The feed to a sieve-tray distillation column operating at \(1 \mathrm{~atm}\) is \(700 \mathrm{lbmol} / \mathrm{hr}\) of \(45 \mathrm{~mol} \%\) benzene and \(55 \mathrm{~mol} \%\) toluene at \(1 \mathrm{~atm}\) with a bubble-point temperature of \(201^{\circ} \mathrm{F}\). The distillate contains \(91.6 \mathrm{~mol} \%\) benzene and boils at \(179.4^{\circ} \mathrm{F}\). The bottoms product contains \(94.6 \mathrm{~mol} \%\) toluene and boils at \(226.6^{\circ} \mathrm{F}\). The column has 23 trays spaced \(18 \mathrm{in}\). apart, and its reflux ratio is 1.25 . Column pressure drop is neglected. Estimate the total bare-module cost of the column, condenser, reflux accumulator, combined reflux and distillate pump, reboiler, and reboiler pump. Also, estimate the total permanent investment using either the Lang or Guthrie methods. Compute the results using (1) the equations in Sections 16.5 and 16.6 (possibly using the Equipment Costing.xlsx spreadsheet in Section 16.7), and/or APEA. Compare the results.

Figure 16.20:-

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Data Overall U of total condenser = 100 Btu/hr-ft-F Cooling water from 90F to 120F Reboiler heat flux to avoid film boiling = 12,000 Btu/hr-ft Reflux accumulator residence time = 5 min at half full. L/D = 2. Centrifugal pump pressure rise = 100 psi (for each pump). Suction pressure = 1 atm. Use sieve trays with A,,/A = 0.1. Calculate the flooding velocity of the column using the procedure in Example 13.3. Use 35% of the flooding velocity to determine the column diameter. Saturated steam is available at 60 psia.