三氯餾塔的工藝計算(理想版附本)

1、一.已知 (一進料1. 組成(Kg/Kg:CH 2Cl 2:0.00030CHCl 3:0.77331CCl 4:0.226392. 進料溫度t =253.分子量CH 2Cl 2:84.933CHCl 3:119.378CCl 4:153.823(二塔釜CHCl3的含量為10%(三塔頂1.產品純度為99.95%2.產量:60t/d二.物料衡算 1.產品產量D= 60 × 1000 ÷ 24 =2500.00Kg/h2.進料量 F 根據公式:F*xF = W*xW +D*xD F =W+DF=3339.84Kg/h3.進料的各組分流量及組成 (1.進料組分的流量CH 2Cl

2、2=3231.52×0.03% =1.002Kg/hCHCl 3=3231.52×77.331% =2582.734Kg/hCCl 4=3231.52×22.639% =756.107Kg/hCH 2Cl 2=0.969×1000÷3600÷84.933 =0.0033mol/sCHCl 3=2498.969×1000÷3600÷119.378 =6.0097mol/sCCl 4=731.585×1000÷3600÷153.823 =1.3654mol/s 三氯餾塔的工藝計算

3、F= 0.0032+ 5.8148 + 1.3211 =7.3784mol/s (3進料組成 (mol/molCH 2Cl 2=0.0032÷7.1391×100 =0.044CHCl 3=5.8148÷7.1391×100 =81.450CCl 4=1.3211÷7.1391×100 =18.5052.塔釜的組成及流量(1 塔釜流量 WW =839.843Kg/h(2各組分的流量CHCl 3= 731.524 × 10% =83.9843Kg/hCCl 4= 731.524 - 73.1524 =755.8591Kg/hC

4、HCl 3=73.1524÷119.378÷3600×1000 =0.1954mol/s CCl 4=658.3712÷153.823÷3600×1000 =1.3650mol/s (3 塔釜物料的流量 WW = 0.1702+ 1.1889 =1.5604mol/s(4.塔釜各作用于分的組成(mol/molCHCl 3 = 0.1702 ÷ 1.3591 =0.1252mol/molCCl 4 = 1.1889 ÷ 1.3591 =0.8748mol/mol3.塔頂流量及組成(1.塔頂?shù)牧髁緿=2500.00Kg

5、/h(已知(2塔頂各組分的流量CH 2Cl 2=1.0020Kg/hCHCl 3=2500×99.95 % =2498.750Kg/hCCl 4 =0.2480Kg/hCH 2Cl 2=0.9695÷84.933÷3600×1000 =0.00328mol/s CHCl 3=2498.750÷119.378÷3600×1000 =5.81428mol/s CCl 4 =0.2805÷153.823÷3600×1000 =0.00045mol/s (3.塔頂?shù)牧髁緿=0.00317 + 5.814

6、28 + 0.00051 =5.8180mol/s (2.塔頂物料組成(mol/mol%CH 2Cl 2=0.00317÷5.8180×100=0.0563CHCl 3=5.81428÷5.8180×100=99.9360CCl 4 =0.00051÷5.8180×100=0.0077三.回流比 R 的確定(1.易揮發(fā)組分的氣相平衡濃度 y F *查表得:在64.395時,x F = 0.81494(含二氯甲烷 時,y F * =0.87437(2最小回流比的確定R min =(xd-y F *÷(yF *-x F =(0.

7、999913-0.87437÷(0.87437-0.81494R min =2.112.回流比R的確定取R=1.8 RminR=2.11×1.8 =3.80所以,回流比取 4四.塔板數(shù)的確定1.確定q線方程(1.q大小范圍的確定該蒸餾近似確定進料溫度為25則:0q1(2.泡點溫度的選定泡點溫度時,近似認為汽液相達到平衡時,根據公式:Yi = Ki *ZiZ i 組分進料分率 Y i 組分氣相分率K i 汽液平衡常數(shù)Y i = 1用試差法計算相平衡的溫度t,得到:t =64.395(3進塔物料的單位摩爾汽化潛熱 r查表得:在64.395 時各組分的汽化潛熱CH 2Cl 2:2

8、98.679KJ/KgCHCl 3:250.343KJ/KgCCl 4:182.887KJ/Kg即:CH 2Cl 2:25.3677KJ/molCHCl 3:29.8854KJ/mol CCl 4:28.1323KJ/mol進塔物料的平均汽化潛熱:r =25.3677×0.00044+29.8854×0.81450+0.18505×28.1323r =29.5590KJ/mol(4.進塔物料的C Pa.在進料溫度下的C P當t 進 =298.15 K 時,各組分的比熱容為:CH 2Cl 2:(8.000+15.6×298.15×10-3

9、5;4.2 =53.1348J/mol.KCHCl 3:(7.52+35.598×10-3×298.15-21.68×10-6×298.152×4.2=68.0666 CCl 4:(23.34+2.32×10-3×298.15-36.1×10-6×298.152×4.2 =87.4674 進料溫度下的C P 為:C P =53.1348×0.00044+68.0666×0.81450+87.4674×0.18505C P =71.6502J/mol.Kb.泡點溫度下

10、的C Pt 泡 =337.545 K 時,各組分的比熱容為 :CH 2Cl 2:(8.000+15.6×337.545×10-3×4.2 =55.7159J/mol.KCHCl 3:(7.52+35.598×10-3×337.545-21.68×10-6×337.5452×4.2=71.6763 CCl 4:(23.34+2.32×10-3×337.545-36.1×10-6×337.5452×4.2 =84.0615 泡點下物料的C P 為:C P =55.715

11、9×0.00044+71.6763×0.81450+84.0615×0.18505C P =73.9611J/mol.K(5.q值的確定根據公式:q =C P (t進 -t 泡 +r/ rq =(71.602×298.15-73.9611×337.545÷1000+29.559÷29.559q =0.8175(6.q 線方程Y =q/(q-1X-Z F /(q-1 得:Y =-4.48002 X+4.465922.精餾段操作線方程Y n+1 =R /(R+1Xn +1/(R+1XD 所以Y n+1 =0.697X n +0.

12、199983.提餾段的操作線方程y =(L+qF/(L+qF-Wx-W/(L+qF-WX WL = RD = 5.8180 ×2.3 =23.2720mol/sy =1.076 x -0.009533.相圖的制作根據公式:X A = (P-P 0B /(P0A -P 0B Y A =XA *P0A /P X A 易揮發(fā)組分的液相分率P 系統(tǒng)壓力P 0A 平衡分壓Y A 易揮發(fā)組分的汽相分率得出以下表:(注:P=101325Pa 4.確定理論板數(shù)根據精餾段操作方程、提餾段方程、q線方程和平衡相圖作出理論板數(shù)為:N =44塊其中精餾段33塊,提餾段11塊五.精餾段的質量流量1.液體平均質

13、量流量L J(1.液體平均摩爾濃度X JCH 2Cl 2=(0.0004+0.0006÷2 =0.000504m ol/mol混合液CH 2Cl 2=(0.8932+0.9989÷2 =0.906931m ol/mol混合液CCl 4 =(0.1061+0.00033÷2=0.092566m ol/mol混合液(2.液相平均摩爾質量M X,JM X,J =M A X A +MB X B +MC X C =84.933×0.000495+119.378×0.906935+153.823×0.092571 M X,J =122.5491g

14、/mol(3.精餾段的液體平均質量流量L J =D*R*Mx,J =5.8180×4×1212.5496÷1000L J =2.8520Kg/s2.氣體平均質量流量查表得:各組分在進料口處的汽相組成為(塔內Y CH2Cl2=0.00099mol/molY CHCl3=0.873379mol/molY CCl4=0.125631mol/mol(1.各組分汽相的平均摩爾濃度Y JY CH2Cl2=(0.00099+0.0006÷2=0.00078mol/molY CHCl3=(0.8734+0.9994÷2=0.93637mol/molY CCl4

15、=(0.1256+0.00009÷2=0.06285mol/mol(2.上升蒸氣平均分子量M y,J =84.933×0.00077+119.378×0.93637+153.823×0.06286M y,J =121.5163g/mol(3.精餾段蒸氣的平均質量流量G J =D*(1+R*My,J = 5.8180×(1+4×121.5167÷1000 =3.5349Kg/s六、提餾段的質量流量1、提餾段液體平均質量流量X CH2Cl2= (0.0004+0÷2 =0.0002mol/molX CHCl3=(0.1

16、252+0.8145÷2=0.4699mol/molX CCl4=(0.8748+0.18505÷2=0.5299mol/mol(2.提餾段中液體的平均摩爾質量M X,T =M 1X 1+M2X 2+M3X 3M X,T =84.933×0.0002+119.378×0.4699+153.823×0.5299M X,T =137.623g/mol(3.進料中液相的平均摩爾質量 MFM F =84.933×0.00044+119.378×0.8145+153.82×0.18505M F =125.7369g/mol(

17、4.塔頂中液體的平均摩爾質量 MDM D =84.933×0.000545+119.378×0.999368+153.823×0.000087M D =119.3613g/mol(5.進料中液體的質量流量 FLFL =3231.52 ÷ 3600FL =0.9277Kg/s(6.塔頂?shù)馁|量流量 DD =2500÷3600D =0.6944Kg/s(7.提餾段液體的平均質量流量 LTLT =DRM x,T /MD +FMx,T /MFLT =0.6944×4×137.623÷119.3622+0.8976×

18、137.623÷125.7369 =4.2182 2.提餾段氣體的質量流量 GT(1.提餾段中氣體的平均摩爾組成a.塔釜中各組分的飽和蒸汽壓 P0在溫度 t = 74.415 ,根據安托尼公式,各組分的飽和蒸汽壓為:P 0CHCl3:147274.974PaP 0CCl4:94717.649Pab.塔釜中氣相組成為:(P取 101325PaY CHCl3=X2P 0/P =0.18223mol/molY CCl4=X3P 0/P =0.81777mol/molc.提餾段中氣體的平均摩爾組成根據公式: YT = (YW +YF ÷2Y CHCl3=(0.1822+0.8733

19、8÷2=0.5278mol/molY CCl4=(0.8178+0.12563÷2=0.4717mol/mol(2提餾段中蒸汽的平均摩爾質量 My,TMy,T =M 1Y 1+M2Y 2+M3Y 3My,T =84.93×0.0005+119.38×0.5278+153.82×0.4717My,T =135.6087g/mol(3.提餾段中蒸汽的平均質量流量 GTG T =D (R+1MY,T /MDG T =0.6944×(4+1×135.6087÷119.3622 =3.9449Kg/s七.蒸汽速度與塔徑1、精

20、餾段平均溫度 t J 和提餾段的平均溫度 t T根據塔釜和塔頂組成可得出塔釜t W 和塔頂溫度t DT W =74.415 T D =62.181查得進料點溫度 t F =64.395 ,那么:t J =(64.395-62.181/ln(64.395/62.181 =63.282 t T =(75.415-64.395/ln(75.415/64.395 =69.284 2.蒸汽平均密度(1.精餾段的蒸汽平均密度 y,Jy,J =M y,J T 0/(22.4(T0+tJ y,J =121.5167×273/22.4×(273+63.282 =4.4044Kg/m3 (2.

21、提餾段的蒸汽平均密度 y,Ty,T =M y,T T 0/(22.4(T0+tT y,T =135.6087×273/(22.4×(273+69.284 =4.8291Kg/m3 3.液體平均密度(1.精餾段液體的平均密度 x,Ja.在t J =63.282 時,各組分的密度為CH2Cl2 =1242.01Kg/m3CHCl3 =1387.52Kg/m3CCl4 =1498.28Kg/m3b.精餾段中液體的平均摩爾組成X CH2Cl2=(XF +XD ÷2 = (0.00044+0.00055÷2 =0.0005mol/mol X CHCl3=(XF +

22、XD ÷2 = (0.81450+0.99936÷2 =0.9069mol/mol X CCl4=(XF +XD ÷2 = (0.18505+0.000087÷2 =0.0926mol/mol c.精餾段液體平均密度為x,J =1242.01×0.0005+1387.52×0.9069+1498.28×0.0926x,J =1397.70Kg/m3(2.提餾段液體的平均密度 x,Ta.在t T =69.284 時,各組分的密度為CH2Cl2 =1231.06Kg/m3CHCl3 =1375.66Kg/m3CCl4 =1489

23、.65Kg/m3b.提餾段中液體的平均密度x,T =1231.06×0.0002+1375.66×0.4699+1489.65×0.5299x,T =1436.04Kg/m34.液體平均動力粘度(1.精餾段液體的平均動力粘度a.在t = 63.282 時各組分的動力粘度為查表得各組分的動力粘度為:2 =0.30762毫帕秒 2 二氯甲烷動力粘度3 =0.40006毫帕秒 3 三氯甲烷動力粘度4 =0.56851毫帕秒 4 四氯化碳動力粘度b.精餾段液體的平均動力粘度x,J =0.30762×0.0005+0.40006×0.9069+0.568

24、51×0.0926x,J =0.4156毫帕秒x,J =0.000416厘泊(2.提餾段液體的平均動力粘度a.在t = 69.417 時各組分的動力粘度查表得各組分的動力粘度為:2 =0.29411毫帕秒 2 二氯甲烷動力粘度3 =0.38370毫帕秒 3 三氯甲烷動力粘度4 =0.53835毫帕秒 4 四氯化碳動力粘度b.提餾段液體的平均動力粘度x,T =0.29411×0.0002+0.38370×0.4699+0.53835×0.5299x,T =0.4656毫帕秒x,T =0.000466厘泊6.蒸汽的極限速度(1.精餾段的蒸汽極限速度u f,j

25、根據公式:u 2f,Jy,J x,J 0.16/g3x,J = 1.2exp-4(LJ /GJ 0.25(y,J /x,J 0.125u 2f,J ×450×4.4045×0.0004160.16/(9.8×0.753×1397.70 =1.2exp-4(2.8520/3.53490.25(4.7106/1394.550.125u 2f,J =2.4852u f,J =1.5765m/s(2.提餾段的蒸汽極限速度u f,T根據公式:u 2f,T y,T x,T 0.16/g3x,T = 1.2exp-4(LT /GT 0.25(y,T /x,T

26、 0.125 u 2f,T ×450×4.8291×0.0004660.16/(9.8×0.753×1436.04 =1.2exp-4(4.1852/3.94480.25(4.8291/1436.040.125u 2f,T =1.5203u f,T =1.2330m/s7.塔徑的確定(1.操作速度的確定操作速度一般極限速度的0.60.8倍,取0.7倍極限速度,則:u J = 0.7×uf,J = 1.5765×0.7 =1.1035m/su T = 0.7×uf,T = 1.2354×0.7 =0.863

27、1m/s(2.塔徑的計算和確定a.精餾段的塔徑d Jd J =(4GJ/u J y,J 0.5 =(4×3.5349/(3.14×1.1035×4.40450.5d J =0.96mb.提餾段的塔徑d Td T =(4GT/u T y,T 0.5 =(4×3.9448/(3.14×0.8648×4.82910.5d T =1.10mc.塔徑d的確定取塔徑為d = 1.2m(3.實際操作速度u J =1.1035×(0.96/1.22 =0.7100m/su T =0.8648×(1.1/1.22 =0.7227m/

28、s八.填料層高度及塔高1.蒸汽的動力粘度(1.精餾段蒸汽的動力粘度a.在t = 63.282時各組分的動力粘度為查表得各組分的動力粘度為:2 =0.01122毫帕秒 2 二氯甲烷蒸汽動力粘度4 =0.01085毫帕秒 4 四氯化碳蒸汽動力粘度 b.精餾段蒸汽的平均動力粘度y,J =0.00116×0.01122+0.96376×0.01139+0.01085×0.08798y,J =0.01136毫帕秒y,J =1.1359E-05厘泊(2.提餾段蒸汽的動力粘度a.在t = 69.417時各組分的蒸汽動力粘度為查表得各組分的動力粘度為:2 =0.01148毫帕秒

29、2 二氯甲烷動力粘度 3 =0.01158毫帕秒 3 三氯甲烷動力粘度 4 =0.01096毫帕秒 4 四氯化碳動力粘度 b.提餾段蒸汽的平均動力粘度y,T =0.0008×0.01148+0.5554×0.01158+0.4439×0.01096y,T =0.01129毫帕秒y,T =1.1291E-05厘泊2.等板高度關于液泛時等板高度,可用下式計算H D =28u f 0.2yy -0.2-1.2v(G/L0.342(x /y 0.19(y /x 0.038 lg(L/mG/(1-mG/L(1.精餾段的等板高度H D,J =28×1.65710.2

30、×4.7928×(1.2033×10-5 -0.2×450-1.2×0.75×(0.8628/0.54120.342×(1394.55/4.71060.19×(0.01131/0.41080.038×lg(0.5412/0.552925/0.8628/(1-0.552925×0.8628/0.5412 H D,J =0.4603m(2.提餾段的等板高度H D,J =28×1.37750.2×4.7928×(1.1308×10-5 -0.2×450

31、-1.2×0.75×(0.6185/0.90000.342×(1434.31/4.79280.19×(0.01308/0.46950.038×lg(0.9000/1.09496/0.6815/(1-1.09496×0.6815/0.9000 H D,J =0.6778m3.填料層高度的估算(1.精餾段填料層的高度H J =0.4760×14H J =15.1909m(2.提餾段填料層的高度1111H T =0.6367×20H T =7.4562m(3.塔中填料層總高度的估算H = HJ + HT =22.6471

32、m一節(jié)填料取2米,則塔的填料層總節(jié)數(shù)為12節(jié),其中,精餾段為8節(jié),提餾段為4節(jié). 4.精餾塔總高度H Z精餾塔總高度可按下式計算:HZ =Zn +(n-1h p +ZJ +ZT式中:Z 每節(jié)填料層高度,m;n 填料節(jié)數(shù),節(jié);h P 相鄰兩節(jié)填料層的距離,m,其間裝有液體分布器,取hp=0.5m; Z J 填料上方分離空間的高度,m,參考下表;Z T 填料與塔底間的距離,m,參照下表。故塔的總高 HZ =24+(12-1×0.5+1.0+2.0 =32.5m附表:塔徑與填料上、下方離空間高度 九、填料的液體阻力1.精餾塔的雷諾準數(shù)(1.精餾段的雷諾準數(shù):Re y,J =u J d e

33、y,J /(y =0.4889×1.2×4.6668÷(0.75×0.1195×10-3 Re y,J =440485.49(2.提餾段的雷諾準數(shù):Re y,T =u T d e y,T /(y =0.4981×1.2×4.7928÷(0.75×0.02231×10-3 Re y,T =494520.162.精餾塔的阻力系數(shù)(1.精餾段的阻力系數(shù):該液體為湍流動力狀態(tài)。對于湍流狀態(tài),陶瓷波紋填料的干填料阻力系數(shù)為J =16/Re y,J 0.21212J = 16÷4404850490

34、.2 =1.189(2.提餾段的阻力系數(shù):該液體為湍流動力狀態(tài)。對于湍流狀態(tài),陶瓷波紋填料的干填料阻力系數(shù)為T =16/Rey,T0.2T = 16÷494520.160.2 =1.1623、干填料的液體阻力 P C(1.精餾段的干填料的液體阻力:P C,J =HJu 2J y,J /(2de 2P C,J =1.189×16×0.48892×4.6668÷(1.2×0.752×2P C,J =75.61Pa(2.提餾段的干填料的液體阻力:P C,J =HTu 2J T,J /(2de 2P C,J =1.162×

35、10×0.4981×4.7928÷(1.2×10-3×0.752×2P C,J =8.68Pa4.噴淋密度(1精餾段的噴淋密度U J =LJ/(0.75×x,J ×d2U J =0.8097÷(0.75×1393.67×0.82U J =0.00425m 3/(·s(1提餾段的噴淋密度U T =LT/(0.75×x,T ×d2U T =1.2455÷(0.75×1434.31×0.82U T =0.00629m 3/(

36、3;s5.塔中被噴淋填料的總阻力(1.精餾段被噴淋填料的流體阻力P J =10169U J PC,J=10169×0.00121×6087.78P J =395.36Pa(2.提餾段被噴淋填料的流體阻力P J =10169U J PC,J=10169×0.00186×298.05P J =100.30Pa1313(2.精餾塔中被噴淋填料的總流體阻力P =P J +P T =395.36+100.30P =495.66Pa141471.331濃度 密度 m 3/hKg/hCH 2Cl 2:56.41289CHCl 3:38.31475CCl 4:5.315

37、843750 1375.8731515161699.99230.931.39(25.756353.569512#(25756.271225756.2712#0.25760.53570.15801120.97850.02382.9240623.92640.87680.00100.12221.240.6666666671月0日 0.8666510.19993320.133350.93330.9999830.003450122#REF!#REF!#REF!0.6666666670.3331717J/mol.KJ/mol.K摩爾分率 mol/mol0.6HCl 0.000000 62.1806-4.480019454CH 3Cl 0.0000 J/mol.K-4.237753844CH 2Cl 20.0006 J/mol.K-1.351183125CHCl 30.9994 -243.2129625CCl 40.0001 -63.2130-158.0324062