team power-工藝計算和財務(wù)分析匯總表冊團隊

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 總物料衡 第二章能量衡 能量衡算的意 能量衡算的原 能量衡 亞硝酸甲酯與一氧化碳的混合氣加熱器計 草酸二甲酯合成固定床反應(yīng)器能量與物料衡 草酸二甲酯冷凝分離過程由冷凝分離塔完 亞硝酸甲酯再生過程物料與能量衡 亞硝酸甲酯冷凝分離能量衡 氫氣與草酸二甲酯混合氣的加熱 加氫制乙二醇過程的設(shè)計物料與能量衡 乙二醇冷凝分離能量衡 第3章原料、公用工程消耗及三廢排放量一覽 原料及輔助材料用 公用工程消耗 三廢排放 第4章設(shè)備一 反應(yīng)器一覽 反應(yīng)器工藝操作及設(shè)計參數(shù)匯總 反應(yīng)器工藝操作及設(shè)計參數(shù)明細 塔設(shè)備一覽 塔工藝設(shè)計及操作參數(shù)一覽 塔盤工藝設(shè)計一覽 容器數(shù)據(jù)一覽 換熱器一覽 機泵一覽 壓縮機一覽 管道一覽 第5章財務(wù)分析一覽 總投資及籌措 現(xiàn)金流量 生產(chǎn)成本匯總 銷售收入 資產(chǎn)損益 主要技術(shù)經(jīng)濟指標 第一章料衡物料衡算的意義物料衡算遵循的原則乙二醇的流量制乙二醇工段CH3ONO（MN）的CH3ONO90%（COOCH3）2(DMO)的收率為72%。乙二醇合成工段DMO的轉(zhuǎn)化率為95%，選擇總物料衡算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 分子質(zhì)量質(zhì)量流量2第二章量衡能量衡算的意能量衡算的原QinQoutQoutQl——表示損失熱量的總和。QWHout-∑Hout——離開設(shè)備的各物料焓之和∑Hin——進入設(shè)備的各物料焓之和亞硝酸甲酯與一氧化碳的混合氣加熱器計算A亞硝酸甲酯與一氧化碳都與40℃經(jīng)混合器后進入加熱器。進口溫度40℃，B用0.608MpaC混合氣流量CO=4002.26kmol/h，MN=4002.26kmol/h CO與MN在40℃與135℃的定壓熱進口帶入熱 出口帶出熱 熱損比按10%算，0.608Mpa水蒸汽冷凝潛熱為草酸二甲酯合成固定床反應(yīng)器能量與物料衡算將反應(yīng)得到的亞硝酸甲酯與經(jīng)過純化的CO固定床反應(yīng)器進行催化偶聯(lián)反應(yīng)。操作壓力2Mpa，反應(yīng)溫度135℃。DMO轉(zhuǎn)化 副反應(yīng)：2CH3ONO+CO=CH3OCOOCH3(DMC) 物料衡算：反應(yīng)器進口 反應(yīng)器出口 CH3ONO 能量衡算：反應(yīng)器進口熱量Q1；反應(yīng)熱Q2;反應(yīng)器出口熱量Q3;反應(yīng)器帶走熱量Q4。忽略熱損失，有Q1+Q2=Q3+Q4. 在135℃時，CO,DN,DMO,NO,DMC的比熱容與標準焓 反應(yīng)器放熱：主反應(yīng)：ΔHT1=(2×90.37-704.22-110.53×2-副反應(yīng)：ΔHT2=(2×90.37-584.55-124.89×2)×103-Q22=4002.26×0.08×(-3.667×104)=-Q2=Q21+Q22=- 所以反應(yīng)器需要轉(zhuǎn)移走1.61×108(KJ/h)的熱量草酸二甲酯冷凝分離過程由冷凝分離塔完成圖2-2塔頂帶出熱：Q2= Q4=Q2+Q3－Q1=8.366×106+1.337×107-3.536×107=-1.365×107(KJ/h)1.365×107(KJ/h)亞硝酸甲酯再生過程物料與能量衡算圖2-3 0反應(yīng)器進口 反應(yīng)器出口 對于反應(yīng)熱Q4=Q1+Q2－Q3(亞硝酸甲酯冷凝分離能量衡算Q4=Q1－(Q2+Q3)冷凝分離塔需要移走5.774×106(KJ/h)的熱量 \混合器進口Q1=28.2×3219363.631×108(KJ/h)Q2=1440.82×170.6×166=4.08×107(KJ/h)Q3= 氫氣與草酸二甲酯混合氣的加熱器圖2-4A氫氣與草酸二甲酯都在43.3℃經(jīng)混合器后進入加熱器。進口溫度43.3℃，B用2.40MpaC混合氣流量H2=321936kmol/h，DMO=1440.82kmol/h(2)出口 ×28.26)×200=1.9194Q3=1.9194×109-4.39×108=1.4804熱損比按10%算，2.40Mpa水蒸汽冷凝潛熱為加熱水蒸氣用量：W=1.4804加氫制乙二醇過程的設(shè)計物料與能量衡由合成氣乙二醇主要分為草酸二甲酯的合成與草酸二甲酯的加氫兩個加氫乙二醇是連串反應(yīng)，首先是草酸二甲酯(DMO)JJfl氫乙醇酸甲酯成少量如1，2．丙二醇(PG)、1，2一丁二醇(BDO)、(一縮二乙二醇，DEG)等物質(zhì)。轉(zhuǎn)化率95%，選擇性98%，收率93.1%，反應(yīng)壓力2Mpa。 在200℃時，各組分的定壓熱容與298K標準焓0反應(yīng)器進口：DMO:H2:進口帶入熱 對于反應(yīng)熱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故反應(yīng)器需要移走9.2×107(KJ/h)的熱量乙二醇冷凝分離能量衡算 ( Q4=冷凝分離塔需要移走1.5741×109(KJ/h)的熱量原料及輔助材料用煤公用工程消耗電反應(yīng)器一覽表反應(yīng)器工藝操作及設(shè)計參數(shù)匯總表3443壁厚內(nèi)徑ZSM-ZSM-ZSM-反應(yīng)器工藝操作及設(shè)計參數(shù)明細表34346塔設(shè)備一覽表塔工藝設(shè)計及操作參數(shù)一覽表度浮閥精餾是浮閥精餾是脫碳酸二甲酯篩板精餾是浮閥精餾是浮閥精餾是浮閥精餾是脫輕組分浮閥精餾是浮閥精餾6是塔盤工藝設(shè)計一覽C3N塊mDm---mmmm--99999999tsN個㎡Φ%θS-%-%度--容器數(shù)據(jù)一覽1罐12Q235-133415361718罐1192Q235-1罐1換熱器一覽表流量）程））TB-0121TB-0121QBKF-2611油焦151泵TB-0121QBKF--311QBKF--1141IH80--2171134414281IH80--621IH80--111721４醇4141泵53518428112GDF50-75224262塔225232624622232622242224232625441IH65--8311116381414121號數(shù)Q揚程電機效率H功η）率））TB-0121TB-0121151TB-0121QBKF--311QBKF--11輸41IH80--217114414281IH80--621IH80--1117212187515351乙乙42并8118聯(lián)12752242622252劑3262462223262224222423262IH65--831111638121壓縮機一覽表流量556111L1BH212L1BH313L1BH414L1BH515L1BH621L1BH722L1BH833L1BH934L1BH35L1BH36L1BH37L1BH38L1BH49L1BH4L1BH5L1BH5L1BH5L1BH5L1BH5L1BH5L1BH11L1BH12L1BH13L1BH14L1BH15L1BH16L1BH17L1BH18L1BH19L1BH1L1BH1L1BH1L1BH11L1BH12L1BH234L1BH24L1BH252L1BH26L1BH37L1BH38L1BH396L1BH3L1BH37L1BH3L1BH31L1BH3L1BH4L1BH4L1BH4L1BH43L1BH4L1BH42L1BH4L1BH4L1BH45L1BH4L1BH5L1BH5L1BH5L1BH5L1BH5L1BH5L1BH56L1BH54L1BH5L1BH52L1BH5L1BH11L1BH12L1BH23L1BH24L1BH25L1BH26L1BH27L1BH28L1BH29L1BH2L1BH2L1BH2L1BH2L1BH2L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH3L1BH34L1BH3L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH49L1BH49L1BH49L1BH49L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH48L1BH48L1BH48L1BH43L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH4L1BH47L1BH47L1BH47L1BH47L1BH44L1BH4L1BH4L1BH4L1BH4L1BH45L1BH43L1BH48L1BH4L1BH4L1BH43L1BH4L1BH4L1BH48L1BH48L1BH44L1BH45L1BH45L1BH45L1BH48L1BH4L1BH4L1BH47L1BH4L1BH48L1BH43L1BH43L1BH45L1BH45L1BH4L1BH51L1BH5L1BH5L1BH5L1BH5L1BH5L1BH59L1BH59L1BH59L1BH56L1BH56L1BH54L1BH54L1BH5L1BH52L1BH5L1BH5L1BH5L1BH5L1BH5L1BH5L1BH51L1BH51L1BH32L1BH33L1BH34L1BH55L1BH56L1BH51L1BH11L1BH12L1BH13L1BH34L1BH45L1BH46L1BH47L1BH41L1BH22L1BH23L1BH34L1BH35L1BH36L1BH37L1BH38L1BH49L1BH5L1BH5L1BH5L1BH51L1BHN12L1BHN13L1BHN11L1BH11L1BH11L1BH22L1BH23L1BH34L1BH35L1BH36L1BH37L1BH38L1BH49L1BH5L1BH5L1BH5L1BH5財務(wù)分析一總投資及籌措表5-1總投資 123456123456100000000000000002000000