Consider Figure E17.6(a), in which the overall heat transfer coefficient (U) is assumed to be 25 W/m

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Consider Figure E17.6(a), in which the overall heat transfer coefficient (U) is assumed to be 25 W/m °C. It can be noted that in Figures E17.6(b) and E17.6(c)(b), the transients in exit temperature and CO concentration appear to be negligible. Now increase the flowrate of benzene to 0.01 kmol/h, while keeping the flowrate of air constant. Simultaneously increase the temperature of air to 520°C. Did you notice any difference in the transient profile of temperature and benzene and CO concentration at the exit of the reactor compared to what is obtained in Example 17.6? Why or why not?


Example 17.6Figure E17.6(a) shows the schematic of a cooled tubular reactor in which maleic anhydride is being produced

C6H6+4.502  C4HO3 + 2CO2 + 2HO C6H6+7.502  6CO2 + 3HO C4H2O3 + 302  4CO2 + HO

These reactions are carried out using excess air to avoid

runaway reactions. As a result, the reactions can be considered as pseudo-first-order reactions. The reaction


Since these reactions are highly exothermic, a molten, eutectic salt is circulated in a multitube reactor to

1. Develop a dynamic simulation of this cooled tubular reactor assuming that the dimensions of the reactor

Figure E17.6Air 510C 2.75bar 0.20 kmol/h Pure Benzene 510C 2.75 bar 0.001 kmol/h Steam 490C 143.7 bar Remote Set Point

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Analysis Synthesis And Design Of Chemical Processes

ISBN: 9780134177403

5th Edition

Authors: Richard Turton, Joseph Shaeiwitz, Debangsu Bhattacharyya, Wallace Whiting

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