With the information from Problem 1.28 and the topology given in Figure 1.5, accurately sketch a plant layout (plot plan) of the toluene HDA process using a grade-mounted, horizontal, in-line arrangement similar to the one shown in Figure 1.10. You should assume that the area of land available for this process unit is surrounded on three sides by an access road and that a pipe rack runs along the fourth side. Use the information in Table 1.11 as a guide to placing equipment.

Problem 1.28

Using the data from Table 1.7, estimate the footprints of all the equipment in the toluene HDA process. For the shell-and-tube exchangers, assume 12 ft, 1.25-in tubes on a 1.5-in square pitch, and assume 2 ft additional length at either end of the exchanger for tube return and feed header.

For double pipe exchangers, assume an 8-in schedule-20 OD and a 6-in schedule-40 ID pipe with a length of 12 ft including ubend.

For the footprints of pumps, compressors, and fired heater, assume the following:

P-101 use 2 m by 1 m, P-102 use 2 m by 1 m

C-101 (+D-101) use 4 m by 2 m

H-101 use 5 m by 5 m

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V-101 Toluene Feed Drum Toluene KEY Temperature (°C) Pressure (bar) Mass Flow (1000 kg/h) Hydrogen 100 1.9 6.32 25 P-101A/B Toluene Feed Pumps 25.5 E-101 Feed Preheater LV-101 P-101A/B H-101 R-101 Heater Reactor 25.2 hps E-101 4 Air C-101A/B Recycle Gas Compressor Combustion Products 0₂ 600 25 fg H-101 654 E-102 Reactor Effluent Cooler R-101 V-102 High-Pres. Phase Sep. /25.5 C-101A/B 9 CW V-103 High-Pres Phas e Sep. E-102 Xox V-102 V-103 E-10 3 Feed Preheater 18 E-106 T-101 Benzene Benzene Reboiler Columni E-103 Ips mps E-106 T-101 E-104 Benzene Condenser Xa E-104 CW 112 V-104 V-104 Reflux Drum P-102A/B P-102A/B E-105 Reflux Pump Product Cooler CW E-105 Figure 1.5 Benzene Process Flow Diagram (PFD) for the Production of Benzene via the Hydrodealkylation of Toluene Fuel Gas TBWS Designs-Toluene HDA Process Drawn by Checked by Approved by Drawing No Date Date Dabe Revision Benzene