Download Chemical Engineering Volume 3, Third Edition: Chemical and by D G Peacock, J.F. Richardson PDF

By D G Peacock, J.F. Richardson

The book of the 3rd version of 'Chemical Engineering quantity three' marks the crowning glory of the re-orientation of the fundamental fabric inside the first 3 volumes of the sequence. quantity three is dedicated to response engineering (both chemical and biochemical), including dimension and method regulate. this article is designed for college students, graduate and postgraduate, of chemical engineering.

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Extra resources for Chemical Engineering Volume 3, Third Edition: Chemical and Biochemical Reactors & Process Control

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The economic optimum proportion of steam is, however, rather less than in the case of ethylbenzene. We will suppose that the reaction is to be carried out in an isothermal tubular reactor which will be maintained at 900OC. 5 mok steam: I mok ethane. 6 (the conversion per pass is relatively low to reduce byproduct formation; unconverted ethane is separated and recycled). e. the pressure drop through the reactor will be neglected. Laboratory experiments, confirmed by data from large scale operations, have shown that ethane decomposition is a homogeneous first order reaction, the rate constant (9- ') being given by the equation in SI units"?

The heat released in the reaction is retained in the reaction mixture so that the temperature rise along the reactor parallels the extent of the conversion a. 3). Adiabatic operation is important in heterogeneous tubular reactors and is considered further under that heading in Chapter 3. Constant heat transfer coe#cient: This case is again similar to the one for batch reactors and is also considered further in Chapter 3, under heterogeneous reactors. Constant hear flux: If part of the tubular reactor is situated in the radiant section of a furnace, as in Fig.

3. Maximum Production Rate For most reactions, the rate decreases as the reaction proceeds (important exceptions being a number of biological reactions which are autocatalytic). For a reaction with no volume change, the rate is represented by the slope of the curve of x (moles converted per unit volume) versus time (Fig. l . l O ) , which decreases steadily with increasing time. The maximum reaction rate occurs at zero time, and, if our sole concern were to obtain maximum output from the reactor and the shutdown time were zero, it appears that the best course would be to discharge the reactor after only a short reaction time t,, and refill with fresh reactants.

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