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A1A0A2A3A4A5A6A7A81目录摘要错误未定义书签。ABSTRACT错误未定义书签。1综述111甲醇的性质、用途及重要性2111甲醇的性质2112甲醇的用途及其在国民生产中的作用212甲醇生产技术的发展2121世界甲醇生产技术的发展2122中国甲醇生产的发展概况213甲醇生产原理2131天然气转化过程2132甲醇的合成2133甲醇的精馏214设计方案的确定3141原料的选择3142工艺流程的选择3143工艺参数的确定3144厂址选择及设备布置32工艺计算321甲醇合成工艺计算3211物料衡算3212热量衡算922甲醇精馏工艺计算13221物料衡算14222热量衡算1423设备选型及其计算1431厂房布置19311甲醇合成厂房的布置19312甲醇精馏厂房的布置19A9A10A11A12A13A14A15A16A17232设备布置19321甲醇合成设备的布置19322甲醇精馏设备的布置19甲醇工艺技术1911合成气制备2012甲醇合成2013甲醇精馏201综述11甲醇的性质、用途及重要性111甲醇的性质112甲醇的用途及其在国民生产中的作用12甲醇生产技术的发展121世界甲醇生产技术的发展122中国甲醇生产的发展概况13甲醇生产原理以天然气为原料制甲醇工艺装置主要由合成气制备（包括天然气压缩、加氢脱硫、烃类转化、蒸汽动力和废热回收）、甲醇合成（包括合成气压缩、甲醇合成、甲醇分离）和甲醇精馏三部分组成。各部分涉及的主要工艺技术如下。131天然气转化过程1311天然气转化过程工艺原理1312天然气转化过程的工艺条件1313天然气转化流程和主要设备132甲醇的合成1321合成甲醇的基本原理1322合成甲醇催化剂1323合成甲醇工艺条件1324合成甲醇工艺流程和主要设备133甲醇的精馏1331甲醇精馏的任务1332甲醇精馏工艺流程A18A19A20A21A22A23A24A25A2631333甲醇精馏工艺条件1334甲醇精馏主要设备14设计方案的确定141原料的选择142工艺流程的选择143工艺参数的确定144厂址选择及设备布置2工艺计算G9035G2347G3835G4410G7460料G994化工G4410G19510G712G5192产30G987G2556甲醇生产G17722G19400工艺G2033G8505设计本设计G17993G5502G256G12538合国G5785、技术G1820G17839、G13475G8994G10627G1457G257的原G2029G712在综合分G7524G16844G3822甲醇生产方G8873的基G11796G990G712G18331用以天然气为原料G712G13475脱硫G803G1120G8585转化G803合成气G712在G1314压下G3278定G12661G7507G2027G12661G5347合成G3624中合成甲醇的技术G17347G13459G727精甲醇的生产G18331用G256三G3624精馏工艺（G2375）。G8504G3818G712G1017G7696G6523制G256三废G257的G6502G6930、G12366气中甲醇的G2559量以及G1457G16789生产G4445G1852、G10627G3671G2367生G12573方G19766参G10043国G1881G3818G1820G17839G13475G20576和方G8873。21甲醇合成工艺计算甲醇合成的工艺参数G712甲醇合成G3624G1849G3624压力514MPA、G1998G3624压力49MPAG712G2115产蒸汽压力为39MPA。甲醇合成G3624G1849G3624G9213G5242225G263、G1998G3624G9213G5242255G263。G5192产30000G2556甲醇G712G5192G5332工G7097为330天G712G7097产甲醇90909G2556。211物料衡算原料天然气G16280G7696（V）G712CH49793、C2H6071、C3H8004、CO2074、N2056、其G4439G7446质002。合成G3624中发生的化G4410G2465G5224G726主G2465G5224CO2H2CH3OH（1）CO23H2CH3OHH2O（2）G2115G2465G52242CO4H2G11CH3G122OH2O（3）CO3H2CH4H2O（4）4CO8H2C4H9OH3H2OG115）8CO17H2C8H188H2O（6）CO2H2COH2O（7）G463G88921G726G13582G311G12907甲醇组成G727G312精甲醇中甲醇G2559量G727G313G464工G1006生产中G8991G5483G1314压G7114G712G8611生产1G2556G12907甲醇G4613G1262产生152M3（G7643G5589）的甲A27A28A29A30A31A32A33A34A354G9931G712G2375152/224007KMOLCH4G712设计中G8611G4579G7114甲G9931的生成量为152G1044282（G7097产G12907甲醇量）6357NM3/HG7126357/224284KMOL/H。（G12907甲醇G4579G7114产量为4282T/H）由G1122甲醇G1849G3624气中G8712G2559量G5468G4581G712G5585G11065G1849G3624气G5114G1849的G8712。由G2465G5224（3）G794（6）G5483G1998G2465G5224（2）、（7）生成的G8712分为（7）13008G11G12907甲醇中的G2559G8712量G12381（G2465G52243生成的G8712量）284（G2465G52244生成的G8712量）1473（G2465G52245生成的G8712量）1178（G2465G52246生成的G8712量）G3210959KMOL/H由G1122合成G2465G5224中甲醇主要由CO合成G712CO2主要发生G17882G2476G6454G2465G5224生成CO和H2OG712G1000G1849G3624气中CO2的G2559量G980G14336G993G17241过5G712G6164以计算中G5585G11065G2465G5224（2）。G2029G2465G5224（7）中生成的G8712量为10959KMOL/HG712G237510959G104224G32245481M3/HG463由G1122CO2生成G111410959KMOL/HG712G2375245481M3/H的G8712和CO。G464G12907甲醇中气G1319的G9354G16311量G712G7609氮肥工艺设计手册气G1319压缩氨合成甲醇合成P358附图2气G1319在甲醇中的G9354G16311G5242G994G9213G5242的关系G463表G4645MPA、40G263G7114G712G86111G2556G12907甲醇中G9354G16311其G4439组分如表1G6164示。表1G12907甲醇中气G1319的G9354G16311量气G1319H2COCO2N2ARCH4G9354G16311量（M3/TG12907甲醇）436408157780036502431680G2029G12907甲醇中的G9354G16311气G1319量H24182G104436418250M3/HG2375816KMOL/HCO4182G10408153408M3/HG2375153KMOL/HCO24182G104778032526M3/HG23751452KMOL/HN24182G10403651527M3/HG2375069KMOL/HAR4182G10402431017M3/HG2375015KMOL/HCH44182G10416807023M3/HG2375315KMOL/HG12907甲醇中甲醇扩散损失40G263G7114液G1319甲醇释G6930的G9354G16311气中G712G86111M3G2559有37014G甲醇G712假设减压后液相中除G1120甲醚G3818G712其G4439气G1319G1852部释G6930G1998G712G2029甲醇扩散损失为G（1825325263408152710177023）G1040037014237KG/HG712G2375074KMOL/HG7121658M3/H合成G2465G5224中各气G1319的消耗和生成G5785况表弛G6930气组成A27A28A29A30A31A32A33A34A355气G1319CH3OHH2COCO2N2ARCH4组成0618112916311321082189表合成G2465G5224中消耗原料G5785况消耗项单位消耗原料气成分COCO2H2N2ARG2465G5224（1）M3/H2487894975758G2465G5224（3）M3/H171034200G2465G5224（4）M3/H635719071G2465G5224（5）M3/H1316126328G2465G5224（6）M3/H2103G2465G5224（7）M3/H（2454081）245481245481G8892G726括号G1881的为生成量G712G2465G5224（1）项G993包括扩散甲醇和弛G6930气中甲醇消耗的原料量A27A28A29A30A31A32A33A34A356表合成G2465G5224中生成物G5785况生成项单位生成物组分CH4CH3OHG11CH3G122OC4H9OHC8H18H2OG2465G5224（1）M3/H2487879G2465G5224（3）M3/H8558550G2465G5224（4）M3/H63576357G2465G5224（5）M3/H32919870G2465G5224（6）M3/H262821030G2465G5224（7）M3/H245481表其G4439G5785况原料气消耗消耗项单位A36A37A38A39A40A41A42COCO2H2N2ARCH4A43A44A45A46A47A48M3/H34083252618250152710177023A49A50A51A44A45M3/H16563315A52A53A40M3/H916A54G311A54G8120A54G8120A54G082A54G189A54GA52A53A40A46A44A45M3/H061A54G122A54GG8892G726G为弛G6930气量新鲜气和弛G6930气气量确定CO各项消耗总和新鲜气中CO量G712G23752487879171006357131612103G80324548134081656061G104G916G104G230511977G104G同理G712原料气中其G4439各气G1319的量该气G1319的各项消耗量之和G712由G8504可G5483新鲜气中各气G1319流量。表新鲜气组成A41A42A55A56COCO2H2N2ARCH4A40A57M3/H230511977A54G278007311A54G5367218242A54G1527321A54G1017082A54G666189A54GA58A59A40M3/H795340810183A54GA27A28A29A30A31A32A33A34A357新鲜气中惰性气G1319（N2AR）百分比G1457持在042G712G2465G5224过程中惰性气G1319的量G1457持G993G2476G712（N2AR）2544403G104GG712G2029795340810183G（2544403G104G）/042G16311G5483G856680M3/HG712G2375弛G6930气的量为856680M3/HG712由G可G5483新鲜气量为8825766M3/H。由弛G6930气的组成可G5483表弛G6930气的组成A40A60CH3OHH2COCO2N2ARCH4A41A610618182916311321082189A40A57M3/H5226695622784712664627498702916188表新鲜气组成A40A60CH4H2COCO2N2ARA41A6101968812707345033009A40A57M3/H1685460731582388807304653290258043G5502G10627气气量的确定G1G3G4G5G6G803G7G803G8G5347中G1G1998G3624气气量G712M3/HG3新鲜气气量G712M3/HG4G5502G10627气气量G712M3/HG5主G2465G5224生成气量G712M3/HG6G2115G2465G5224生成气量G712M3/HG7主G2465G5224消耗气量G712M3/HG8G2115G2465G5224消耗气量G712M3/HG524878791656061G10485668249476M3/HG68558556357635732919872628210324548124548155758M3/HG7248787949765816563312061G104856687484283M3/HG8171003420063571907113161263282103044691245481245481672894M3/H已知G1998G3624气中甲醇G2559量为584G712G2029（G40618566806124878791656）/G100584A27A28A29A30A31A32A33A34A358G16311G5483G443492107M3/H表G5502G10627气组成A40A60CH3OHH2COCO2N2ARCH4A41A610618182916311321082189A40A57M3/H26530235315592398387713526041396098356637822000G5502G10627比、CO和CO2单程转化率的确定G5502G10627比RG4/G343492108/8825766493CO单程转化率G726（23017025226）/（23888073983877）G104100362CO2单程转化率G726245481/（3046531352604）G1041001481G1849G3624和G1998G3624气组成G1G3G4G5G6G803G7G803G847226882M3/HG7122108334KMOL/HG2G3G45231787M3/HG7122108334KMOL/H表G1849G3624气组成A40A60CH3OHH2COCO2N2ARCH4A41A6100679111218317272070160A40A57M3/H265303413887563726841657257142512336468838854KMOL/H1332184771228449673986636211628138649表G1998G3624气组成A40A60H2COCO2N2ARCH3OHA41A617629861293302077584A40A57M3/H36029463406575613851331425123364682760063KMOL/H1608459181506618366368116281123216A40A60CH4A62CH3A632OC4H9OHC8H18H2OA41A61179001800070006062A40A57M3/H84521185532912628291228KMOL/H3772838114711713002G1849G3624气COG5502G10627气中CO新鲜气中COG712G2375238887939838776372684M3/HG1998G3624气中COG1849G3624气中COG803G2465G5224消耗的COG2465G5224中生成的COG712G23756372684G8032487879G80317100G8036357G80313161G803210301656061G1048566802454814065756M3/HA27A28A29A30A31A32A33A34A359甲醇分离器G1998口气G1319组成的确定甲醇分离器G1998口气G1319组分G5502G10627气气G1319组分弛G6930气气G1319组分G712G2029甲醇分离器G1998口气G1319中CO气量G5502G10627气中CO弛G6930气中CO3983868784814062348M3/H表分离器G1998口气G1319组成A40A60CH3OHH2COCO2N2ARCH4A41A610618182916311321082189A40A57M3/H27054636011202406237513792801423566363687838185KMOL/H12078160764318135661575635521623637419原料计算合成气总量AG72613322844967398638649398463KMOL/HG8611M3天然气中AG2559量B1/100G104（9793G104071）/16043（071A6413553）/3007（00420102）/44097（07419760）/4401G320044461KMOL/HG2029G8611G4579G7114天然气用量CG726CA/B896104M3/H燃料用天然气87103M3/HG712总用量983104M3/H212热量衡算1）合成G3624的热平衡计算G1852G3624热平衡方程G5347为G726Q1QRQ2Q3QR（1）G5347中Q1G1849G3624气各气G1319组分焓G712KJ/HQR合成G2465G5224G994G2115G2465G5224的G2465G5224热G712KJ/HQ2G1998G3624气各气G1319组分焓G712KJ/HQ3合成G3624热损失G712KJ/HQ沸腾G8712吸收热量G712KJ/HQ1（G1CM1TM1）（2）G1G1849G3624气各组分流量G712M3/HCM1G1849G3624气各组分的比热容G712KJ/KMOLKTM1G1849G3624气G1319G9213G5242G712KQ2（G2CM2TM2）（3）G2G1998G3624气各组分流量G712M3/HCM2G1998G3624气各组分的比热容G712KJ/M3KA27A28A29A30A31A32A33A34A3510TM2G1998G3624气G1319G9213G5242G712KQRQR1QR2QR3QR4QR5QR6QR7（4）QR1、QR2、QR3、QR4、QR5、QR6分别为甲醇、甲G9931、G1120甲醚、异丁醇、辛G9931、G8712的生成热G712KJ/HQR7CO2G17882G2476G6454G2465G5224的G2465G5224热G712KJ/HQRGRH（5）GR各组分生成量G712KMOL/HH生成G2465G5224的热量G2476化G712KJ/KMOL（1）G1849G3624热量计算通过计算可G5483到514MPA、225G263G7114G1849G3624气G1319各组分的热容G712根据G1849G3624气G1319各组分的量G712算G1998甲醇合成G3624G1849G3624热量如表G6164示。表甲醇合成G3624G1849G3624热量A40A60CH3OHH2COCO2N2ARCH4A65A66KJ/KMOLK6704295429884418294725164682A40A57A67KMOL/H133218477122844967398663621628137449A68A69A65A70A71KJ/HK8959854581412850108832687011874914096291753362A72A73A74A57A75A7670478400KJ/HKG6164以G712Q170478400498153511108KJ/H（2）G3624G1881G2465G5224热的计算G5585G11065甲醇合成G3624中G2465G5224（2）生成的热量G712按G2465G5224（1）、（3）、（4）、（5）、（6）、（7）生成的热量如表G6164示。表甲醇合成G3624G1881G2465G5224热A40A60CH3OHA62CH3A632OC4H9OHC8H18CH4COA77A61A74KJ/KMOL102374962200399579811569A644292A77A61A57A67KMOL/H1220253811471141300810959A78A79A74A67KJ/H1249169925189052202945733011208366150489552A6447036028A75A761369108KJ/H（3）合成G3624G1998G3624气G1319总热量计算A27A28A29A30A31A32A33A34A3511表甲醇合成G3624G1998G3624气G1319组分热容和热量A40A60H2COCO2N2ARCH3OHA65A66KJ/KMOLK295630014504296125167205A40A57A67KMOL/H1608459181506618366362116281123206A80A69A65A70A71KJ/HK4754604954469952785092188346316281123216A40A60CH4A62CH3A632OC4H9OHC8H18H2OA75A76A65A66KJ/KMOLK481418031923101733625A40A57A67KMOL/H3772838114711413002A80A69A65A70A71KJ/HK1816227687028291159847132469257598G1998G3624气G1319G9213G5242为255G263G712G237552815K。Q269257598528153658108KJ/H（4）G1852G3624热量损失的确定G1852G3624热损失为4G712G2375Q3（Q1QR）G1044（3511G1041081369G104108）G1044195G104107KJ/H（5）沸腾G8712吸收热量的确定由公G5347（1）可G5483G712QQ1QRG803Q2G803Q31027G104108KJ/H表G1852G3624热平衡表A40A60A40A60A81A74A78A79A74A82A83A74A84A85A86A87A74A75A76A72A73A40A60KJ/H3511A881081369A88108A89A90A91A91A92A88108A93A73A40A60KJ/H3658A88108195A88107A94A90A92A95A96A88108A89A90A91A91A92A881082）G1849G3624气G6454热器的热量计算（1）G1849G6454热器的被加热气G1319热量的确定表G1849G6454热器的被加热气G1319的各组分的热容和显热A40A60CH3OHH2COCO2N2ARCH4A74A97KJ/KMOLA98K9587292529443847294725183966A40A57KMOL/H1332184771228449673986636211628137449A74A57KJ/HA98K12769854045576837556228462411874914096291485228A75A76A74A5769164844KJ/HA98KG6454热器的G1849口G9213G5242为40G263G712G2029G1849G6454热器的被加热气G1319热量为69164844313152166G104108KJ/H（2）G1998G6454热器的被加热气G1319热量的确定A27A28A29A30A31A32A33A34A3512G1998G6454热器的被加热气G1319的显热G1849合成G3624气G1319的显热G712G23753511G104108KJ/H（3）G1849G6454热器的热气G1319热量的确定G1849G6454热器的加热气G1319的显热G1998合成G3624气G1319的显热G712G23753658G104108KJ/H（4）G1998G6454热器的热气G1319热量的确定被加热气G1319吸收的热量G1998G6454热器的被加热气G1319的显热G803G1849G6454热器的加热气G1319热量的显热3511G104108G8032166G1041081345G104108KJ/HG6164以G712G1998G6454热器的加热气G1319的显热量G1849G6454热器的加热气G1319的显热量G803被加热气G1319吸收的热量3658G104108G8031345G1041082313G104108KJ/H（5）G1998G6454热器的加热气G1319的G9213G5242的确定假设G1998G6454热器的加热气G1319各组分热容G994G1998G3624G7114相同G712G2029G1998口G9213G5242为2313G104108/6916G10410833395KG712G2375608G2633）G8712冷器热量的计算（1）G8712冷器热平衡方程G5347Q1Q2Q3Q4Q5G5347中Q1G1849G6454热器气G1319显热G712KJ/HQ2气G1319冷凝G6930热G712KJ/HQ3G1998G8712冷器气G1319显热G712KJ/HQ4G12907甲醇液G1319显热G712KJ/HQ5冷却G8712吸热G712KJ/H（2）G8712冷器G1849口气G1319显热的确定G8712冷器G1849口气G1319的显热G1849G3624气G6454热器G1998口加热气G1319的显热G712G23752313G104108KJ/H（3）G8712冷器G1998口气G1319显热的确定表G8712冷器G1998口气G1319各组分的热容和热量A40A60CH3OHH2COCO2N2ARCH4A74A97KJ/KMOLA98K9587292529443847294725183966A40A57KMOL/H12078160764318135661575635521623612078A74A57KJ/HA98K1157919470235575339121236879118728764084981484037A75A76A81A7459654799KJ/HA98KG8712冷器的G1998口G9213G5242为40G263G712G2029G1998G8712冷器的气G1319热量为59654799313151868G104108KJ/HA27A28A29A30A31A32A33A34A3513（4）G1998G8712冷器的G12907甲醇液G1319热量的确定表G12907甲醇中液G1319组分气化热和液G1319热容A41A42A62CH3A632OC4H9OHC8H18H2OCH3OHA85A99A74KJ/KG531755778130705226098111793A100A60A101A74A97KJ/KGA98A102263825962264187272表G1998G3624气在G8712冷器中冷凝G6930热量A41A42A62CH3A632OC4H9OHC8H18H2OCH3OHA103A104A57KG/H17565108721338323419239060A53A74A57KJ/H934018862819494109250529503429436663458A75A76A105A103A106A46A103A104A53A74A57492A88107KJ/H表G12907甲醇中各组分液G1319显热A41A42A62CH3A632OC4H9OHC8H18H2OCH3OHA100A60A101A74A97KJ/KGA98A102263825962264187272A74A57KJ/HA98A10246335282243024698056210624320A75A7611709687KJ/HA98A102G12907甲醇G9213G5242为40G263G712G2029G12907甲醇的热量为1170968731315367G104107KJ/H（5）G8712冷器冷却G8712吸收的热量由G8712冷器热平衡方程G5347可知G712Q5Q1Q2G803Q3G803Q4G2375Q52313G104108492G104107G803367G104107G8031868G104108570G104107KJ/H（6）冷却G8712用量的确定G1849口冷却G8712G9213G5242为20G263G712G1998口冷却G8712G9213G5242为35G263G712平均比热容为4187KJ/KGA98A102A67A107570G104107/（3520）4187G32907105KG/HG712G2375907T/HG463流程中并联G11142个G8712冷器G712G6164以G8611个G8712冷器用G8712量为4535T/HG712吸收热量为285G104107KJ/HG712G2375719G104107W（WKJ/H）G46422甲醇精馏工艺计算G5192产精甲醇30G987G2556G712G5332工G7114G19400为G8611G5192330天G712连续操作G712G8611G4579G7114精甲醇的产量为3789G2556。通过三G3624精馏工艺G712精甲醇的纯G5242可达999G712G12538合精甲醇国家G980级G7643准。三G3624精馏工艺甲醇的收率达97G712G2029G1849预精馏G3624的G12907甲醇中甲醇G2559量3789/0973706T/H。由G12907甲醇的组成通过计算可G5483G712A108A109A110A111A112A113A114A115A11614G12907甲醇3706/093404182T/HG1120甲醚4182100004217564KG/HG712G2375381KMOL/HG712855M3/H高级醇（以异丁醇计）4182100002610872KG/HG712G2375147KMOL/HG7123291M3/H高级G9931烃（以辛G9931计）4182100003213383KG/HG712G2375117KMOL/HG7122628M3/HG87124182100056234192KG/HG712G237513008KMOL/HG712291354M3/H221物料衡算222热量衡算23设备选型及其计算1）甲醇合成G3624（1）传热G19766积的确定选用G2027G12661G5347合成G3624G712传热量为1027G104108KJ/HG712合成G3624G1881的总传热系数取300W/M2G263G712由公G5347QKATMG5483G712AQ/KTM1027G104108/3003695092M2（2）催化剂用量的确定G1849G3624气G12366速为12000HA1171G712G1849G3624气量为522987873M3/HG712G6164以催化剂G1319积为522987873/1200043581M3（3）传热G12661数的确定传热G12661选3235、长G5242为12000M的钢G12661G712G7460质为00CR18NI5MO3SI2钢。由公G5347A314DLNG712G5483NA/314DL95092/3140025129347其中因要G4445G6502拉杆需要减G458132根G712故实际G12661数为9315根。（4）合成G3624壳G1319直径的计算合成G3624G1881G12661子G6502布G18331用正三角形G6502G2027G712G12661G19400距A40MMG712壳G1319直径DI为DIA（BG8031）2LG5347中AG12661G19400距G712MM。为40MMBB11N05119347051062L传热G12661长G5242G712M。125G6164以G712DIA（BG8031）2L40（1062G8031）21254457G712圆整后取4600MM。（5）合成G3624壳G1319厚G5242的确定壳G1319G7460料选用13MNIMONBR钢。壁厚的计算公G5347为A118A119A120A121A122A123A124A125A12615SPCDI/2TG803PCG5347中S合成G3624壳G1319厚G5242G712MMPCG712为5MPADI合成G3624壳G1319直径G712MMG712为4600MMT1900MPA（取壳G1319G9213G5242为50G263）085SPCDI/2TG803PC54600/（21900085G8035）7232MM取C22MMG712C1025MMG712圆整后取S75MMG712复G2057675645025G712故最终取C1025MMG712S75MM（6）合成G3624G4565G3848的确定G990下G4565G3848均取G2334G10711形G4565G3848G712G7460质选用和G12582G1319相同。由G4565G3848厚G5242计算公G5347SPCDI/4TG803PCG5347中S合成G3624G4565G3848厚G5242G712MMPCG712为55MPADI合成G3624G4565G3848直径G712MMG712为4600MMT1900MPA（取壳G1319G9213G5242为50G263）10SPCDI/4TG803PC554600/（4190010G80355）3354MM取C22MMG712C1025MMG712圆整后取S36MMG712复G20576366216025G712故最终取C1025MMG712S36MM实际制G17908中取G4565G3848和G12582G1319均为75MMG712G2029G4565G3848为DN460075（7）G6521G12661的确定G1849G3624气和G1998G3624气G6521G12661G18129G18331用35022的钢G12661G712G18209用G8873G1860WNG803FF350G80363HG20595。G1849G3624沸腾G8712和G1998G3624蒸汽G6521G12661G18331用25018的钢G12661G712G18209用G8873G1860WNG803FF350G80363HG20595。G1166G4392选用G7643准圆形DN450MM的G1166G4392。G2380催化剂G6521G12661DN600MMG712G16045G5243G1166G4392DN600MM。G6164有的G5332G4392G17839G15904G12573G19766积G15929G5390G712在G5332G4392G3818G19766G9950G6521G990G980G3371G994容器G7460料和厚G5242G18129相同的20R钢G7507。（8）G6252流G7507的确定A118A119A120A121A122A123A124A125A12616G6252流G7507为G5351形H3/4DI3/446003450MMG712G6252流G7507数量为5G712G19400距取2000MMG712G6252流G7507最G4579厚G5242为22MMG712G7460料为Q235G803A钢。拉杆16G712G186132根G712G7460料为Q235G803AF钢。定距G126612525。（9）G12661G7507的确定G12661G7507直径4600MMG712厚G5242100MMG712G12661G7507G9950G6521在G12582G1319和G4565G3848之G19400。（10）G16045G5243的确定G6915G5243G18331用G16045G5243G712G16045G5243G5243G1319厚G5242为75MMG712基G11796G10627G1881径为4000MMG712G3818径4850MMG712基G11796G10627厚G5242为20MMG712G3332G14062G15758G7655公G12228直径M30G712数量为24个。（11）合成G3624设计G13479G7536G8731总2）G8712冷器的设计（1）传热G19766积的确定G1016G13941流G1319的G17839G1998口G9213G5242为热流G1319（G1998G6454热器的气G1319）608G27940G263冷流G1319（G5502G10627G8712）35G27720G263表合成G3624设计G13479G7536G8731总表A127A128A129A130MM4600A131A132A133A134A1355A136A137MM75A138A139MM2000A140A141A142A143A144A145A146A143A130MM2300A147A148MM750A136A137MM75A149A150A150A15112000A152A153A154A155MM16A134A1359315A134A13532A154A155MM3225传热G6524动力TM（608G80335）G803（4020）/LN（608G80335）/（4020）2278G263取总传热系数K900W/M2G263G712由传热速率方程G5347QAKTM，可G5483AQ/KTM791199468/2268900386M2G5347中AG8712冷器的传热G19766积G712M2Q传热量G712WK总传热系数G712W/M2G263TM传热G9213G5058G712G263（2）G12661子数N的确定选用2525的G7092G13553钢G12661G712G7460质20号钢G712G12661长75MG712由公G5347A314DLNG5483G712G5347中AG8712冷器的传热G19766积G712M2A118A119A120A121A122A123A124A125A12617DG8712冷器的G12661径G712MLG8712冷器的G12661长G712MNG8712冷器的G12661子数G712MNA/314DL386/31400275820根G712其中G4445G6502拉杆需要减G45818根G712实际G12661数为812根。（3）G12661子的G6502G2027方G5347、G12661G19400距的确定正三角形G6502G2027G712G12661G19400距取A32MM（4）壳G1319直径的确定DIA（BG8031）2LG5347中DIG8712冷器壳G1319G1881径G712MMAG12661G19400距G712MMB正G1857角形G4557角G13459G990的G12661子数G712G7609有关表取29L最G3818G4630G12661子的中G5527到壳壁G17805G13548的距离G712MM。取L2D0D0G12661子的G3818径G712MMG6164以G712DIA（BG8031）2L32（29G8031）2225996MMG712取DI1000MMG6454热器为G2363G5347G712G980G14336要G87266G728L/DIG72810G7127500/100075G712G9397G17287要G8726。（5）壳G1319厚G5242的计算壳G1319G7460料选用20R钢G712壁厚的计算公G5347为G726SPCDI/2TG803PCG5347中SG8712冷器壳G1319厚G5242G712MMPC计算压力G712取4911539MPADIG8712冷器壳G1319直径G712MMG712为1000MM50132MPA（取壳G1319G9213G5242为50G263）085SPCDI/2TG803PC5351000/（2132085G803539）2461MM取C22MMG712C1025MMG712圆整后取S28MMG712复G20576286168025G712故最终取C1025MMG712S28MM（6）G8712冷器G4565G3848的确定G990、下G4565G3848均G18331用G7643准G7937圆形G4565G3848G712G4565G3848为DN100028。G7366G19766高G5242H1250MMG712直G17805高G5242H240MMG712G7460料选用20R钢。（7）G8712冷器G8873G1860的确定A118A119A120A121A122A123A124A125A12618选用16MNR钢G712根据JB47032000G7643准G712选用PN64MPAG712DN1000MM的G8063G8145G4506G4565G19766长G20060G4557G9950G8873G1860。（8）G6252流G7507的设计G6252流G7507为G5351形G712H3/41000750MMG712G6252流G7507G19400距取1500MMG712最G4579厚G5242为10MM。G6252流G7507G3818径994MMG712G6252流G7507G5332G4392直径为258。G7460料为Q235A钢G712拉杆选用16G712G18618根G712G7460料为Q235AF钢。（9）G5332G4392G15929G5390G8712冷器G4565G3848和壳G1319G990的G6521G12661G18129需要G15929G53