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1、石化年产55万吨对二甲苯项目能量平衡计算书附录二目录能量平衡计算书- 1 -1.1 总述- 1 -1.2热量衡算的原理和准则- 1 -1.3热量衡算任务- 2 -1.4热量衡算- 2 -1.4.1 三苯分离工段热量衡算- 2 -1.4.2甲苯歧化及烷基转移工段热量衡算- 4 -1.4.3甲苯甲醇烷基化工段热量衡算- 8 -1.4.4异构化工段热量衡算- 12 -1.5总结- 16 -能量平衡计算书1.1 总述拟建一套年产值55万吨的对二甲苯装置，在全工艺段中伴随着物料从一个体系或单元进入另一个体系或单元，在发生质量传递的同时也伴随着能量的消耗、释放和转化。其中的能量变换数量关系可以从能量衡算求
2、得，对于新设计的车间，可以由此确定设备的热负荷。再根据设备的热负荷大小、所处理物料的性质及工艺要求选择恰当的设备。总之，通过下述能量衡算，可以为后续设计工作中提高热量的利用率，降低能耗提供主要依据。1.2热量衡算的原理和准则工程依据化工设计中关于热量衡算的基本思想和要求，遵循基本规范与实际工艺相结合的原则，进行热量衡算书的编制。其中一个主要依据是能量平衡方程：其中，表示输入设备热量的总和；表示输出设备热量的总和；表示损失热量的总和。对于连续系统： Q + W = Hout - Hin 其中， Q设备的热负荷。 W输入系统的机械能。Hout离开设备的各物料焓之和。Hin进入设备的各物料焓之和。在
3、进行全厂热量衡算时，是以单元设备为基本单位，考虑由机械能转换、化学反应释放和单纯的物理变化带来的热量变化。最终对全工艺段进行系统级的热量平衡计算，进而用于指导节能降耗设计工作。1.3热量衡算任务在进行对二甲苯装置的热量衡算中，主要通过定量计算完成下述基本任务： 确定工艺单元中物料输送机械（如泵）所需要的功率，以便于进行设备的设计和选型； 确定精馏等单元操作中所需要的热量或冷量以及传递速率，计算换热设备的尺寸，确定加热剂和冷却剂的消耗量，为后续设计中比如供汽、供冷、供水等专业提供设备条件； 确定为保持一定反应温度所需移除或者加入的热传递速率，指导反应器的设计和选型； 提高热量内部集成度，充分利用
4、余热，提高能量利用率，降低能耗； 最终计算出总需求能量和能量的费用，并由此确定工艺过程在经济上的可行性。1.4热量衡算1.4.1 三苯分离工段热量衡算1.4.1.1二甲苯塔表2.1热负荷表-冷凝器再沸器QHeat duty/Gcal/hr-28.011593527.6057722-0.4058213表2.2流股焓变计算表inout物流编号104C8C9Temperature C166.8247146.3796188.978Pressure bar1.81.21.8Vapor Frac000Total Flow kmol/hr638.6267512.8306125.796Total Flow k
5、g/hr69566.3754447.1215119.24Total Flow cum/hr94.9234972.3835721.01181Enthalpy Gcal/hr0.04376390.1035486-0.4656058Hin(Gcal/hr)0.0437639413Hout(Gcal/hr)-0.362057135表2.3热量平衡计算一览表QHinHoutError-0.40582130.043763943-0.362057135-5.51228E-071.4.1.2第一三苯分离分隔壁塔表2.4热负荷表-冷凝器再沸器QHeat duty/Gcal/hr-22.763009324.239
6、54111.4765318表2.5流股焓变计算表inout物流编号103PRO-BENC7104Temperature C12086.23632124.6322166.8247Pressure bar1.51.21.4162791.8Vapor Frac0000Total Flow kmol/hr1418.447257.3201522.5638.6267Total Flow kg/hr13780620100.2148139.4169566.37Total Flow cum/hr178.281924.8866462.8722594.92349Enthalpy Gcal/hr5.7146383.5
7、363543.611170.0437639Hin(Gcal/hr)5.71463767Hout(Gcal/hr)7.19128852表2.6热量平衡计算一览表QHinHoutError1.47653185.714637677.191288528.06281E-051.4.2甲苯歧化及烷基转移工段热量衡算1.4.2.1第一汽提塔表2.7热负荷表-冷凝器再沸器QHeat duty/Gcal/hr-2.34258892.692108450.34951955表2.8流股焓变计算表inout物流编号213GAS-1PRO-BEN2REBTXTemperature C100-4-4146.0659Pres
8、sure bar21.21.21.8Vapor Frac0.1437583100Total Flow kmol/hr291.402635.6631418.14916237.5903Total Flow kg/hr26958.791514.1251314.74924129.92Total Flow cum/hr665.0603649.90841.54671432.16755Enthalpy Gcal/hr-0.4874231-0.819930.07699050.6050359Hin(Gcal/hr)-0.487423142Hout(Gcal/hr)-0.137903591表2.9热量平衡计算一览
9、表QHinHoutError0.34951955-0.48742314-0.1379035912.86107E-091.4.2.2甲苯歧化及烷基转移反应器表2.10热负荷表-QHeat duty/Gcal/hr0表2.11流股焓变计算表inout物流编号205206Temperature C379.0565379.1717Pressure bar3030Vapor Frac11Total Flow kmol/hr2269.1992269.199Total Flow kg/hr36033.9136033.91Total Flow cum/hr4155.9324157.381Enthalpy Gc
10、al/hr8.4004438.400443Hin(Gcal/hr)8.400443Hout(Gcal/hr)8.400443表2.12热量平衡计算一览表QHinHoutError08.4004438.40044301.4.2.3气液分离器表2.13热负荷表-QHeat duty/Gcal/hr0.0217006361表2.14流股焓变计算表inout物流编号208209211Temperature C252525Pressure bar302525Vapor Frac0.868687710Total Flow kmol/hr2269.2591977.856291.4026Total Flow
11、kg/hr36034.529075.72426958.79Total Flow cum/hr1690.1791989.28832.46717Enthalpy Gcal/hr-4.408758-2.820834-1.566223Hin(Gcal/hr)-4.408758Hout(Gcal/hr)-4.38706表2.15热量平衡计算一览表QHinHoutError0.0217006361-4.408758-4.387061.29501E-141.4.2.4 E201歧化原料预热器表2.16热负荷表-QHeat duty/Gcal/hr9.24766834表2.17流股焓变计算表inout物流编号
12、204207204-1208-1Temperature C95.7786379.0565342.5878120Pressure bar30303030Vapor Frac0.892601110.9120873Total Flow kmol/hr2269.1992269.1992269.1992269.199Total Flow kg/hr36033.9136033.9136033.9136033.91Total Flow cum/hr2136.6444155.8563923.6612315.304Enthalpy Gcal/hr-2.0150328.0986067.232636-1.14906
13、2Hin(Gcal/hr)6.08357375Hout(Gcal/hr)6.08357375表2.18热量平衡计算一览表QHinHoutError9.247668346.083573756.0835737501.4.2.5多级压缩机表2.19热负荷表-QWHeat duty/Gcal/hr-0.09430598330.12615744282029234表2.20流股焓变计算表inout物流编号H2203Temperature C25144.4174Pressure bar1.0132530Vapor Frac11Total Flow kmol/hr37.9115537.91155Total F
14、low kg/hr76.4251476.42514Total Flow cum/hr928.068744.4553Enthalpy Gcal/hr1.03378E-050.0318618Hin(Gcal/hr)1.03377546e-05Hout(Gcal/hr)0.0318617974表2.21热量平衡计算一览表QWHinHoutError-0.09430598330.1261574421.03378E-050.03186188.41314E-081.4.2.6单级压缩机表2.22热负荷表-WHeat duty/Gcal/hr0.30854577472055028表2.23流股焓变计算表in
15、out物流编号209210Temperature C2545.30285Pressure bar2530Vapor Frac11Total Flow kmol/hr1977.8561977.856Total Flow kg/hr9075.7249075.724Total Flow cum/hr1989.2881775.455Enthalpy Gcal/hr-2.820834-2.512288Hin(Gcal/hr)-2.820834Hout(Gcal/hr)-2.512288表2.24热量平衡计算一览表WHinHoutError0.30854577472-2.820834-2.5122887.
16、30133E-071.4.3甲苯甲醇烷基化工段热量衡算1.4.3.1第一甲醇塔表2.25热负荷表-冷凝器再沸器QHeat duty/Gcal/hr-2.717782943.196695420.478912表2.26流股焓变计算表inout物流编号319320WATER-1GAS-3Temperature C8049116.970549Pressure bar1.81.21.81.2Vapor Frac0001Total Flow kmol/hr721.133780.90311620.928219.30234Total Flow kg/hr14305.42541.53611186.2577.66
17、5Total Flow cum/hr16.4393.33639612.42794426.4341Enthalpy Gcal/hr-46.56182-4.491261-41.34812-0.243531Hin(Gcal/hr)-46.5618217Hout(Gcal/hr)-46.0829093表2.27热量平衡计算一览表QHinHoutError0.478912-46.5618217-46.08290938.35227E-071.4.3.2第二甲醇塔表2.28热负荷表-冷凝器再沸器QHeat duty/Gcal/hr-2.427942935.268610892.840668表2.29流股焓变计
18、算表inout物流编号309310GAS-4311Temperature C1002020136.6848Pressure bar1.81.21.21.8Vapor Frac0.0187133010Total Flow kmol/hr2098.101126.393131.321091940.387Total Flow kg/hr1932427829.71929.6273184483Total Flow cum/hr904.00299.106194630.4664245.1991Enthalpy Gcal/hr6.276166-2.6805370.242411.55496Hin(Gcal/hr)
19、6.27616588Hout(Gcal/hr)9.11682126表2.30热量平衡计算一览表QHinHoutError2.8406686.276165889.116821264.44262E-061.4.3.3第二三苯分离分隔壁塔表2.31热负荷表-冷凝器再沸器QHeat duty/Gcal/hr-39.729646439.0024227-0.72722表2.32流股焓变计算表inout物流编号311PRO-BEN3313314Temperature C136.684886.752124.2059161.2972Pressure bar1.81.21.3851061.8Vapor Frac0
20、000Total Flow kmol/hr1940.3877.7404681548.654383.9924Total Flow kg/hr184483607.249814310840767.47Total Flow cum/hr245.19910.7525778186.802155.8242Enthalpy Gcal/hr11.554960.104938410.425690.2971022Hin(Gcal/hr)11.5549577Hout(Gcal/hr)10.8277329表2.33热量平衡计算一览表QHinHoutError-0.7272211.5549610.82773-1.5126E
21、-061.4.3.4甲苯甲醇反应器表2.34热负荷表-QHeat duty/Gcal/hr-6.97333673表2.35流股焓变计算表inout物流编号304305Temperature C384.2304384.2304Pressure bar55Vapor Frac11Total Flow kmol/hr2791.8062918.625Total Flow kg/hr210396210396Total Flow cum/hr29859.1231238.85Enthalpy Gcal/hr18.3487411.3754Hin(Gcal/hr)18.3487413Hout(Gcal/hr)1
22、1.3754046表2.36热量平衡计算一览表QHinHoutError-6.8490417.7817710.93273-4.68929E-071.4.3.5气液分离器表2.37热负荷表-QHeat duty/Gcal/hr-1.18290293表2.38流股焓变计算表inout物流编号306GAS-2307Temperature C503535Pressure bar51.81.8Vapor Frac0.0041461310Total Flow kmol/hr2918.62599.390372819.235Total Flow kg/hr2103962848.145207547Total F
23、low cum/hr310.32611397.985237.5367Enthalpy Gcal/hr-43.11510.5796227-44.87763Hin(Gcal/hr)-43.1151024Hout(Gcal/hr)-44.2980053表2.39热量平衡计算一览表QHinHoutError-1.1829-43.1151-44.298-2.53613E-081.4.3.6烷基化反应进口预热器表2.40热负荷表-QHeat duty/Gcal/hr45.8585026表2.41流股焓变计算表inout物流编号303305303-1306-1Temperature C96.39687384
24、.2304351.8646120Pressure bar5555Vapor Frac0110.0947037Total Flow kmol/hr2791.812918.632791.812918.63Total Flow kg/hr210397210397210397210397Total Flow cum/hr262.444231238.928252.511989.713Enthalpy Gcal/hr-31.1472411.3753514.71127-34.48315Hin(Gcal/hr)-19.7718838Hout(Gcal/hr)-19.7718838表2.42热量平衡计算一览表Q
25、HinHoutError45.8585026-19.7718838-19.771883801.4.4异构化工段热量衡算1.4.4.1邻二甲苯塔表2.43热负荷表-冷凝器再沸器QHeat duty/Gcal/hr000表2.44流股焓变计算表inout物流编号405RE-BOT1RE-TOP1430423Temperature C144.8725167.457144.7039144.7502167.4561Pressure bar1.61.81.21.21.8Vapor Frac01010Total Flow kmol/hr546.47248499.9048028.928353.5418721.
26、755Total Flow kg/hr58018.63902461852405886869926015Total Flow cum/hr76.561511638561134.9722321851243.533Enthalpy Gcal/hr0.236699784.043075.51255978.209811.58253Hin(Gcal/hr)89.7923258Hout(Gcal/hr)89.7923258表2.45热量平衡计算一览表QHinHoutError089.792325889.792325801.4.4.2第二汽提塔表2.46热负荷表-冷凝器再沸器QHeat duty/Gcal/hr
27、-1.267571151.632504770.364934表2.47流股焓变计算表inout物流编号416PRO-BEN4GAS-5401Temperature C1401010162.568Pressure bar81.21.21.8Vapor Frac0.00231185010Total Flow kmol/hr332.85976.3774958.550242317.932Total Flow kg/hr34480.56506.2024220.511633753.85Total Flow cum/hr49.045180.5755242166.537545.8586Enthalpy Gcal
28、/hr0.005945330.0610403-0.14173730.451576Hin(Gcal/hr)0.00594533144Hout(Gcal/hr)0.370878953表2.48热量平衡计算一览表QHinHoutError0.3649340.0059450.3708791.03701E-061.4.4.3 异构化反应器表2.49热负荷表-QHeat duty/Gcal/hr0表2.50流股焓变计算表inout物流编号410412Temperature C373.5394376.7692Pressure bar8.358.35Vapor Frac11Total Flow kmol/hr
29、2652.1332652.133Total Flow kg/hr53281.1453281.14Total Flow cum/hr17130.9317215.63Enthalpy Gcal/hr-2.026962-2.026962Hin(Gcal/hr)-2.026962Hout(Gcal/hr)-2.026962表2.51热量平衡计算一览表QHinHoutError0-2.026962-2.02696201.4.4.4气液分离器表2.52热负荷表-QHeat duty/Gcal/hr-0.658248784表2.53流股焓变计算表inout物流编号413414415Temperature C
30、2555Pressure bar8.3588Vapor Frac0.876040210Total Flow kmol/hr2652.1332319.273332.8597Total Flow kg/hr53281.1418800.5834480.56Total Flow cum/hr6949.3256710.92239.33669Enthalpy Gcal/hr-17.8091-16.38111-2.086235Hin(Gcal/hr)-17.8090972Hout(Gcal/hr)-18.467346表2.54热量平衡计算一览表QHinHoutError-0.65825-17.8091-18
31、.4673-2.43069E-081.4.4.5单机压缩机表2.55热负荷表-WHeat duty/Gcal/hr0.019659表2.56流股焓变计算表inout物流编号H2-2407Temperature C96.39687384.2304Pressure bar55Vapor Frac01Total Flow kmol/hr2791.812918.63Total Flow kg/hr210397210397Total Flow cum/hr262.444231238.9Enthalpy Gcal/hr2.24883E-060.0196613Hin(Gcal/hr)2.24883E-06H
32、out(Gcal/hr)0.0196613表2.57热量平衡计算一览表WHinHoutError0.0196592.25E-060.0196611.63095E-061.4.4.6异构化反应进口预热器表2.58热负荷表-QHeat duty/Gcal/hr12.2212617表2.59流股焓变计算表inout物流编号409412409-1413Temperature C67.3434376.7692330102.7449Pressure bar8.358.358.358.35Vapor Frac0.8858858110.9159968Total Flow kmol/hr2652.1332652
33、.1332652.1332652.133Total Flow kg/hr53281.1453281.1453281.1453281.14Total Flow cum/hr8023.57517215.6315972.859136.057Enthalpy Gcal/hr-16.04628-2.026963-3.825014-14.24822Hin(Gcal/hr)-18.0732379Hout(Gcal/hr)-18.0732379表2.60热量平衡计算一览表QHinHoutError12.2212617-18.0732379-18.073237901.5总结通过本次热量衡算，我们计算所有塔设备、
34、反应器、气液分离器的能量流动，并以典型换热器和压缩机为例，指导所有换热器和流体输送机械的能量衡算，最终将收集到的数据进行整理，以便于设备选型以及热量集成。以下为流体输送机械和换热器的设备选型结果，其他详见附录四。表2.61 泵选型一览表泵编号流量/(L/s)总扬程/m泵型号电机功率/KWP10136.5761695.7493147XA80/16（2台并联）2.4510158P2015.83668622399.6333750GDL18-15（3台串联）31.3338512P2024.26731612380.677708IS65-40-315（3台串联）30P3017.1956338451.270
35、614IX180-65-160B（2台串联）5.19407277P30213.197376847.7279619IX180-65-160（2台串联）7.57151981P3040.9267727450.8679173IX132-25-160A（2台串联）1.19115348P3052.5294324645.0665376IX150-32-160B（2台串联）2.36222229P30651.889583948.1163956IS50-32-160B（单泵）24.8271025P40112.748020897.0787452IX180-65-160（3台串联）14.6833856P40221.2
36、6755445.38229602IS100-80-125（2台并联）1.2596129表2.62 压缩机选型一览表编号品牌型号功率kw流量m3/min串并联方式1CP201德鸿DH-30AG223.69台并联2CP401开山LG-1.2/84.51.23台并联3CP402ABBVW-45/845284台并联4CP403开山LGS-78/13G560906台并联5MC201蚌埠VF-6/306663台并联表2.63 换热器选型一览表序号编号用途型号换热管数目数目材料1E101第一甲醇回收塔塔釜再沸器（二甲苯塔顶冷凝器）BFM1100-0.6-237-3/19-113691Q345R2E102二甲
37、苯塔顶冷凝器BEM1300-0.6-269-3/19-2 15141Q345R3E201歧化原料预热器BEM1700-4-2078-9/19-1 39994Q345R4E203反应产物冷却器BEM1000-4/0.6-218-3/19-112651Q345R5E204第一汽提塔进料预热器BEM600-0.6-156-6/19-24421Q345R6E301烷基化反应进口预热器BEM1800-0.6-964-4/19-2423712Q345R7E303烷基化反应器出口冷却器BEM1300-0.6-86-3/19-25001Q345R8E304对二甲苯产品冷却器BEM600-0.6-131-4.5
38、/19-24981Q345R9E305第二甲醇塔进料预热器BEM600-1.6/0.6-56-3/19-23231Q345R10E307第二汽提塔进料预热器BEM600-0.6/1-104-4.5/19-43933Q345R11E308结晶器进料冷却器BEM700-0.6-106-3/19-26121Q345R12E401异构化反应进料预热器BFM900-1.0-169-3/19-29813Q345R13E403异构化反应出料冷却器BEM1200-1.0/0.6-311-3/19-218092Q345R14E404邻二甲苯塔釜再沸器（邻二甲苯塔塔顶冷凝器）BEM1800-0.6-1055-4.
39、5/19-240714Q345R15E405混合芳烃进料预热器BFM1500-0.6-473-3/19-227708Q345R16E406邻二甲苯塔顶冷凝器BEM1100-0.6-120-3/19-27001Q345R17T-101-R二甲苯塔再沸器BEM1000-4/0.6-180-3/25-18022Q345R18T-201-R第一汽提塔再沸器BEM500-4/0.6-25-2/25-11671Q345R19T-301-C第一甲醇回收塔冷凝器BEM700-0.6-183-6/19-25181Q345R20T-302-C第二甲醇回收塔冷凝器BEM700-0.6-91-3/19-15221Q345R21T-302-R第二甲醇回收塔再沸器BEM700-4/0.6-56-2/25-13791Q345R22T-402-R第二汽提塔再沸器BEM800-4/0.6-4
