精馏塔课程设计计算模板

1、乙醇摩尔质量g/mol水的摩尔质量g/mol46.0718.02精馏塔工艺计算1物料衡算（1）全塔物料衡算质量分数摩尔分数x平均摩尔质量kg/kmol质量流率kg/h摩尔流率kmol/h进料0.430.22784303924.410997255217.91296213.7525521塔顶0.9260.83035276241.311394982335.85858656.54271872塔底0.0280.01114197818.332532472882.054375157.20983332)选定回流比R实值放大倍数泡点进料qXd/(Rmin+1)(%)YqRmin1.5162204910.33R3

2、.9421732772.61L kmol/hV kmol/hL kmol/hV kmol/h摩尔流率222.9011947279.4439134436.6537468279.4439134（2）物性计算1）进料温度乙醇液密度kg/m3 水液密度kg/m3平均密度kg/m3体积流率m3/h82.7270073733.5592703970.5292671852.15789546.123176222)精馏段气相温度蒸气密度kg/m3蒸汽质量流量kg/h蒸汽体积流量m3/h y1=Xd78.316083921.4324947211544.217888058.8205440.830352762液相液相摩

3、尔组成液平均摩尔质量g/mol乙醇液密度kg/m3水液体密度kg/m3液相质量分数0.81506713340.88263308737.6232243973.30912830.9183916083)提馏段液相温度乙醇液密度kg/m3 水液密度kg/m3平均液密度kg/m3下降液体体积流量m3/h96.85720.4026216960.7412042951.84971258.409908504气相气相摩尔组成平均气摩尔质量g/mol上升蒸汽密度kg/m3上升蒸汽质量流量kg/h上升蒸汽体积流量m3/h0.1195221.3725360.703980985972.42518483.7875912.确

4、定NT、Np及加料位置1)计算理论塔板数总精馏提馏理论板块数121022)板效率ETa顶a底a定性温度乙醇粘度cP水粘度cP1.1105460312.047383863.65775536387.583041963)实际塔板数的计算总精馏提馏加料位置实际塔板数23.0817671221.98342465242221.塔径及塔间距的初步计算1)精馏段乙醇临界温度水临界温度平均临界温度K25时表面张力(达因/cm)精馏温度表面张力243374.1540.394698922.8160839216.93141505FlvHT/mmC20C液泛气速Uf m/s0.0344414855000.0920.08

5、89857532.037565532有效横截面积Anlw/DAf/AtAt m2D m1.5694929120.650.0681.6840052711.464288954反算At m2An m2UnUn/uf1.5393798841.4347020521.5602969680.7657652942)提馏段乙醇临界温度水临界温度平均临界温度K25时表面张力(达因/cm)精馏温度表面张力243374.1645.789286769.938452.97292358FlvHT/mmC20C液泛气速Uf m/s0.0364506454000.0750.0911309833.349724746有效横截面积A

6、nlw/DAf/AtAt m2D m1.0823427380.80.151.2733443971.273291981反算At m2An m2UnUn/uf1.5393798841.0775659192.1869730870.6528814312.溢流装置的设计(1)溢流程数因为DF(a)29897.693852VsVh639897.6938522.7493594039897.693852(3)液相负荷下限线2.794414062000Lh2.79441406100002.79441406(4)液相上限线Lh14.52055734200014.520557340.00403348814.5205

7、573410000（5）溢流液泛线abcd0.008323980.201427077101.93931311.097387619操作弹性2.63596251370605040302010002000400060008000100001200014000160001800020000严重漏液线过量雾沫夹带线液体流量下限线液体流量上限线Series5溢流液泛线操作点直线2提馏段（1）严重漏液线VsVh23972.3385131.1034273653972.338513683972.338513(2)过量雾沫夹带线211694.01896VsVh6811694.018963.248338601116

8、94.01896(3)液相下限线3.4392788433000Lh3.439278843120003.439278843(4)液相上限线Lh15.46728449300015.467284490.00429646815.4672844912000（5）溢流液泛线abcd0.0058797990230933370.94439321操作弹性2.943862645六换热器设计（冷凝器设计）1塔顶热负荷计算塔顶液体温度塔顶冷凝器进口温度t1塔顶冷凝器出口温度t2温差t塔顶汽化潜热KJ/kg塔顶汽化潜热KJ/kmol78.32205030988.882271740852.106

9、112初步估计设备尺寸tm假设总传热系数K传热面积A41.52957185700109.08150253校核传热面积内外A计A实际K4579.3611962127.152178101.0261786120.6755.8145111外液体密度Mqm混合液蒸汽752.49354760.2449825310.0005109110.014294023.206727189内液体密度Mqm水994.8250.6084840.000760131.83810911tRePr流速u3526176.161035.05631 所选冷凝器规格：Dn/mm管程数管数中心排管数管程流通面积管长/m8004352140.0

10、2764.54接管选取（1）塔顶蒸汽管8070605040302010002000400060008000100001200014000160001800020000严重漏液线过量雾沫夹带线液相下限线液相上限线Series5溢流液泛线Series770605040302010002000400060008000100001200014000160001800020000严重漏液线过量雾沫夹带线液体流量下限线液体流量上限线Series5溢流液泛线操作点直线d流速u选择管径/mm壁厚/mm0.436017614154509（2）回流管d流速u选择管径/mm壁厚/mm0.0462885062481（

11、3）进料管d流速u选择管径/mm壁厚/mm由泵进料0.0329145032340.5（4）塔釜出料管d流速u选择管径/mm壁厚/mm0.0652019430.7683（5）塔釜蒸汽管d流速u选择管径/mm壁厚/mm0.3874305092040295储槽V高径比储罐半径d液料高度h原料罐61.23176221.53.7325469645.598820446V高径比储罐半径r液料高度h回流罐152.14278421.55.0554926267.583238939V高径比储罐半径r液料高度h产品罐31.041576281.52.9761920364.4642880546选泵(1)原料泵进料高度Hz

12、=H2原料液高度Z1u1u2板压降p4.235.59882044601.9896501591.558980755管长l总阻力Hf1R/dqv357.283336786.12317622弯头（90）截止阀底阀Hf2个数2阻力系数0.756.4124.170781386（2）回流泵七塔高计算1封头设计精馏段Hc0.375提馏段Hc0.3752塔顶空间HD13主体高度1）人孔数S与开设人孔处板间距HTSHT/mm人孔塔板位置2600 1,10,20,242）进料段高度HF进料口个数精馏段1.52HZ精馏段10.95提馏段0.4总计11.354塔底空间HB1.1836888755塔高裙座HSH1.51

13、5.40868887八热量衡算注：热量均以0的液体为起点作计算进入系统的热量1加热蒸汽带入量 QB加热蒸汽用量 GB加热蒸汽汽化潜热RWQB1.6082098062177.63502.0376742进料带入热量 QFFG kg/sCpf kJ/kg/ tF QF1.4494202674.3382.7519.02435283回流带入热量 QRRDG kg/sCpRkJ/kg/tR QR3.9421732770.6488496073.3278.31608392665.0722118离开系统的热量1塔顶蒸汽带出热量 QVDRCpDtDRD0.6488496073.9421732773.3278.31

14、608392988.88227172残液带出热量 QWWGCpwtWQW0.800570664.2796.85331.0755963散于周围的热量 QL基于热量衡算的再沸器预热器选择1再沸器t1t2rwQBK1301302177.63502.037674700DNPN管程数管子根数中心排管数管程流通面积9000.611009350.17832预热器1T1T2t1t2T定性96.8560254578.425tmCp136.29039027 AA实际4.24.8774943325.7DNPN管程数管子根数中心排管数管程流通面积3251.6468110.0033预热器2Tt1t2T定性t定性1104

15、78311065A实际tmKArwCp28.342.488010047007.4036324512232.44.22DNPN管程数管子根数中心排管数管程流通面积273425680.00493直接预热器t1t2TRwtm25831202205.254单纯加热402352.385体积流率m3/h3.1041576283.02784603215.21427842体积流率m3/s0.001700882X1气相质量分率0.815067133 0.9258741262.238561262平均液体密度kg/m3下降液体体积流量m3/h下降液体质量流量kg/h0 12.11012752.4935476 12.

16、110120799112.787756 0.0033640 8058.821下降液体质量流量kg/h8004.968992 0.0023360860.0023360860 8.409909气相质量分率2.3566076642.3566076640 8483.7880.257370平均粘度cP板效率0.54176 0.476566631精馏塔工艺计算351.52空塔气速u1.426295872圆整 m1.4Af0.104677832空塔气速u2.177321085圆整 m1.4Af0.230906983hw mm48.57292324hw mm48.91382788xAa m20.4619539

17、45 1.090442506xAa m20.37 0.907174129底边/mm排间距 t圆整开孔率实际开孔数实际流通面积实际孔速F075 64.7925213565 0.174136209 0.249543 8.970648 10.73669底边/mm排间距 t圆整开孔率实际开孔数实际流通面积实际孔速F075 73.0399580865 0.128512155 0.185068 12.73376 10.68408四、流体力学计算与校核hp mhl /m临界气速u0压降0.0742371790.03258.140540833 547.4574KsAa11.33002422Hp mhl /m压

18、降0.0626731620.03584.6232229KsAa1 1.0775659190 4.9200336150 17712.120.000277778 4.8625411171 17505.150.000555556 4.8282146222 17381.570.000833333 4.7989893013 17276.360.0011111114.772500964171810.001388889 4.7477700715 17091.970.001666667 4.7242706296 17007.370.001944444 4.7016786677 16926.040.002222

19、222 4.679776557816847.20.0025 4.6584089919 16770.270.002777778 4.63746004610 16694.860.0030555564.6168401311 16620.620.003333333 4.59647804412 16547.320.003611111 4.57631588613 16474.740.003888889 4.5563056491416402.70.004166667 4.53640686415 16331.06五塔板负荷性能图70605040302010002000400060008000100001200

20、014000160001800020000严重漏液线过量雾沫夹带线液体流量下限线液体流量上限线Series5溢流液泛线操作点直线0.015555556 3.6088063955612991.70 5.0692483580 18249.290.000277778 5.0012637761 18004.550.000555556 4.9606838782 17858.460.000833333 4.9261706263 17734.210.001111111 4.8949340664 17621.760.001388889 4.8658189555 17516.950.001666667 4.83

21、82052946 17417.540.001944444 4.8117114547 17322.160.002222222 4.7860812448 17229.890.0025 4.7611319649 17140.080.002777778 4.73672734910 17052.220.003055556 4.71276218111 16965.940.003333333 4.68915291712 16880.950.003611111 4.66583168913 16796.990.003888889 4.64274229314 16713.870.004166667 4.61983

22、740515 16631.410.004444444 4.59707660216 16549.48塔顶热负荷Qc/kw冷却水比热Cp/KJ/kg/K冷却水用量Gc/kg/s3171.0756673.3231.83810911比值1.193749993l实际管数nt纯乙醇纯水纯乙醇纯水78.32 0.1707160.6084840.000460.00076ll圆整4.260499794.5管径估计管数n管长L管程总管数实际总管数0.02 101.922701917.0424 407.6908352换热面积12.670605040302010002000400060008000100001200014000160001800020000严重漏液线过量雾沫夹带线液体流量下限线液体流量上限线Series5溢