team power-工艺计算和财务分析汇总表册团队

第一章物料衡 物料衡算的意 物料衡算遵循的原 物料衡 乙二醇的流 总物料衡 第二章能量衡 能量衡算的意 能量衡算的原 能量衡 亚硝酸甲酯与一氧化碳的混合气加热器计 草酸二甲酯合成固定床反应器能量与物料衡 草酸二甲酯冷凝分离过程由冷凝分离塔完 亚硝酸甲酯再生过程物料与能量衡 亚硝酸甲酯冷凝分离能量衡 氢气与草酸二甲酯混合气的加热 加氢制乙二醇过程的设计物料与能量衡 乙二醇冷凝分离能量衡 第3章原料、公用工程消耗及三废排放量一览 原料及辅助材料用 公用工程消耗 三废排放 第4章设备一 反应器一览 反应器工艺操作及设计参数汇总 反应器工艺操作及设计参数明细 塔设备一览 塔工艺设计及操作参数一览 塔盘工艺设计一览 容器数据一览 换热器一览 机泵一览 压缩机一览 管道一览 第5章财务分析一览 总投资及筹措 现金流量 生产成本汇总 销售收入 资产损益 主要技术经济指标 第一章料衡物料衡算的意义物料衡算遵循的原则乙二醇的流量制乙二醇工段CH3ONO（MN）的CH3ONO90%（COOCH3）2(DMO)的收率为72%。乙二醇合成工段DMO的转化率为95%，选择总物料衡算CH3OH:1341.40/(0.72×0.931)×2=4002.26kmol/h=128072.32kg/hH2:1341.40/0.931×4×60=321936kmol/h=643872kg/hO2:1341.40/(0.72×0.931)×0.5=1110.565kmol/h=32018.08kg/h(COOCH3)2:1341.40/0.931=1440.82kmol/h=170016.76kg/hCH3ONO:1341.40/(0.72×0.931)×2=4002.26kmol/h=244137.86kg/h 分子质量质量流量2第二章量衡能量衡算的意能量衡算的原QinQoutQoutQl——表示损失热量的总和。QWHout-∑Hout——离开设备的各物料焓之和∑Hin——进入设备的各物料焓之和亚硝酸甲酯与一氧化碳的混合气加热器计算A亚硝酸甲酯与一氧化碳都与40℃经混合器后进入加热器。进口温度40℃，B用0.608MpaC混合气流量CO=4002.26kmol/h，MN=4002.26kmol/h CO与MN在40℃与135℃的定压热进口带入热 出口带出热 热损比按10%算，0.608Mpa水蒸汽冷凝潜热为草酸二甲酯合成固定床反应器能量与物料衡算将反应得到的亚硝酸甲酯与经过纯化的CO固定床反应器进行催化偶联反应。操作压力2Mpa，反应温度135℃。DMO转化 副反应：2CH3ONO+CO=CH3OCOOCH3(DMC) 物料衡算：反应器进口 反应器出口 CH3ONO 能量衡算：反应器进口热量Q1；反应热Q2;反应器出口热量Q3;反应器带走热量Q4。忽略热损失，有Q1+Q2=Q3+Q4. 在135℃时，CO,DN,DMO,NO,DMC的比热容与标准焓 反应器放热：主反应：ΔHT1=(2×90.37-704.22-110.53×2-副反应：ΔHT2=(2×90.37-584.55-124.89×2)×103-Q22=4002.26×0.08×(-3.667×104)=-Q2=Q21+Q22=- 所以反应器需要转移走1.61×108(KJ/h)的热量草酸二甲酯冷凝分离过程由冷凝分离塔完成图2-2塔顶带出热：Q2= Q4=Q2+Q3－Q1=8.366×106+1.337×107-3.536×107=-1.365×107(KJ/h)1.365×107(KJ/h)亚硝酸甲酯再生过程物料与能量衡算图2-3 0反应器进口 反应器出口 对于反应热Q4=Q1+Q2－Q3(亚硝酸甲酯冷凝分离能量衡算Q4=Q1－(Q2+Q3)冷凝分离塔需要移走5.774×106(KJ/h)的热量 \混合器进口Q1=28.2×3219363.631×108(KJ/h)Q2=1440.82×170.6×166=4.08×107(KJ/h)Q3= 氢气与草酸二甲酯混合气的加热器图2-4A氢气与草酸二甲酯都在43.3℃经混合器后进入加热器。进口温度43.3℃，B用2.40MpaC混合气流量H2=321936kmol/h，DMO=1440.82kmol/h(2)出口 ×28.26)×200=1.9194Q3=1.9194×109-4.39×108=1.4804热损比按10%算，2.40Mpa水蒸汽冷凝潜热为加热水蒸气用量：W=1.4804加氢制乙二醇过程的设计物料与能量衡由合成气乙二醇主要分为草酸二甲酯的合成与草酸二甲酯的加氢两个加氢乙二醇是连串反应，首先是草酸二甲酯(DMO)JJfl氢乙醇酸甲酯成少量如1，2．丙二醇(PG)、1，2一丁二醇(BDO)、(一缩二乙二醇，DEG)等物质。转化率95%，选择性98%，收率93.1%，反应压力2Mpa。 在200℃时，各组分的定压热容与298K标准焓0反应器进口：DMO:H2:进口带入热 对于反应热ΔHT2=(-200.66×2-389.22+704.22)×103+(127.2×2+123.1-212.5-Q2=－7.765×104×1341.4=－1.042×108(KJ/h)Q4=Q1+Q2－Q3故反应器需要移走9.2×107(KJ/h)的热量乙二醇冷凝分离能量衡算 ( Q4=冷凝分离塔需要移走1.5741×109(KJ/h)的热量原料及辅助材料用煤公用工程消耗电反应器一览表反应器工艺操作及设计参数汇总表3443壁厚内径ZSM-ZSM-ZSM-反应器工艺操作及设计参数明细表34346塔设备一览表塔工艺设计及操作参数一览表度浮阀精馏是浮阀精馏是脱碳酸二甲酯筛板精馏是浮阀精馏是浮阀精馏是浮阀精馏是脱轻组分浮阀精馏是浮阀精馏6是塔盘工艺设计一览C3N块mDm---mmmm--99999999tsN个㎡Φ%θS-%-%度--容器数据一览1罐12Q235-133415361718罐1192Q235-1罐1换热器一览表流量）程））TB-0121TB-0121QBKF-2611油焦151泵TB-0121QBKF--311QBKF--1141IH80--2171134414281IH80--621IH80--111721４醇4141泵53518428112GDF50-75224262塔225232624622232622242224232625441IH65--8311116381414121号数Q扬程电机效率H功η）率））TB-0121TB-0121151TB-0121QBKF--311QBKF--11输41IH80--217114414281IH80--621IH80--1117212187515351乙乙42并8118联12752242622252剂3262462223262224222423262IH65--831111638121压缩机一览表流量556111L1BH212L1BH313L1BH414L1BH515L1BH621L1BH722L1BH833L1BH934L1BH35L1BH36L1BH37L1BH38L1BH49L1BH4L1BH5L1BH5L1BH5L1BH5L1BH5L1BH5L1BH11L1BH12L1BH13L1BH14L1BH15L1BH16L1BH17L1BH18L1BH19L1BH1L1BH1L1BH1L1BH11L1BH12L1BH234L1BH24L1BH252L1BH26L1BH37L1BH38L1BH396L1BH3L1BH37L1BH3L1BH31L1BH3L1BH4L1BH4L1BH4L1BH43L1BH4L1BH42L1BH4L1BH4L1BH45L1BH4L1BH5L1BH5L1BH5L1BH5L1BH5L1BH5L1BH56L1BH54L1BH5L1BH52L1BH5L1BH11L1BH12L1BH23L1BH24L1BH25L1BH26L1BH27L1BH28L1BH29L1BH2L1BH2L1BH2L1BH2L1BH2L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH34L1BH3L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH49L1BH49L1BH49L1BH49L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH48L1BH48L1BH48L1BH43L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH47L1BH47L1BH47L1BH47L1BH44L1BH4L1BH4L1BH4L1BH4L1BH45L1BH43L1BH48L1BH4L1BH4L1BH43L1BH4L1BH4L1BH48L1BH48L1BH44L1BH45L1BH45L1BH45L1BH48L1BH4L1BH4L1BH47L1BH4L1BH48L1BH43L1BH43L1BH45L1BH45L1BH4L1BH51L1BH5L1BH5L1BH5L1BH5L1BH5L1BH59L1BH59L1BH59L1BH56L1BH56L1BH54L1BH54L1BH5L1BH52L1BH5L1BH5L1BH5L1BH5L1BH5L1BH5L1BH51L1BH51L1BH32L1BH33L1BH34L1BH55L1BH56L1BH51L1BH11L1BH12L1BH13L1BH34L1BH45L1BH46L1BH47L1BH41L1BH22L1BH23L1BH34L1BH35L1BH36L1BH37L1BH38L1BH49L1BH5L1BH5L1BH5L1BH51L1BHN12L1BHN13L1BHN11L1BH11L1BH11L1BH22L1BH23L1BH34L1BH35L1BH36L1BH37L1BH38L1BH49L1BH5L1BH5L1BH5L1BH5财务分析一总投资及筹措表5-1总投资 123456123456100000000000000002000000