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By Rafael Kandiyoti

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08 throughout the reactor. 05 bar. Calculate: (i) (ii) (iii) the global rate of reaction, the external concentration gradient (expressed in terms of the partial pressures), and, the temperature gradient between the bulk gas stream and external catalyst pellet surfaces, at the selected point in the reactor. Bulk gas properties may be taken as those of the diluent. The pressure drop along the reactor axis may be neglected. 4 ; Re 2/ 3 ; jH d p G / PB ­ C p PB ½ ® ¾ C p G ¯ OB ¿ h 2/ 3 . com 31 IV.

Improve cooling and/or reduce reactant concentrations and/or dilute the catalyst. Part C: The main difficulty arises from ignoring the radial temperature distribution. In dealing with highly exothermic reactions, when the maximum temperature along the central axis turns out to be much larger than the radially averaged temperature, runaway may occur under conditions where the 1-dimensional model would predict “safe” operation. The disadvantage of 2-dimensional operation is the requirement for accurate additional data for radial heat (and mass) transport: Orad ,effective , Drad ,effective .

Both sets of experiments were carried out under conditions where external temperature and concentration gradients were negligible. Global rates of reaction, measured as a function of temperature, using approximately similar external surface concentrations of A and B for all experiments, are given in the table below. Assuming the 50 μ particles to be isothermal under all operating conditions, (a) Calculate from this data, the energy of activation most likely to approximate the true value for the chemical reaction step at the catalytic sites.

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