The reaction A + B => R (MWA-95 lb/mol; MwBF 134 lb/mol, MWR= 229 lb/mol) is essentially irreversible at all conditions of interest. A stoichiometric mixture of A and B (with no diluent) contains 0.035 lb mol/gal of each component and has a density of 8.00 lb/gal. The heat capacities of A and B are both equal to 68 cal/g-mol- C and are essentially independent of temperature. The heat of reaction, AHR, is 65 kcal/g mol, and also is independent of temperature. You have recently been put in charge of a facility that manufactures R. The facility operates 7890 h/year. The reaction is carried out in a single, ideal CSTR with a volume of 1000 gal. The reactor operates at 550 °F. The feed is a stoichiometric mixture of A and B at 100 F. Heat is removed through a cooling coil in the reactor. The fractional conversion of A, XA, in the reactor effluent is 0.95 The rate equation for the reaction at 550 °F is: -rA-kca/(1+ Kca) where the rate is in [lb-mol/h gal. The rate coefficient is reported to be k = 1.82 h-1, and the constant K is K 85.0 gal/lb-mol. a. What is the annual production rate of R in pounds per year in the existing reactor? b. What is the required rate of heat removal (BTU/h) through the cooling coil in the existing reactor? c. The capacity of the plant is to be increased to 10,000,000 lbs/year, with the same fractional conversion of A. Propose a reactor system that will do the job, and specify the volume of any additional reactors that you add. The system should include the existing CSTR. Minimizing the additional reactor volume is a sufficient design criterion. Assume that the new reactor system will operate isothermally at 550°F d. What is the required rate of heat removal through the cooling coil in the existing CSTR, as it operates in the expanded plant? The feed to the CSTR will remain at 100 °F a. b. c. d.