年产13000吨叔丁胺项目10.doc

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1、目录第一章 概述1第二章 能量衡算的原理1第三章 能量衡算的任务2第四章 异丁烯水合-制叔丁醇工段热量衡算34.1 泵34.1.1 泵（P0101）34.1.2 泵（P0102）44.1.3 泵（P0103）44.1.4 泵（P0104）54.2换热器64.2.1 换热器（E0101）64.2.2 换热器（E0102）74.2.3 换热器（E0105）84.2.4 换热器（E0108）84.3 塔94.3.1 塔（T0101）94.3.2 塔（T0102）104.4 反应器114.4.1 反应器（R0101）11第五章 叔丁醇-精制异丁烯工段热量衡算135.1 泵135.1.1 泵（P0201

2、）135.1.2 泵（P0202）145.2 换热器145.2.1 换热器（E0201）145.2.2 换热器（E0204）155.2.3 换热器（E0207）165.2.4 换热器（E0208）175.3 塔185.3.1 塔（T0201）185.3.2 塔（T0202）195.4 反应器195.4.1 反应器（R0201）19第六章 合成叔丁胺工段热量衡量216.1 泵216.1.1 泵（P0301）216.1.2 泵（P0302）226.1.3 泵（P0303）226.1.4 泵（P0304）236.1.5 泵（P0305）246.2 换热器256.2.1 换热器（E0301）256.2

3、.2 换热器（E0302）266.2.3 换热器（E0303）266.2.4 换热器（E0306）276.3 塔286.3.1 塔（T0301）286.3.2 塔（T0302）296.3.3 塔（T0303）306.4 反应器316.4.1 反应器（R0301）31第一章 概述热量衡算是指根据能量守恒定律而进行的热量平衡的计算，对任何一个生产过程，其中输入的热量应为输出热量与损失热量之和。通过热量衡算，可知热量的利用、消耗和损失的情况，从而可推算热量的利用效率。例如利用热量衡算，可以确定蒸馏釜中加热蒸汽的消耗量以及分(冷）凝器和冷却器中冷却水的消耗量。第二章 能量衡算的原理能量衡算的基本依据是

4、能量守恒定律。而能量守恒定律是以化工过程的能量衡算结果为基础进行的。本工艺所需的主要设备有泵、换热器、反应器、精馏塔等。输入生产系统的能量主要有电能、热公用工程带入的热量和原料的焓值，输出的能量主要有冷公用工程带走的热量和产物的焓值。根据能量守恒定律，对于连续系统有：Q+W+Q损=Hout-HinQ设备的热负荷；Q=Hout-HinW机械能，输入为正，输出为负；Q损系统损失的热量，本计算书中忽略不计，即Q损=0；Hout进料带入系统的能量之和，本计算书中即为物料焓值；Hin出料带出系统的能量之和，本计算书中即为物料焓值。利用以上关系，可以对整个工艺系统或子系统进行能量衡算误差Error：E=Q

5、+W-(Hout-Hin)第三章 能量衡算的任务对于本厂，工艺采取年开工300天的连续操作，物料衡算的主要任务在于：确定工艺单元中物料输送机械（如泵）和其他操作机械所需要的功率，以便于进行设备的设计和选型；确定精馏等各个单元操作中所需要的热量或冷量以及传递速率，计算换热设备的尺寸，确定加热剂和冷却剂的消耗量，为后续设计中比如供汽、供冷、供水等专业提供设备条件；确定为保持一定反应温度所需移除或者加入的热传递速率，指导反应器的设计和选型；提高热量内部集成度，充分利用余热，提高能量利用率，降低能耗；最终计算出总需求能量和能量的费用，并由此确定工艺过程在经济上的可行性。第四章 异丁烯水合-制叔丁醇工段

6、热量衡算4.1 泵4.1.1 泵（P0101）表4-1 热负荷表WQHeat Duty（Gcal/hr）0.003780表4-2 流股焓变计算表INOUTStream1-11-2Temperature C2525.45935Pressure MPa18Vapor Frac00Liquid Frac11Mole Flow kmol/hr136.15281.84Mass Flow kg/hr2452.8161474.371Volume Flow cum/hr2.4677291.483996Enthalpy kcal/mol-68.2324-68.22217Enthalpy kcal/kg-3787

7、.48-3786.906Enthalpy Gcal/hr-9.28998-5.583302表4-3 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.003780-0.928619-9.2861904.1.2 泵（P0102）表4-4 热负荷表WQHeat Duty（Gcal/hr）00表4-5 流股焓变计算表INOUTStream1-41-5Temperature C25.5607125.56071Pressure MPa2020Vapor Frac00Liquid Frac11Mole Flow kmol/hr215.

8、8257215.8257Mass Flow kg/hr6936.8866936.886Volume Flow cum/hr9.4245159.424515Enthalpy kcal/mol-46.6555-46.6555Enthalpy kcal/kg-1451.58-1451.58Enthalpy Gcal/hr-10.0695-10.0695表4-6 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-10.0695-10.069504.1.3 泵（P0103）表4-7 热负荷表WQHeat Duty（Gcal/hr）

9、0.00080表4-8 流股焓变计算表INOUTStream1-111-12Temperature C2525.45935Pressure MPa18Vapor Frac00Liquid Frac11Mole Flow kmol/hr81.8481.84Mass Flow kg/hr1474.3711474.371Volume Flow cum/hr1.4833341.483996Enthalpy kcal/mol-68.2324-68.22217Enthalpy kcal/kg-3787.48-3786.906Enthalpy Gcal/hr-5.58414-5.583302表4-9 热量平

10、衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00080-5.58414-5.583304.1.4 泵（P0104）表4-10 热负荷表WQHeat Duty（Gcal/hr）0.0000010表4-11 流股焓变计算表INOUTStream1-171-18Temperature C83.1177983.12464Pressure MPa1.12921.2Vapor Frac00Liquid Frac11Mole Flow kmol/hr4.5246934.524693Mass Flow kg/hr189.7152189.7

11、152Volume Flow cum/hr0.24619670.2462Enthalpy kcal/mol-73.40483-73.4045Enthalpy kcal/kg-1750.699-1750.69Enthalpy Gcal/hr-0.332134-0.33213表4-12 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.0000010-0.332134-0.3321304.2换热器4.2.1 换热器（E0101）表4-13 热负荷表WQHeat Duty（Gcal/hr）0.1545560.154556表4-1

12、4 流股焓变计算表INOUTStream1-51-6Temperature C25.5607156.45Pressure MPa2020Vapor Frac00Liquid Frac11Mole Flow kmol/hr215.8257215.8257Mass Flow kg/hr6936.8866936.886Volume Flow cum/hr9.4245159.996416Enthalpy kcal/mol-46.6555-45.9394Enthalpy kcal/kg-1451.58-1429.3Enthalpy Gcal/hr-10.0695-9.9149表4-15 热量平衡计算一览

13、表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.1545560.154556-10.0695-9.914904.2.2 换热器（E0102）表4-13 热负荷表WQHeat Duty（Gcal/hr）00.152831表4-14 流股焓变计算表INOUTStream1-61-91-71-10Temperature C56.4592.127018565.3105Pressure MPa20152015Vapor Frac0000Liquid Frac1111Mole Flow kmol/hr215.8257197.9802215.8257

14、197.9802Mass Flow kg/hr6936.8866936.8876936.8866936.887Volume Flow cum/hr9.99641610.5190310.656019.914382Enthalpy kcal/mol-45.9394-49.8331-45.2313-50.6051Enthalpy kcal/kg-1429.3-1422.25-1407.27-1444.28Enthalpy Gcal/hr-9.9149-9.86597-9.76207-10.0188表4-15 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（

15、Gcal/hr）Error00.152831-19.7809-19.780904.2.3 换热器（E0105）表4-16 热负荷表WQHeat Duty（Gcal/hr）0.264840.26484表4-17 流股焓变计算表INOUTStream1-141-15Temperature C4.76464142Pressure MPa1.21.2Vapor Frac0.37533460.9996192Liquid Frac0.62466540.000380758Mole Flow kmol/hr58.7622558.76225Mass Flow kg/hr3247.373247.37Volume

16、Flow cum/hr413.64151252.408Enthalpy kcal/mol-14.04192-9.534807Enthalpy kcal/kg-254.0933-172.5355Enthalpy Gcal/hr-0.825135-0.5602867表4-18 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.264840.26484-0.825135-0.56028674.2.4 换热器（E0108）表4-19 热负荷表WQHeat Duty（Gcal/hr）-0.009930表4-20 流股焓变计算表INO

17、UTStream1-181-19Temperature C83.1246425Pressure MPa1.21.2Vapor Frac00Liquid Frac11Mole Flow kmol/hr4.5246934.524693Mass Flow kg/hr189.7152189.7152Volume Flow cum/hr0.24620.224516Enthalpy kcal/mol-73.4045-75.5992Enthalpy kcal/kg-1750.69-1803.03Enthalpy Gcal/hr-0.33213-0.34206表4-21 热量平衡计算一览表W（Gcal/hr）

18、Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error-0.009930-0.33213-0.3420604.3 塔4.3.1 塔（T0101）表4-22 热负荷表WQCondenserReboilHeat Duty（Gcal/hr）00-0.4290280.883885表4-23 流股焓变计算表INOUTStream1-101-121-131-22Temperature()56.4592.127018565.3105Pressure(Mpa)20152015Vapor Frac0000Liquid Frac1111Mole Flow(kmol/hr)215.8257

19、197.9802215.8257197.9802Mass Flow(kg/hr)6936.8866936.8876936.8866936.887Volume Flow(cum/hr)9.99641610.5190310.656019.914382Enthalpy kcal/mol-45.9394-49.8331-45.2313-50.6051Enthalpy kcal/kg-1429.3-1422.25-1407.27-1444.28Enthalpy(Gcal/hr)-9.9149-9.86597-9.76207-10.0188表4-24 热量平衡计算一览表W（Gcal/hr）Q（Gcal/h

20、r）Hin（Gcal/hr）Hout（Gcal/hr）Error00-15.6021-15.147204.3.2 塔（T0102）表4-25 热负荷表WQCondenserReboilHeat Duty（Gcal/hr）00-0.2969480.210694表4-26 流股焓变计算表INOUTStream1-151-161-17Temperature()421.10017283.11779Pressure(Mpa)1.211.1292Vapor Frac0.999619210Liquid Frac0.00038075801Mole Flow(kmol/hr)58.7622554.237554.

21、524693Mass Flow(kg/hr)3247.373057.655189.7152Volume Flow(cum/hr)1252.4081201.0380.2461967Enthalpy kcal/mol-9.534807-5.796839-73.40483Enthalpy kcal/kg-172.5355-102.826-1750.699Enthalpy(Gcal/hr)-0.5602867-0.3144063-0.3321343表4-27 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-0.560287-0

22、.64654104.4 反应器4.4.1 反应器（R0101）表4-28 热负荷表WQHeat Duty（Gcal/hr）0-0.10389表4-29 流股焓变计算表INOUTStream ID1-71-8Temperature()8565.3105Pressure(Mpa)2015Vapor Frac00Liquid Frac11Mole Flow(kmol/hr)215.8257197.9802Mass Flow(kg/hr)6936.8866936.887Volume Flow(cum/hr)10.656019.914382Enthalpy kcal/mol-45.2313-50.605

23、1Enthalpy kcal/kg-1407.27-1444.28Enthalpy(Gcal/hr)-9.76207-10.0188表4-30 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-0.10389-9.76207-9865970第五章 叔丁醇-精制异丁烯工段热量衡算5.1 泵5.1.1 泵（P0201）表5-1 热负荷表WQHeat Duty（Gcal/hr）0.000540表5-2 流股焓变计算表INOUTStream2-52-6Temperature()78.9262778.48525Pressure(Mp

24、a)13Vapor Frac00Liquid Frac11Mole Flow(kmol/hr)50.4017550.40175Mass Flow(kg/hr)2545.6682545.668Volume Flow(cum/hr)3.3621023.359459Enthalpy kcal/mol-76.1315-76.1207Enthalpy kcal/kg-1507.33-1507.12Enthalpy(Gcal/hr)-3.83716-3.83662表5-3 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.000540

25、-3.83716-3.8366205.1.2 泵（P0202）表5-4 热负荷表WQHeat Duty（Gcal/hr）0.000050表5-5 流股焓变计算表INOUTStream2-82-9Temperature()100100.0229Pressure(Mpa)33.2Vapor Frac00Liquid Frac11Mole Flow(kmol/hr)55.2088955.20889Mass Flow(kg/hr)2545.6682545.668Volume Flow(cum/hr)3.5919913.592163Enthalpy kcal/mol-67.8907-67.8896Ent

26、halpy kcal/kg-1472.37-1472.35Enthalpy(Gcal/hr)-3.74817-3.74811表5-6 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.000050-3.74817-3.7481105.2 换热器5.2.1 换热器（E0201）表5-7 热负荷表WQHeat Duty（Gcal/hr）-0.34120表5-8 流股焓变计算表INOUTStream2-22-3Temperature()85.417783Pressure(Mpa)1.21.2Vapor Frac0.1218350

27、Liquid Frac0.8781651Mole Flow(kmol/hr)268.3085268.3085Mass Flow(kg/hr)6471.3246471.324Volume Flow(cum/hr)803.51257.56023Enthalpy kcal/mol-67.7214-68.9935Enthalpy kcal/kg-2807.81-2860.55Enthalpy(Gcal/hr)-18.1702-18.5115表5-9 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error-0.34120-18.1702-1

28、8.511505.2.2 换热器（E0204）表5-10 热负荷表WQHeat Duty（Gcal/hr）0.050820表5-11 流股焓变计算表INOUTStream2-62-7Temperature()78.48525100Pressure(Mpa)33Vapor Frac00Liquid Frac11Mole Flow(kmol/hr)50.4017550.40175Mass Flow(kg/hr)2545.6682545.668Volume Flow(cum/hr)3.3594593.497711Enthalpy kcal/mol-76.1207-75.1123Enthalpy kc

29、al/kg-1507.12-1487.15Enthalpy(Gcal/hr)-3.83662-3.78579表5-12 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.050820-3.83662-3.7857905.2.3 换热器（E0207）表5-13 热负荷表WQHeat Duty（Gcal/hr）-0.087920表5-14 流股焓变计算表INOUTStream2-112-12Temperature()110.937830Pressure(Mpa)3.26523.2652Vapor Frac00Liquid Fr

30、ac11Mole Flow(kmol/hr)50.4156450.41564Mass Flow(kg/hr)1120.7561120.756Volume Flow(cum/hr)1.3331541.19827Enthalpy kcal/mol-67.8151-69.5591Enthalpy kcal/kg-3050.57-3129.02Enthalpy(Gcal/hr)-3.41894-3.50687表5-15 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error-0.087920-3.41894-3.5068705.2.4 换

31、热器（E0208）表5-16 热负荷表WQHeat Duty（Gcal/hr）-0.000080表5-17 流股焓变计算表INOUTStream2-152-16Temperature()30-8Pressure(Mpa)3.26523.2652Vapor Frac10Liquid Frac01Mole Flow(kmol/hr)0.01494050.0149405Mass Flow(kg/hr)0.83834290.8383429Volume Flow(cum/hr)0.10697410.0013342Enthalpy kcal/mol-4.100614-10.10972Enthalpy kc

32、al/kg-73.07933-180.171Enthalpy(Gcal/hr)-6.13E-05-0.000151表5-18 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error-0.000080-6.13E-05-0.00015105.3 塔5.3.1 塔（T0201）表5-19 热负荷表WQHeat Duty（Gcal/hr）-3.023373.11936表5-20 流股焓变计算表INOUTStream2-32-42-5Temperature()83100.586578.92627Pressure(Mpa)1.21.0341

33、Vapor Frac000Liquid Frac111Mole Flow(kmol/hr)268.3085217.906750.40175Mass Flow(kg/hr)6471.3243925.6562545.668Volume Flow(cum/hr)7.560234.2778533.362102Enthalpy kcal/mol-68.9935-66.9019-76.1315Enthalpy kcal/kg-2860.55-3713.62-1507.33Enthalpy(Gcal/hr)-18.5115-14.5784-3.83716表5-21 热量平衡计算一览表W（Gcal/hr）Q（

34、Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-18.5115-18.415505.3.2 塔（T0202）表5-22 热负荷表WQHeat Duty（Gcal/hr）-0.4924340.591739表5-23 流股焓变计算表INOUTStream2-92-102-11Temperature()100.022924.6112110.9378Pressure(Mpa)3.233.2652Vapor Frac000Liquid Frac111Mole Flow(kmol/hr)55.2088925.3960950.41564Mass Flow(kg/hr)254

35、5.6681424.9121120.756Volume Flow(cum/hr)3.5921632.4193161.333154Enthalpy kcal/mol-67.8896-9.051147-67.8151Enthalpy kcal/kg-1472.35-161.3178-3050.568Enthalpy(Gcal/hr)-3.74811-0.229864-3.418941表5-24 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-3.74811-3.6488105.4 反应器5.4.1 反应器（R0201）表5

36、-25 热负荷表WQHeat Duty（Gcal/hr）0.037620表5-26 流股焓变计算表INOUTStream2-72-8Temperature()100100Pressure(Mpa)33Vapor Frac00Liquid Frac11Mole Flow(kmol/hr)50.4017555.20889Mass Flow(kg/hr)2545.6682545.668Volume Flow(cum/hr)3.4977113.591991Enthalpy kcal/mol-75.1123-67.8907Enthalpy kcal/kg-1487.15-1472.37Enthalpy(

37、Gcal/hr)-3.78579-3.74817表5-27 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.037620-3.78579-3.748170第六章 合成叔丁胺工段热量衡量6.1 泵6.1.1 泵（P0301）表6-1 热负荷表WQHeat Duty（Gcal/hr）0.009190表6-2 流股焓变计算表INOUTStream3-13-2Temperature()24.5926234.35358Pressure(Mpa)350Vapor Frac00Liquid Frac11Mole Flow(kmol/h

38、r)25.4110325.41103Mass Flow(kg/hr)1425.7511425.751Volume Flow(cum/hr)2.4206422.473928Enthalpy kcal/mol-9.05177-8.69008Enthalpy kcal/kg-161.329-154.883Enthalpy(Gcal/hr)-0.23001-0.22082表6-3 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.009190-0.23001-0.2208206.1.2 泵（P0302）表6-4 热负荷表WQHea

39、t Duty（Gcal/hr）00表6-5 流股焓变计算表INOUTStream3-33-4Temperature()2525Pressure(Mpa)5050Vapor Frac00Liquid Frac11Mole Flow(kmol/hr)25.4125.41Mass Flow(kg/hr)432.7465432.7465Volume Flow(cum/hr)0.719290.71929Enthalpy kcal/mol-15.8225-15.8225Enthalpy kcal/kg-929.063-929.063Enthalpy(Gcal/hr)-0.40205-0.40205表6-6

40、 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-0.40205-0.4020506.1.3 泵（P0303）表6-7 热负荷表WQHeat Duty（Gcal/hr）0.02530表6-8 流股焓变计算表INOUTStream3-143-15Temperature()46.2036949.48217Pressure(Mpa)1450Vapor Frac00Liquid Frac11Mole Flow(kmol/hr)264.2592264.2592Mass Flow(kg/hr)7905.5177905.517Volume Flow(cu