Page 67 - Analysis, Synthesis and Design of Chemical Processes, Third Edition

d. Shell and tube exchanges may require periodic cleaning and tube bundle replacement.

e. Pipes located at ground level present a tripping hazard.

f. The prevailing wind is nearly always from the west.

Estimate the footprint for a shell-and-tube heat exchanger from the following design data:

• Area = 145 m 2

• Hot side temperatures: in at 300°C out at 195°C

17.
• Cold side temperature: bfw at 105°C mps at 184°C

• Use 12 ft, 1″ OD tubes on a 1-1/4″ square pitch, use a single shell and tube pass because of change
of phase on shell side

• Use a vapor space above boiling liquid = 3 times liquid volume

Make a sketch of a layout (plot plan only) of a process unit containing the following process
equipment:

• 3 reactors (vertical – diameter 1.3 m each)

• 2 towers (1.3 and 2.1 m in diameter, respectively)
18.
• 4 pumps (each mounting pad is 1 m by 1.8 m)

• 4 exchangers (footprints of 4 m by 1m, 3.5 m by 1.2 m, 3 m by 0.5 m, and 3.5 m by 1.1 m)

The two columns and the 3 reactors should all be aligned with suitable spacing and all the exchangers
should have clearance for tube bundle removal.

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″ tubes on a 1.5″ square pitch and assume 2 ft
additional length at either end of the exchanger for tube return and feed header.

19. • For double pipe exchangers, assume an 8″ schedule 20 OD and a 6″ schedule 40 ID pipe with a
length of 12 ft including u-bend.

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

• P-101 use 2m by 1m, P-102 use 2m by 1m
• C-101 (+D-101) use 4m by 2m
• H-101 use 5m by 5m

With the information from Problem 19 and the topology given in Figure 1.5, accurately sketch a plant