Reconfigure the heating system to operate in countercurrent fashion. Retain the same utility stream input and IPA conversion (90\%).

a. Determine the change in process feed rate.

b. Determine the percent change in process feed rate.

Problems 23. 21-23.26 investigate the performance of the acetone reactor system. The reaction kinetics are presented in Section 23. 5.3. The reactor and internal heat exchanger are fixed. For the base case, the active volume of the reactor is \(5.1 \mathrm{~m}^{3}\) at the operating conditions given in Figure 23. 10. Unless otherwise stated, the heat transfer coefficient and reactor pressure drop are to be assumed constant. The feed temperature, pressure, and component concentrations remain constant. For these calculations, assume the utility fluid to be n-heptadecane (at pressures more than \(30 \mathrm{bar}\) ). At the base case, the utility flow is \(58 \mathrm{kmol} / \mathrm{h}\).

Figure 23.10

Data from section 23.5.3

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Reactor Feed 234 2.16 Equipment Specifications 407 HTM in R-401 R-401 HTM out MOC - carbon steel 357 Vessel Size: Diameter - 1.85 m Length - 8 m Reactor Effluent Tubes: 350 Number - 448 1.91 Diameter - 2 in (5.1 cm) Flowrates (kmol/h) Length - 20 ft (6.1 m) Stream 2a 3 Heat Transfer Coefficient: Hydrogen 34.78 60 W/mC Acetone 0.16 34.94 IPA 38.64 3.86 Temperature (C) Water 19.04 19.04 Pressure (bar)