干气LPG烟气油品工艺计算.xls

干气平均分子量计算 输入数据干气流量= 组 分体积组成分子量扣除非烃 质量分率质量流率 %mimivim%kg/h 一氧化碳0.92825.201.42971.447 二氧化碳2.5444111.766.337316.863 空气13.1129380.1921.5581077.917 硫化氢1.633455.4255.423.143157.127 氢气33.77267.5467.543.830191.490 甲烷25.4516407.20407.2023.0901154.496 乙烷10.7430322.20322.2018.270913.504 乙烯9.1328255.64255.6414.496724.792 丙烷0.44417.6017.600.99849.900 丙烯1.044243.6843.682.477123.842 异丁烷0.545831.3231.321.77688.799 正丁烷0.062583.603.600.20410.195 1-丁烯0.335618.4818.481.04852.395 反丁烯-20.062563.473.470.1979.844 顺丁烯-20.062563.473.470.1979.844 正戊烷0.167211.5211.520.65332.662 总五烯0.075705.255.250.29814.885 合计100.0011763.541246.39100.005000.00 干气焓值计算 输入数据 组 分v%计算系数 一氧化碳0.9023.396430.13848 -0.0164118.89712 二氧化碳2.5414.001370.67027 -0.87505-8.57364 氮气12.3623.699590.097640.0594915.60296 氧气2.7519.755830.24852 -0.2710918.86205 硫化氢1.6320.843960.33672 -0.0941019.44200 氢气31.77 341.34548 -0.175412.33140 -129.56586 甲烷25.4536.817032.00616 -0.3824646.1381574.90000 乙烷10.7414.008543.13570 -3.0512143.45345160.80000 乙烯9.1315.988192.49064 -2.5935238.01414150.50000 丙烷0.48.038203.49075 -3.9606027.52980166.17000 丙烯1.049.689102.91098 -3.3155240.47386164.20000 异丁烷0.546.525863.59274 -4.301442.02567155.69500 正丁烷0.0628.293483.46000 -4.0210930.35096153.04400 1-丁烯0.338.449313.07222 -3.6219519.83025160.43500 反丁烯-20.0629.291502.98685 -3.4396119.90524168.46300 顺丁烯-20.0625.838753.10120 -3.5778960.73675166.56000 正戊烷0.168.023143.44880 -4.0567221.82802149.20900 总五烯0.0758.950463.09325 -3.6484316.67593150.41100 100.001 125.388261.14921 -0.04672-17.8432154.46931 温度过程变量焓值kj/kg 焓值kcal/kg 803.5315 0.2831662365.67565.03 1203.9315 0.2543562602.07621.49 干气氢含量计算 5000 kg/h 组分氢含量氢流量干气氢含量 m%kg/h% 0.000.0000.0000 0.000.0000.0000 0.000.0000.0000 5.929.3020.1860 100.00191.4903.8298 25.13290.1255.8025 20.11183.7063.6741 14.37104.1532.0831 18.299.1270.1825 14.3717.7960.3559 17.3415.3980.3080 17.341.7680.0354 14.377.5290.1506 14.371.4150.0283 14.371.4150.0283 16.675.4450.1089 14.372.1390.0428燃烧后组成 合计氢含量840.80516.816h2o 合计碳含量2692.97co2 计算过程变量 0.210570.00125-0.000150.170070.00000 0.355630.01702-0.02223 -0.217770.00000 2.929270.012070.007351.928530.00000 0.543290.00683-0.007450.518710.00000 0.339760.00549-0.001530.316900.00000 108.4455-0.055730.74069 -41.16310.00000 9.369930.51057-0.09734 11.74216 19.06205 1.504520.33677-0.327704.66690 17.26992 1.459720.22740-0.236793.47069 13.74065 0.032150.01396-0.015840.110120.66468 0.100770.03027-0.034480.420931.70768 0.035240.01940-0.023230.010940.84075 0.005140.00215-0.002490.018820.09489 0.027880.01014-0.011950.065440.52944 0.005760.00185-0.002130.012340.10445 干气焓值计算 0.003620.00192-0.002220.037660.10327 0.012840.00552-0.006490.034920.23873 0.006710.00232-0.002740.012510.11281 125.38826031.149206016 -0.0467234 -17.8432 54.46931 液化气平均分子量计算液化气平均氢含量计算 组成v%mmivim%组成v% 硫化氢03400硫化氢0.00 已烷乙烯1.252936.25 0.7463962已烷乙烯1.25 丙烷10.5844465.52 9.5851684丙烷10.58 丙烯37.17421561.14 32.144247丙烯37.17 异丁烷16.9858984.84 20.278092异丁烷16.98 正丁烷4.658266.85.493476正丁烷4.60 1-丁烯14.4956811.44 16.7077441-丁烯14.49 反丁烯-26.7456377.44 7.7715801反丁烯-26.74 顺丁烯-25.3356298.48 6.1457748顺丁烯-25.33 正戊烷2.8672205.92 4.2399422正戊烷2.86 总五烯07000总五烯0.00 合计10050.0783 103.11242合计100.00 液化气焓值计算 组 分v%abcde计算过程变量 硫化氢0 20.8440.33672-0.094119.4420.00000 乙烷1.2514.00853.1357 -3.05121 43.45345160.80.17511 丙烷10.58 8.03823.49075-3.960627.5298166.170.85044 丙烯37.17 9.68912.91098 -3.31552 40.47386164.23.60144 异丁烷16.986.525863.59274 -4.30144 2.025669155.6951.10809 正丁烷4.68.293483.46 -4.02109 30.35096153.0440.38150 1-丁烯14.498.449313.07222 -3.62195 19.83025160.4351.22431 反丁烯-26.74 9.29152.98685 -3.43961 19.90524168.4630.62625 顺丁烯-25.335.838753.1012 -3.57789 60.73675166.560.31121 正戊烷2.868.023143.4488 -4.05672 21.82802149.2090.22946 总五烯08.950463.09325 -3.64843 16.67593150.4110.00000 100 8.5078 3.1701441 -3.668279 28.31662 161.8474 8.507797 温度过程变量焓值kj/kg 1203.9315 0.2543558 1708.0812 803.5315 0.2831658 1631.8875 m%组分氢含量mihi 05.920 0.72386617.24 0.124795 9.29584318.291.70021 31.1739814.37 4.479701 19.66617.34 3.410085 5.32765717.34 0.923816 16.2034314.37 2.328432 7.53699714.37 1.083066 5.96026614.370.85649 4.11196116.76 0.689165 014.370 10015.59576 0.000000.000000.000000.00000 0.03920-0.038140.543172.01000 0.36932-0.419032.91265 17.58079 1.08201-1.23238 15.04413 61.03314 0.61005-0.730380.34396 26.43701 0.15916-0.184971.396147.04002 0.44516-0.524822.87340 23.24703 0.20131-0.231831.34161 11.35441 0.16529-0.190703.237278.87765 0.09864-0.116020.624284.26738 0.000000.000000.000000.00000 3.170144-3.668279 28.31662 161.8474 液化气平均氢含量计算 液化气焓值计算 计算过程变量 空空气气自自t1升升（降降）温温到到t2的的平平均均比比热热 初始温度t1（）=5最终温度t2（）=201 组分v%mmivim%abc n278.8028.0022.0676.600.9661.04e-04-3.44e-09 o220.9032.006.6923.220.802.07e-04-4.38e-08 h2o0.3018.000.050.191.663.07e-043.56e-08 合计100.0028.81100.00 一一二二再再混混合合烟烟气气自自t1升升（降降）温温到到t2的的平平均均比比热热 初始温度t1（）=0最终温度t2（）=250 组分v%mmivim%abc n280.72822.6073.0520.9661.039e-04 -3.440e-09 o20.12320.040.1240.8002.070e-04 -4.380e-08 co216.6447.3023.6130.6034.830e-04 -1.080e-07 co3.25280.912.9420.9501.350e-04 -1.330e-09 h2o0180.000.0001.6603.070e-043.560e-08 so20.13640.080.2690.43913.594e-04 -1.042e-07 合计100.830.93100.00 二二再再混混合合烟烟气气自自t1升升（降降）温温到到t2的的平平均均比比热热 初始温度t1（）=25最终温度t2（）=725 组分v%mmivim%abc n276.12821.3171.1640.9661.039e-04 -3.440e-09 o24.4321.414.7020.8002.070e-04 -4.380e-08 co214.1446.2020.7200.6034.830e-04 -1.080e-07 co0280.000.0000.9501.350e-04 -1.330e-09 h2o5.5180.993.3061.6603.070e-043.560e-08 so20.05640.030.1070.43913.594e-04 -1.042e-07 100.1529.94100.00 空空气气焓焓值值计计算算 组 分v%计算系数计算过程变量 氮气7923.699590.097640.0594915.6029618.72268 氧气2119.755830.24852 -0.2710918.862054.14872 水020.843960.33672 -0.0941019.442000.00000 10022.871400.12932 -0.0099316.287370.00000 22.8714004 温度（）过程变量焓值kj/kg 62.79150.35823 282.3929 2305.0315 0.198748 510.4798 烟气焓值计算 输入数据 组 分v%计算系数计算过程变量 一氧化碳0.9023.396430.13848 -0.0164118.897120.21057 二氧化碳2.5414.001370.67027 -0.87505-8.573640.35563 氮气10.3623.699590.097640.0594915.602962.45528 氧气2.7519.755830.24852 -0.2710918.862050.54329 硫化氢1.6320.843960.33672 -0.0941019.442000.33976 18.183.904520.04071 -0.025202.404380.00000 3.90452206 温度（）过程变量焓值kj/kg 252.9815 0.33540252.4158 515.37.8845 0.126831 146.6811 t1t2组分cpcpimi 278.15474.151.042670.7986 278.15474.150.936710.2175 278.15474.151.906410.0036 计算比热1.0197 kj/kg.k t1t2组分cpcpimi 273.15523.151.04700.7649 273.15523.150.94330.0012 273.15523.150.93460.2207 273.15523.151.05680.0311 273.15523.151.92200.0000 273.15523.150.67410.0018 计算比热1.0196 kj/kg.k t1t2组分cpcpimi 298.15998.151.09590.7799 298.15998.151.00780.0474 298.15998.151.07980.2237 298.15998.151.12320.0000 298.15998.152.10720.0697 298.15998.150.76090.0008 计算比热1.1215 kj/kg.k 0.077140.0470012.326340.00000 0.05219 -0.056933.961030.00000 0.000000.000000.000000.00000 0.1293248 -0.00993 16.2873690 空空气气自自t1升升（降降）温温到到t2的的平平均均比比热热 一一二二再再混混合合烟烟气气自自t1升升（降降）温温到到t2的的平平均均比比热热 二二再再混混合合烟烟气气自自t1升升（降降）温温到到t2的的平平均均比比热热 空空气气焓焓值值计计算算 计算过程变量 0.00125 -0.000150.170070.00000 0.01702 -0.02223-0.217770.00000 0.010120.006161.616470.00000 0.00683 -0.007450.518710.00000 0.00549 -0.001530.316900.00000 0.0407095-0.0252 2.40438130 烟气焓值计算 计算过程变量 油品特性因数计算 名称 密度 恩氏蒸馏馏程() 过程变量 g/cm310%30%50%70%90%tv()xlx 直馏腊油0.8912389430475512550471.222.29705 焦化腊油0.8888389430475512550471.222.29705 常压渣油0.9221374431494558642499.83.4 3.118299 减压渣油0.9554486498512578628540.41.8 2.034165 混合原料0.9221374431494558642499.83.4 3.118299 回 炼 油0.954936738639841044440111.37262 油 浆1.0153486498512578659546.62.2 2.328054 粗 汽 油0.73362871121371671131.3 2.161715 稳定汽油0.723462871121371671131.3 2.161715 轻 柴 油0.89452252402562732912570.8 1.370983 重 柴 油0.92353253463683964153701.1 1.601152 分馏顶循环 0.765495115146179198146.61.3 2.079493 分馏一中0.91255269289308365297.21.4 1.953177 分馏二中0.954936738639841044440111.37262 油品分子量计算 名 称特性因数t中密度分子量质量流量 摩尔流量 kg/cm3kg/hmol/h 直馏腊油12.31734.4050.8912439.57 焦化腊油12.34734.4050.8888440.84 常压渣油11.98750.3420.9221452.56 减压渣油11.84805.9040.9554538.66 混合原料11.98750.3420.9221452.56 回 炼 油11.14670.2040.9549323.23 油 浆11.16809.4921.0153507.68 粗 汽 油11.99377.4640.73395.12 稳定汽油12.15377.4640.723490.64 轻 柴 油10.97526.2110.8945195.24 重 柴 油11.33638.1910.9235290.14 分馏顶循环11.82411.750.7654112.86 分馏一中11.03563.2990.91221.63 分馏二中11.14670.2040.9549323.23 油品焓值计算 名 称液相温度密度特性因数液相焓气相温度 气化潜热汽相焓液相焓 g/cm3kj/kgkj/kgkj/kgkcal/kg 直馏腊油1910.891212.31455.160490.0316.2821521.935108.7132 焦化腊油1730.888812.34410.166515.0315.8581608.97097.96652 常压渣油1730.922111.98392.644515.0316.8121567.64493.78131 减压渣油1800.955411.84396.790500.0306.7261492.70294.77158 混合原料1950.922111.98447.380506.0316.8121538.119106.855 回 炼 油3470.954911.14819.232506339.5131464.309195.6701 油 浆1901.015311.16386.926506304.4911431.34292.41558 粗 汽 油800.73311.99208.966120404.133610.87449.91066 稳定汽油2000.723412.15531.735517.3401.2971679.199127.0028 轻 柴 油2000.894510.97443.597517.3376.7741516.302105.9512 重 柴 油0.923511.3329.302517.3346.1821528.3326.998746 分馏顶循环800.765411.82202.613517.3396.8701635.96748.39319 分馏一中1870.9111.03408.788517.3 366.630771513.32597.63735 分馏二中2070.954911.14445.265339.51342350.868106.3497 蒸汽焓值计算 温度压力蒸汽焓值 mpakj/kg 1200.01 2721.005 1750.182822.11