附录一 物料平衡计算书

NHD脱硫-甲醇合成法年产4.5万吨甲硫醇项目设计物料平衡计算书2017年“东华科技-陕鼓杯”第十一届全国大学生化工设计竞赛NHD脱硫-甲醇合成法年产4.5万吨甲硫醇项目设计参赛学校：桂林理工大学参赛团队：快乐的小鸡参赛队员：廖坚良 陈志和 邓家炬 陈燕萍 林小芳指导教师：李和平 杨 文 黎 燕 及方华 刘 峥物料平衡计算书目 录1.1 物料恒算的意义11.2 物料衡算的步骤11.3 物料恒算遵循的原则11.4 聚乙二醇二甲醚脱硫工段11.5 甲硫醇合成工段31.6 主要设备物料衡算51.6.1 T0101吸收塔51.6.2 T0102浓缩塔61.6.3 T0103再生塔71.6.4 R0201反应器81.6.5 T0201精馏塔91.6.6 T0202精馏塔101.6.7 T0203精馏塔111.6.8 T0204精馏塔121.1 物料恒算的意义物料衡算是确定化工生产过程中物料比例和物料转变的定量关系的过程，是化工工艺计算中最基本、最重要的内容之一。在化学项目中，设计或改造工艺流程和设备，了解和控制生产操作过程，核算生产过程的经济效益，确定主副产品的产率，确定原材料消耗定额，确定生产过程的损耗量，便于技术人员对现有的工艺过程进行分析，选择最有效的工艺路线，确定设备容量、数量和主要尺寸，对设备进行最佳设计以及确定最佳操作条件等都要进行物料核算。毫不夸张的说，一切化学项目的开发和放大都是以物料衡算为基础的。1.2 物料衡算的步骤（1）确定衡算范围，画出衡算示意图，标明各股物料的方向及组成。（2）定出衡算基准，对连续操作常以单位时间为基准如：kg/h，件/h，t/h；对间歇操作，常以一批物料（即一个操作循环为基准）。基准选定后，各流股按所选基准进行计算。1.3 物料恒算遵循的原则物料衡算的理论基础是质量守恒定理。它是研究某一体系内进出物料量及组成的变化。进行物料衡算时，必须先确定衡算的体系。对一般体系，均可用如下表示：系统中的积累 = 输入 输出 + 生成 消耗在稳定状态下有：输入 = 输出 生成 + 消耗特别地，当系统没有化学反应时，则可简化为：输入 = 输出1.4 聚乙二醇二甲醚脱硫工段图1-1 NHD脱硫工段工艺示意图表1-1 硫化氢提纯工段总物料衡算项目进出流股编号S1S15S29S30S3S6S12S36Temperature C403539.140403539.5-22Pressure bar361053032.5249.55Vapor Frac0.5810001110Enthalpy MMkcal/hr-1.201-0.133-75.693-0.003-0.218-0.001-0.142-1.543N21575.7580001485.7152.02683.8934.124CH47.620006.5840.0090.890.137CO2243.154000101.3460.24565.52876.034C3H817.63900000.005017.634C3H6-11441.26200000.29201440.97H2S4789.3560000.0052.6349.3754777.339C4H10-259.57600000.006059.571C4H10-121.79600000.002021.795C4H8-5340.85300000.030340.823C4H8-3151.4900000.010151.48C4H8-2120.63100000.0080120.624C5H12-218.03800000.001018.037C12H26O60133.16776135.422.663000135.8761.5 甲硫醇合成工段图1-2 甲硫醇合成工段工艺示意图表1-2 甲硫醇合成工段总物料衡算项目进出流股编号S35S36S42S46S55S58S59S60S61Temperature C-2240452.5-28.3-16-16-45-11.3Pressure bar564.710.05550.50.5Vapor Frac000110010Enthalpy MM kcal/hr-1.543-9.68-8.848-0.045-0.076-0.767-1.8340.2-1.631N24.124004.070000.0540CH40.137000.1330000.0040CO276.0340065.36800010.6660C3H817.634008.3110009.3230C3H6-11440.9700393.0470.067001047.9490.008H2S4777.339000000164.3610C4H10-259.5710012.0730.0410044.5382.918C4H10-121.795003.8210.003000.82917.141C4H8-5340.8230083.1570.02200140.664116.981C4H8-3151.48007.3510.707003.498139.927C4H8-2120.624007.8980.951000.746111.028C5H12-218.0370000.51900017.518C12H26O6135.87600000135.87600CH4O05479.2090010.5370921.81104.593CH4S00003.3250012.2646187.416C2H6S-20000376.7015.67406.073H2O002347.18500200.2086.437001.6 主要设备物料衡算1.6.1 T0101吸收塔图1-3 T0101吸收塔表1-3 T0101吸收塔物料衡算表项目进出流股编号S1S2S3S4Temperature C40404053.6Pressure bar363532.532.5Vapor Frac0.581010Enthalpy MMkcal/hr-1.201-32.536-0.218-33.519N21575.75801485.71590.043CH47.6206.5841.036CO2243.1540101.346141.808C3H817.6390017.639C3H6-11441.262001441.262H2S4789.35600.0054789.351C4H10-259.5760059.576C4H10-121.7960021.796C4H8-5340.85300340.853C4H8-3151.4900151.49C4H8-2120.63100120.631C5H12-218.0380018.038C12H26O6032739.39032739.39121.6.2 T0102浓缩塔图1-4 T0102浓缩塔表1-4 T0102浓缩塔物料衡算表项目进出流股编号S9S11S12S13Temperature C38.931.539.537Pressure bar10139.59.5Vapor Frac00.07810Enthalpy MMkcal/hr-43.15-33.898-0.142-76.906N2089.29983.8935.406CH401.0430.890.153CO20143.21665.52877.688C3H8017.666017.666C3H6-101442.67701442.677H2S04812.2149.3754802.839C4H10-2059.591059.591C4H10-1021.799021.799C4H8-50340.9170340.917C4H8-30151.5060151.506C4H8-20120.6420120.642C5H12-2018.038018.038C12H26O643398.7332739.39076138.121.6.3 T0103再生塔图1-5 T0103再生塔表1-5 T0103再生塔物料衡算表项目进出流股编号S21S24S25S26Temperature C3535383.8194.3Pressure bar3.5252.52.5Vapor Frac0001Enthalpy MMkcal/hr-76.108-0.997-60.763-0.27N20.0044.1204.124CH40.0010.13600.137CO25.45870.575076.034C3H88.6948.94017.634C3H6-1817.601623.36801440.97H2S1348.7283428.61104777.339C4H10-244.11115.46059.571C4H10-117.554.245021.795C4H8-5261.6579.1730340.823C4H8-3122.84128.6390151.48C4H8-299.40621.2180120.624C5H12-216.5271.51018.037C12H26O676138.12133.16776135.42135.8761.6.4 R0201反应器图1-6 R0201反应器表1-6 R0201反应器物料衡算表项目进出流股编号S38S39Temperature C320320Pressure bar56Vapor Frac11Enthalpy MMkcal/hr-7.391-8.815N24.1414.141CH40.1370.137CO278.82878.828C3H817.67717.677C3H6-11749.8951749.895H2S5103.456490.589C4H10-259.63159.631C4H10-121.80221.802C4H8-5344.289344.289C4H8-3158.832158.832C4H8-2120.659120.659C5H12-218.03718.037C12H26O6135.876135.876CH4O5479.213936.945CH4S621.2346824.094C2H6S-20398.445H2O02553.831.6.5 T0201精馏塔图1-7 T0201精馏塔表1-7 T0201精馏塔物料衡算表项目进出流股编号S43S44S45Temperature C30031.62.5Pressure bar43.022Vapor Frac101Enthalpy MMkcal/hr-0.002-0.452-0.083N24.0910.0044.088CH40.13300.133CO269.0310.86968.162C3H89.2190.8668.353C3H6-1804.524102.654701.87H2S340.38114.152326.228C4H10-217.8965.76212.133C4H10-16.9653.1363.829C4H8-5124.65738.03586.622C4H8-336.58921.88814.702C4H8-226.14918.2157.934C5H12-23.6063.6060C12H26O6000CH4O83.34883.3440.004CH4S1874.1491253.061621.088C2H6S-248.12948.1290H2O1.6251.62501.6.6 T0202精馏塔图1-8 T0202精馏塔表1-8 T0202精馏塔物料衡算表项目进出流股编号S49S50S51S53Temperature C42.91.435.269.6Pressure bar10111Vapor Frac0100Enthalpy MMkcal/hr-3.984-0.57-0.359-2.276N20.0540.05400CH40.0040.00400CO210.66610.66600C3H89.3239.32300C3H6-11048.0251047.9580.0670H2S164.361164.36100C4H10-247.49847.4560.0410C4H10-117.97417.9710.0030C4H8-5257.667257.6450.0220C4H8-3144.131143.4240.7040.003C4H8-2112.726111.7750.9450.005C5H12-218.03717.5180.5190C12H26O6135.87601.568134.308CH4O936.9414.593141.181791.167CH4S6203.0066199.683.3250C2H6S-2398.4456.073391.6990.674H2O206.64503.164203.4811.6.7 T0203精馏塔图1-9 T0203精馏塔表1-9 T0203精馏塔物料衡算表项目进出流股编号S50S60S61Temperature C1.4-45-11.3Pressure bar10.50.5Vapor Frac110Enthalpy MMkcal/hr-0.570.2-1.631N20.0540.0540CH40.0040.0040CO210.66610.6660C3H89.3239.3230C3H6-11047.9581047.9490.008H2S164.361164.3610C4H10-247.45644.5382.918C4H10-117.9710.82917.141C4H8-5257.645140.664116.981C