30万吨年丙烷脱氢制丙烯生产项目82附录二能量平衡计算书.docx

1、30万吨年丙烷脱氢制丙烯生产项目82附录二能量平衡计算书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 16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，

2、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；Hut 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，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

3、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4.1.1E0101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)1405.7111405.711)Mass Flow (kg/hr )66462.6266

4、462.62Volume 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 )Error01.03911-25.969-24.9404.1.2T0102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inout物流编号011601170120Temperature (C)5742.796.

5、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 ( Gcal/hr)Error0-24.93-24.59904.1.3E0104C4液化气

6、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表4-9热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr )Hin (G

7、cal/hr)Hout (Gcal/hr )Error0-9.999026-9.817-10.81604.1.4E0105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 )41078.07641078.076Volume Flow ( cum/hr )93.592117.184Enth

8、alpy ( 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 )Error00.902227-14.741-13.83904.1.5T0103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)69.544.9-18.971.6Pressure (bar)303028.529Vapo

9、r 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)Hout ( Gcal/hr)Error00-24.93-24.59904.1.6E0108

10、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 )107763.39471181.241107763.39471181.241Volume Flow (cum/hr )2892.0311009.57721

11、8.7075450.939Enthalpy (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 )Error0086.28-86.2804.1.7T0104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 )19.214.820.114.820.1Pressure (bar)988.58.0058.495Va

12、por 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 )-45.011-222.391-330.058-172.327-425.135表4-21热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr)Hin (G

13、cal/hr)Hout (Gcal/hr )Error00-597.46-597.4604.1.8T0105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)13375.08612477.14712505.08413347.148Mass Flow ( kg/hr )578428.252524659.063541845

14、.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 )Error00-165.664-165.66404.1.9E0109 换热器表4-25热负荷表WQHeat Duty ( Gcal/hr)49.36060表4-26流股焓变计算表inout物流编号0138013501390134Temperat

15、ure (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 )70.045-379.41820.684-330.058表4-27热量平衡计算一览表W (Gcal/hr)Q (Gca

16、l/hr)Hin (Gcal/hr)Hout (Gcal/hr )Error0-309.373-309.3740.0014.1.10C0101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/hr )561242.3561242.3Volume Flow ( cum/hr )35998.

17、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)Error13.3182056.72770.04504.1.11E0110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)

18、13347.14813347.148Mass Flow (kg/hr )561242.3561242.3Volume Flow ( cum/hr )10616.2531069.367Enthalpy ( Gcal/hr )20.6847.128表4-33热量平衡计算一览表W (Gcal/hr)Q (Gcal/hr )Hin (Gcal/hr)Hout (Gcal/hr )Error0-13.556620.6867.1280.0024.2丙烷脱氢反应工段4.2.1 E0203丙烷、氢气预热器表4-34热负荷表WQHeat Duty (Gcal/hr)00表4-35流股焓变计算表inout物流编号0207021702080206Temperature (C)71.4300180174.2