苯-甲苯精馏装置的设计

A1A2A3A1A0A4A5A6A7A8A9A10A111化工过程课程设计课程题目姓名学号指导老师专业化学工程与工艺化学化工学院2011年7月8号A1A2A3A1A0A4A5A6A7A8A9A10A112目录1本科学生课程设计任务书511设计任务及操作条件512学生应完成的工作52设计方案的确定及流程概述621设计方案的确定622流程概述63工艺计算731物性数据的收集732精馏塔物料衡算833回流比的确定94主体设备计算1341填料塔的塔径的计算13411平均分子质量的计算14412平均密度的计算14412平均粘度的计算15413泛点的计算15414塔径的计算16A1A2A3A1A0A4A5A6A7A8A9A10A11342计算塔高17421填料的选择17421液体的平均表面张力M17422精馏段高度18423提馏段高度18424塔顶高度18425中间高度18426底部高度18427塔体总高度1943塔体厚度设计1944塔体水压校核1945塔体封头的选择195填料层压力降的计算206塔主要附属构件结构尺寸计算设计2061液体分布器20611喷淋密度的确定及分布器的设计20612布液计算2162导流板2263接管的设计22631塔顶蒸汽管22632回流管22633进料管23634釜液出口管23635塔釜蒸汽管24A12A13A14A12A15A16A17A18A19A20A21A22A2347主要辅助设备2471进料加热器24711进料加热器24712进料加热器所需的加热介质量2572进料泵2573冷凝器26731冷凝器26732冷凝器所需的加热介质量2674再沸器27741再沸器27742再沸器所需加热介质量2775冷却器278设计结果及总结2881设计结果表2881设计结果汇总表2882综合评述299附录30A12A13A14A12A15A16A17A18A19A20A21A22A2351本科学生课程设计任务书11设计任务及操作条件1处理量及原料6T/H混合物料，温度25，质量含量为苯30，甲苯70。2主设备类型钢鲍尔环填料型精馏塔。3操作条件及要求1馏出液中苯含量99质量，釜液中甲苯含量99质量；2泡点进料，常压操作；3加热介质为05MPA饱和水蒸汽，冷却介质为25循环冷却水。12学生应完成的工作1设计方案的确定及流程概述；2填料塔的塔径、填料层高度、塔高、填料层压降计算；3塔及主要附属构件结构分布器、导流板、接管尺G4556设计；4主要G17753G2173设备计算G994选型进料G8905、进料加热器、再沸器、冷凝器；5G13484G2058PIDG5049G14414流程G3282、G17722间布G13634G3282、填料塔G16025G18209G3282；6G4557G7424设计的G13520合G16792述。A24A25A26A24A27A28A29A30A31A32A33A34A3562设计方案的确定及流程概述21设计方案的确定G7424设计为分G12175苯甲苯的G1120G1815混合物，G5194G18331G11004钢鲍尔环填料精馏塔进G15904G17842G13505精馏，设计中G18331G11004泡点进料，常压操作。G17902G17819进料加热器G4570原料液加热G14279泡点，进G1849填料塔，塔顶G990G2331蒸汽G17902G17819冷凝器冷凝，G5194确定G1866G7380G1351回流G8616，G980部分作为回流液流G1849塔G1881，G1866G1325馏出液G17877G14279G1660G13604。釜液G11004间接蒸汽加热，釜底G1147G2709G13475G17819冷却G17877G14279G1660G13604。22流程概述苯甲苯的精馏分G12175G16025G13634G2265G6336主设备填料精馏塔、G1660G13604、进料G8905、原料加热器、再沸器和冷凝器。填料精馏塔G17836G2265G6336G1866G17753G2173设备，G3926液体分布器、导流板和接管G12573。原料液G1186原料液G1660G13604中G17767出，G17902G17819原料G8905进G1849原料加热器，原料加热器G4570原料液加热G14279泡点，泡点原料进G1849填料塔中进G15904精馏分G12175。塔顶G990G2331蒸汽G13475G17819冷凝器冷凝，部分进G15904回流G17832回塔G1881，馏出液进G1849G12540G1660G13604中G1660G4396。釜液部分G13475G17819再沸器G8680G2282进G1849塔底，G1866G1325G4570进G1849流G1849甲苯G1660G13604G1660G4396。A36A37A38A39A38G328221苯G16甲苯精馏分G12175方G7706流程G3282A40A41A27A28A42A43A44A45A46A47A45A48A49A45A40A41A50A51A45A40A41A24A25A26A24A27A28A29A30A31A32A33A34A3573工艺计算31物性数据的收集表31苯G16甲苯的物G5627G6980G6466A52A53A29A54A55A29A54A56A57A58A59A60A57A59A61A62A63A64A65A66A57A67A59A60A57A61A68A69A49A70A57A71A72A73A74A44A57A67A75A76A57A59A60A69A77A44A57A75A76A57A67A59A60A78A75A69A79A66A57A80A81A82A68A83A84A78A85A86A87A88A89A90A91A57A67A80A81A82A92A57A75A69A93A94A95A96A57A67A80A81A82A92A97A57A61A69A24A98A99A100A99A101A102A103A80A80A102A101A104A102A81A103A80A105A104A105A103A104A80A103A101A106A81A103A101A105A101A80A107A103A108A107A102A103A106A26A24A98A109A100A110A104A107A103A80A105A102A106A101A80A80A81A103A106A105A106A105A103A108A80A103A101A81A103A106A101A111A80A81A103A104A107A101A103A104表32苯G16甲苯的温度G994密度、粘度及表面张力G1863G13007表A112A113A114G2529G12228温度/6080100120苯的密度KG/M38366815079257689甲苯的密度KG/M38293810079037700苯的粘度MPS0381030802550215甲苯的粘度MPS0373031102640229苯的表面张力MN/M2374212718851649甲苯的表面张力MN/M2394216919491734表33苯G16甲苯的G11468平G15925G6980G6466平G15925温度TG708G709液G11468苯XG8680G11468苯Y平G15925温度TG708G709液G11468苯XG8680G11468苯Y110560090115575510991125888607911087937118763658251076151128652708571050510208854475885102792037784480912A115A116A117A115A118A119A120A121A122A123A124A125A126898842544283338593971330507822590959955835566811195989409406198066979889269456678021999961914507138001100100表34钢鲍尔环的结构G10317G5627G2454G6980G1856G12228G11464径/MM16253850G1022G6980/1/3M14300055900130006500G3546G12227密度/G7083MKGG709216427365395G4392G19565G10587/G7050928093409450949G8616表面G12227/1M2392191291123填料G3252子/G7081MG70929926915313132精馏塔物料衡算G11013G1122精馏G17819程的计算均G1209G6717尔分G6980为G1946，需G1820G6238设计要求中苯和甲苯的质量分G6980G17728G2282为G6717尔分G6980。原料液G13464G6116中苯的G6717尔分G6980336092/7078/3078/30876666HCHCHCFNNNX塔顶馏出液含苯的G6717尔分G6980992092/178/9978/99876666HCHCHCDNNNX塔底釜液含苯的G6717尔分G6980012092/9978/178/1876666HCHCHCWNNNX原料液的平均G6717尔质量A127A128A129A127A130A131A132A133A134A135A136A137A1389KMOLKGNNMHCHCF/3896640923360783360133608766塔顶G1147G2709的平均G6717尔质量KMOLKGNNMHCHCD/1780080929920789920199208766塔底G1147G2709的平均G6717尔质量KMOLKGNNMHCHCW/8919880920120780120101208766G4557G1122G2464G13464分的G17842G13505精馏塔，G11013总物料平G15925及分物料平G15925G7389FWDFXWXDXFWDG5483HKMOLF/1967HKMOLD/2122HKMOLW/4498表35G1852塔物料G15925算G2529G12228原料液塔顶液釜液苯的质量分G6980/30991苯的G6717尔分G6980/033609920012平均G6717尔质量/KG/KMOL893781918流量/KMOL/H67192221449833回流比的确定G7693G6466G7380G4579回流G8616G4557G1122G7092G12363G3371塔板，G3698加回流G8616G2499G1209降G1314所需的塔板G6980，G1955G4581塔板G17165G11004。G1306回流G8616的G3698G3835G1075G1262G3698G3835塔顶冷凝器和塔底再沸器的G1268热面G12227，设备G17165G11004G2465G19555回流G8616的G3698加G13792G7389所G990G2331。回流G8616G994G17165G11004的G1863G13007G3282中G4557G5224G7380G1314G17165G11004G7389G7380G17878回流G8616POTR。G980G14336G7380G17878回流G8616的G6980G1552G14551G3272G7171MIN221RRPOTG20056G1820G2474MIN51RRPOTG17902G17819G36SPEN确定G1866G7380G17878回流G8616112POTRA139A140A141A139A142A143A144A145A146A147A148A149A15010G11004G36SPEN进G15904模拟计算，为泡点进料，常压操作，馏出液中苯的质量分G6980为99，釜液中甲苯的质量分G6980为99。填料塔的压降较G4579，G1866冷凝器G994再沸器的压差不G3835。多次计算确定G7380G17878回流G8616。G17767G1849G994G17767出见下G3282G328231流程G3282示G328232进料G17767G1849G328233精馏塔的G17767G1849A151A152A153A151A154A155A156A157A158A159A160A161A16211G328234G17767出结果G328235G17767出结果A151A152A153A151A154A155A156A157A158A159A160A161A162121进料线2塔底G1147G27093塔顶G1147G2709计算机模拟结果G3926下操作回流G8616211R实际板G698023N进料版序号12FN塔顶的温度776DT塔底的温度5116WT进料版的温度695FTG11013G1852塔物料G15925算所G5483HKMOLD/925HKMOLW/143HKMOLF/069泡点进料，塔顶G1852部冷凝。精馏段HKMOLRDL/654925112HKMOLDRDLV/58092511121提馏段HKMOLQFLL/61230691654HKMOLFQVV/580069115801则精馏段方程32068011XRXXRRYD提馏段方程A163A164A165A163A166A167A168A169A170A171A172A173A17413006405411111NWXXFQDRDFXFQDRQFRDYG328235逐板计算4主体设备计算41填料塔的塔径的计算计算泛点G8680速G18331G11004埃克G10317泛点G8680速G1863联G3282法，G1820求G5483横坐标50LVVLWWX然后查埃克G10317泛点G8680速G1863联G3282G5483G4557G5224的纵坐标，G7389202202LLVLLVVGUGWYG7693G6466纵坐标的计算式G2499G1209求出泛点G8680速U，再G7693G6466UVDPI4就G2499求出塔径。A175A176A177A175A178A179A180A181A182A183A184A185A18614411平均分子质量的计算精馏段塔顶99201DXY，97901XG708查G11468平G15925G6980G6466G709KG/KMOL1789299201117899201VMKG/KMOL37892979017897901LM加料板520FY，350FXG708查G11468平G15925G6980G6466G709KG/KMOL784925201785202VMKG/KMOL187923501783502LM精馏段的平均G6717尔质量KG/KMOL4812/784178VMKG/KMOL7822/187378LM计算质量流速塔顶G994进料口的算术平均G1552HKGWV76552580481HKGWL425415654782412平均密度的计算塔顶温度776T，G11013此查表3MKG67818A187，3MKG28813A188A189结合苯的质量分G6980A99G7053L1L100MKG3381811A190A191A191AA进料口温度695FT，G11013此查得3MKG37796A187，3MKG69793A192A193结合苯的质量分G6980A30G7053L2L200MKG7945311A194A195A195AA则3L4380625379433818MKGG4557G1122G8680G11468，G7693G6466NRTPV。A196A197A198A196A199A200A201A202A203A204A205A206A20715塔顶31792776273273422178MKGV进料口32782695273273422784MKGV3V78522782792MKG412平均粘度的计算查G5483塔顶粘度SMP3200A208，SMP3210A209A210，同样G7693G6466质量分G6980计算0320MPS11L1100LAAA211A212A212查G5483塔底粘度SMP2660A208，SMP2270A213A214，G11004G11468同方法计算0237MPS11L2200LAAA215A216A216SMPL2780223703200413泛点的计算代G1849横坐标计算式G7389049050LVVLWWXG328241埃克G10317G3282A217A218A219A217A220A221A222A223A224A225A226A227A22816G1186埃克G10317G3282G990查G5483纵坐标Y018。G11013202202LLVLLVVGUGGY代G1849G1209G990G6980G6466解G5483SMF1321安G1852G13007G698005G1608之间，G2474安G1852G13007G6980为05，G7380终圆整G2499G5483U106M/S。414塔径的计算精馏段塔径MUVDS8860061143360078527655244PIA229提馏段提馏段G994精馏段的计算方法G980致,求G5483平均G6980G6466G3926下平均G11468G4557分子质量KMOLKGMV/288KMOLKGML/389A230A231A232A230A233A234A235A236A237A238A239A240A24117平均质量流量HKGWV/17100HKGWL/4811037平均密度3/7652MKGV3/8783MKGL液G11468平均粘度SMPL2580代G1849横坐标计算式G73890923050LVVLWWXG1186埃克G10317G3282G990查G5483纵坐标Y012。G7380后计算G2499G5483SMF5012。G2474安G1852G13007G6980为05，G7380终圆整G2499G5483U075M/S。提馏段塔径MUVDS10081750143360076521710044PIA242向G990圆整后G2474塔径D1200MM。42计算塔高421填料的选择在精馏操作时，填料塔的接触效G10587要求很高，G11013G1122处理量G8616较G3835。G7424次选G11004G1856G12228G11464径为38MM的金属鲍尔环，421液体的平均表面张力M塔顶MN/M6721,A243D；MN/M0622,A244A245DG708767G709MN/M67219790962620210672106226721DBBDXXA246A247A247A246A247A247进料板MN/M3919,A248F；MN/M9719,A249A250BFG708956G709MN/M76193509719650391997193919FABBFXXA251A252A252A251A252A252A253A254A255A253A3A0A1A2A4A5A6A7A818精馏段MN/M71202/67196721M422精馏段高度G7693G6466G13475验G1856式计算HETPA9A10A11LLHHETPLN471LN2921LNH70779精馏段MMHETP470111NMNHETPH251147001A12423提馏段高度提馏段G994精馏段做法G980致提馏段MMHETP380122NMNHETPH641238002A13424塔顶高度塔顶G2474空间高度MH51A14425中间高度填料层间高度G2474MH50A15426底部高度塔底高度设G1866持液量为10MIN。4612DHWVLLPIA16。加G990安G16025接管G12573，塔底高度为MH2A17。A18A19A20A18A21A22A23A24A25A26A27A28A2919427塔体总高度塔体总高MHHHHHH813250516425A30A31A32A33A34A35塔体总高为13800MMG708除封头的高度G709。43塔体厚度设计选择塔体材料为16MNRA36A37A38,G18331G11004G2464面焊接，百分之百G7092损检测，焊接接头G13007G69801。KPAPC3111103101计算壁厚1200,3902MMDMMPDPICTIC设计壁厚2392239022CCDG2529义壁厚250MMC3121圆整CCNG13475稳定G5627校核G24745MM。44塔体水压校核G11013G1856式MPAPPTT14017017011130251251MMCNE7522523MPADPEEITT6302MPAST531013459090G1866水压强度足够。45塔体封头的选择G11013塔径为1200MM。选择标G1946椭圆形封头1K。A39A40A41A39A42A43A44A45A46A47A48A49A50201200,400502MMDMMPDKPICTIC250MMC3121圆整CCN稳定G5627校核后G24744MM5填料层压力降的计算实际速度的计算精馏段实际空塔汽速SMDVSU/980/42PI,提馏段实际空塔汽速SMDVSU/690/42PIG7693G6466ECKERTG1863联G3282求乱G3546填料的压降精馏段横坐标0049纵坐标1930202LLVGUYG11013此G2499G5483到精馏段填料总压降为255KPA。提馏段横坐标00923纵坐标130LLVFGUG11013此读G3282G2499G5483提馏段填料总压降为451KPA。6塔主要附属构件结构尺寸计算设计61液体分布器611喷淋密度的确定及分布器的设计G7693G6466ECKERT建议A515A52，G11013DG3835G1122G12573G11221200,喷淋密度为42点/MA53,G11013G1122负荷较G3835，故喷淋密度G2474120点/MA53液点G6980为222/1362002178502007850MDNA54设计结果为G1120级槽共设7道，在槽侧面开G4392，槽宽度为80MM，两槽间距A55A56A57A55A58A59A60A61A62A63A64A65A6621为160MM，槽高度为120MM布点G18331G11004三角形G6502G2027，实际布点G6980为132。G328261分布器示G5859G3282612布液计算布液分布G11013HGNDLS2420PIG2474MMH160,600G5114G1849G1209G990G6980G6466G2499G5483G1856式MMHGNLDS424500PI设计G2474MMDO4。A67A68A69A67A70A71A72A73A74A75A76A77A782262导流板在G16825设计中，液体的流速G18129较G4579，不G5529G16025设导流板导流板。63接管的设计A79A80A81A82A83A84A85A86A87A88A89A90A91A92A93A94A92A95A96A97A98A99A92A100A101A82A83A102A103A104A105A84A106A107A108A109A92A110A101A82A83A102A103A104A105A84A111A112A68A106A112A107A108A109A113631塔顶蒸汽管G11013G2081面物料G15925算G5483SMV/627036007852178580，蒸汽管G980G14336G17878G4464流速为15G79425M/SG2474蒸汽管流速为U15M/S，则塔顶蒸汽管管口G1881径为MVD22205162704154PIPI选G2474G7092G13553钢管G158245G1047MM。设计流速校核SMU4971207004520627042PIG13475校核管道G17878合。632回流管G11013G2081面物料G15925算G5483SKGHMLWL1861KG34264178654G7389G990面密度求算结果G2499G11705回流液密度3KG33818MLG18331G11004G8905G17767G17877回流液，G17878G4464流速为10G79420M/S。G2474回流液流速U15M/S，则回流管G1881径为MUWDLLL033703381851186144PIPI选G2474G7092G13553钢管为G15845G10435MM。校核设计流速A114A115A116A114A117A118A119A120A121A122A123A124A12523SMDWULL/1810035020450338181431861442PIG13475校核在G7380G17878G14551G3272G1881。633进料管进料口的物料G15925算G5483SKGSKGWL/6671/36006000，G1000G2460CTFO695，G6566G1552算出进料液密度，3/53794MKGF。进料G17878G4464流速为04G79408M/S。G2474进料流速U06M/S,则进料管G1881径为MUWDFLF066705379460667144PIPI选G2474G7092G13553钢管G15876G1044MM。设计流速的校核22138905476/0070000252764844FFUKGSDPIPISMDWUFL/6040004020760537941436671442PIG13475校核在G7380G17878G14551G3272G1881。634釜液出口管G11013G2081面物料G15925算G5483SKGHMWWL0991KG63956891143。回流液密度3KG7838ML釜液出口管G980G14336的G17878G4464流速为05G79410M/S。G2474釜液流速U07M/S，则釜液出口管G1881径为MUWDLLL0500878370099144PIPI选G2474G7092G13553钢管G15857G10435MM。校核设计流速，SMDWULL/660003502057087831430991442PIA126A127A128A126A129A130A131A132A133A134A135A136A13724G13475校核所选管道G17878G11004。635塔釜蒸汽管G11013G2081面物料G15925算G5483SMV/7130360076522885803蒸汽管G980G14336G17878G4464流速为15G79425M/SG2474蒸汽管流速为U18M/S，则塔釜蒸汽管管口G1881径为MVD24208171304184PIPI选G2474G7092G13553钢管G158245G1047MM。校核设计流速SMU71207002450713042PIG13475校核所选钢管G17878G11004。表61接管G8731总表管口G2529G12228G7092G13553钢管的G16280G7696塔顶蒸汽管G158245G1047MM回流管G15845G10435MM进料管G15876G1044MM釜液出口管G15857G10435MM塔釜蒸汽管G158245G1047MM7主要辅助设备71进料加热器711进料加热器设计操作条件要求泡点进料，原料温度为25，G13792进料时的泡点温度为956。加热介质为05MPA饱和水蒸G8680，G1866在G16825压力下的温度为1519。饱和水蒸汽冷凝后温度为100。故G1268热条件为91511T，1002T，6952T，251T。A138A139A140A138A141A142A143A144A145A146A147A148A14925G1268热温度差1357LN12211221TTTTTTTTT原料液温G2331所需的热量A150A151A151PWPWXX1PM表71G4557G5224温度下的G8616热G4493G2529G12228温度/25956苯的G8616热G4493/KG45/KG74G4617281698甲苯的G8616热G4493/KG45/KG74G4619371955平均G8616热G4493KKGKJP/8311295417071所需G1268G17894的热量SKJTMQP/25136002569583116000选21000/KWMK,则G2499算出所需G6454热器面G12227为G2474G4439的安G1852G13007G698011所需G1268热面G12227为2841000135710002511111MTKQA选型所选为G5203G5042G6475G10607G6454热设备G7389G19492G1856G2508，选G11004管G3783式G6454热器。见附G5417。G1866G13605G3348为HTTP/G90G90G90G74G93G77IEMACG82M/PRG82G71UCT5HTMG79G3926下表72进料加热器选型A152A153A154A155A156A157A158A156A159A160A158A156A157A161A162A163A164A165A166A167A168A163A164A169A170A167A168A156A171A169A169A172A170A173A170A172A170A174A175A174A174A173A173A173A170A174A174A174712进料加热器所需的加热介质量05MPA饱和水蒸汽为151，冷凝后为100。G2474在G16825温度G14551G3272G1881的平均G8616热G4493为KKGKJCP/264。G11013G1856式SKGTTCQMP135110091512642512172进料泵原料的流量HMV/5575379460003G7693G6466所G5483流量选择式G9177水G8905，G13783G15397安G1852G13007G6980和G17767G17877高度，选择G44G54型G2345G7509G2345G2572G12175G5527G8905。A176A177A178A176A179A180A181A182A183A184A185A186A18726型号G44G5450G25232G252125A188A189A190，G17728速2900N/R/MIN,流量125MA191/H,G6208程20M，效G1058760，G17736G2163G10587113KG90，G11017机G2163G1058722KG90，G5529需G8680G15444G1325量20M，质量32/64KG74。73冷凝器731冷凝器G11013G2081面的物料G15925算G2499G11705冷凝器的热量流量SKGVS/74613600580178冷凝器为G1852凝器，G2474冷却水G2331温后的温度为40，G2033G3999温度为25。G2474冷却后塔顶液体的温度为50。CNO302550407761255040767T查表的767时，KKGKJCP/87911。50时，KKGKJCP/81312。平均G8616热G4493SKGKJCP/8461281318791所要G1268G17894的热量SKJTCVQPS/18072674618461G2474总G1268热G13007G698021000/KWMKG2474G4439的安G1852G13007G69801123033010001018011K11QAMT选型所选为G5203G5042G6475G10607G6454热设备G7389G19492G1856G2508，选G11004管G3783式G6454热器。见附G5417。G1866G13605G3348为HTTP/G90G90G90G74G93G77IEMACG82M/PRG82G71UCT5HTMG79G3926下表73冷凝器选型A192A193A194A195A196A197A198A196A199A200A198A196A197A201A202A203A204A205A206A207A208A203A204A209A210A207A208A196A211A209A209A210A212A213A212A210A214A215A216A215A215A217A218A219A216A213A210A215A215A215732冷凝器所需的加热介质量冷却水G2331温后的温度为40，G2033G3999温度为25。G2474在G16825温度G14551G3272G1881的平均G8616热G4493为KKGKJCP/174。A220A221A222A220A223A224A225A226A227A228A229A230A23127G11013G1856式SKGTTCQMP28125401741802174再沸器741再沸器塔底温度为CT05116A232,KJ/KG0663A233，KJ/KGK3564A234A233G11013G1856式A235A236A2361PWWXXG5483，KKGKJ/5365P热量SKJ010843600/5365389123QG18331G11004间接蒸汽加热，G5062G11705加热介质05MPA的饱和水蒸G8680，G2375温度为151的水蒸G8680，查G17176料G5483此时水蒸G8680的汽G2282G9520热为R20898KG45/KG74,冷凝后为100。则G2499G5483出51MT，选21000/KWMK则G2499算出所需G6454热器面G12227为2M4235110001110001084TK11QAM选型所选为G5203G5042G6475G10607G6454热设备G7389G19492G1856G2508，选G11004管G3783式G6454热器。见附G5417。G1866G13605G3348为HTTP/G90G90G90G74G93G77IEMACG82M/PRG82G71UCT5HTMG79G3926下表74再沸器器选型A237A238A239A240A241A242A243A241A244A245A243A241A242A246A247A248A249A250A251A252A253A248A249A254A255A252A253A241A17A254A254A22A0A0A22A255A24A1A0A23A0A0A1A1A255A1A23A20A22A2A0A0742再沸器所需加热介质量05MPA饱和水蒸汽为151，冷凝后为100。G2474在G16825温度G14551G3272G1881的平均G8616热G4493为KKGKJCP/284。G11013G1856式SKGTTCQMP4801009151284241072175冷却器塔底G17767出温度为CT05116A3,KJ/KGK2015A4，KJ/KGK2042A5A4A6A7A8A6A9A10A11A12A13A14A15A16A1828G11013G1856式A19A21A211P1WWXXG5483，KKGKJ/0412P1冷却后的温度为CT040，KKGKJ/7141P2平均KKGKJPP/8771221PSKJ71643600/40511698448918771Q凝器为G1852凝器，G2474冷却水G2331温后的温度为40，G2033G3999温度为25。CNO737254040511612540405116TG2474总G1268热G13007G698021000/KWMKG2474G4439的安G1852G13007G6980112345737100010716411K11QAMT选型所选为G5203G5042G6475G10607G6454热设备G7389G19492G1856G2508，选G11004管G3783式G6454热器。见附G5417。G1866G13605G3348为HTTP/G90G90G90G74G93G77IEMACG82M/PRG82G71UCT5HTMG79G3926下表75冷却器选型A25A26A27A28A29A30A31A29A32A33A31A29A30A34A35A36A37A38A39A40A41A36A37A42A43A40A41A29A44A42A42A43A45A46A45A43A47A48A49A48A48A50A51A47A49A46A52A48A48A488设计结果及总结81设计结果表81设计结果汇总表G2529G12228设计结果塔径1200MM塔总高13800MM金属鲍尔环G1856G12228G11464径为38MM精馏段高度52M提馏段高度46M塔体厚度5MA53A54A55A53A56A57A58A59A60A61A62A63A6429精馏段填料总压降255KPA提馏段填料总压降451KPA塔体封头厚度为5MM的标G1946椭圆封头喷淋密度120点/MA65液体分布器G1120级槽共设7道，点G6980为132导流板G16G16G16G16G16G16G16G16G16布液计算4MM塔顶蒸汽管G158245G1047MM回流管G15845G10435MM进料管G15876G1044MM釜液出口管G15857G10435MM塔釜蒸汽管G158245G1047MM进料加热器G6454热面G1222748MA66，选型见表8进料G8905G44G5450G25232G252125冷凝器G6454热面G1222730MA66，选型见表9再沸器G6454热面G12227234MA66，选型见表10冷却器G6454热面G12227544MA66，选型见表1182综合评述G256G17347G9471G9471G1866G1474G17840G1858，G2578G4570G990下G13792求G13046G257G17837G7171G6117G13475G17819G17837三G2620设计后G7380G5831G16840的G980G2489G16817。G15441然G14270G5061的设计结果不够理G5831，G1306G7171G1196出G17819，G2174力G17819，G1075G5527G9914G17819，G3268G5797G17819。G8611G5415G14270G5061做出G980G8505就G3921G10317G2047G7389G6116就G5875。G17902G17819此次G16850程设计G6496G6581G1114精馏的方法和流程，G17902G17819查G16822G17176料，G1075G1114解G1114填料塔的构G17908及原理，很多G999G1006G11705G16794G1209及G999G1006G6228G14033G990的提G2331，G1363G6117G7368加G6178实的G6496G6581G1114G11468G1863方面的G11705G16794。G1363G6117G4557G6289G16949的理G16782G7389G1114G1867体的G16760G16794。在设计的G17819程中G17947到很多G19394G20076，G2499G1209G16840G5483G7171G3268G19602G18337G18337，G1075G7304G19718出G1114G2081G7411G6117在G17837方面的G11705G16794G8436G13582和G13475验不足，G1306G2499G2928的G7171在G13781G5084的G6363导下G19394G20076G5483到解决，G17837次G16850程设计终G1122顺G7380A53A54A55A53A56A57A58A59A60A61A62A63A6430终G18129G5483到G1114解决。不G5483不G5875慨实践出真G11705，只G7389G14270G5061动手，才G14033解决G19394G20076，加深印G16949，G1363G6117们G6496G6581的G11705G16794不再G7171纸G990谈兵。在今后社G1262的发展和学习实践G17819程中，不G14033学什么G18129G7171G980G11705半解，G14270G1209为什么G18129G1262，虚G5527学习。让G6117G11705道只要G16760真钻研，动脑思G13783，动手实践，就没G7389弄不懂的G11705G16794。G17837样才G14033在今后的道G17347G990劈荆斩棘，G13792不G7171G11705G19602G13792退，那样永G17840不G2499G14033收获G6116G2163，收获G2928悦，G1075永G17840不G2499G14033G5483到社G1262及他人G4557你的G16760G24999附录A25A26A27A28A67A68A69A31A70A71A72A43A47A73A29A32A33A31A29A30A34A35A36A37A38A39A40A41A36A37A42A43A42A42A42A43A40A41A29A44A42A42A45A47A48A48A43A48A48A48A52A48A48A48A74A47A48A48A75A48A48A48A45A47A46A45A45A45A48A49A48A48A52A50A45A49A52A45A49A51A43A49A75A76A76A43A45A46A45A43A47A48A49A48A48A50A51A43A49A46A52A49A46A47A49A46A76A76A43A51A