【《异丙醇生产工艺的物料衡算和热量衡算计算案例》1700字】

异丙醇生产工艺的物料衡算和热量衡算计算案例工艺流程2.1生产原理本设计合成异丙醇采用的是气相直接水合法。主反应：CH3CH=CH2+H2O→(CH3)2CHOH副反应：2CH3CH=CH2+H2O→[(CH3)2CH]2OCH3CH=CH2+H2O→CH3(CH2)2OH观察上述反应式，根据反应物与生成物的特性，需选择一种动力学方程，在此选择了基于表面液膜反应的动力学方程：式中其中—异丙醇P—丙烯W—水蒸气2.2工艺流程简介混合丙烯远在经原料预处理塔和经气化过的除盐水在丙烯水合反应器总混合反应，经高压分离塔脱氢分离器，从脱水塔里分出两股物料，一股为循环水，一股进入乙二醇萃取塔，经乙二醇处理后，生产主产物异丙醇。通过脱水塔实现水循环，能量节省。图2-1IPA合成工段2.3原料、产品的品种及规格表2-2主要原辅材料的消耗量和来源表项目名称数量（吨/年）来源运输方式主要原料丙烯50000燕山石化丙烯生产装置管道输送除盐水28000母厂自供水装置管道输送辅助原料活性炭40北京市太平洋制品有限公司汽运（30%wt%）磷酸20天津市天河试剂厂汽运2.4公用工程表2-3公用工程消耗一览表公用工程名称单位消耗使用方式来源小时耗量年耗量电度1195.59564096连续变电站250℃低压蒸汽t43.948351584连续母厂动力中心350℃中压蒸汽t4.1833446.72连续母厂动力中心32℃冷却水t2696.6221572960连续母厂自供水系统氮气Nm39.55076400间歇母厂内的空压站仪表空气Nm35.6385100连续母厂内的空压站物料衡算3.1物料衡算原则由质量守恒定律得积累量=输入量-输出量+生产量-消耗量假设系统无泄漏，则：当无反应发生且系统稳定时，则：在稳定状态下，则：3.2丙烯回收塔T0102的物料衡算图3-1丙烯回收塔示意图（T0102）表3-1塔T0102物料衡算表流股编号进口出口01240125-280129-34温度℃11018040压力KPa1919.118.9气相分率101摩尔流量kmol/h2807.62200.3752607.24质量流量kg/h1120088938.27103070DIPA180.64584.928995.716C3H6-287468.80.00464358887468.8H201344.011343.60.402429CH4634.4380634.438C2H2412.6720412.672C2H49360.5509360.55C2H62055.1802055.18C3H4575.6080.00102487575.607C3H82463.610.0009902922463.61C3H8O-199.883399.88310.0001228IPA7412.447409.852.59156F=180.645/7.59+8768.8/7.2+1344.01/10+634.48/65+412.672/11.2+9360.55/11.78+2055.18/3.62+575.608/6.0+2463.61/18.3+99.8833/8.04+7412.44/7.86=14801.6358kmol/hXF=（7412.44/7.86)/14801.6358=0.064kmol/hD=84.9289/7.59+0.0046/7.2+1346.6/10+0.001/6+0.00099/18.3+99.8831/8.04+7409/7.86=1100.59kmol/hXD=（7409.85/7.86）/1100.89=0.857kmol/hW=95.716/7.59+887468.6/7.2+0.40249/10+634.438/65+412.672/11.2+9360.55/11.78+2055.18/3.62+575.607/6+2463.61/18.3+0.0001228/18.3+2.59156/7.86=124912.06kmol/hXW=(2.59/7.86)/124912.016=2.6396×10-6kmol/hFXF=DXD+WXW由计算得知符合质量守恒定律。3.3IPA合成工段总物料衡酸表3-2IPA合成工段总物料衡算表项目单位进口物料出口物料0101011203170102-0501350138Phase液相液相液相液相汽相液相Temperature℃45.219404058.20340.1875103.576Pressurebar18.501.011.0118.518.919.100VolumeFlowcum/hr13.0313.66516.1711.4973.59429.655MassFlowskg/hr6200.0023589.60015837.487760.045103.07124763.694IPAkg/hr0.0000.0000.0000.0000.0037418.118DIPAkg/hr0.0000.0000.0000.0000.09684.929C3H6-2kg/hr5823.1610.0000.000399.52687.4691.371H20kg/hr0.0003589.60015837.4870.0000.00017158.216EGkg/hr0.0000.0000.0000.0000.0000.000CH4kg/hr0.6500.0000.0000.0000.6340.013C2H2kg/hr0.4840.0000.0000.0000.4130.070C2H4kg/hr9.6930.0000.0000.0009.3610.304C2H6kg/hr2.1120.0000.0000.0002.0550.050C3H4kg/hr62.1180.0000.00061.3780.5760.138C3H8kg/hr34.9270.0000.00032.2842.4640.015C3H8O-1kg/hr0.0000.0000.0000.0000.000100.470C4H8kg/hr8.5820.0000.0008.5820.0000.000N-C4H10kg/hr2.3110.0000.0002.3110.0000.000P-C4H10kg/hr1.1980.0000.0001.1980.0000.000N-C4H8kg/hr8.4840.0000.0008.4840.0000.000P-C4H8kg/hr42.9170.0000.00042.9170.0000.0001,3-C4H6kg/hr0.5420.0000.0000.5420.0000.000C6H6kg/hr23.0230.0000.00023.0230.0000.000C7H8kg/hr2.4870.0000.0002.4870.0000.000C5H12kg/hr177.3130.0000.000177.3130.0000.000TOTALkg/hr25627.08925626.81能量衡算4.1能量衡算原则在化工生产上，各种物料在不同设备间传递时，就会发生能量转换。由能量衡算，可得到设备与流股之间的焓、熵、热负荷关键信息。最后，对塔、换热器、反应器等传热设备进行设备计算。能量衡算公式对于连续系统4.2塔设备热量衡算表4-1塔T0102流股焓变计算表UnitInOUTMoleFlowKMOL/HR2805.603200.3232605.281MassFlowKG/HR111928.4498937.379102991.070VolumeFlowCUM/HR4704.01615.1293591.117TemperatureC110.000180.00540.185PressureBAR19.00019.10018.900VaporFraction1.0001.0000.000LiquidFraction0.0000.0001.000SolidFraction0.0000.0000.000MolarEnthalpyJ/kmol5357929.218-277296163.84120546214.835MassEnthalpyJ/kg134302966519740.732MolarEntropyJ/kmol-K-137272.950-270648.290-146828.284MassEntropyJ/kg-K-3440.890-6066.320-3714.195EnthalpyFlowWatt4175617.720-15430201.29214869070.527流入与流出流股的焓值：WW输入设备的机械能：设备热负荷：能量计算：Q+W=∑Hout-∑Hin4.3换热器热量衡算表4-2换热器E0103流股焓变计算表UnitInOUTMoleFlowKMOL/HR3810.4723683.6993810.4723683.699MassFlowKG/HR127754.707127754.809127754.707127754.809VolumeFlowCUM/HR2144.9146772.9585538.7623829.834TemperatureC74.030200.150155.00099.368PressureBAR22.00020.00022.00020.000VaporFraction0.4600.4601.0000.935LiquidFraction0.5400.5400.0000.065SolidFraction0.0000.0000.0000.000MolarEnthalpyJ/kmol-65827798.664-47556898.511-49914759.419-64017578.559MassEnthalpyJ/kg-1963410.981-1371261.932-1488781.165-1845891.368MolarEntropyJ/kmol-K-149575.340-102206.665-109892.488-141087.346MassEntropyJ/kg-K-4461.305-2947.041-3277.705-4068.131EnthalpyFlowWatt-69676387.284-48662585.123-52833000.329-65505972.079流入与流出流股的焓值：=11.83×107W输入设备的机械能：设备热负荷：能量计算：Q+W=∑Hout-∑Hin4.4压缩机热量衡算表4-3压缩机C0101流股焓变计算表UnitInOUTMoleFlowKMOL/HR2602.6752602.675MassFlowKG/HR102888.079102888.079VolumeFlowCUM/HR3587.5263167.038TemperatureC40.18548.830PressureBAR18.90022.000VaporFraction1.0001.000LiquidFraction0.0000.000SolidFraction0.0000.000MolarEnthalpyJ/kmol20546214.83521101189.867MassEnthalpyJ/kg519740.732533779.480MolarEntropyJ/kmol-K-146828.284-146343.955MassEntropyJ/kg-K-3714.195-3701.943EnthalpyFlowWatt14854201.45615255429.176流入与流出流股的焓值：输入设备的机械能：设备热负荷：能量计算：Q+W=∑Hout-∑Hin4.5气液分离器热量衡算表4-4流股焓变计算表UnitInOUTMoleFlowKMOL/HR3683.699878.0962805.603MassFlowKG/HR127754.80915826.360111928.449VolumeFlowCUM/HR3507.63917.3883490.251TemperatureC80.00080.00080.000PressureBAR19.50019.50019.500VaporFraction0.8760.0001.000LiquidFraction0.1241.0000.000SolidFraction0.0000.0000.000MolarEnthalpyJ/kmol-66515870.655-284033443.9661562636.052MassEnthalpyJ/kg-1917927.454-15759061.85739169.102MolarEntropyJ/kmol-K-147564.747-150529.623-146636.802MassEntropyJ/kg-K-4254.902-8351.853-3675.604EnthalpyFlowWatt-680