McCabe Thiele Method.xlsx
7
X D 0.99 X F 0.55 x y X B 0.01 0 0 1 1 α 3 R min 1 x y 0.99 0.99 R 1.2 0 0.450 q 0.5 Slope -1 x y 0.55 0.55 0.3 0.8 a1 0.545454545 x y a2 -1 0.01 0.01 b1 0.45 0.421 0.679 b2 1.1 a1 = a2 = b1 = b2 = 45 line top Section q-line bottom Section 1 q q Slope
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Transcript of McCabe Thiele Method.xlsx
7/21/2019 McCabe Thiele Method.xlsx
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XD 0.99
XF 0.55 x y
XB 0.01 0 0
1 1
α 3
Rmin 1 x y
0.99 0.99
R 1.2 0 0.450
q 0.5
Slope -1 x y
0.55 0.55
0.3 0.8
a1 0.545454545 x y
a2 -1 0.01 0.01
b1 0.45 0.421 0.679
b2 1.1
a1 =
2
45 line
top Section
q-line
bottom Section
1
qqSlope
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x y
0 0
0.1 0.250
0.2 0.429
0.3 0.563
0.4 0.667
0.5 0.750
0.6 0.818
0.7 0.875
0.8 0.923
0.9 0.964
1 1
equilibrium curve
0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
0.9
1
0 0.1 0.2 0.3 0.
x
x y
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0.5 0.6 0.7 0.8 0.9 1
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Binary Distillation with McCabe Thiele Methodhttp://excelcalculations.blogspot.com
Parameters
Feed Flowrate F 75 kmol h-1
Feed Frac Light Component xF 0.4 mol frac
Top Prod Frac Light Component xD 0.99 mol frac
Bottom Prod Frac Light Component xW 0.1 mol frac
Reflux Ratio R 3
Relative Volatility α 4
q-line 0.75
CalculationsTop Product Flowrate D 25.2809 kmol h
-1
Bottom Product Flowrate W 49.7191 kmol h-1
Liquid Flow at Top of Column L 75.8427
Vapour Flow in Top of Column V 101.124
Liquid Flow in Bottom of Column L' 132.093
Vapour Flow in Bottom of Column V' 82.3736
X Coords of Op Line Intersection qx 0.36067
Number of Plates (plus Reboiler) 6
Feed Plate (From Top of Column) 5
Minimum Reflux Ratio (Underwood) 1.02224Minimum Num Theoretical Places (Fenske) 4.89964
Assumptions:
Equilibrium Reboiler
Total Condensor
Constant Relative Volatility
Constant Molar Overflow
0.0
1.0
0.0
M o l e F r a c t i o n o f L i g h t e r C o m p o n e n t i n V a p o u r P h a s e
Mole Fraction of Lighter Component in Liqu
Binary Distillation with the McCabe-Thiele
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1.0 id Phase
Method
