年處理14萬(wàn)噸混合芳烴精餾系統(tǒng)模擬及工藝設(shè)計(jì)

1、年處理14.21第1章物料衡算41.1設(shè)計(jì)計(jì)算說明 41.1.1主要設(shè)計(jì)條件及技術(shù)參數(shù)41.1.2設(shè)計(jì)基礎(chǔ)數(shù)據(jù)41.2物料衡算71.2.1苯塔物料衡算81.2.2甲苯塔物料衡算 81.2.3對(duì)二甲苯塔物料衡算91.2.4各塔物料衡算匯總1.0.1.3核實(shí)清晰分割 1.11.3.1求解相對(duì)揮發(fā)度1.11.3.2核實(shí)清晰分割.14第2章熱量衡算182.1苯塔熱量衡算 182.1.1塔進(jìn)料液代入熱量1.8.2.1.2塔頂出料帶出液1.9.2.1.3塔底餾出液中帶出的熱量192.1.4塔頂冷凝器帶出的熱量 202.1.5塔釜蒸汽帶入的熱2.12.2甲苯塔熱量衡算212.2.1塔頂出料帶出的熱量212.

2、2.2塔底餾出液帶出的熱量222.2.3塔頂冷凝器帶出的熱量 222.2.4塔釜再沸器加入的熱量 23第3章甲苯塔設(shè)備計(jì)算 243.1苯塔設(shè)計(jì)的主要依據(jù)和條件243.1.1苯塔塔頂條件下的流量及物性參數(shù) 243.1.2塔釜條件下的流量及物性參數(shù)253.1.3進(jìn)料條件下的流量及物性參數(shù)273.1.4精餾段的流量及物性參數(shù)283.1.5提餾段流量及物性參數(shù) 293.2甲苯塔塔體工藝尺寸的計(jì)算303.2.1塔徑的計(jì)算30安全系數(shù)：313.2.2塔高的計(jì)算313.3塔板主要工藝尺寸的計(jì)算323.3.1溢流堰裝置的計(jì)算323.3.2塔板布置333.3.3篩板的流體力學(xué)驗(yàn)算353.4塔板負(fù)荷性能圖37.3

3、.4.1霧沫夾帶線373.4.2液泛線383.4.3液相負(fù)荷上限383.4.4漏液線38803.4.5液相負(fù)荷下限.第4章甲苯塔附屬設(shè)備計(jì)算. 4.1苯塔冷凝器設(shè)計(jì)及選型4.1.14.1.24.1.33941.41確定流體流動(dòng)的空間 熱負(fù)荷 有效平均溫差 初選冷凝器 核算總傳熱系數(shù) 換熱器內(nèi)流體的流動(dòng)阻力 甲苯冷凝器的有關(guān)參數(shù).4141414.1.44.1.54.1.64.1.74.2再沸器4.3回流罐的選擇4.4泵的選型4.5主要接管尺寸的選取4.5.14.5.241.4. 1 .434444.45.454.5.34.5.44.5.5進(jìn)料管.回流管.釜液出口管塔頂蒸汽管加熱蒸汽管46.464

4、6474747第1章物料衡算1.1設(shè)計(jì)計(jì)算說明1.1.1主要設(shè)計(jì)條件及技術(shù)參數(shù)1年處理量:14.2萬(wàn)噸混合芳烴2生產(chǎn)方法：精餾3. 生產(chǎn)時(shí)間：8000小時(shí)/年4. 原料規(guī)格表1-1原料規(guī)格組分精餾原料組成 %（ wt）苯53.000甲苯26.000二甲苯19.500C91.500合計(jì)100.05. 各塔產(chǎn)品回收率T0201 （苯塔）：99.9% （苯）T0202 （甲苯塔）：99.5%（甲苯）T0203（二甲苯塔）：98.0%（二甲苯）6. 操作壓力表1-2操作壓力項(xiàng)目T0201T0202T0203塔頂（kPa）101.3101.3101.3塔底（kPa）140.3145.3180.31.1.

5、2設(shè)計(jì)基礎(chǔ)數(shù)據(jù)表1-3各組分的相對(duì)分子質(zhì)量組分苯甲苯二甲苯異丙苯相對(duì)分子質(zhì)量（kg/kmol）78.1292.13106.16120.19表1-4各組分的安托因常數(shù)組分ABCTmax (C)Tmin (C)苯20.79362788.51220.79103.856.85甲苯20.90653096.52219.48136.856.85對(duì)二甲苯20.98913346.65215.31166.8526.85止丙苯20.89903433.84207.14180.8537.85注：InPs=A-B/(T+C) ( Ps： Pa； T：C)表1-5苯的物性常數(shù)表(101.325kPa) 2溫度C蒸汽壓 毫米

6、水柱汽化熱 卡/克分子密度 克/厘米3熱容 卡/克分 子C表面張力 達(dá)因/厘米黏度厘泊導(dǎo)熱系數(shù)X 10-5 卡 /厘米秒1045.52981400.887331.64930.090.74235.82075.19880440.877432.02228.800.63834.930119.3379420.867532.44027.520.55434.040182.7778360.857332.96326.250.48533.150271.2777230.847033.48514.990.42932.360391.4576060.836634.00823.740.38131.570550.807482

7、0.825934.53022.500.34230.780757.6273530.815035.09821.270.30830.0904020.972180.803935.76920.060.27929.21001350.470770.792536.44118.850.25528.51102.31369300.780837.29217.660.23327.71202.96467760.768938.18816.490.21527.01303.74666140.756739.08415.320.19826.31404.67464460.744139.97914.170.18425.71505.76

8、562690.731140.87513.040.17125.01607.03560830.717641.83111.920.16124.31708.50158880.703742.80110.820.15023.7表1-6甲苯物性常數(shù)表2溫度C蒸汽壓 毫米水柱汽化熱 卡/克分子密度 克/厘米熱容3卡/克分子C表面張力 達(dá)因/厘米黏度厘泊導(dǎo)熱系數(shù)X 10-5 卡 /厘米秒1012.42991950.876336.31929.710.66035.02021.83590820.867036.98928.510.58034.1續(xù)表1-6甲苯物性常數(shù)表溫度蒸汽壓汽化熱密度熱容表面張力黏度導(dǎo)熱系數(shù)C毫米水

9、柱卡/克分子克/厘米3卡/克分達(dá)因/厘米厘泊X 10-5 卡 /厘子C米秒3036.66489670.857637.71327.370.51433.24059.15488490.848238.66726.220.45932.35092.10987290.838839.62125.070.41231.560138.9586050.829340.36923.940.37330.770203.7484790.819741.11822.810.34029.9溫度c蒸汽壓 毫米水柱汽化熱 卡/克分子密度 克/厘米3熱容 卡/克分 子C表面張力 達(dá)因/厘米黏度厘泊導(dǎo)熱系數(shù)X 10-5 卡 /厘米秒c802

10、91.2183490.810041.86621.690.31129.190406.7382160.800242.61520.590.28628.4100556.3180800.790343.36319.490.26427.7110746.5879390.780344.49718.410.24527.0120984.7077940.770045.63217.340.22826.31301278.476440.759546.46116.270.21325.61401635.774900.748847.30415.230.20025.01502.72773300.737848.16414.190.1

11、8824.31603.40571640.726549.04813.170.17723.71704.20369910.715049.96012.610.16723.0表1-7二甲苯物性常數(shù)表2溫度蒸汽壓汽化熱密度熱容表面張力黏度導(dǎo)熱系數(shù)c毫米水柱卡/克分子克/厘米3卡/克分達(dá)因/厘米厘泊X 10-5 卡 /厘子C米秒c10104280.877542.5130.220.70033.120103230.869043.0929.120.61532.630102130.860344.3028.020.54732.14018.931100970.851645.5126.940.49131.55031.14

12、599760.842746.4025.860.44430.96049.41798500.833747.2924.780.40430.47075.91197190.824548.1823.720.36929.880113.2695820.815249.0722.670.33929.290164.6294390.805849.9621.620.31328.6100233.6692910.796250.8520.580.28928.0110324.5891380.786551.7419.560.26827.4120442.1289780.776652.6418.540.24926.8130591.5

13、388130.766553.5417.530.23226.2140778.5786410.756154.4416.540.21725.61501009.484630.745655.3515.550.20424.91601290.882780.734856.2714.570.19224.31702.14880860.723857.2113.610.18123.6表1-8異丙苯物性常數(shù)表2溫度蒸汽壓汽化熱密度熱容表面張力黏度導(dǎo)熱系數(shù)c毫米水柱卡/克分子克/厘米3卡/克分達(dá)因/厘米厘泊X 10-5 卡 /厘子C米秒c101.70109840.870229.270.90032.7203.3410878

14、0.862128.260.78032.0306.22107670.853951.6327.260.68231.24011.00106510.845652.6626.270.60130.55018.62105290.837253.7025.280.53529.76030.31104030.828654.8424.300.47929.07047.63102700.820055.9923.320.43128.38072.54101330.811256.9122.350.39127.790107.4099900.802357.6021.390.35627.0100155.0298410.793258.

15、2920.430.32626.4110218.9896870.784059.3919.490.30025.7120301.9895280.774760.4818.550.27725.1130404.1993620.765161.5317.620.25724.5140544.8691910.755462.5816.690.24023.9150714.0090130.745563.6315.780.22423.31601.212988290.735464.6814.870.21022.71701.545186390.7225165.7313.970.19722.2表1-9水的物性數(shù)據(jù)物質(zhì)分子式相對(duì)

16、分子量比熱容（kJ kg-1 K-1)25 C35 C水H2O18.024.1784.174表1-10蒸汽的物性數(shù)據(jù)物質(zhì)絕對(duì)壓強(qiáng)溫度汽化熱飽和水蒸氣8.08 X 103kPa180 C2049.4kJ/kg1.2物料衡算本設(shè)計(jì)中的物系，二甲苯取對(duì)二甲苯，c9選取異丙苯。在以下的計(jì)算的過程中：1代表苯，2代表甲苯，3代表對(duì)二甲苯，3代表異丙苯。 由表1-1和表1-3計(jì)算原料組分的摩爾分?jǐn)?shù)為：0.53/78.12Xf1 =0.59130.53/78.12 +0.26/92.13+0.195/106.16 +0.015/120.190.26/92.13Xf2=0.24350.53/78.12 +0.

17、26/92.13+0.195/106.16 +0.015/120.190.195/106.16Xf3=0.15650.53/78.12 +0.26/92.13+0.195/106.16 +0.015/120.190.015/120.19Xf4=0.00870.53/78.12 +0.26/92.13+0.195/106.16 +0.015/120.19原料的平均摩爾質(zhì)量M=0.5913 X 78.12+0.2435 X 92.13+0.1565 X 106.16+0.0087 X 120.19=86.29kg/kmol 單位處理量Q=14.2X 104x 103/8000=17800kg/h=

18、206.28kmol/h進(jìn)料質(zhì)量流率： F1=17800 X 0.53=9434kg/hF2=17800 X 0.26=4628kg/hF3=17800X 0.195=3471kg/h F3=17800 X 0.015=267kg/h摩爾流率：F1=206.281 X 0.5913=121.974kmol/h F 2=206.281 X 0.2435=50.229kmol/hF3=206.281 X 0.1565=32.283kmol/hF4=206.281 X 0.0087=1.795kmol/h1.2.1苯塔物料衡算F1=D 1+W1F1Xf=D1Xd+W1Xw求得d1=9435.07 X

19、 0.999=9425.63kg/h d2=9435.07-9425.63=9.44kg/h d3=0 d1=9425.63/78.12=120.66kmol/hDi=9435.07kg/hWi=8364.93kg/h塔頂：質(zhì)量流率摩爾流率d4=0d4=0d2=9.44/92.13=0.1025kmol/hd3=0摩爾分?jǐn)?shù)0.999/78.12塔底：質(zhì)量流率摩爾流率yD1=99.91% yD2=1-99.91%=0.09%0.999/78.120.001/92.13W1=8364.93 X 0.001=8.36kg/hW2=8364.93-8.36-3471-267=4618.57kg/hW3

20、=3471kg/hW4=267kg/hW1 =8.36/78.12=0.1071kmol/hW2=4618.57/92.13=50.1310kmol/hw 3=3471/106.16=32.6959kmol/hW4=267/120.19=2.2215kmol/h 質(zhì)量分?jǐn)?shù)：Wwi=0.1%ww2=4618.57/8364.93 X 100%=55.21%ww3=3471/8364.93 X 100%=41.49%ww4=267/8364.93 X 100%=3.19%0.001/ 78.12摩爾分?jǐn)?shù):xW1 =0.13%0.001/ 78.12 0.5521/ 92.13 0.4149 /10

21、6.160.0319/120.190.5521/ 92.13XW2 =58.880.001/ 78.120.5521/ 92.13 0.4149/106.160.0319/120.19%XW3 =0.4149 /106.160.001/ 78.120.5521/ 92.13 0.4149/106.160.0319/120.19=38.390.0319/120.19XW4=2.600.001/ 78.12 +0.5521/ 92.13+0.4149/106.16 +0.0319/120.191.2.2甲苯塔物料衡算進(jìn)料 F2=8364.93F2=D2+W2F2XF = D 2XD+W 2XW求得

22、塔頂：質(zhì)量流率 d1=8.36kg/hD2=4637.74W2=3727.19d2=4637.74 X 0.995=4614.55kg/hd3=4637.74-8.36-4614.55=14.83kg/h摩爾流率 di=0.1071kmol/hd2=4614.55/92.13=50.0874kmol/hd3=14.83/106.16=0.1397kmol/h質(zhì)量分?jǐn)?shù)摩爾分?jǐn)?shù)wd1=8.36/4637.74 X 100%=0.18%wd3=14.83/4637.74 X 100%=0.32%0.0018/ 78.12wd2=99.5%yD1 =0.0018/78.12 0.995/92.13 0

23、.0032/106.160.995/92.13=0.21%塔底：質(zhì)量流率摩爾流率質(zhì)量分?jǐn)?shù)yD2=0.0018/78.12 0.995/92.13 0.0032/106.160.0032/106.16=99.51%=0.28%yD3=0.0018/78.12 0.995/92.13 0.0032/106.16W2=3727.19 X 0.00仁3.73kg/h w 3=3727.19-3.73-267=3456.46kg/h W4=267kg/hW2=3.73/92.13=0.0405kmol/h w 3=3456.46/106.16=32.5590kmol/h W4=2.2215kmol/hW

24、W2=0.1%ww3=3456.46/3727.19 X 100%=92.74%ww4=267/3727.19 X 100%=7.16%摩爾分?jǐn)?shù)0.001/92.13XW2=0.12%0.001/92.13 0.9274/106.16 0.0716/120.190.9274/106.16XW3=93.50%0.001/92.13 0.9274/106.16 0.0716/120.190.0716/120.19Xw4=6.38%0.001/92.13 0.9274/106.16 0.0716/120.191.2.3對(duì)二甲苯塔物料衡算進(jìn)料 F3=3727.19kg/hF3=D 3+W 3F3XF

25、= D 3XD+W 3XW求得塔頂：質(zhì)量流率d2=3.73kg/hD3=3526.93kg/hW3=200.26kg/hd3=3526.93 X 0.98=3456.39kg/hd4=3526.93-3.73-3456.39=66.81kg/h摩爾流率 d2=0.0405kmol/hd3=3456.39/106.16=32.5683kmol/hd4=66.81/120.19=0.5559kmol/h質(zhì)量分?jǐn)?shù) wd2=3.73/3526.93 X 100%=0.11% wd3=98.0%wd4=66.81/3526.93 X 100%=1.89%0.0011/ 92.13摩爾分?jǐn)?shù)yD2=0.13

26、%0.0011/ 92.13 0.98 /106.160.0189/120.190.98/106.16yD3=98.20%0.0011/ 92.13 0.98 /106.160.0189/120.190.189 /120.19yD4=1.67%0.0011/ 92.13 0.98 /106.160.0189/120.19塔底：質(zhì)量流率摩爾流率質(zhì)量分?jǐn)?shù)摩爾分?jǐn)?shù)Ww3=0.1%ww4=99.9%0.001/106.16XW3=0.11%0.001/106.16 +0.999/120.19W3=200.26 X 0.00仁0.20kg/hW3=0.20/106.16=0.0019kmol/hW4=2

27、00.26-0.20=200.06kg/hW4=200.06/120.19=1.6645kmol/hXW4 =0.999/120.19=98.89%0.001/106.16 0.999/120.191.2.4各塔物料衡算匯總表1-11苯塔物料衡算結(jié)果項(xiàng)目苯塔T0201苯甲苯對(duì)二甲苯C9摩爾分?jǐn)?shù)mol%59.1324.3515.650.87進(jìn)料F1質(zhì)里分?jǐn)?shù)kg%532619.51.5摩爾流（kmol/h）121.97450.22932.2831.795質(zhì)量流率（kg/h）943446283471267摩爾分?jǐn)?shù)mol%99.910.09塔頂D1質(zhì)量分?jǐn)?shù)kg%99.90.1-摩爾流（kmol/h）1

28、20.65580.1025質(zhì)量流率（kg/h）9425.639.44-摩爾分?jǐn)?shù)mol%0.1358.8838.392.60塔釜W1質(zhì)量分?jǐn)?shù)kg%0.155.2141.493.19摩爾流（kmol/h）0.107150.131032.69592.2215質(zhì)量流率（kg/h）8.364618.573471267表1-12甲苯塔物料衡算結(jié)果甲苯塔T0202項(xiàng)目苯甲苯對(duì)二甲苯C9摩爾分?jǐn)?shù)mol%0.1358.8838.392.60進(jìn)料F2質(zhì)量分?jǐn)?shù)kg%0.155.2141.493.19摩爾流率（kmol/h ）0.107150.131032.69592.2215質(zhì)量流率（kg/h）8.364618.5

29、73471267摩爾分?jǐn)?shù)mol%0.2199.510.28塔頂D2質(zhì)量分?jǐn)?shù)kg%0.1899.50.32-摩爾流率（kmol/h ）0.107150.08740.1397質(zhì)量流率（kg/h）8.364614.5514.83摩爾分?jǐn)?shù)mol%0.1293.506.38塔釡W2質(zhì)量分?jǐn)?shù)kg%0.192.747.16摩爾流率（kmol/h ）0.040532.55902.2215質(zhì)量流率（kg/h）3.733456.46267表1-13二甲苯塔物料衡算結(jié)果對(duì)二甲苯塔T0202項(xiàng)目苯甲苯對(duì)二甲苯C9摩爾分?jǐn)?shù)mol%0.1293.506.38進(jìn)料F3質(zhì)量分?jǐn)?shù)kg%0.192.747.16摩爾流率（kmol

30、/h ）0.040532.55902.2215質(zhì)量流率（kg/h）3.733456.46267摩爾分?jǐn)?shù)mol%一0.1398.201.67塔頂D3質(zhì)量分?jǐn)?shù)kg%一0.11981.89摩爾流率（kmol/h ）一0.040532.56830.5559質(zhì)量流率（kg/h）一3.733456.3966.81摩爾分?jǐn)?shù)mol%一00.1199.89塔釡W3質(zhì)量分?jǐn)?shù)kg%一00.199.9摩爾流率（kmol/h ）一00.00191.6645質(zhì)量流率（kg/h）一00.20200.061.3核實(shí)清晰分割1.3.1求解相對(duì)揮發(fā)度用Aspen軟件通過嚴(yán)格計(jì)算模擬的各塔溫度（C）見表 1-14。= 20.793

31、6 -2788.5180.3 220.79之 Ps =101.946kPasln P2-20.9065 -3096.5280.3 219.48sn P2 -39.230kPa表1-14各塔溫度（C）塔名稱進(jìn)料塔頂塔底苯塔（T0201 ）96.680.3120.3甲苯塔（T0202）120.3111.0139.4對(duì)二甲苯塔（T0203）139.4138.9152.6用Antoine方程計(jì)算飽和蒸汽壓表1-15各物質(zhì)A.B.C 值A(chǔ)BC苯20.79362788.51220.79甲苯20.90653096.52219.48對(duì)二甲苯20.98913346.65215.31異丙苯20.86503463.

32、60209.78苯塔：塔頂溫度80.3C，進(jìn)料溫度 120.3 C,塔釜溫度96.6 C塔頂各組分相對(duì)揮發(fā)度:sss sHP /P2 =101.946/39.230 =2.599 aP1 /P 2 1進(jìn)料中各組分的相對(duì)揮發(fā)度:In Pf =A= 20.7936 -2788.5196.6 220.79PS= 164.029 kPaSB3096 52sIn P； =AB 20.9065F2 = 66.830 kPaT C96.6 219.48SB3346.65sln PS =A20.9891P3 -28.555kPaT C96.6 215.31SB3463.40sln PS =A20.8650P=

33、14.187kPaT C96.6 209.78=RS/ F2S =164.029/66.830 =2.454 a? =P2S/P2S =1a3 二 PS / PS =28.555/66.830 =0.427Ssa4 二 F4/F2 =14.187/66.830 =0.212塔釜各組分的相對(duì)揮發(fā)度：B2788.51In P =A-=20.7936=a R =302.036kPaT C120.3 220.79SB3096 52SIn P；二 A -20.9065P? =132.349kPaT+C120.3+219.48In PS =A 旦 20.98913346.65卩3$ = 60.919kPa

34、T C120.3 215.31SB3463.40sIn P； =A20.8650P4 =31.946kPaT C120.3 209.78印=Ps/F2S =302.036/132.349 =2.282a2 二卩；/卩育=1s saF3 / P2 =60.919/132.349 =0.460QQa4 =巳 /P2 =31.946/132.349 =0.241甲苯塔：塔頂溫度 111.0C，塔釜溫度139.4 C 塔頂各組分的相對(duì)揮發(fā)度：B2788 51In Ps =A-=20.7936 :& Ps = 240.193kPaT C111.0 220.79In P?=A旦20.9065309

35、6.52P?'= 102.406kPa2 T C111.0 219.48In Ps=A旦20.98913346.65P3S= 45.849kPaT C111.0 215.31s s/ Pj =240.193/45.849 =5.239QQa2=P2/P3 = 10 2. 406/45.8492. 2 3 4a3 =PS/P3S =1進(jìn)料各組分相對(duì)揮發(fā)度：由 苯塔得： rS =302.036kPaP2$ = 132.349kPaP3$ = 60.919kPaSF4 =31.946 kPaQQ=R / F3 =302.036/60.919 =4.958QQaP2/P 3-13 2. 349

36、/ 60.9192. 1 7 3a3 =RS/P3S -1a4 =P4S/RS =31.946/60.919 =0.524塔釜各組分相對(duì)揮發(fā)度：SB3096.52sIn P/ -A20.9065P2 =214.958kPaT C139.4 219.48ln RS =A B 20.98913346.65 RS = 104.214kPa3 T C139.4 215.31sB3463.40sln P4 =A20.8650F4 56.715kPaT C139.4 209.78SSS Sa2=F2/F3 =214.958/104.214 =2.063 a3=P3/P3=1QQa4 =F4S/P3S =5

37、6.715/104.214 =0.544 對(duì)二甲苯塔：塔頂溫度1389C，塔釜溫度152.6 Cln RS=A旦20.90653096.52P?' = 212.394kPa2 T C138.9 219.48In RS=A旦20.98913346.65RS =102.837kPaT C138.9 215.31In P；二 A旦20.86503463.40RS =55.910 kPaT C138.9 209.78SSSSa2 =F2 / F4 =212.394/55.910 =3.799 a3 二P3 / F4 =102.837 /55.910 =1.839 a4 二 F4S / RS =

38、1進(jìn)料中各組分相對(duì)揮發(fā)度：SSS由甲苯塔得：F2 =214.958kPaF3 =10 4. 2 k4F a P4 =5 6. 7 1k5F aQQaF2 / F4 =214.958/56.715 =3.790a3 =p3/PS4 = 1 0 4. 214/56.7151. 838a4 制/ RS =1 塔釜各組分相對(duì)揮發(fā)度:SB3346.65sIn Ps =A20.9891P3 =146.18kPaT C152.6 215.31sB3463.40sIn PS -A20.8650P4 =81.398kPaT C152.6 209.78a3 二ps / F4S =146.181/ 81.398 =

39、1.796 a4 二 P：/ P： = 1表1-16相對(duì)揮發(fā)度各組分的平均相對(duì)揮發(fā)度a1a2a3a4苯塔（T0201）2.44210.4430.226甲苯塔（T0202）5.0972.15510.534對(duì)二甲苯塔（T0203）一3.7941. 82411.3.2核實(shí)清晰分割用underwood計(jì)算最小回流比，F(xiàn)enske計(jì)算最小理論板數(shù)。 對(duì)苯塔清晰分割進(jìn)行核實(shí)：表1-17苯塔數(shù)據(jù)編號(hào)組分aiX i.FX i.D1苯2.4420.59130.99912甲苯10.24350.0009寸 aj.XiF 門 2.442 7.5913 丄仆0.2435Z -=0 =+i aj *2.442 - v1

40、-用試差法求得v -1.2081Nm毗MW"Igad1 =120.66kmol /hw0. 1 0 7k1m o I /h代入式：、,，Xi.D1=2442 O."911 O.。009 =730i2.443 -1.2081 1 -1.2081d2 = 0.1025kmol / hw2 =5 0. 13 k0n o I h代入上式：ig( 120-66)!/(50131)2Ig 2.442N m 0.10715°.131°15為了核實(shí)清晰分割的假設(shè)是否合理，計(jì)算塔頂流出液中對(duì)二甲苯的和異丙苯的含量:3471上=d3i.Hd 4618.571r352 10

41、kg"10.4439.44X3=3.52 10 主 / 9435.07 =3.73 10 J同理：267_j2d4618.57 5"71 10 向小 1 0.2269.44x4 =5.71 102/9435.07 =6.05 10-6可見苯塔清晰分割是合理的。對(duì)甲苯塔清晰分割進(jìn)行核實(shí):表1-18甲苯塔數(shù)據(jù)編號(hào)組分ajXj .fXj.D1苯5.0970.59130.00212甲苯2.1550.24350.99513二甲苯10.15650.0028aj.Xj.Fc 5.097 0.5913 2.155 0.2435 1 0.15650 二 i5.097 - J2.155- J1

42、-二用試差法求得：v -1.1239 代入式弋 aj.Xj.D 廠丄* 5.097 漢0.0021 丄 2.155漢 0.9951 丄 1漢 0.0028 Km 1 -i a5.097 -1.1239 2.155 -1.1239 1 -1.1239=Rm =1.0599Nmig(-)2/(-)3w wIgad2 二 50.0874kmol / hd3 = 0.1397kmol / hw2 = 0. 0 4 0k5m o l /hw3 =3 2. 55k0nol hNmig(50.08740.0405)2“加lg 2.042核實(shí)甲苯塔清晰分割，計(jì)算塔頂異丙苯和塔釜液中苯的含量:di2.2215-

43、2.22 10°kg/hX4 =2.22 10衛(wèi)/50.33 =4.41 100.10710.139732.55905.09717= 3.08 10J1kg/hXw =3.08x10/34.82 =8.85漢103可見對(duì)甲苯塔清晰分割是合理的。對(duì)進(jìn)行核實(shí)對(duì)二甲苯塔清晰分割:表1-19對(duì)二甲苯塔數(shù)據(jù)編號(hào)組分aiXi .fXi.D1苯3.7940.24350.00132甲苯1.8240.15650.98203二甲苯10.00870.0167=Rm = 0.5533皿=0 = 3.794 O.2435 J824 0.15651 O.O。873.794 - v1.824 - J1一二Nmlg

44、(W)3/(W)4lgad3 =32.5683kmol / hw3 = 0. 0 0 1k9m o l /hd4 二 0.5559kmol / hw4 = 1. 6 6 4k5m o l /hNmlg(32.56830.00190.5559KE=19lg1.824核實(shí)清晰分割計(jì)算釜液中甲苯的含量:0.04051 05559 3.794191.6645= 1.2 10%/hxw.2 =7.13 燈03可見對(duì)對(duì)二甲苯塔清晰分割是合理的。第2章熱量衡算I1II2-1熱量衡算示意圖Qf :進(jìn)料帶入熱Qd :塔頂出料帶出熱Qc :冷凝器帶出熱Qw :塔底出料帶出熱Qs :再沸器加入熱2.1苯塔熱量衡算以

45、圖2-1所示為研究系統(tǒng)進(jìn)行熱量衡算，選取0 C為計(jì)算基準(zhǔn)：熱量衡算式Qf Qs二Qc QD QW +Q損2.1.1塔進(jìn)料液代入熱量tF =96.6 C 則定性溫度 tF =（0 * 96.6）/2 =48.3 C表2-1各組分的比熱容（卡/克分子C）溫度C苯（卡/克分子C）甲苯（卡/克分子C）對(duì)二甲苯（卡/克分子C）正丙苯（卡/克分子C）4032.96338.66744.5752.665033.48539.62145.3853.7當(dāng)t =48.3 C 內(nèi)差法求得Cpi =39.459 4.18585= 139.791kJ/(kmol.°C)CP2 =39.459 4.18585 =

46、165.169kJ/(kmol.°C)Cp3 =45.242 4.18585=189.376kJ/(kmol.°C)Cp4 =53.523 4.18585 = 224.039kJ/(kmol.°C)Cp = X1CP1X2CP2 ' X3CP3 ' X4CP4= 0.5913 139.791 0.2435 165.169 0.1565 189.376 0.0087 224.039= 154.464kJ /(kmol.°C)6Qf =F Cp tF =206.281 154.464 96.6 =3.077965 10 kJ /h2.1.2塔

47、頂出料帶出液tD =80.3°C則定性溫度：tD =(° 80.3)/2 =40.15°C表2-2各組分的比熱容(卡/克分子C)溫度C苯甲苯對(duì)二甲苯正丙苯4032.96338.66744.5752.485033.48539.62145.3853.52當(dāng)t =40.15 C內(nèi)差法求得Cp1 =32.971 4.18585 = 138.012kJ/(kmol.°C)Cp2 =38.681 4.18585 = 161.913kJ/(kmol.°C)CpX2CP2= 0.991 138.012 0.009 161.913 =138.034kJ/(kmol.°C)6Qd =D Cp tD -120.76 138.034 80.3 =1.338520 10 kJ / h2.1.3塔底餾出液中帶出的熱量tw =120.3°c則定性溫度 L=(0 120.3)/2 =60.15°C表2-3各組分的比熱容（卡/克分子C）溫度C苯甲苯對(duì)二甲苯正丙苯6034.00840.36946.1854.557034.53041.11847.0555.99當(dāng)t =60.15