Use the design algorithm to compose a general list ofequations and parameters that are needed to solve this chemicalreaction engineering problem.

Jeffreys, in a treatment of the design of an acetic anhydride manufacturing facility, states that one of the key steps is the vapor-phase cracking of acetone to ketene and methane: CH3COCH3CH2CO + CHA A → B + c He states further that this reaction is first-order w.r.. acetone and that specific reaction rate can be expressed by: k=8.19733.10'4e where k is in sol and T is in K. 34222 In this design it is desired to process 7850 kg of acetone per hour (37.6 mol/s) in a tubular reactor. The reactor consists of a bank of 1000 1-inch schedule 40 tubes (ID = 2.66 cm) arranged in parallel where each tube is 180 cm long. Consider the following five cases: CASE 1: The reactor is operated isothermally. CASE 2: The reactor is operated adiabatically. CASE 3: The reactor is surrounded by a heat exchanger where the heat-transfer coefficient is 110 J/m2sk, and the T of the heating medium, To, is constant at 1250 K. CASE 4: The heat exchanger in Case 3 now has a variable To. The reactant and the heating medium flow in the same direction. CASE 5: Same as Case 4, but the reactant and the heating medium flow in opposite directions. In the last two cases, air (CPair = 34.5 J/mol-K) at a rate of 0.11 mol/s with Too = 1250 K is available for heating. The inlet T & P are the same for all cases at 1035 K & 162 kPa, respectively. AHºrxn(298K)= 80.77 kJ/mol; CpA= 163, CPE=83, & Cpc= 71 J/mol K.