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PROCESS DESIGN

DISTILLATION COLUMN

How do we design?

Mass fractions

Overall Material Balance

Overall Alcohol Balance

Mass Fractions

F= W+D

F×Xf= W×Xw+D×Xd

F=1537.3 kmole/h

D=23.24 kmole/h

W=1514.1 kmole/h

X= msolute/mtotal

Number of Trays

Effectiveness

Xf=0.033

Xd=0.84

Xw=0.02

The number of theoretical trays is 4.83

The Actual Number of Trays: 6.46

Effectiveness: 0.60

The Feed enters on Tray: 4

Relative Volatility (a)

Rmin and R

Enriching Operation Line

a=(Y_A ⁄ X_A )/((1-Y_A) ⁄ (1-X_A ))

a=10,94

R_min=1/(X_F×(a-1))=3.05

R=R_min×1.3=3.97

Y_(n+1)=(R/(R+1))×X_n+X_D/(R+1)

Y_(n+1)=0,8×X_n+0,17

McCabe Thiele Diagram

Enriching Operating Line

Equilibrium Line

Stripped Operating Line

q Line

y=x

What are?

Distillation: Seperation Process

The End

Suma: Intermediate Product

%92-94

Grape mash: Feed Stock

%8-9

What are?

Presenters

"10. Group"

Why design the distillation coloumn?

How do we design?

Eda BAYRAM

Büşra UYSUN

Şule UYSAL

Arzu SARUKAN

Rabia ÖZDEMİR

How much?

Feed Stock: Grape mash

Product: Suma

The End

Equipment: 800 €

Capacity: 10000000 L/y = 23.24 kmole/h

Total Direct: 1885.12 €

Total Indirect: 626.7 €

Feed(F)=1537.3 knole/h

Distilled(D)=1514.1 kmole/h

Total capital: 4315.4 €

General Material Balance

General Alcohol Balance

Relative volatility

Rmin, R

Enriching Equation

Eriching Operation Line

q Line

Equilibrium Line

Stripped Operation Line

Number of Trays

Efficiency

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