1120 LIQ. FlOll noli./n in f l ASlltU FLASIILU FLASHED r.AS yen lio. 1120 LIO. i'LUW FLOW FLOW MM.F/N1N NL* /NJN MOLL/HIM 101AL pVL 10IAL WON OAS fOTAL wen lio. PHOOUCLU EnissiON EMISSION LONOLF MMOl L LMnOLF 0.60*00 0.00*00 0.70*00 0.00*00 0.10*00 9.00*00 1.10*00 1.20*00 1.40*00 9'lOtOO 1.50*00 `>'00*00 1.70100 1.00*00 1.10*00 1 >0*01 3.02*01 2,12t|ll 2.03*01 2.71*01 2,01*01 2.66*01 2.16*01 2.31*01 2.27*01 2.10*01 2.01*01 2.00*ol 1.11*01 1.02*01 1.73*01 1.01*01 2.60-01 2.37-01 2,21-01 2.12-01 2.01-01 1.01-01 1.71-01 1.60-01 1.60-01 1.11-01 1.10-01 1.31-01 1.23-01 l.H-01 1.07-01 1.11-02 1,03*00 0,70*00 0.62*00 0.2L400 0,00*00 7.71*00 7.10*00 7.21*00 6,16*00 6,60*00 6.12*00 6,16*00 6,00*00 6,61*00 6.36*00 6.07*00 3.06*01 2.16*01 2,06*01 2,76*01 2,67*01 2,67*01 2.10*01 2.31*01 2.21*01 2.20*01 2,11*01 2.01*01 1,12*01 1.03*01 1,71*01 1.06*01 .00 .00 ,00 .ou .00 .01) .00 .00 .00 .00 .00 .00 .00 6.21-03 1.07-02 1*67-02 0.16*00 0.70*00 0,16*00 0.20*00 7.95*00 7.70*00 7,11*00 7,11*00 6,13*00 6,07*00 6.lUftil 6.11*00 6,00*00 5.61*00 5.35*00 6,07*00 1.05*01 1 .05*01 1.05*01 1,06*01 1,05*01 1.05*01 1*06*01 1.06*01 1,06*01 1,06*01 1.06*01 1*06*01 1.06*01 1.06*01 1.06*01 1*06*01 7.06*02 7.01*02 7.92+02 7.91+02 7.97+02 0.00*02 0,02*02 0,06*02 0.07*02 0.09+02 0.11*02 0,13*02 0,16*02 0.17+02 0.19+02 0,20+02 1.01+00 1,01+00 1.01*00 1,01+00 1.01+00 1,09*00 1,01*00 1,01+00 l.al+00 1.01+00 1.09+00 1,09+00 1,09+00 1.09+00 1.09>00 1 .09 + 00 ucc 026744 t APPEHDES 0 Metric Hales Conversion Table D-l ucc 026745 APPENDS d Metric doles Conversion Tabis Multiply (English Units) English dolt Abbreviation by Conversion To Obtain (Metric doits) Abbreviation Metric Unit British Thermal Unit cubic fast degrees Fahrenheit feet gallon kllovate-hour pounds pound per square inch square feet square inches Symbo^ BTd eu ft *7 ft gal kwh 16 psi sq. ft sq in 0.252 0.023 0.555(*7-32)* 0.3048 0.003735 3.6 x 10* 0.454 6.8948 0.0929 6.452 Symbol kg cal cu a c a cu a J kg k?a sq a 39 a*'," kilogramcalories ' cubic meters degrees Celsius asters cubic asters joules kilograms kilopascals square asters square centl- , maters' *Actual Conversion, ooc a aultipLiar. D-2 ucc 026746