50000 nm3 h焦炉煤气中苯族烃回收

本科生毕业设计姓名学号学院应用技术学院专业化学工程与工艺设计题目50000NM3/H焦炉煤气中苯族烃回收专题指导教师职称讲师2010年6月15大学毕业设计任务书学院应用技术学院专业年级06化学工程与工艺学生姓名任务下达日期2010年3月22日毕业设计日期2010年3月22日至2010年6月15日毕业设计题目50000NM3/H焦炉煤气中苯族烃回收毕业设计专题题目毕业设计主要内容和要求（1）回收工艺论证。（2）主要设备计算和选型。（3）绘制带控制点工艺流程图、设备平面布置图、管道平面和立面布置图、绘制一张主要设备图（必须与自己的设备计算一致），并用AUTOCAD绘制所有图纸。（4）编制设计说明书（5）按425孔JN6082焦炉配套规模进行计算。计算条件苯回收率095占干煤重量硫铵工段来煤气温度/饱和温度56/50终冷温度21（6）翻译一篇原版英文文献。（7）撰写专题报告。院长签字指导教师签字大学毕业设计指导教师评阅书指导教师评语（基础理论及基本技能的掌握；独立解决实际G19394题的能G2159；G313G11752G12362G1881G4493的理论G1393G6466和技G7427G7053G8873；G314G2474G5483的主要G6116G7536及G2031G7044点；G315工G1328G5589度及工G1328量；G316G5647G1319G16792G1227及G5326G16770G6116G13501；G317G4396G3324G19394题；G318G7171G2554G2528G5859G12584G17789G12573）成绩指导教师签字年月日大学毕业设计评阅教师评阅书评阅教师评语（选题的G5859G1053；基础理论及基本技能的掌握；G313G13520G2524G17828用所G4410G11705G16794解决实际G19394题的能G2159；G313工G1328量的G3835G4579；G314G2474G5483的主要G6116G7536及G2031G7044点；G315写G1328的规G14551程度；G316G5647G1319G16792G1227及G5326G16770G6116G13501；G317G4396G3324G19394题；G318G7171G2554G2528G5859G12584G17789G12573）成绩评阅教师签字年月日大学毕业设计答辩及综合成绩答辩情况G6564G1998G19394题回G12584G19394题A1A2A3A0A1A2A5A4A7A6A9A8A5A10A12A6A9A8A13A5A14A11G12584G17789G4008G2604G1262G16792G16833及G5326G16770G6116G13501G12584G17789G4008G2604G1262主G1231G12626G4395G5192G7388G7097G4410G19510G20058G4560G4579G13464G13520G2524G16792G4462G6116G13501G4410G19510G20058G4560G4579G13464G17139G17143G1166G5192G7388G7097内容摘要本设计G717150000NG80G22G18G75焦炉煤气回收G12907苯工段的设计。主要G2265G6336G1857G18108G2010G29一、工艺G7053G8873的论证及选G6333G11煤气的终冷G19512G14828G15G12907G12540的G2572收和G14085G1998G12G15工艺流程G16826G17860和说明。G1120、主要设备的计算，论证和选型G11终冷G3624、G8939苯G3624、G14085苯G3624、G17151G8845冷G2376G3132G12573G12573G12。G989、设备平面布置说明。G3247、G19762工艺G18108G2010要G8726（自G2172G2282G1214G15932，G19462G9791G19462G10202，G13485G8712G6502G8712，G1391G11017，G1391气，G3315G5326，G4445G1852与G2183G1457G12573）。G1128、G6817G1328G4715G1313的G11842G4462和G1166G2604编制。G1857、G13475济概算。本设计所采用的工艺流程G2010两G18108G2010终冷G8939苯G18108G2010和蒸馏G14085本G18108G2010。终冷G8939苯G18108G2010采用的G7171横管终冷轻质焦G8845G8939G14828，焦G8845G8939G8845G8939苯工艺。该工艺对煤气的终冷采用间接冷G2376，因此不产生含酚废G8712，冷G2376的G2528时轻质焦G8845G8939G14828效G7536好，G8939苯采用塑料花环填料G3624，其有阻G2159G4579，G8939苯效G7536好G12573优点。蒸馏G14085苯G18108G2010采用的G7171管式炉加热生产一种苯的工艺。该工艺具有富G8845预热温度高，节省蒸汽耗量，G14085苯效G7536好G12573优点，另外，G17151G8845冷G2376G3132采用螺旋板换热G3132，G17151富G8845换热G3132采用浮头式换热G3132，其具有传热系数G3835，省钢材G12573优点。该工艺的G5647投资42045G22万元，投资回收期为1G51928个G7388。ABSTRACTTHISDESIGNISABOUTACRUDEBENZENERVCOVERYRECOVERYWORKSHOPWITH5000NM3/HCOVENGASITINCLUDESMAINLYSIXPARTSTHEFIRSTDEMONSTRATIONANDSELECTIONOFTHEPROCESSTHEPROCESSOFGASFINALCOOLINGANDNAPHTHALENEREMOVAL,ABSORBTIONANDRECOVERINGOFBENZOL,ANDEXPLANATIONOFTECHNOLOGICALPROCESSTHESECONDCACULATION,DEMONSTRATIONANDSELECTIONOFMAINEQUIPMENTTHEFINALCOOLINGTOWER,THEBENZENESCRUBBINGTOWER,THEBENZENEREMOVINGTOWER,THELEANOILCOOLERS,ETC,THETHIRSTEXPLANATIONOFEQUIPMENTSLOCATIONTHEFORTHNONPROCESSSECTIONAUTOINSTRUMENT,FIREPROOF,GIVINGANDDRAWINGOFWATER,FEEDINGOFSTEAMANDELECTRICITY,BUIDING,SAFETYANDPROTECTIONETCTHEFIFTHSTUFFSTATION,THESIXTHECONOMICBUDGETARYESTIMATIONTHEDESIGNISDIVIDEDINTOTWOPARTSTHEFINALCOOLINGANDBENZENESCRUBBINGSECTION,THEBENZENEREMOVALSECTIONINFORMERSECTION,THEHORIZONTALFINALCOOLERWITHSPLASHINGLIGHTTARFORNAPHTHALREMOVALANDWITHWASHINGOILLIGHTTARSCRUBBINGBENZENEAREUSEDBECAUSEOFCOOLINGINDIRECT,THEPROCESSDOESNOTPRODUCEPHENOLBEARINGWASTEWATERMEANWHILE,ASARESULTOFUSINGLIGHTTAR,ITWILLACHIEVEGOODEFFECTSOFNAPHTHALENEREMOVALBENZENESCRUBBINGTOWERWITHPLASTICPETALRINGPACKINGBEINGUSEDTOABSORBBENZENE,COMPAREDWITHTHETOWERPACKEDWITHTIMBERGRATES,ITHASTHEADVANTAGESINCLUDINGLESSRESISTANCE,LARGERSPECIFICSURFACEAREA,ANDBENZENESCRUBBINGEFFICIENCY,ETCTHEDISTILLATIONSECTIONUSESPIPEFURNACETOHEATTHESTEAMANDRICHOILTOPRODUCETHECRUDEBENZENETHEPROCESSCONSUMESLESSDIRECTSTEAMCONSUMPTIONBECAUSEOFTHEHIGHPREHEATINGTEMPERATUREOFTHERICHOIL,ANDTHEBENZENEREMOVEDISBETTERINADDITION,THEHEATEXCHANGERARESPIRALPLATEHEATEXCHANGERESLEANOILANDRICHOILHEATEXCHANGERAREFLOATINGHEADHEATEXCHANGER,ITHASTHEADVANTAGESINCLUDINGHIGHTRANSFERCOEFFICIENT,ANDLITTLESTEALMATERIALCONSUMPTION,ETCTHETOTALINVESTMENTOFTHISPROCESSISABOUT4205MILLIONYUANANDTHEPERIODOFRECOVERINGISONEYEARANDEIGHTMONTHS目录1、绪论111炼焦煤气中回收苯族烃的G5859G1053112G12907G12540的性质11G22设计G1231务G22（1）徐州地区的气相条件G22（2）工段规模和煤气处理能G2159的计算42、G12907G12540工段的工艺过程及工艺选G6333521煤气终冷及G8939奈工艺522G8939苯工艺92G22G14085苯工艺1224本设计工艺G16826G17860143、主要设备论证及选型16G221G8939苯G362416G222G14085苯G362418G22G22终冷G362418G224G17151富G8845换热G3132194、主要设备和管道的工艺计算、选型2141终冷G3624的计算21411物料衡算21412热量恒算2241G22终冷G3624设计2G22414冷G2376面积的计算24415终冷G3624G3624高的计算2442G8939苯G3624的计算25421G8939G8845循环量的计算26422G17151富G8845中G12907苯含量的计算2642G22G3624径、填料面积、填料量和G3624高的G11842G4462274G22管式炉的计算与选型274G221物料衡算284G222能量衡算G2214G22G22管式炉的选型G22G2244再生G3132的计算选型G224441物料衡算G224442再生G3132选型G22645G14085苯G3624的计算选型G22646换热G3132G229461G17151富G8845换热G3132G229462G17151G8845冷G2376G31324246G22冷凝冷G2376G313242464G2010缩G31324G2247主要管道4G22471煤气管道4G22472蒸气管道4G2247G22富G8845管道44474G17151G8845管道4448泵的计算与选型445、工艺说明4751G6817G1328技G7427指标4752设备的布置485G22G6817G1328G4715G1313的G11842G4462及G4715G1313G4462G26044954G4715G1313G6817G1328规程506设备及管道材料汇G5647G15932527、G19762工艺G18108G20106071自G2172G2282G1214G15932的要G87266072G19462G9791G19462G10202和采暖通风627G22G1391汽和G13485G6502G87126G2274检G2282验项目6G2275G11017G2159G3315G53266476G4445G1852与G2183G1457648、G13475济概算6581编制说明6582G13475济概算658G22G13475济G2010析68设计图纸目录1、设备平面布置图2、带控制点的工艺流程图（终冷G8939苯G18108G2010）G22、带控制点的工艺流程图（G12907苯蒸馏G18108G2010）4、终冷G8939苯G18108G2010平面管线图5、G12907苯蒸馏G18108G2010平面管线图6、G12907苯蒸馏G18108G2010里面管线图（II剖面）7、G8939苯G3624G3624参考资料70英文翻译71A15A162010A17A18A19A20A21A22A23A24A251A261绪论11炼焦煤气中回收苯族的意义煤G3324炼焦时一般7278转G2282为焦炭，其中2228转G2282为荒煤气，苯族烃G7171煤干馏过程中产生的芳香烃G2282G2524物中G2010子较低的G18108G2010，其产率占炼焦干煤脏入量的0814产率的波G2172主要受炼焦煤料的性质炼焦温度的影G2721，G17829G5192来，G11013G1122G11719G8845G2282G4410工G1006的G17817G17907G2469G4649，G2499G1209G6564G1391G12540G12879，苯酚G12879G12573产G2709，对煤炼焦G2282G4410工G1006产生G1114G5052G3835的影G2721，G1306G7171焦G2282工G1006G6564G1391的G16780G3822种芳香族G2282G2524物和G7446环G2282G2524物G7171G11719G8845G2282G4410工G1006所不能G1207G7379的，G4439G1216不G2499能G6122G13785不能G13475济的G1186G11719G8845加工过程中G14731G5483，G1182G2530G17837G12879产G2709主要G1393G17194炼焦G2282G4410产G2709的G2572收与加工，因此G17837G1135G2282G4410产G2709对G13520G2524G2045用煤炭资G9316和G6117G3281G12050G1262主G1053G13475济G5326设有G11540重要G5859G1053。苯族烃回收G12946制加工G2530，G2499G5483G2052的轻苯，重苯，G12946苯，G11014苯，G1120G11014苯，G9354G2070G8845G12573产G2709。G11014苯，G1120G11014苯，G989G11014苯，G1069基G11014苯，G2488G20544G19546，G14574，G3151G2557，酚。G17837G1135产G2709具有G7509为G5203G8879的用G17896，G7171塑料G2524G6116G13432G13512，G2524G6116G8245G14026，G7591料，G9046料，G2319G14659，G13796高温材料及G3281G19462工G1006G7509为G4465G17161的原料，对G1122G6117G3281的G12050G1262主G1053G5326设具有G2325G2010重G3835的G6931G8847G5859G1053和G13475济G5859G1053。12粗苯的性质G12907苯G3324G5132G5589G991为G9141G21656G14406G17891明G9354G1319，此G8712轻，不G9354G1122G8712，G3324G17154G4396时，G11013G1122其中的G6110G9923G12879，环G6110G1120G9923G12573不G2524和G2282G2524物的G8699G2282G2524G13870G2524G13792G5430G6116G7653G14038G10378物质，G6937G1363G12907苯G5058G14406G2476G7275，G12907苯G7143G10135G7143G10202，G19390点为12G6680G8675度，G12907苯苯气G3324G12366气中的G8999度G33241475（G1319积）G14551G3272G1881时，能G5430G6116G10202G9868性G9163G2524物。G12907苯的G2520主要G6116G2010G11354G3324180G6680G8675度G2081馏G1998，180G6680G8675度G1209G2530馏G1998的G7171G12907苯中所含的G8939G8845轻质馏G2010，G12228为G9354G2070G8845。G3324G8991G4462G12907苯中G2520G13464G2010的含量和计算其加工过程中的产量时，通G5132G4570180G6680G8675度G2081的馏G1998量G1328为G18504G2047G12907G12540质量的指标G1055一。G12907苯G3324180G6680G8675度G2081的馏G1998量G2474决G1122G12907G12540的工艺流程和G6817G1328制度。180G6680G8675度G2081的馏G1998量G17246G3822，G12907苯的质量G4613G17246好，一般要G8726G12907G12540G3324180G6680G8675度G2081馏G1998量G178109G2295，G12907G12540中G19512G1114主要的苯G12879物质G1055外，G17836有饱和G2282G2524物和硫G2282物，G17837G7171G11013G1122G1186煤气中回收G12907苯的G2528时，煤气中的G9923烃，一G8699G2282G11911G12573G12573的G14026质生G6116物及有G7438硫G2282G2524物G1075一G2528进入G1114G12907苯中。G12907苯的G13464G6116G2474决G1122炼焦配煤的G13464G6116及炼焦产物G3324炭G2282G4472G1881热解的程度。G12907苯G2520G13464G6116的平G3355含量G3926G159321G2521。此外，G12907苯中酚G12879的含量通G5132G332401G25210G1055间，G2549G2890G11909G12879的含量不G17241过05。G5415硫铵工段G1186煤气回收G2549G2890G11909G12879时，G2029G12907苯中的G2549G2890G11909G12879含量不G17241过001。G2520产G2709的质量指标G16277G159321G2521、1G2522、1G252G22。G12907苯中G2520G13464G2010的含量A27A28A29A28A30A31A31A32A33A34A35A36A37A38A38A39A40A41A42A432010A44A45A46A47A48A49A50A51A522A53A54A37A55A54A37A56A54A37A57A58A59A60A61A62A63A64A65A66A67A55A68A37A69A68A37A70A71A72A73A74A75A62A76A73A74A75A62A77A60A62A78A79A77A80A81A63A64A65A55A77A60A82A83A84A85A86A87A86A85A86A87A88A78A85A87A89A81A90A85A86A87A91A78A85A87A89A81A89A85A86A87A90A78A85A87A89A81A90A92A92A85A88A87A86A85A86A87A88A85A87A85A87A89A85A93A87A86A94A85A95A87A88A92A92A85A96A89A85A91A87A91A96A28A97A39A97A97A97A98A41A39A99A97A98A41A39A38A40A39A28A97A41A98A99A39A28A98A97A41A98A38A39A28A98A41A28A98A41A39A97A98A41A28A98A38A39A97A98A38A41A98A100A39A28A98A38A41A98A100A39A28A98A38A41A98A97A39A28A98A97G11013G1122G12907苯G7171G7143G10135的物质，G12907苯蒸汽G3324G12366气中的G8999度G332414G25275（G1319积）G14551G3272G1881时，能G5430G6116G10202G9868性G9163G2524物，因此该工段要严禁烟G9791，G11017G7438G19462G10202。G12907苯和轻苯的质量指标A27A28A29A97A101A102A103A104A105A106A107A108A37A109A110A107A108A37A111A37A112A113A114A115A116A117A118A119A120A121A122A123A124A125A126A41A98A127A40A28A39A41A98A128A41A129A41A98A128A41A41A129A41A98A127A127A41A130A131A65A40A38A132A133A130A134A35A122A135A36A92A129A100A92A28A127A41A132A133A130A134A35A122A136A137A36A138A128A100A138A128A28A130A134A128A99A36A78A135A36A81A139A140A141A122A132A92A92A129A28A38A41A142A31A143A140A78A28A127A39A97A38A132A81A144A145A146A147A148A149A57A109A150A139A142重苯和重质苯的质量指标A27A28A29A100A101A102A103A104A121A37A121A151A37A78A152A153A100A41A100A92A99A124A81A42A432010A44A45A46A47A48A49A50A51A523A53A78A154A155A101A102A81A156A157A55A157A120A121A123A124A125A126A41A98A128A28A39A41A98A128A127A41A98A128A28A39A41A98A128A127A41A98A128A28A39A41A98A128A127A130A131A65A158A130A159A122A132A138A28A100A128A138A28A99A41A138A28A99A41A28A38A41A132A133A130A134A35A122A160A137A36A129A28A41A92A92A97A41A41A132A133A130A134A35A122A160A137A36A138A38A41A138A127A38A138A127A41A142A31A122A160A137A36A92A129A41A98A38A129A41A98A3813设计任务本设计为50000NG80A161G18G75焦炉煤气G12907苯回收工段设计。（1）徐州地区气象条件本设计G7171参考徐州市环宇焦G2282厂G12907苯工段设计的。厂址徐州郊区，东G1347511718，北纬G22417，海拔度G224米本地区属海洋性气候，具有G3835陆性气候特点。G5192平G3355气温14G7509端最高气温406（1972611）G7509端最底气温226（196926）G3835气压G2159冬季767G80G80HG夏季751G80G80HG降G8712量（G5192）8699G80G80降G8712天数（G5192）917DAY平G3355相对温度71最G3835积雪厚度25CG80最高地G991G8712G1313125G252175G80G80最G3835风G179072G224G80G18S最G3835平G3355风G1790719G22G80G18SA162A1632010A164A165A166A167A168A169A170A171A1724A173最G3822风向几频率G1852G5192东、东北夏季东、东南G3315壤G13796压G2159（砂质黏G3315）12TG18G80地G991G8712质对硅酸盐G8712泥G9163泥G3315无侵蚀G1328用。（2）工段规模和煤气处理能G2159的计算本设计采用焦G8845G8939G8845G2572收煤气中的苯族烃，对焦G8845G8939G8845的质量要G8726G16277G1593214焦G8845G8939G8845质量标准G11YB29764G12A174A175A176A177A178A179A180A181A182A183A184204DA185A186A187A188A189A190A191A192A193A186A194A195A184A196A185A197A198A190A191A191A192A193A186A194A195A184A183A195A185A197A198A199A200A195A184A196A185A197A198A201A200A195A184A183A195A185A197A198A202A203A184A204A205A189A206A185A207A208A197A198A175A206A192A209A210A211A175A212A191A177A213A175A212A191A214A215A190A216A217A191A215A191A212A206A215A175A190A215A189A215A175A212A191A218计算G1393G6466；炉型G7171425孔JN6082型焦炉炭G2282G4472有效G4493积G2285G80炉G13464孔数425孔设计结焦时间195G75煤饼堆积密度74484TG18G80焦G2282厂G5192产能G2159G煤/A219A220A221A222A223NNVA162A1632010A164A165A166A167A168A169A170A171A1725A173425G228574484G1819514705882KGG18G75式中G煤G29装炉干煤量NG29每个焦炉G13464的焦炉座数NG29每座焦炉G11911G2282G4472孔数G29周转时间G75A224A225A226VG11911G2282G4472有效G4493积A227A228干煤堆积密度2粗笨工段的工艺过程及工艺选择焦炉煤气G13475硫铵工段G14085G19512氨G2530进入G12907苯工段G15G12907苯工段的主要G1231务G7171G4570煤气进行煤气终冷G19512G14828G15G2572收苯族烃和G14085苯G991面G2010G2047进行对完G6116G17837G989G2721G1231务的工艺论证21煤气的终冷及洗萘工艺回收煤气中的苯族烃的适量温度为2127左右G15G3324饱和G3132G2530温度通G5132G7171G33245056G155056的煤气进入终冷G3624，被有喷淋G991来的富G8845G8939G14828。富G8845进G3624温度比煤气温度高57，煤气含G14828G2499G1101320002500G80GG18NG80降G2052500800G80GG18NG80。G19512G14828G2530的煤气进入终冷G3624，该G3624为隔板式，G2010两段。G991段用G1186凉G8712架来的循环G8712冷G2376至202G22的循环G8712喷淋，G4570煤气再冷G237625左右，额外G8712G1186终冷G3624底G18108G13475G8712封管流入热G8712池；然G2530用泵送至凉G8712架，G13475冷G2376G2530自流入冷G8712池。再用泵送至终冷冷G3624的上G991两端，送往上端的G8712须G1122间冷G3132用低温G8712冷G2376，G11013G1122终冷G3132只G7171为G1114冷G2376煤气，所G1209终冷循环G8712量G2499减至25G22吨G181000标米煤气左右G15因此G15G3324回收苯族烃G1055G2081G15煤气必须进行最终冷G2376G11013G1122G3324煤气冷G2376和G18108G2010G8712蒸气冷凝的G2528时G15G1075有G14828G1186煤气中析G1998G15所G1209G15煤气的最终冷G2376G2528时G1075兼有G19512G14828的G1328用G6117G3281焦G2282厂目G2081所采用的煤气终冷及G19512G14828的工艺流程主要有G3247种G15即G29煤气终冷和G7438械G19512G14828工艺煤气终冷和焦G8845G8939G8845工艺G8939G8845G14828和煤气最终冷G2376工艺横管终冷喷洒轻焦G8845G8939G14828工艺211煤气终冷和机械化除萘工艺该工艺流程G3926图21所示来自硫铵工段煤气G3324终冷G3624G1881自G991G13792上流G2172G15G3324流G2172过程中与G13475G11013隔板孔眼喷淋G13792G991的冷G2376G8712流密切接触，G11865560冷G2376至2127G15G18108G2010G8712汽被冷凝G991来G15G2528时G17836有相G5415数量的G14828G1075G1186煤气中析G1998G15并被G8712冲G8939G991来G15煤气含G14828量G2499G11862000G22000G80GG18NG80G15降G20528001200G80GG18NG80。冷G2376G2530的煤气去G8939苯G3624G14085苯。含G14828冷G2376G8712G11013G3624底G13475G8712封管自流入G7438械G2282刮G14828槽G15G8712和G14828G3324槽中G2010离G2530G15G8712自流入凉G8712架冷G2376G2052G220G222G15再G11013泵抽送G13475冷G2376G3132冷G2376G205221左右G2530G15回终冷G3624循环G1363用。G3324刮G14828槽中积G13870的G14828G15G4462期用G8712蒸气间接加热熔G2282G2530流入G14828的扬液槽，再用G8712蒸汽压送往焦G8845槽G6122焦G8845氨G8712澄清槽。亦G2499用冷凝工段的初冷冷凝液来熔G2282G14828，熔G14828G2530的冷凝液自流返冷凝鼓风段，G17837样既简G2282G1114G6817G1328又改善G1114G2183G2172条件。A229A2302010A231A232A233A234A235A236A237A238A2396A240A241A242A243A244A245A246A242A247A248A249A250A251A252A253A242A254A255A15A0A19A242A20A1A2A3A24A242A25A2A4A27A242A20A1A2A244A5A6A7A8A9A10A11A12A13A14A16A17A18A21A22A23A26A28A29A30A31A32A33A34A35A36A35A35A37A35A38A37A39A40A41A42A41A42A39A29A29A39A43A44A45A36A35A37A38该流程的优点G7171G6817G1328稳G4462G15便G1122管理G15G13582点G7171该工艺流程的G19512G14828率受冷G2376G8712温的影G2721，G6937G3624G2530的煤气含G14828量较高。G8712和G14828不能G1817G2010G2010离G15G18108G2010G14828被G8712带G2052凉G8712架G15G3698加G1114凉G8712架清G6207工G1328，因其G6502G8757G8712量G3835，刮G14828槽结G7512G3809G7446G1000G12540重，基G5326G17165高。该G8939G14828G8873G1177用G1122硫铵生产工G5219G1055G2530。212煤气终冷和焦油洗萘工艺煤气终冷和焦G8845G8939G14828工艺流程G3926图22G29煤气G3324终冷G3624G1881的过程G2528G2081所G17860。含G14828冷G2376G8712G1186终冷G3624底G18108流G1998，G13475液封管G4560入焦G8845G8939G14828G3132底G18108并向上流G2172。热焦G8845G13475G1292入G3132的G2010布管G3355G2260喷洒G3324G12591板上，通过G12591板孔眼向G991流G2172，G3324与G8712对流接触过程中G4570G8712中含G14828降G2052800G80GG18NG80G1209G991。G8939G14828G2530的焦G8845G1186G8939G14828G3132G991G18108G6502G1998，G13475液G1313G16855节G3132流入焦G8845槽。焦G8845G3324循环G1363用24G4579时G2530，G13475加热G19757G8502G14085G8712用泵送往焦G8845G17722间加工处理，送G12366的焦G8845槽再接受冷鼓工段的G7044G21104焦G8845G1209备循环G8939G14828G1363用。G1186G8939G14828G3132上G18108流G1998的G8712进入G8712澄清槽，G2010离G1998G8543G1325焦G8845G2530，自流G2052凉G8712架。G2010离G1998的焦G8845及浮G3324G8712面上的G8845G12879、G14828G12573G9163G2524物自流G2052焦G8845槽。焦G8845G8939G14828比G7438械G2282G19512G14828效率高，G1306G6817G1328G3809G7446。A229A2302010A231A232A233A234A235A236A237A238A2397A240A46A47A48A49A50A48A51A52A53A54A55A56A57A46A56A57A58A59A56A57A60A61A48A47A48A49A55A62A63A48A64A65A64A65A64A65A66A51A67A68A69A70A71A56A57A72A73A74A75A62A63A48A76A56A57A62A63A76A56A57A77A48A78A79A77A80A81A82A83A74A62A63A48A51A84A74A56A57A76A85A86A87A86A88A89A90A91A92A93A94A95A96A97A98A99A100该流程的优点G7171不G1177G2499G1209G6238冷G2376G8712中的G14828几G1058G1852G18108清G19512，G13792G1000对G8712中的酚有一G4462G14807G2474G1328用结G7536，减G4581凉G8712架的清G6207G8437数，有G2045G1122冷G2376G8712的进一G8505处理。G13582点G7171G6817G1328G3809G7446，G1998G2487煤气含G14828量高，用G8712量G3835，G2530期G1185G19668进行G8757G8712处理。213油洗萘和煤气终冷工艺G8845G8939G14828和煤气终冷工艺流程图G3926图2G22A101A102A103A104A105A106A107A108A109A105A102A110A104A105A106A111A105A102A112A113A114A115A105A116A117A102A102A102A112A113A118A119A120A121A122A119A120A121A123A124A125A126A127A128A129A130A131A132A133A129A130A131A134A135A136A137A125A138A139A140A137A141A128A127A140A131A142A138A139A140A131A127A140A143A137A140A143A144A145A146A147A130A123A133A148A134A135A136A137A149A150A151A152饱和G3132来的5055的煤气进入G7420G7696填料G8939G14828G3624底G18108，G3624G20042喷洒温度为5557的G8939苯富G8845进行G8939G14828。富G8845进G3624温度比煤气温度高57，G1363煤气含G14828G2499G1101320002500G80GG18NG80降G2052500800G80GG18NG80。G19512G14828G2530的煤气进入终冷G3624，该G3624为隔板式，G2010两段。上段用G1186凉G8712架来的循环G8712冷G2376至202G22的循环G8712喷淋，G4570煤气再冷G237625左右，额外G8712G1186终冷G3624底G18108G13475G8712封管流入热G8712池；然G2530用泵送至凉G8712架，G13475冷G2376G2530自流入冷G8712池。再用泵送至终冷冷G3624的上G991两端，送往上端的G8712须G1122间冷G3132用低温G8712冷G2376，G11013G1122终冷G3132只G7171为G1114冷G2376煤气，所G1209终冷循环G8712量G2499减至25G22吨G181000标米煤气。A229A2302010A231A232A233A234A235A236A237A238A2398A240该流程的优点G7171G3624G2530煤气含G14828量要G2081两种工艺流程，用G8712量为G8712G8939G14828的一G2334，因G13792G2499减G4581含酚G8757G8712的G6502G6930量。G13582点G7171该流程G8845G8939G14828G3324较为高的温度G991进行，G3624G2530煤气含G14828量G1185较高，煤气温度波G2172；G6817G1328G3809G7446，G8939G8845耗量G3835，G14085苯G3268G19602，G1185G19668进行G8757G8712处理。214横管终冷喷洒轻质焦油洗萘工艺横管终冷喷洒轻质焦G8845G8939G14828工艺G3926图24A153A154A155A156A157A158A159A160A161A162A163A164A165A166A164A165A167A168A169A170A168A169A171A172A173A156A174A175A176A177A178A162A163A164A165A179A180A181A182A178A183A184A181A185A186A187A181A188A178A162A163A164A165A189A190A178A191A187A189图24横管终冷喷洒轻质焦油洗萘工艺A192G1186硫铵工段来的煤气G11013G3624G20042进入，与G17842G13505喷洒的轻质焦G8845并流G5058G17907接触G17907冷，至横管段G13499G13505冷G2376至2125，G2528时G14085G14828至450G8639G1823G18标米G1209G991，然G2530G1186G3624底G6502G1998，进入旋风G6441G19666G3132G19512G6493G3853带的焦G8845，G14828和凝结G8712G19666，然G2530去G8939苯G3624。轻质焦G8845G11013其G15929G1817至G3624底循环G8845槽，循环G8845G11013槽底泵G1998至槽中G18108，G20042G18108喷洒，与横管G7475和煤气接触换热，G2528时G9354解煤气中析G1998的G14828，然G2530G13475液封回循环槽。（此过程中，循环G8845槽G1881，入G3624处，G1998G3624处G8845温基本相G2528）。焦G8845循环至一G4462程度，用泵送至焦G8845上段。18的冷G1935G8712G11013G3624G991G18108横管冷G2376G3132进入，向上G13475G1030G13864G11540的G2520横管G3132与G3624G1881循环G8845，煤气间接换热G13511温，然G2530G1186G3624的外G18108G6502G1998。G11013G1122该工程主要G1393G1