工艺与设备设计精馏塔物料衡算丙酮甲醇分离剖析.docx
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工艺与设备设计精馏塔物料衡算丙酮甲醇分离剖析.docx
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工艺与设备设计精馏塔物料衡算丙酮甲醇分离剖析
1、精馏塔的模拟计算
本课程设计采用ChemCAD计算机模拟计算法进行计算,拟合精度达到1*10^-4。
工艺流程各操作单元参数
StreamNo.1234
StreamName
TempC25.0000*25.0000*95.840595.7242*
Presatm1.0000*1.0000*1.00001.0000
EnthMJ/h-951.52-51552.-5.6297E+005-5.6393E+005
Vapormolefraction0.000000.000000.000000.00000
Totalkmol/h3.3306213.43722008.29022011.6210
Totalkg/h60.00008333.329936195.197036255.1987
TotalstdLm3/h0.060010.421236.210036.2701
TotalstdVm3/h74.654783.9145013.1145087.76
Flowratesinkg/h
Acetone0.00003333.32960.00000.0000
Methanol0.00005000.000536.195236.1952
Water60.00000.000036159.001736219.0035
StreamNo.5678
StreamName
TempC99.0000*99.8882*56.052589.8933
Presatm1.0000*1.0000*1.00001.0000
EnthMJ/h-5.6343E+005-5.6236E+005-14536.-6.0069E+005
Vapormolefraction0.000000.000000.000000.00000
Totalkmol/h2011.62102008.290659.15712165.8639
Totalkg/h36255.198736195.20053344.087441243.7686
TotalstdLm3/h36.270136.21014.179442.5112
TotalstdVm3/h45087.7645013.121325.9348544.91
Flowratesinkg/h
Acetone0.00000.00003292.086441.2437
Methanol36.195236.195216.93025019.2636
Water36219.003536159.005235.070736183.261
StreamNo.910
StreamName
TempC55.0000*64.4438
Presatm1.0000*1.0000
EnthMJ/h-50934.-37190.
Vapormolefraction0.000000.00000
Totalkmol/h213.4372157.5737
Totalkg/h8333.32995048.5748
TotalstdLm3/h10.42126.3011
TotalstdVm3/h4783.913531.80
Flowratesinkg/h
Acetone3333.329641.2437
Methanol5000.00054983.0692
Water0.000024.2614
溶剂回收塔各塔板参数
Stage#164.44C1.00atm
Vapkg/hLiqkg/hY/X
Acetone0.00000329.954530.00000
Methanol0.0000039864.585940.00000
Water0.00000194.091320.00000
Totalkg/h0.000040388.6336
Stage#264.74C1.00atm
Vapkg/hLiqkg/hY/X
Acetone371.19821132.775852.47777
Methanol44847.6601639341.554691.01033
Water218.35275482.833130.40081
Totalkg/h45437.212439957.1610
Stage#365.21C1.00atm
Vapkg/hLiqkg/hY/X
Acetone174.0195361.507032.49911
Methanol44324.6250038018.246091.02983
Water507.094511114.155760.40203
Totalkg/h45005.739739193.9103
Stage#466.19C1.00atm
Vapkg/hLiqkg/hY/X
Acetone102.7507235.195142.55944
Methanol43001.3085935104.562501.07389
Water1138.417242473.476810.40349
Totalkg/h44242.478437613.2366
Stage#568.37C1.00atm
Vapkg/hLiqkg/hY/X
Acetone76.4388423.413542.81769
Methanol40087.6289129050.179691.19099
Water2497.738045288.341310.40764
Totalkg/h42661.804734361.9325
Stage#673.29C1.00atm
Vapkg/hLiqkg/hY/X
Acetone64.6572312.850064.23395
Methanol34033.2460918041.873051.58729
Water5312.6025410440.487300.42817
Totalkg/h39410.504228495.2113
Stage#782.87C1.00atm
Vapkg/hLiqkg/hY/X
Acetone54.093763.6367012.48286
Methanol23024.941416221.913573.10563
Water10464.7490216160.961910.54342
Totalkg/h33543.783022386.5110
Stage#892.32C1.00atm
Vapkg/hLiqkg/hY/X
Acetone44.880404.1556428.10421
Methanol11204.981455309.457035.49178
Water16185.2236355561.847660.75804
Totalkg/h27435.086260875.4626
Stage#996.58C1.00atm
Vapkg/hLiqkg/hY/X
Acetone4.155600.2941637.04210
Methanol5273.261232027.508546.81955
Water19402.8476657512.156250.88460
Totalkg/h24680.263859540.0000
Stage#1098.75C1.00atm
Vapkg/hLiqkg/hY/X
Acetone0.294120.0183042.01318
Methanol1991.31323688.548287.55951
Water21353.1582058354.550780.95648
Totalkg/h23344.765659043.1195
Stage#1199.60C1.00atm
Vapkg/hLiqkg/hY/X
Acetone0.018260.0010844.01678
Methanol652.35303216.267767.85867
Water22195.5507858660.117190.98578
Totalkg/h22847.922558876.3853
Stage#1299.89C1.00atm
Vapkg/hLiqkg/hY/X
Acetone0.001040.0000444.71781
Methanol180.0725736.195207.96349
Water22501.1152336159.000000.99608
Totalkg/h22681.190136195.1934
溶剂回收塔各板物性参数
LIQUIDActualActualThermalSurface
Averagevolratedensityviscosityconduct.tension
Stgkg/hmolwtm3/hkg/m3Pa-secW/m-KN/m
14038932.0453.81750.590.00030.1890.019
23995731.7953.16751.630.00030.1910.019
33919431.3751.98754.070.00030.1930.019
43761330.4949.50759.790.00030.2000.020
53436228.6244.40773.970.00040.2170.022
62849524.9335.09812.060.00040.2740.028
72238720.5125.20888.370.00030.4410.042
86087518.7365.07935.500.00030.5880.053
95954018.2962.73949.110.00030.6400.056
105904318.1161.84954.840.00030.6630.058
115887618.0461.53956.880.00030.6720.058
123619518.0237.80957.560.00030.6750.059
StgLiqH
MJ/h
1-2.9752e+005
2-2.9735e+005
3-2.9718e+005
4-2.9687e+005
5-2.9626e+005
6-2.9571e+005
7-2.9781e+005
8-9.041e+005
9-9.0955e+005
10-9.124e+005
11-9.1352e+005
12-5.6236e+005
溶剂回收塔各塔板蒸汽参数
VAPORActualActualThermal
Averagevolratedensityviscosityconduct.Compr.
Stgkg/hmolwtm3/hkg/m3Pa-secW/m-Kfactor
100.0000.00000.00000.0000.000
24543732.04386171.17660.00000.0190.982
34500631.82385771.16660.00000.0190.982
44424231.44384981.14920.00000.0190.983
54266230.67383361.11290.00000.0200.984
63941129.02380251.03640.00000.0200.985
73354425.79375100.89430.00000.0220.988
82743521.97370650.74020.00000.0230.990
92468019.88373180.66140.00000.0240.991
102334518.71377300.61870.00000.0240.991
112284818.24379740.60170.00000.0250.991
122268118.08380730.59570.00000.0250.992
StgVapH
MJ/h
10
2-2.8462e+005
CHEMCAD5.2.0Page2
JobName:
1Date:
01/07/2015Time:
14:
03:
02
3-2.8445e+005
4-2.8428e+005
5-2.8397e+005
6-2.8337e+005
7-2.8281e+005
8-2.8491e+005
9-2.9051e+005
10-2.9596e+005
11-2.9881e+005
12-2.9992e+005
溶剂回收塔各塔板物流参数
TempPresLiquidVaporFeedsProductDuties
StgCatmkg/hkg/hkg/hkg/hMJ/h
164.41.0040388.635048.58-5.009E+004
264.71.0039957.1645437.21
365.21.0039193.9145005.74
466.21.0037613.2444242.48
568.41.0034361.9342661.80
673.31.0028495.2139410.50
782.91.0022386.5133543.78
892.31.0060875.4627435.0941243.77
996.61.0059540.0024680.26
1098.81.0059043.1223344.77
1199.61.0058876.3922847.92
1299.91.0022681.1936195.195.124E+004
MassRefluxratio8.000
1、物料衡算
1)原料液及塔顶、塔底产品的摩尔分数
水的摩尔质量MA=18.01kg/kmol
甲醇的摩尔质量MB=32.04kg/kmol
丙酮的摩尔流量MC=58.08kg/kmol
xf=(ma/MA)1/[ma/MA+mB/MB+mC/MC]1=0.0723
xD=(ma/MA)2/[ma/MA+mB/MB+mC/MC]2=0.987
xw=(ma/MA)3/[ma/MA+mB/MB+mC/MC]3=0.000562
2)原料液及塔顶、塔底产品的平均摩尔质量
Mf=xfMB+(1-xf)MA=19.02
MD=xDMB+(1-xD)MA=31.86
MW=xwMB+(1-xw)MA=18.02
3)物料衡算
丙酮-甲醇的处理量为6.5万吨/年,每年按325个工作日计。
原料液的处理量F=2166.43
总的物料衡算F=D+W
丙酮的物料衡算Fxf=DxD+Wxw
联立求解D=157.58
W=2008.85
操作回流比R=8.000
理论板数NT=12
进料板序数NF=8
塔顶温度tD=64.4
塔釜温度tw=99.9
进料板温度tF=92.3
塔顶第1块板有关参数
气相流量V1=1418.22
液相流量L1=1260.64
液相组成y1=.09801
气相组成x1=0.9869
气相平均摩尔质量Mv1=32.04
液相平均摩尔质量ML1=31.76
气相密度Ρv1=0.89kg/m^3
液相密度ΡL1=750.59kg/m^3
液相粘度µL1=0.3MPa·s
进料板(第8块板)有关参数
气相流量V8=1249.17
液相流量L8=3250.84
液相组成y8=0.051
气相组成x8=0.28
气相平均摩尔质量Mv8=18.73
液相平均摩尔质量ML8=321.94
气相密度Ρv8=0.7402
液相密度ΡL8=935.50
液相粘度µL8=0.3MPa·s
2、精馏塔的塔体工艺尺寸计算
1)塔径的计算
采用气相负荷因子法计算适宜的空塔气速
(1)精馏段塔径计算
精馏段塔径按第1块板的数据近似计算
液相质量流速为:
WL=L1ML1=1260.64*31.76=40037.93kg/h
气相质量流速为
WV=V1MV1=1418.22*32.04=45439.77kg/h
流动参数为
Ψ=(WL/WV)*(pv/pL)^0.5=0.0304
查图得
Cs,max=0.081
Cs=0.8Cs,max=0.8*0.081=0.0648
由Cs=u[pv/(pL-pv)]^0.5得
u=Cs/[pv/(pL-pv)]^0.5=1.88m/s
D=(4Vs/Πu)^0.5=0.87m
(2)提馏段塔径计算
提馏段塔径按进料板的数据近似计算,计算方法同精馏段。
计算结果为
D=0.95m
比较精馏段与提馏段计算结果,二者基本相同。
圆整塔径,取
D=1.0m
2)液体喷淋密度及空塔气速核算
精馏段液体喷淋密度为
U=(WL/pL1)/(0.785D^2)=7.55m^3/(m^2·h)
精馏段空塔气速为
u=(WV/pv1)/(0.785*3600D^2)=2.007m/s
提馏段液体喷淋密度为
U=(WL/pL8)/(0.785D^2)=7.67m^3/(m^2·h)
提馏段空塔气速为
u=(WV/pv8)/(0.785*3600D^2)=2.015m/s
3、填料层高度计算
填料层高度计算采用理论板当量高度法
对500Y金属孔板波纹填料,查表得,每米填料理论板数为4~4.5块,取nt=4,则HETP=1/nt=1/4=0.25m
由H=NT·HETP得
精馏塔段填料层高度为
H精=NT精·HETP=7*0.25m=1.75m
H´精=1.25H精=2.30m
提馏塔段填料层高度为
H提=NT提·HETP=5*0.25m=1.25m
H´提=1.25H提=1.56m
设计取精馏段填料层高度为2.30m,提馏段填料层高度为1.60m。
根据h=(15~20)HETP,取填料层的分段高度为
h=7*HETP=7*0.25m=1.75m
故精馏段需要分为2段,每段高度为1.2m,提馏段不分段。
4、液体分布器简要设计
1)液体分布器的选型
该精馏塔塔径较大,故选用溢流槽式布液器。
2)分布点密度计算
按Eckert建议值,D>1000mm,喷淋点密度为42点/㎡,因该塔液相负荷较大,设计取喷淋点密度为120点/㎡。
布液点数为:
n=120*0.785D^2=94.2点≈95点
按分布点几何均匀与流量均匀的原则,进行布点设计。
设计结果:
槽共设五道,在槽底部开孔,槽宽度为100mm,高度为120mm,两槽中心距为150mm,分布点采用三角形排列,实际布点数为n=120,布点数示意图如下图所示。
3)布液计算
Ls=Πd0^2nφ(2gΔH)^0.5/4
取φ=0.6,ΔH=160mm
d=[4Ls/(Πnφ(2gΔH)^0.5)]^0.5
=[4*40037.93/(3.14*120*0.6*(2*9.81*0.16)^0.5)]^0.5m
=0.00405m
设计取d0=4.05mm
液体分布器形式与液体分布器相同,设计原则也相同。
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