Page 278 - Process Equipment and Plant Design Principles and Practices by Subhabrata Ray Gargi Das

Further reading 279

Eq. 10.11 gets modified by replacing (G/A T ) with m V;op as e
h y
Z bed Z 2
m V;op :dy
k a
h bed ¼ dz ¼
0
y
0 y 1 ð1 yÞðy y i Þ
ð1 yÞ iM
Numerical integration of the above gives h bed ¼ 2.67 m.
Bed dimension-Active bed: Diameter ¼ 2020 mmf,H ¼ 2670 mm. The L/D ratio (1.32) is
slightly low. However, the active bed will have additional larger size packing layers below and above
for fluid distribution and bed stabilization. The total L/D is expected to be reasonably OK. For details
see Chapter 14.
Some specific terms with symbol and typical units used in this chapter:
m L ¼ Liquid mass flow rate (kg/s)
m V ¼ Vapor/Gas mass flow rate (kg/s)
2
m L ¼ Liquid mass flow rate per unit tower cross sectional area (kg/s$m )
2
m V ¼ Vapor/Gas mass flow rate per unit tower cross sectional area (kg/s$m )
3
q L ¼ Liquid volumetric flow rate (m /s)
3
q V ¼ Vapor/Gas volumetric flow rate (m /s)
L ¼ Liquid molar flow rate (kmol/s)
2
L ¼ Liquid molar flow rate per unit tower cross sectional area (kmol/s$m )
G ¼ Gas/Vapour molar flow rate (kmol/s)
2
G ¼ Vapour/Gas molar flow rate per unit tower cross sectional area (kmol/s$m )
L ¼ Solute free Liquid molar flow rate (solvent component only) (kmol/s) or (kmol/hr)
0
G ¼ Solute free Vapor/Gas molar flow rate (nonabsorbable component only) (kmol/s) or (kmol/hr)
0
Further reading
1. Treybal, R. E. (1981). Mass transfer operations (3rd ed.). McGraw Hill.
2. Geankoplis, C. J. (2003). Transport processes and separation process principles (4th ed.). PHI Learning Pvt
Ltd.
3. B.D. Smith. Design of equilibrium stage processes. McGraw Hill Book Company. NY.
4. Towler, G., & Sinnott, R. (2013). Chemical engineering design (2nd ed.). Elsevier Limited.