i ill be grateful for your replies.
The liquid reaction A + 2B ! C is to be carried out continuously to produce 20 x 106 lb
of C/yr. Separate feeds of A and B will be fed to one or more CSTR’s to achieve a 95%
conversion of A. Recovery of C in downstream purification is expected to be 97%.
The following data has been collected:
1. Laboratory batch experiments with mixtures of A & B resulted in the following
rate expression: r (gmoles/liter/hr) = 1.8CA
1/3CB @ 200°F, CA, CB in gmoles/liter.
MWA = 50, MWB = 75.
2. The reaction is exothermic with "Hr @ 200°F = -8,000 cal/gmole A converted.
3. Density of all compounds is 1.08 gm/cm3 at 200°F.
4. Thermal conductivity of all compounds is 0.08 Btu/hr/ft/°F. Viscosity of A is 1.0
cp, B 1.5 cp, and the viscosity of C = exp(0.6057+4474/T) cp, T in °R.
5. Cooling water is available at 90°F.
6. Cost of available stainless steel jacketed reactors, installed is as follows:
Reactor Volume (gal) Installed Cost
300 $80,000
500 $110,000
1,000 $150,000
5,000 $336,000
10,000 $474,000
7. Compounds A and B are fed at 60°F. The molar ratio of B/A in the feed is 2.15.
Assume the heat capacity Cp = 0.6 Btu/lb/°F for all components.
To Do:
1. Design a system of one or more jacketed CSTR’s at 200°F which gives the
desired production rate of C for the minimum reactor capital cost. Assume the
reactor is filled to no more than 85% of maximum capacity. If more than one
CSTR is required, assume identical size and design for this problem.
2. Draw a sketch of the reactor and indicate jacket heat transfer medium
requirements (flow rate, temperature). Neglect the jacket side heat transfer
coefficient.
3. Assuming the reactor vessel will be cylindrical with the “standard configuration.”
Indicate power and impeller speed required for agitation.

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