编 号
1234组 分
甲烷乙烯乙烷丙烯
摩尔组成z i 0.0002
0.88010.1160.0036系数
甲烷乙烯乙烷丙烯A
5.963551
6.402225 6.106759 6.088812B
438.5193800.8744720.7483851.3585C 272.2106287.1486264.2263256.242
(1)计算馏出液组成
假设清晰分割，轻关键组分乙烯（2）、重关键组分乙烷（3）
0.000230.9990.00077000.029850.940.02934
(2)求解相对挥发度
以重关键组分乙烷（3）为参比组分r
a.求塔顶温度，全凝器 --> 计算馏出液泡点温度
计算2.13MPa下，乙烯的饱和温度，作为泡点温度计算初始温度T0T K1K2K3K4
-22.14 6.7570599150.9998717220.561449520.118005377
-23 6.6635604180.9774739760.5478939650.114417569
-22.17 6.7537872240.9990843060.5609726940.117878798相对挥发度α1,H
α2,H α3,H α4,H 12.039 1.78110.21
b.求塔釜温度，釜液泡点温度
计算2.13MPa下，乙烷的饱和温度，作为泡点温度初始温度T0
T K1K2K3K4
0.129.399258828 1.71443009 1.00003930.2441617419.512181863 1.748372441 1.021*******.250632951
0.189.406938418 1.716729811 1.0014650120.244598997相对挥发度α1,H
α2,H α3,H α4,H 9.393 1.71410.244
附表3-1 乙烯精馏塔进料组成表附表3-2各组分安托因方程系数
c.求进料温度，泡点进料
以乙烯饱和温度为初始温度T0
T K1K2K3K4
-22.17 6.7537872240.9990843060.5609726940.117878798 -21 6.882014271 1.0301222810.5797823690.122892536 -20.04 6.988131469 1.0560967540.5955454720.127126058
-20.06 6.985912394 1.0555509220.5952140230.127036746 -177.324681725 1.1423225720.6468279210.141185065相对挥发度α1,Hα2,Hα3,Hα4,H
11.737 1.77310.213平均相对挥发度
α1,Hα2,Hα3,Hα4,H
10.98965218 1.75574385710.221817722（3）计算θ
q=1
θα*x/(α-θ)α*x/(α-θ)α*x/(α-θ)α*x/(α-θ)
1.010.000220241
2.072065568-11.6-0.001013146
1.110.00022247
2.392945983-1.054545455-0.000899076
1.210.000224745
2.831420178-0.552380952-0.000808094
1.310.000227067 3.466632562-0.374193548-0.000733833
1.410.000229437 4.469291754-0.282926829-0.000672072
1.510.000231858 6.287970687-0.22745098-0.0006199
1.610.0002343310.60236913-0.190163934-0.000575244
1.710.00023685533.78005865-0.163380282-0.00053659
1.050.000221127
2.189505659-2.32-0.000964213
1.060.00022135
2.220975655-1.933333333-0.000952709 1.0531390250.000221197 2.199287706-2.182953101-0.000960572 1.0527451730.000221189 2.198055563-2.199253392-0.000961027 1.0527891580.00022119 2.198193101-2.1974209-0.000960976
1.05280.00022119
2.198227004-2.196969697-0.000960964
1.0017770.00022006
2.049466968-65.27855937-0.001023828 (4)计算最小回流比
α*x/(α-θ)α*x/(α-θ)α*x/(α-θ)α*x/(α-θ)
1.05280.000254368
2.495203701-0.0145833330 R=1.4Rmin X
2.073224630.192745395
Nmin=Y
18.862948730.466724934
N=(Nmin+Y)/(1-Y)Y'=
36.247098140.466724934
进料流量200kmol/h 5
x2,D>0.999mol/mol 丙烷x3,B<0.94mol/mol 0.0001操作压力
2.4MPa 2400kPa
泡点进料
q=1丙烷
6.079206
873.837
256.7609199.8B+D=200B=(176.02-0.999D)+0.94B+0.72+0.02
0.00081K5lg(p1)lg(p2)
lg(p3)lg(p4)lg(p5)0.0943042280.000858 4.2099693.380156
3.129522 2.452113 2.3547420.091375332-0.02155
4.2039183.370316
3.118908 2.438704 2.341040.0942008617.05E-05
4.2097593.379813 3.129153 2.451647 2.354266α5,H
0.168
K5lg(p1)lg(p2)
lg(p3)lg(p4)lg(p5)0.198277918-0.00146 4.3533053.614331
3.380228 2.767889 2.6774860.2036516250.019531
4.3584913.622845
3.389275 2.779249 2.6890990.198640916-
4.1E-05 4.353663.614913
3.380847 2.768666 2.67828
α5,H
0.198)
::(℃；T kPa p S i )/(lg T C B A p S i +-=11-∑=C i i i x K
K5
lg(p1)lg(p2)lg(p3)lg(p4)lg(p5)0.094200861
-0.05385 4.2097593.379813 3.129153 2.451647 2.3542660.098297046
-0.02431 4.217927 3.3931 3.143476 2.469737 2.3727520.101758724
0.000419 4.2245723.403915 3.155126 2.484446 2.3877830.101685668-0.0001 4.224434 3.40369 3.154884 2.484141 2.3874710.1134458880.082375
4.245 3.438 3.191 2.53 2.435
α5,H
0.171
α5,H
0.178507662
α*x/(α-θ)f(θ)=0
-2.14683E-05-9.52875
-1.91636E-05 1.337705
-1.73058E-05 2.278439
-1.57763E-05 3.091916
-1.44952E-05 4.185908
-1.34066E-05 6.060118
-1.247E-0510.41185
-1.16558E-0533.61637
-2.0483E-05-0.13126
-2.02506E-050.286891
-2.04095E-050.015575
-2.04187E-05-0.00196
-2.04176E-05 1.2E-05
-2.04174E-050.000497
-2.16828E-05-63.2299
α*x/(α-θ)Rmin
0 1.480875()()()??
?
???+-+-=X X X X Y 2.1171114.541exp 1
H L LB HB HD LD m x x x x N ,lg *lg α?????????? ?????? ??=