As discussed in Example 6.7, the following stream at \(100^{\circ} \mathrm{F}\) and 484 psia is to be separated by two distillation columns into the Products \(1-3\) in the following table.

Two different distillation sequences are to be examined as shown in Figure 7.32. In the first sequence, \(\mathrm{H}_{2}\) and \(\mathrm{CH}_{4}\) are removed in the first column.
If using ASPEN PLUS, the DSTWU module is used to estimate the reflux ratio and theoretical tray requirements for both sequences. In addition, the RK-SOAVE option is used. Specify a reflux ratio equal to 1.3 times the minimum. Use design specifications to adjust the isobaric column pressures so as to obtain distillate temperatures of \(130^{\circ} \mathrm{F}\); however, no column pressure should be less than 20 psia. Also, specify total condensers but note that a partial condenser is used when \(\mathrm{H}_{2}\) and \(\mathrm{CH}_{4}\) are taken overhead.

Data From Example 6.7:-

Figure 6.12:-

Figure 7.32:-

Species Flow Rates (lbmol/hr) Feed Recycle Gas Recycle H 0 0 2,045.9 CH 0 0 3,020.8 CH, (benzene) 0 3.4 42.8 CH, (toluene) CH10 (biphenyl) 274.2 82.5 5.3 0 1.0 0 Feed 75F, 569 psia Recycle 250F, 569 psia Vapor Gas Recycle Product 121F 569 psia U=50 AP-5 psi 100 F FLASH DRUM U-60 AP = 5 psi 120F CW 90F 1,200F 1,000F ww FURNACE AP-70 psi 1,150F 1,268F REACTOR QUENCH PUMP Liquid Product AP=0 psi Figure 7.31 Reactor section of the toluene hydrodealkylation process.