化工系统工程基础（邱彤）第1题

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1、大作业1化92张圣夫20009011878题：高低压脱丙烷塔是乙烯生产装置中分离部分的重要流程，目的是将裂解气中C3以下组分（包含C3）与C3以上组分分离开来。木题的目的是对该流程进行模拟，通过调节两塔的操作参数（冋流比、蒸出比等），使高压塔塔顶和低压塔塔釜采出的浓度要求达到标准。流程图和相关数据如下：表1塔器数据高压塔HP-DEC3低压塔LP-DEC3塔板数3955冷凝器无全凝再沸器釜式釜式进料位置（塔顶为第一块板，塔釜为最后一块板）Stream2:20Stream8:1Stream9:5StreamlO:23塔顶

2、压力/kPa1212790塔釜压力/kPa1240838表2物流数据12345TemperatureC16.000-8.300-27.10461.76571.516Pressurebar13.74013.51012.12012.4008.380VaporFrac1.0000.9191.0000.0000.000MoleFlowkmol/hr3565.9903565.9903855.361402.396254.190MassFlowkg/hr90244.26190244.26191864.79321027.447147

3、79.649VolumeFlowcum/hr574&8984904.413584&77510.01927.332EnthalpyGcal/hr-0.966-3.122-0.098-0.875-1.565MoleFlowkmol/hrco2.4602.4602.5500.0000.000H2486.490486.490491.6300.0000.000CH4950.940950.9401030.6000.0000.000C2H2乙烘29.74029.74029.7400.0010.000C2H4乙烯1248.67012

4、48.6701516.3400.0000.000C2H6132.730132.730169.5700.0090.000C3H4丙炊26.25026.25029.89715.1920.583C3H6丙烯422.620422.620566.011126.7530.000C3II8丙烷12.39012.3901&8804.2570.0001,3-C4H61,3T二烯127.430127.4300.116129.618127.344C4H10正丁烷88.54088.5400.02888.83688.532C5H12正戊烷37

5、.73037.7300.00037.73037.730678910TemperatureC12.56214.125-46.00014.10445.213Pressurebar7.90017.24012.12012.1408.100VaporFrac0.0000.0000.2850.0000.142MoleFlowkmol/hr14&20614&206543.560148.207402.396MassFlowkg/hr6247.7986247.79816400.1536247.82621027.447VolumeFlo

6、wcum/hr11.59511.648234.67711.647193.563EnthalpyGcal/hr0.5880.5940.1790.594-0.875MoleFlowkmol/hrco0.0000.0000.0900.0000.000H20.0000.0005.1400.0000.000CH40.0000.00079.6600.0000.000C2II2乙烘0.0010.0010.0000.0010.001C2H4乙烯0.0000.000267.6700.0000.000C2H60.0090.00936.8

7、400.0090.009C3H4丙烘14.60814.6084.23014.60815.192C3II6丙烯126.753126.753143.390126.754126.753C3I18丙烷4.2574.2576.4904.2574.2571,3-C4H61,3T二烯2.2742.2740.0302.274129.618C4H10正丁烷0.3030.3030.0200.3038&836C5H12正戊烷0.0000.0000.0000.00037.730解:使用Aspen软件对该高低压脱丙烷塔系统机型模拟，搭建流程图

8、如图2所示:EPUMP1COOLER—□——s{3——图2：高低压脱丙烷塔流程图1.参数设置：1.1塔器参数设置：首先，对高低压脱丙烷塔塔器参数进行设置：•高压塔HP-DEC3：采用RadFrac模型的塔设备进行模拟，所需设置参数有塔板数（39）,无冷凝器，物流量（无冷凝回流，为模拟实际生产操作，选用蒸岀比，经试验可选0.14,暂定），各物流进