8-3 附录三 能量平衡计算书

目 录1.概述12.能量衡算目的13.能量衡算方法14.系统能量衡算24.1 催化干气脱硫工段24.2 胺液再生工段34.3 硫醚合成工段54.4 产物预分离工段64.5 硫醚精制及甲醇回收工段74.6 亚砜合成工段94.7 亚砜精制工段10 中化泉州石化3万吨/年干气脱硫制二甲基亚砜项目能量平衡计算书1.概述本项目拟建一套年产2.7万吨的二甲基亚砜装置，在全工艺段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。对于新设计的装置，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。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.能量衡算目的（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率，确定加热蒸汽和冷却剂的用量，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。3.能量衡算方法根据能量守恒：输入系统的能量 = 输出系统的能量 + 系统积累的能量本装置主要设备有反应器、精馏塔、换热器、蒸发器、闪蒸罐、碱洗罐、压缩机和泵，输入整个生产系统的能量主要有电能、加热蒸汽带入的能量和进入物料的焓，输出的能量有冷却剂带走的能量和输出物料的焓。Hout = Q + W + Hin式中：Q设备的热负荷；W输入系统的机械能；Hin进入设备的各物料焓之和；Hout离开设备的各物料焓之和。SSR 12 4.系统能量衡算4.1 催化干气脱硫工段图4-1 催化干气脱硫工段流程图表4-1 干气脱硫塔T0101能量衡算表InOutStream ID1-11-21-31-4Temperature 27.0045.0046.9088.40Pressure bar7.507.507.207.20Vapor Frac1.000.001.000.00Mole Flow kmol/hr215.41788.36169.05834.71Mass Flow kg/hr3750.0021033.262148.1122635.18Volume Flow cum/hr716.7521.08624.7126.10Enthalpy kW-1954.6-64968.6-1743-65180.2H(kW)-66923.15-66923.15QC(kW)0QR(kW)0W(kW)0Total(kW)-66923.15-66923.15表4-2 富液闪蒸罐V0101能量衡算表InOutStream ID1-51-71-91-10Temperature 84.50 45.00 45.80 85.20 Pressure bar1.40 7.50 1.40 1.40 Vapor Frac0.01 0.00 1.00 0.00 Mole Flow kmol/hr834.71 62.20 0.06 896.85 Mass Flow kg/hr22635.18 1659.44 0.70 24293.92 Volume Flow cum/hr125.07 1.66 1.14 27.80 Enthalpy kW-65180.15 -5125.76 -0.76 -70305.14 H(kW)-70305.91 -70305.91 Q(kW)0.00 W(kW)0.00 Total(kW)-70305.91 -70305.91 4.2 胺液再生工段图4-2 胺液再生工段流程图表4-3 胺液再生塔T0102能量衡算表InOutStream ID1-111-191-231-121-13Temperature 90.00 113.00 70.00 103.80 112.10 Pressure bar1.40 1.43 1.40 1.30 1.43 Vapor Frac0.01 1.00 0.00 1.00 0.00 Mole Flow kmol/hr896.85 361.36 214.94 277.95 1195.21 Mass Flow kg/hr24293.92 6554.10 3884.58 5786.83 28945.75 Volume Flow cum/hr199.01 8096.71 3.99 6701.58 30.48 Enthalpy kW-70079.69 -23946.40 -16846.01 -15511.44 -95360.73 H(kW)-110872.10 -110872.10 QC(kW)0.00 QR(kW)0.00 W(kW)0.00 Total(kW)-110872.10 -110872.10 表4-4 热泵工质压缩机C0101能量衡算表InOutStream IDR-600-1R-600-2Temperature 54.40132.50Pressure bar4.9527.00Vapor Frac1.001.00Mole Flow kmol/hr911.85911.85Mass Flow kg/hr53000.0053000.00Volume Flow cum/hr4443.41653.73Enthalpy kW-31319.06-30002.01H(kW)-31319.06-30002.01Q(kW)0.00W(kW)1317.05Total(kW)-30002.01-30002.01表4-5 吸附脱水塔T0103能量衡算表InOutStream ID1-161-201-30Temperature 70.00 70.00 70.00 Pressure bar1.30 1.30 1.30 Vapor Frac1.00 1.00 1.00 Mole Flow kmol/hr63.00 15.22 47.78 Mass Flow kg/hr1902.25 274.21 1628.05 Volume Flow cum/hr1382.69 0.28 1048.65 Enthalpy kW-1270.92 -1194.15 -254.93 续表4-5H(kW)-1270.92 -1449.08 Q(kW)-178.16 W(kW)0.00 Total(kW)-1270.92 -1270.92 4.3 硫醚合成工段图4-3 硫醚合成工段流程图表4-6 一级压缩机C0201能量衡算表InOutStream ID2-42-5Temperature 68.90 175.80Pressure bar1.10 3.50Vapor Frac1.00 1.00 Mole Flow kmol/hr230.43 230.43 Mass Flow kg/hr7694.98 7694.98 Volume Flow cum/hr5956.56 2457.58 Enthalpy kW-9038.92 -8713.33 H(kW)-9038.92 -8713.33 Q(kW)0.00 W(kW)325.59 Total(kW)-8713.33 -8713.33 表4-7 二级压缩机C0202能量衡算表InOutStream ID2-62-7Temperature 90.00 142.00Pressure bar3.50 6.10Vapor Frac1.00 1.00 Mole Flow kmol/hr230.43 230.43 Mass Flow kg/hr7694.98 7694.98 Volume Flow cum/hr1987.82 1303.75 Enthalpy kW-8978.20 -8821.40 H(kW)-8978.20 -8821.40 Q(kW)0.00 W(kW)156.80 Total(kW)-8821.40 -8821.40 表4-8 硫醚合成反应器R0201能量衡算表InOutStream ID2-82-9Temperature 210.00 230.00Pressure bar6.10 6.00Vapor Frac1.00 1.00 Mole Flow kmol/hr230.43 230.43 Mass Flow kg/hr7694.98 7694.98 Volume Flow cum/hr1517.44 1606.59 Enthalpy kW-8599.61 -9741.76 H(kW)-8599.61 -9741.76 Q(kW)-1142.15 W(kW)0.00 Total(kW)-8599.61 -8599.61 4.4 产物预分离工段图4-4 产物预分离工段流程图表4-9 H2S汽提塔T0201能量衡算表InOutStream ID2-152-162-17Temperature 37.70 37.8071.20Pressure bar2.00 2.002.00Vapor Frac0.05 1.00 0.00 Mole Flow kmol/hr230.43 29.27 201.16 Mass Flow kg/hr7694.98 1160.14 6534.87 Volume Flow cum/hr146.42 378.35 7.90 Enthalpy kW-12572.46 -313.28 -11974.34 H(kW)-12572.46 -12287.62 QC(kW)0.00 QR(kW)284.86 续表4-9W(kW)0.00 Total(kW)-12287.62 -12287.62 表4-10 预分离塔T0202能量衡算表InOutStream ID2-182-192-20Temperature 84.00 50.00 93.70 Pressure bar2.00 1.75 1.88 Vapor Frac0.41 1.00 0.00 Mole Flow kmol/hr201.16 60.00 141.16 Mass Flow kg/hr6534.87 3317.05 3217.83 Volume Flow cum/hr1232.64 921.12 4.01 Enthalpy kW-11191.97 -1134.35 -10353.92 H(kW)-11191.97 -11488.27 QC(kW)-1033.67 QR(kW)737.36 W(kW)0.00 Total(kW)-10454.61 -10454.61 表4-11 萃取精馏塔T0203能量衡算表InOutStream ID2-192-382-212-22Temperature 50.00 86.00 45.10 112.20 Pressure bar1.75 1.53 1.50 1.75 Vapor Frac1.00 0.00 0.00 0.00 Mole Flow kmol/hr60.00 555.13 47.93 567.20 Mass Flow kg/hr3317.05 10001.00 2927.33 10390.72 Volume Flow cum/hr921.12 10.72 3.54 11.62 Enthalpy kW-1134.35 -43348.08 -823.17 -43784.62 H(kW)-44482.43 -44607.79 QC(kW)-1819.99 QR(kW)1694.63 W(kW)0.00 Total(kW)-42787.80 -42787.80 4.5 硫醚精制及甲醇回收工段图4-5 硫醚精制及甲醇回收工段流程图表4-12 硫醇硫醚分离塔T0204能量衡算表InOutStream ID2-402-412-42Temperature 45.20 23.50 58.70 Pressure bar2.20 2.00 2.01 Vapor Frac0.00 0.00 0.00 Mole Flow kmol/hr47.93 3.22 44.71 Mass Flow kg/hr2927.33 154.30 2773.03 Volume Flow cum/hr3.54 0.18 3.42 Enthalpy kW-822.94 -44.44 -757.09 H(kW)-822.94 -801.52 QC(kW)-547.45 QR(kW)568.87 W(kW)0.00 Total(kW)-254.07 -254.07 表4-13 低压甲醇回收塔T0205能量衡算表InOutStream ID2-232-272-242-25Temperature 104.80 101.90 67.00 99.00 Pressure bar1.75 1.23 1.10 1.23 Vapor Frac0.01 1.00 1.00 0.00 Mole Flow kmol/hr708.36 132.40 45.99 794.77 Mass Flow kg/hr13608.54 2649.03 1468.59 14788.98 Volume Flow cum/hr118.58 3347.96 1182.28 16.46 Enthalpy kW-54138.54 -8579.09 -2545.70 -61381.96 H(kW)-62717.63 -63927.66 QC(kW)-1209.82 QR(kW)0.00 W(kW)0.00 Total(kW)-62717.63 -62717.63 表4-14 高压甲醇回收塔T0206能量衡算表InOutStream ID2-292-342-302-35Temperature 102.10 120.10 120.30 161.70 Pressure bar6.34 6.33 6.33 6.43 Vapor Frac0.00 0.00 1.00 0.00 Mole Flow kmol/hr662.38 174.68 189.63 647.43 Mass Flow kg/hr12140.01 5540.98 6017.03 11663.95 Volume Flow cum/hr13.42 8.29 980.01 13.73 Enthalpy kW-51284.48 -11092.00 -10395.13 -49379.73 H(kW)-62376.48 -59774.86 QC(kW)0.00 QR(kW)2601.62 W(kW)0.00 Total(kW)-59774.86 -59774.86 4.6 亚砜合成工段图4-6 亚砜合成工段流程图表4-15 硫醚氧化塔R0301能量衡算表InOutStream ID3-23-33-7TailGas3-4Temperature 40.70 31.00 25.00 25.00 50.00 Pressure bar1.10 1.10 1.10 1.02 1.10 Vapor Frac1.00 1.00 0.00 1.00 0.00 Mole Flow kmol/hr44.71 29.35 12.30 6.38 58.05 Mass Flow kg/hr2773.03 960.90 947.01 209.67 4471.27 Volume Flow cum/hr1060.48 674.80 0.87 155.06 4.18 Enthalpy kW-454.00 15.67 -671.48 5.91 -3117.59 H(kW)-1109.81 -3111.68 Q(kW)-2001.87 W(kW)0.00 Total(kW)-1109.81 -1109.81 4.7 亚砜精制工段图4-7 亚砜精制工段流程图表4-16 碱洗罐V0301能量衡算表InOutStream ID3-63-83-9Temperature 50.0030.0068.50Pressure bar1.101.051.05Vapor Frac0.000.000.00Mole Flow kmol/hr45.7627.4872.70Mass Flow kg/hr3524.25500.004024.25Volume Flow cum/hr3.300.453.82Enthalpy kW-2457.29-2143.51-4600.80H(kW)-4600.80-4600.80Q(