Use the Heuristic rules to design the E-101 of equipment for the hydrodealkylation of Toluene. Comment on any significant differences that you find. Use the following heuristic rules:

1. Distillation is usually the most economical method for separating liquids, superior to extraction, absorption crystallization, or others. 2. For ideal mixtures, relative volatility is the ratio of vapor pressures ₁₂= P₁*/P₂* 3. Tower operating pressure is most often determined by the temperature of the condensing media, 3850C (100120 F) if cooling water is used, or by the maximum allowable reboiler temperature to avoid chemical decomposition/degradation. 4. Sequencing of columns for separating multicomponent mixtures: a. Perform the easiest separation first, that is, the one least demanding of trays and reflux, and leave the most difficult to the last. b. When neither relative volatility nor feed composition varies widely, remove components one by one as overhead products. Heuristics for Towers (Distillation and Gas Absorption)

c. When the adjacent ordered components in the feed vary widely in relative volatility, sequence the splits in order of decreasing volatility. d. When the concentrations in the feed vary widely but the relative volatilities do not, remove the components in order of decreasing concentration. 5. Economical optimum reflux ratio is in the range of 1.2 to 1.5 times the minimum reflux ratio, Rmin. 6. The economically optimum number of theoretical trays is near twice the minimum value Nmin. 7. The minimum number of trays is found with the Fenske-Underwood equation Nmin = ln{[x/(1-x)]_ochd/[x/(1-x)]_btms}/ln .

8. Minimum reflux for binary or pseudo binary mixtures is given by the following when separation is essentially complete (xD 1) and D/F is the ratio of overhead product to feed rate: R_minD/F = 1/(-1), when feed is at the bubble point (R_min + 1) D/F = /(-1), when feed is at the dew point 9. A safety factor of 10% of the number of trays calculated by the best means is advisable. 10. Reflux pumps are made at least 10% oversize. 11. The optimum value of the Kremser absorption factor A = (L/mV) is in the range of 1.25 to 2.0. 12. Reflux drums usually are horizontal, with a liquid holdup of 5 min half-full. A takeoff pot for a second liquid phase, such as water in hydrocarbon systems, is sized for a linear velocity of that phase of 1.3 m/s (0.5 ft/sec), minimum diameter is 0.4 m (16 in).

13. For towers about 0.9 m (3 ft) dia, add 1.2 m (4 ft) at the top for vapor disengagement, and 1.8 m (6 ft) at bottom for liquid level and reboiler return. 14. Limit the tower height to about 53 m (175 ft) max. because of wind load and foundation considerations. An additional criterion is that L/D be less than 30 (20

\begin{tabular}{|lrrrrrrrrr|} Stream Number & 1 & 2 & 3 & 4 & 5 & 6 & 7 & 8 \\ \hline Temperature (C) & 25 & 59 & 25 & 225 & 41 & 600 & 41 & 38 \\ Pressure (bar) & 1.90 & 25.8 & 25.5 & 25.2 & 25.5 & 25.0 & 25.5 & 23.9 \\ Vapor Fraction & 0.0 & 0.0 & 1.00 & 1.0 & 1.0 & 1.0 & 1.0 & 1.0 \\ Mass Flow (tonne/h) & 10.0 & 13.3 & 0.82 & 20.5 & 6.41 & 20.5 & 0.36 & 9.2 \\ Mole Flow (kmol/h) & 108.7 & 144.2 & 301.0 & 1204.4 & 758.8 & 1204.4 & 42.6 & 1100.8 \\ Component Mole Flow & & & & & & & & \\ (kmol/h) & & & & & & & & \\ Hydrogen & 0.0 & 0.0 & 286.0 & 735.4 & 449.4 & 735.4 & 25.2 & 651.9 \\ Methane & 0.0 & 0.0 & 15.0 & 317.3 & 302.2 & 317.3 & 16.95 & 438.3 \\ Benzene & 0.0 & 1.0 & 0.0 & 7.6 & 6.6 & 7.6 & 0.37 & 9.55 \\ Toluene & 108.7 & 143.2 & 0.0 & 144.0 & 0.7 & 144.0 & 0.04 & 1.05 \\ \hline \end{tabular} \begin{tabular}{rrrrrrrrrrr|} \hline 9 & 10 & 11 & 12 & 13 & 14 & 15 & 16 & 17 & 18 & 19 \\ \hline 654 & 90 & 147 & 112 & 112 & 112 & 38 & 38 & 38 & 38 & 112 \\ 24.0 & 2.6 & 2.8 & 3.3 & 2.5 & 3.3 & 2.3 & 2.5 & 2.8 & 2.9 & 2.5 \\ 1.0 & 0.0 & 0.0 & 0.0 & 0.0 & 0.0 & 0.0 & 1.0 & 1.0 & 0.0 & 1.0 \\ 20.9 & 11.6 & 3.27 & 14.0 & 22.7 & 22.7 & 8.21 & 2.61 & 0.07 & 11.5 & 0.01 \\ 1247.0 & 142.2 & 35.7 & 185.2 & 290.7 & 290.7 & 105.6 & 304.2 & 4.06 & 142.2 & 0.90 \\ & & & & & & & & & & \\ 652.6 & 0.02 & 0.0 & 0.0 & 0.02 & 0.0 & 0.0 & 178.0 & 0.67 & 0.02 & 0.02 \\ 442.3 & 0.88 & 0.0 & 0.0 & 0.88 & 0.0 & 0.0 & 123.05 & 3.10 & 0.88 & 0.88 \\ 116.0 & 106.3 & 1.1 & 184.3 & 289.46 & 289.46 & 105.2 & 2.85 & 0.26 & 106.3 & 0.0 \\ 36.0 & 35.0 & 34.6 & 0.88 & 1.22 & 1.22 & 0.4 & 0.31 & 0.03 & 35.0 & 0.0 \\ \hline \end{tabular} \begin{tabular}{|lllllll|} \hline Heat Exchangers & E-101 & E-102 & E-103 & E-104 & E-105 & E-106 \\ \hline Type & Fl.H. & Fl.H. & MDP & Fl.H. & MDP & Fl.H. \\ Area (m2) & 36 & 763 & 11 & 35 & 12 & 80 \\ Duty (MJ/h) & 15,190 & 46,660 & 1055 & 8335 & 1085 & 9045 \\ \hline Shell & & & & & & \\ \hline Temp. (C) & 225 & 654 & 160 & 112 & 112 & 185 \\ Pres. (bar) & 26 & 24 & 6 & 3 & 3 & 11 \\ Phase & Vap. & Par. Cond. & Cond. & Cond. & 1 & Cond. \\ MOC & 316SS & 316SS & CS & CS & CS & CS \\ \hline Tube & & & & & & \\ \hline Temp. (C) & 258 & 40 & 90 & 40 & 40 & 147 \\ Pres. ( bar) & 42 & 3 & 3 & 3 & 3 & 3 \\ Phase & Cond. & 1 & 1 & 1 & 1 & Vap. \\ MOC & 316SS & 316SS & CS & CS & CS & CS \\ \hline Vessels/Tower/ & & & & & & \\ Reactors & V-101 & V-102 & V-103 & V-104 & T-101 & R-101 \\ \hline Temperature (C) & 55 & 38 & 38 & 112 & 147 & 660 \\ Pressure (bar) & 2.0 & 24 & 3.0 & 2.5 & 3.0 & 25 \\ Orientation & Horizn'l & Vertical & Vertical & Horizn'l & Vertical & Vertical \\ MOC & CS & CS & CS & CS & CS & 316SS \\ \hline \end{tabular}