30万吨年丙烷脱氢制丙烯生产项目8-2附录二能量平衡计算书

1、30万吨PDH项目能量平衡计算书30万吨年丙烷脱氢制丙烯生产项目附录二能量平衡计算书西南石油大学Boili ng30万吨PDH项目能量平衡计算书目录1概述22热量衡算的原理23热量衡算任务24系统能量衡算34.1原料预处理工段 34.2丙烷脱氢反应工段94.3氢气分离及选择加氢反应工段 16230万吨PDH项目能量平衡计算书能量平衡计算书1. 概述拟建一套年产值30万吨的丙烯装置，在整个工艺流程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

2、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。2. 热量衡算的原理系统的能量衡算能量守恒为理论基础，研究某一系统内各类型的能量的变 化，即：输入系统的能量=输出系统的能量+系统积累的能量对于连续系统，有：Q W Hout Hin其中，Q 设备的热负荷；W输入系统的机械能；H°ut 离开设备的各物流焓之和；Hin 进入设备的各物流焓之和。本项目的能量衡算以单元设备为对象， 计算由机械能转换、化学反应释放能 量和单纯的物理变化带来的热量变化。3. 热量衡算任务（1）确定流程中机械所需的功率，

3、为设备设计和选型提供依据。（2）确定精馏各单元操作中所需的热量或冷量及传递速率，确定加热剂和 冷剂的用量，为后续换热和公用工程的设计做准备。（3）确定反应过程中的热交换量，指导反应器的设计和选型。(4) 最终计算出所需的能量和费用，判定工艺过程的经济性4. 系统能量衡算4.1原料预处理工段4.1.1 E0101原料预热器表4-1热负荷表WQHeat Duty ( Gcal/hr)01.03911表4-2流股焓变计算表inout物流编号01150116Temperature (C)3557Pressure (bar)1818Vapor Frac00Mole Flow (kmol/hr)1405.

4、7111405.711)Mass Flow (kg/hr )66462.6266462.62Volume Flow (cum/hr )134.254150.552Enthalpy ( Gcal/hr )-25.969-24.93表4-3热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr )Hin (Gcal/hr)Hout (Gcal/hr )Error01.03911-25.969-24.9404.1.2 T0102脱丙烷塔表4-4热负荷表WCondenserReboilerQHeat Duty ( Gcal/hr )0-10.071710.40270表4-5流股焓变计算表inou

5、t物流编号011601170120Temperature (C)5742.796.9Pressure (bar)1817.518Vapor Frac000Mole Flow ( kmol/hr)1405.711962.287443.425Mass Flow ( kg/hr )66462.6241078.0825384.55Volume Flow(cum/hr )150.55294.74460.693Enthalpy ( Gcal/hr )-24.93-14.782-9.817表4-6热量平衡计算一览表W ( Gcal/hr)Q ( Gcal/hr)Hin ( Gcal/hr)Hout ( Gc

6、al/hr)Error0-24.93-24.59904.1.3 E0104C4液化气冷却器表4-7热负荷表WQHeat Duty ( Gcal/hr)0-0.999026表4-8流股焓变计算表inout物流编号01200124Temperature (C)96.940Pressure (bar)【1818Vapor Frac00Mole Flow (kmol/hr)443.425443.425Mass Flow (kg/hr )25384.54625384.546Volume Flow (cum/hr )60.69346.488Enthalpy ( Gcal/hr )-9.817-10.816

7、表4-9热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr )Hin (Gcal/hr)Hout (Gcal/hr )Error0-9.999026-9.817-10.81604.1.4 E0105脱乙烷塔进料预热器表4-10热负荷表WQHeat Duty ( Gcal/hr)00.902227表4-11流股焓变计算表inout物流编号01170119Temperature (C)44.969.5Pressure (bar)3030Vapor Frac00Mole Flow (kmol/hr)962.287962.287Mass Flow (kg/hr )41078.07641078

8、.076Volume Flow ( cum/hr )93.592117.184Enthalpy ( Gcal/hr )-14.741-13.839表4-12热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr)Hin (Gcal/hr)Hout (Gcal/hr )Error00.902227-14.741-13.83904.1.5 T0103脱乙烷塔表4-13热负荷表WCondenserReboilerQHeat Duty ( Gcal/hr )0-8.102269.726780表4-14流股焓变计算表inout物流编号0119012201210123Temperature (C)6

9、9.544.9-18.971.6Pressure (bar)303028.529Vapor Frac0010Mole Flow (kmol/hr)962.2871622.3698.6232486.023Mass Flow (kg/hr )41078.0869005.9022320.584107763.394Volume Flow(cum/hr )117.184159.99157.261306.962Enthalpy (Gcal/hr )-13.839-28.802-0.442-40.574表4-15热量平衡计算一览表W( Gcal/hr)Q ( Gcal/hr)Hin ( Gcal/hr)Ho

10、ut ( Gcal/hr)Error00-24.93-24.59904.1.6 E0108丙烯精制塔进料冷凝器表4-16热负荷表WQHeat Duty ( Gcal/hr)00表4-17流股焓变计算表inout物流编号0126012701280125Temperature (C )19.41.419.21.5Pressure (bar)9595Vapor Frac0.4920.13500.822Mole Flow (kmol/hr)2486.0231616.0462486.0231616.046Mass Flow (kg/hr )107763.39471181.241107763.394711

11、81.241Volume Flow (cum/hr )2892.0311009.577218.7075450.939Enthalpy (Gcal/hr )-40.574-45.706-45.011-41.269表4-18热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr )Hin (Gcal/hr)Hout (Gcal/hr )Error0086.28-86.2804.1.7 T0104丙烯精制塔1表4-19热负荷表WQHeat Duty (Gcal/hr)00表4-20流股焓变计算表inout物流编号01280130013401290131Temperature (C )19.21

12、4.820.114.820.1Pressure (bar)988.58.0058.495Vapor Frac00110Mole Flow (kmol/hr)2486.02312505.08413411.7213375.08615027.74Mass Flow (kg/hr )107763.394541845.014590739.8578428.252661919.945Volume Flow(cum/hr )218.7071079.41932484.7434177.7541357.414Enthalpy (Gcal/hr )-45.011-222.391-330.058-172.327-425

13、.135表4-21热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr)Hin (Gcal/hr)Hout (Gcal/hr )Error00-597.46-597.4604.1.8 T0105丙烯精制塔2表4-22热负荷表WQHeat Duty (Gcal/hr)00表4-23流股焓变计算表inout物流编号0129013701320133Temperature (C)14.87.914.88.1Pressure (bar)8.0057.587.505Vapor Frac1001Mole Flow (kmol/hr)13375.08612477.14712505.08413347.1

14、48Mass Flow ( kg/hr )578428.252524659.063541845.014561242.3Volume Flow (cum/hr )34177.754999.6621079.41935998.344Enthalpy ( Gcal/hr )-172.3276.663-222.39156.727表4-24热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr )Hin (Gcal/hr)Hout (Gcal/hr )Error00-165.664-165.66404.1.9 E0109 换热器表4-25热负荷表WQHeat Duty ( Gcal/hr)49.36

15、060表4-26流股焓变计算表inout物流编号0138013501390134Temperature (C)94.320.144.220.1Pressure (bar)308.5308.5Vapor Frac1001Mole Flow (kmol/hr)13347.14813411.71913347.14813411.719Mass Flow ( kg/hr )561242.3590739.8561242.3590739.8Volume Flow (cum/hr )10036.991211.4361243.94432484.735Enthalpy ( Gcal/hr )70.045-379.

16、41820.684-330.058表4-27热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr)Hin (Gcal/hr)Hout (Gcal/hr )Error0-309.373-309.3740.0014.1.10 C0101丙烯精制塔压缩机表4-28热负荷表WQHeat Duty (Gcal/hr)13.31820表4-29流股焓变计算表inout物流编号01330138Temperature (C)8.194.3Pressure (bar)7.50530Vapor Frac11Mole Flow (kmol/hr)13347.14813347.148Mass Flow (kg

17、/hr )561242.3561242.3Volume Flow ( cum/hr )35998.34410036.99Enthalpy ( Gcal/hr )56.72770.045表4-30热量平衡计算一览表W( Gcal/hr)Q ( Gcal/hr)Hin ( Gcal/hr)Hout ( Gcal/hr)Error13.3182056.72770.04504.1.11 E0110丙烯精制塔2塔顶冷凝器表4-31热负荷表WQHeat Duty ( Gcal/hr)0-13.5566表4-32流股焓变计算表inout物流编号01400141Temperature (C)87.9Pressure (bar)7.57.5Vapor Frac0.2730Mole Flow (kmol/hr)13347.14813347.148Mass Flow (kg/hr )561242.3561242.3Volume Flow ( cum/hr )