10-物料衡算一览表1-设计文档集物料衡算表-2010

镇海炼化厂石油炼制尾气深度脱硫装置设计及年产7.5万吨甲硫醇项目物料衡算一览表目录1 概述12 物料衡算方法22.1物料衡算原理22.2物料衡算基准32.3物料衡算步骤33 物料衡算目的44 物料衡算一览表44.1原料提纯硫化氢工段44.1.1混合器物料衡算44.1.2分流器物料衡算74.1.3泵设备物料衡算104.1.4塔设备物料衡算114.1.5气液分离器物料衡算144.1.6压缩机物料衡算174.1.7换热器物料衡算184.2硫化氢甲醇合成甲硫醇工段264.2.1混合器物料衡算264.2.2分流器物料衡算284.2.3压缩机物料衡算294.2.4泵设备物料衡算304.2.5换热器物料衡算304.2.6反应器物料衡算344.3产品精制工段404.3.1混合器物料衡算404.3.2分流器物料衡算434.3.3气液分离器454.3.4塔设备物料衡算484.2.5泵设备物料衡算544.3.6换热器物料衡算61651 概述本项目以总厂在浙江省宁波市镇海区宁波石化经济技术开发区的镇海炼化总厂柴油加氢装置排出的含硫化氢酸性尾气为原料，经MDEA溶剂吸收、解吸和两级压缩冷凝后提纯硫化氢，硫化氢再与甲醇反应合成产品甲硫醇和副产品甲硫醚。主要流程包括原料硫化氢提纯工段，硫化氢甲醇合成甲硫醇工段和产品精制三个工段。设计过程中利用Aspen Plus对全流程进行模拟，并在此基础上完成物料衡算、能量衡算，Aspen plus全模拟流程如图1-1所示。图1 原料气预处理工段图2 甲硫醇合成工段图3 甲硫醇精制工段2 物料衡算方法2.1物料衡算原理系统累计的质量输入系统的质量输出系统的质量反应生成的质量反应消耗的质量假设系统无泄漏，有：dFdt=FIN-FOUT+GR-CR当系统无化学反应发生时，有：dFdt=FIN-FOUT 在稳定状态下，有：dFdt=FIN-FOUT=0，FIN=FOUT注：FIN进入系统的物料流率；FOUT流出系统的物料流率；GR反应产生物料速率；CR反应消耗物料速率。2.2物料衡算基准在物料、能量衡算过程中，恰当地选择计算基准可以使计算简化，同时也可以减少计算误差。在一般的化工工艺计算中，选择基准大致有以下几种：（1）时间基准对于连续生产过程，以秒、小时、天等的一段时间间隔的投料量或产品量作为计算基准。对于间歇操作过程，一般可以以一釜、一批量的生产周期作为基准。（2）质量基准对液体或固体介质，可取某一基准物流的质量为100Kg，然后计算其他物流的质量。基准物质可以使产品，也可以是原料，也可以是任何一个中间物流。一般情况下，取某一已知变量最多（或未知变量最少）的物流作为基准最为合适。对于有化学反应的过程，由于化学反应是按物质的量（mol）进行的，因此用物质的量作为基准更为方便。（3）体积基准对于气体物料，可采用标准体积基准，这是应将实际情况下的体积换算为标准状态下的体积，用V表示。在标准状态下，1mol气体相当于22.410-3m3标准体积的气体。气体混合物中组分的体积分数与摩尔分数在数值上是相同的。2.3物料衡算步骤（1）搜集计算数据。（2）准确画出物料衡算流程示意图。（3）确定衡算体系。（4）写出化学反应方程式，包括主反应和副反应，标出有用的分子量。（5）选择合适的计算基准，并在流程图上标明所选的基准值。（6）列出物料衡算式，然后用数学方法求解。（7）将计算结果列成输入输出物料表（物料平衡表）。（8）校核计算结果。3 物料衡算目的通过对系统整体以及部分主要单元的详细物料衡算，得到主、副产品的产量，原料的消耗量，“三废”的排放量以及最后产品的质量指标等关键经济技术指标，对所选工艺路线、设计流程进行定量评述，为后阶段的设计提供依据。4 物料衡算一览表4.1原料气预处理工段4.1.1混合器物料衡算表4-1 MDEA溶液混合器（M101）物料衡算INOUTStream No.1-311-221-23Pressure kPa1000.0001000.0001000.000Vapor Frac0.0000.0000.000Mass Flow kg/hr74285.95152.77774337.666Volum Flow cum/hr73.6910.05173.740Enthalpy MMBtu/hr-822.638-0.197-822.822Mass Flow kg/hrH2O48463.2060.00048462.391MDEA25634.37952.77725686.863H2S0.0070.0000.007CO20.0000.0000.000MDEA+148.2400.000148.278H3O+0.0000.0000.000OH-0.7180.0000.722HS-39.3960.00039.398HCO3-0.0020.0000.002S2-0.0020.0000.002CO32-0.0020.0000.002表4-2 富液混合器（E101-M）物料衡算INOUTStream No.1-3-31-3-51-3-6Temperature C265.20187.365104.249Pressure kPa136.000141.000136.000Vapor Frac1.0000.0830.292Mass Flow kg/hr16582.01966328.07782910.096Volume Flow cum/hr20749.3934506.92921193.880Enthalpy MMBtu/hr-135.193-659.639-794.833Mass Flow kg/hrH2O9766.70139024.61448817.345MDEA5166.72812923.37921686.640H2S1522.4193958.8896458.135CO2126.143401.611591.521CH40.0170.0680.085C2H60.0090.0350.043C3H80.0020.0080.010MDEA+0.0007808.9974182.060H3O+0.0000.0000.000OH-0.0000.0430.113HS-0.0002067.5861119.578HCO3-0.000135.79652.086S2-0.0000.2130.266CO32-0.0006.8402.215表4-3 变压吸附进口混合器（M102）物料衡算INOUTStream No.1-373-162-3Temperature C43.32120.00016.595Pressure kPa60.000780.00060.000Vapor Frac1.0001.0001.000Mass Flow kg/hr1593.2204910.9726504.192Volume Flow cum/hr2038.175384.5227170.956Enthalpy MMBtu/hr-0.968-7.218-8.186Mass Flow kg/hrH2O0.0001.9801.980MDEA0.0010.0000.001H2S1580.4933475.6195056.112CO212.725556.366569.091CH40.0000.0110.011C2H60.0000.0340.034C3H80.0000.0270.027CH3OH0.0003.9873.987CH3SH0.000849.304849.304C2H6O-10.0004.6854.685C2H6S-10.0040.0000.004MDEA+0.0000.0000.000H3O+0.0000.0000.000OH-0.0000.0000.000HS-0.0000.0000.000HCO3-0.0000.0000.000S-0.0000.0000.000CO3-0.0000.0000.000OH-0.0000.0000.000HS-0.0000.0000.000HCO3-0.0000.0000.000S2-0.0000.0000.000CO32-0.0000.0000.0004.1.2分流器物料衡算表4-4 吸收塔塔底富液分流器（E101-S）物料衡算INOUTStream No.1-3-11-3-41-3-2Temperature C69.74869.74869.748Pressure kPa151.000151.000151.000Vapor Frac0.0440.0440.044Mass Flow kg/hr82910.09666328.07716582.019Volume Flow cum/hr2692.9022154.322538.580Enthalpy MMBtu/hr-833.763-667.010-166.753Mass Flow kg/hrH2O48736.41538989.1329747.283MDEA11537.0169229.6132307.403H2S3717.7142974.171743.543CO2393.587314.87078.717CH40.0850.0680.017C2H60.0430.0350.009C3H80.0100.0080.002MDEA+14417.48711533.9902883.497H3O+0.0000.0000.000OH-0.0240.0190.005HS-3779.1383023.311755.828HCO3-309.503247.60261.901S2-0.1290.1030.026CO32-18.94515.1563.789表4-5 MDEA解析塔塔底贫液分流器（S101）物料衡算INOUTStream No.1-241-281-251-27Temperature C110.546110.546110.546110.546Pressure kPa135.000135.000135.000135.000Vapor Frac0.0000.0000.0000.000Mass Flow kg/hr106338.65674286.04231901.597151.018Volume Flow cum/hr110.79477.39933.2380.157Enthalpy MMBtu/hr-1151.976-804.748-345.593-1.636Mass Flow kg/hrH2O69372.86848462.48720811.86098.520MDEA36687.36525629.05311006.20952.102H2S0.0610.0430.0180.000CO20.0000.0000.0000.000CH40.0000.0000.0000.000C2H60.0000.0000.0000.000C3H80.0000.0000.0000.000MDEA+219.890153.61065.9670.312H3O+0.0000.0000.0000.000OH-2.1231.4830.6370.003HS-56.30539.33416.8920.080HCO3-0.0040.0030.0010.000S2-0.0410.0290.0120.000CO32-0.0000.0000.0000.0004.1.3泵设备物料衡算表4-6 MDEA溶液泵(P101)B物料衡算INOUTStream No.1-301-31Temperature C40.00040.221Pressure kPa130.0001000.000Vapor Frac0.0000.000Mass Flow kg/hr74285.95174285.951Volume Flow cum/hr73.70173.691Enthalpy MMBtu/hr-822.728-822.638Mass Flow kg/hrH2O48463.20648463.206MDEA25634.37925634.379H2S0.0070.007CO20.0000.000MDEA+148.240148.240H3O+0.0000.000OH-0.7180.718HS-39.39639.396HCO3-0.0020.002S2-0.0020.002CO32-0.0020.002表4-7 热泵精馏回流泵（P102）物料衡算INOUTStream No.1-121-13Temperature C40.00040.035Pressure kPa125.000300.000Vapor Frac0.0000.000Mass Flow kg/hr35202.11035202.110Volume Flow cum/hr35.50335.501Enthalpy MMBtu/hr-526.239-526.229Mass Flow kg/hrH2O35102.55635102.556MDEA0.0000.000H2S96.72996.729CO22.6042.604CH40.0000.000C2H60.0000.000C3H80.0000.000MDEA+0.0000.000H3O+0.0780.078OH-0.0000.000HS-0.1270.127HCO3-0.0160.016S2-0.0000.000CO32-0.0000.0004.1.4塔设备物料衡算表4-8 MDEA吸收塔（T101）物料衡算INOUTStream No.1-11-231-321-2Temperature C40.00040.22166.96569.815Pressure kPa1050.0001000.0001000.0001010.000Vapor Frac0.9340.0001.0000.000Mass Flow kg/hr10000.00074337.6661427.02382910.643Volume Flow cum/hr643.14273.740109.06391.617Enthalpy MMBtu/hr-21.434-822.822-6.286-837.969Mass Flow kg/hrH2O389.99848462.39119.42048629.835MDEA0.00025686.8630.0013079.255H2S8249.9960.007678.4551496.732CO21259.9990.000629.285132.617CH460.0000.00059.9150.085C2H630.0000.00029.9570.043C3H810.0000.0009.9900.010CH3OH0.0000.0000.0000.000C2H6S-10.0000.0000.0000.000MDEA+0.000148.2780.00022947.006H3O+0.0020.0000.0000.000OH-0.0000.7220.0000.005HS-0.00439.3980.0005934.599HCO3-0.0010.0020.000678.430S2-0.0000.0020.0000.061CO32-0.0000.0020.00011.965表4-9 MDEA解析塔（T102）物料衡算INOUTStream No.1-41-261-131-51-24Temperature C105.000174.98840.035102.656110.546Pressure kPa135.000135.000300.000125.000135.000Vapor Frac0.3301.0000.0001.0000.000Mass Flow kg/hr82910.64331901.55835202.11043676.286106338.526Volume Flow cum/hr24154.21334218.38835.50154617.190110.794Enthalpy MMBtu/hr-790.038-290.385-526.229-454.686-1151.975Mass Flow kg/hrH2O48819.43520812.49635102.55635374.49469372.737MDEA22073.44711071.6230.0000.00036687.365H2S6565.06817.43796.7297668.3240.061CO2596.0780.0012.604633.3300.000CH40.0850.0000.0000.0850.000C2H60.0430.0000.0000.0430.000C3H80.0100.0000.0000.0100.000MDEA+3792.2400.0000.0000.000219.889H3O+0.0000.0000.0780.0000.000OH-0.1160.0000.0000.0002.123HS-1015.8800.0000.1270.00056.305HCO3-46.0280.0000.0160.0000.004S2-0.2470.0000.0000.0000.041CO32-1.9660.0000.0000.0000.0004.1.5气液分离器物料衡算表4-10 热泵精馏气液分离器（ F101）物料衡算INOUTStream No.1-101-111-12Temperature C40.00040.00040.000Pressure kPa125.000125.000125.000Vapor Frac0.1141.0000.000Mass Flow kg/hr43676.2868474.17635202.110Volume Flow cum/hr5233.5995198.10635.503Enthalpy MMBtu/hr-539.189-12.950-526.239Mass Flow kg/hrH2O0.0001.9801.980MDEA0.0010.0000.001H2O35374.415271.85935102.556MDEA0.0000.0000.000H2S7668.1937571.46496.729CO2633.319630.7152.604CH40.0850.0850.000C2H60.0430.0430.000C3H80.0100.0100.000MDEA+0.0000.0000.000H3O+0.0780.0000.078OH-0.0000.0000.000HS-0.1270.0000.127HCO3-0.0160.0000.016S2-0.0000.0000.000CO32-0.0000.0000.000表4-11 一级压缩冷凝气液分离器（F102）物料衡算INOUTStream No.1-151-161-17Temperature C30.00030.00030.000Pressure kPa440.000440.000440.000Vapor Frac0.9491.0000.000Mass Flow kg/hr8474.1768243.167231.009Volume Flow cum/hr1326.7401326.5060.233Enthalpy MMBtu/hr-13.594-10.162-3.432Mass Flow kg/hrH2O271.85843.732228.126MDEA0.0000.0000.000H2S7571.4627568.6602.802CO2630.715630.6370.078CH40.0850.0850.000C2H60.0430.0430.000C3H80.0100.0100.000MDEA+0.0000.0000.000H3O+0.0010.0000.001OH-0.0000.0000.000HS-0.0020.0000.002HCO3-0.0000.0000.000S2-0.0000.0000.000CO32-0.0000.0000.000表4-12 二级压缩冷凝气液分离器（F103）物料衡算INOUTStream No.1-191-211-20Temperature C15.00014.94114.941Pressure kPa1090.0001090.0001090.000Vapor Frac0.9910.0001.000Mass Flow kg/hr8243.16737.6798205.488Volume Flow cum/hr473.2500.038473.083Enthalpy MMBtu/hr-10.451-0.546-9.905Mass Flow kg/hrH2O43.73136.0687.663MDEA0.0000.0000.000H2S7568.6601.5667567.094CO2630.6370.044630.593CH40.0850.0000.085C2H60.0430.0000.043C3H80.0100.0000.010MDEA+0.0000.0000.000H3O+0.0000.0000.000OH-0.0000.0000.000HS-0.0000.0000.000HCO3-0.0000.0000.000S2-0.0000.0000.000CO32-0.0000.0000.0004.1.6压缩机物料衡算表4-13 一级压缩冷凝压缩机（C101）物料衡算INOUTStream No.1-111-14Temperature C40.000191.513Pressure kPa125.000450.000Vapor Frac1.0001.000Mass Flow kg/hr8474.1768474.176Volume Flow cum/hr5198.1072139.985Enthalpy MMBtu/hr-12.950-11.671Mass Flow kg/hrH2O271.859271.859MDEA0.0000.000H2S7571.4647571.464CO2630.715630.715CH40.0850.085C2H60.0430.043C3H80.0100.010表4-14 二级压缩冷凝压缩机（C102）物料衡算INOUTTemperature C30.000131.768Pressure kPa440.0001100.000Vapor Frac1.0001.000Mass Flow kg/hr8243.1688243.168Volume Flow cum/hr1326.506706.730Enthalpy MMBtu/hr-10.162-9.377Mass Flow kg/hrH2O43.73243.732MDEA0.0000.000H2S7568.6617568.661CO2630.637630.637CH40.0850.085C2H60.0430.043C3H80.0100.010Temperature C30.000131.7684.1.7换热器物料衡算表4-15 贫富液换热器（E101-2）物料衡算INOUTStream No.1-281-3-41-291-3-5Temperature C110.54669.74882.00187.365Pressure kPa135.000151.000135.000141.000Vapor Frac0.0000.0440.0000.083Mass Flow kg/hr74286.04266328.07774286.04266328.077Volume Flow cum/hr77.3992154.32275.6434506.929Enthalpy MMBtu/hr-804.748-667.010-812.119-659.639Mass Flow kg/hrH2O48462.48738989.13248462.71139024.614MDEA25629.0539229.61325630.51112923.379H2S0.0432974.1710.0193958.889CO20.000314.8700.000401.611CH40.0000.0680.0000.068C2H60.0000.0350.0000.035C3H80.0000.0080.0000.008表4-16 贫液换热器（E102）物料衡算INoutStream No.1-291-30Temperature C82.00140.000Pressure kPa135.000130.000Vapor Frac0.0000.000Mass Flow kg/hr74286.04274286.042Volume Flow cum/hr75.64373.701Enthalpy MMBtu/hr-812.119-822.729Mass Flow kg/hrH2O48462.71148463.297MDEA25630.51125634.379H2S0.0190.007CO20.0000.000表4-17 贫富液换热器（E101-1）物料衡算INOUTStream No.1-81-3-21-91-3-3Temperature C105.00169.74882.020265.201Pressure kPa155.000151.000155.000136.000Vapor Frac0.4960.0440.1621.000Mass Flow kg/hr43676.15616582.01943676.15616582.019Volume Flow cum/hr21970.839538.5806790.60520749.393Enthalpy MMBtu/hr-497.273-166.753-528.833-135.193Mass Flow kg/hrH2O35374.3409747.28335374.2939766.701MDEA0.0002307.4030.0005166.728H2S7668.282743.5437668.1991522.419CO2633.32978.717633.326126.143CH40.0850.0170.0850.017C2H60.0430.0090.0430.009C3H80.0100.0020.0100.002表4-18 富液换热器(E101-3)物料衡算INOUTStream No.1-3-61-3-7Temperature C104.249105.000Pressure kPa136.000135.000Vapor Frac0.2920.330Mass Flow kg/hr82910.09682910.096Volume Flow cum/hr21193.88024154.166Enthalpy MMBtu/hr-794.833-790.033Mass Flow kg/hrH2O48817.34548819.204MDEA21686.64022073.170H2S6458.1356565.006CO2591.521596.072CH40.0850.085C2H60.0430.043C3H80.0100.010MDEA+4182.0603792.262H3O+0.0000.000OH-0.1130.116HS-1119.5781015.884HCO3-52.08646.029S2-0.2660.247CO32-2.215118811.96606552表4-19 热泵精馏换热器（E103）物料衡算INOUTStream No.1-61-251-261-7Temperature C277.144110.546174.988135.559Pressure kPa420.000135.000135.000420.000Vapor Frac1.0000.0001.0000.454Mass Flow kg/hr43676.15631901.59731901.59743676.156Volume Flow cum/hr23731.36633.23834218.4447942.204Enthalpy MMBtu/hr-442.065-345.593-290.385-497.273Mass Flow kg/hrH2O35374.36320811.86020812.53535374.325MDEA0.00011006.20911071.6230.000H2S7668.3240.01817.4377668.253CO2633.3300.0000.001633.329CH40.0850.0000.0000.085C2H60.0430.0000.0000.043C3H80.0100.0000.0000.010MDEA+0.00065.9670.0000.000H3O+0.0000.0000.0000.040OH-0.0000.6370.0000.000HS-0.00016.8920.0000.069HCO3-0.0000.0010.0000.002S2-0.0000.0120.0000.000CO32-0.0000.0000.0000.000表4-20 热泵精馏换热器（E104）物料衡算INoutStream No.1-91-10Temperature C82.02040.000Pressure kPa155.000125.000Vapor Frac0.1620.114Mass Flow kg/hr43676.15643676.156Volume Flow cum/hr6790.6055233.599Enthalpy MMBtu/hr-528.833-539.187Mass Flow kg/hrH2O35374.29335374.284MDEA0.0000.000H2S7668.1997668.193CO2633.326633.319CH40.0850.085C2H60.0430.043C3H80.0100.010表4-21 热泵精馏换热器（E104)物料衡算INOUTStream No.1-91-10Temperature C82.02040.000Pressure kPa155.000125.000Vapor Frac0.1620.114Mass Flow kg/hr43676.15643676.156Volume Flow cum/hr6790.6055233.599Enthalpy MMBtu/hr-528.833-539.187Mass Flow kg/hrH2O35374.29335374.284MDEA0.0000.000H2S7668.1997668.193CO2633.326633.319CH40.0850.085C2H60.0430.043C3H80.0100.010MDEA+0.0000.000H3O+0.0720.078OH-0.0000.000HS-0.1210.127HCO3-0.0060.016S2-0.0000.000CO32-0.0000.000表4-22 一级压缩冷凝换热器（E105）物料衡算INOUTStream No.1-141-15Temperature C191.51330.000Pressure kPa450.000440.000Vapor Frac1.0000.949Mass Flow kg/hr8474.1768474.176Volume Flow cum/hr2139.9851326.740Enthalpy MMBtu/hr-11.671-13.594Mass Flow kg/hrH2O271.859271.858MDEA0.0000.000H2S7571.4647571.462CO2630.715630.715CH40.0850.085C2H60.0430.043C3H80.0100.010MDEA+0.0000.000H3O+0.0000.001OH-0.0000.000HS-0.0000.002HCO3-0.0000.000S-0.0000.000CO3-0.0000.000表4-23 二级压缩冷凝换热器(E106)物料衡算INOUTStream No.1-181-19Temperature C131.76815.000Pressure kPa1100.0001090.000Vapor Frac1.0000.991Mass Flow kg/hr8243.1688243.168Volume Flow cum/hr706.730473.250Enthalpy MMBtu/hr-9.377-10.451Mass Flow kg/hrH2O43.73243.731MDEA0.0000.000H2S7568.6617568.660CO2630.637630.637CH40.0850.085C2H60.0430.043C3H80.0100.010MDEA+0.0000.000H3O+0.0000.000OH-0.0000.000HS-0.0000.000HCO3-0.0000.000S2-0.0000.000CO32-0.0000.0004.2硫化氢甲醇合成甲硫醇工段4.2.1混合器物料衡算表4-24 循环原料混合器 （M201)物料衡算INOUTStream No.1-373-162-3Temperature C43.32120.00016.595Pressure kPa60.000780.00060.000Vapor Frac1.0