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Figure 3. Total butane reaction rate for various butane in air mixtures.

Figure 3 Total butane reaction rate for various butane in air mixtures.

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Table I. Kinetic Parameters for Rate Equations of Centi et al. (1985)* * Ky = 2616 mol/L; a = B = 0.2298; y = 0.6345; 6 = 1.151.
Table I. Kinetic Parameters for Rate Equations of Centi et al. (1985)* * Ky = 2616 mol/L; a = B = 0.2298; y = 0.6345; 6 = 1.151.
Figure 1. Schematic of a circulating fluidized bed as a catalytic reactor.
Figure 1. Schematic of a circulating fluidized bed as a catalytic reactor.
that of n-butane in air. The predicted values of the gas interchange coefficients are of the order of 10°? m/s, while data supplied by G. S. Patience calculated from an ex- perimental gas RTD indicate values for the core-to-annulus gas interchange coefficient in the range of 0.015-0.094 m/s. Thus there is agreement between the simulation and the experimental data.
that of n-butane in air. The predicted values of the gas interchange coefficients are of the order of 10°? m/s, while data supplied by G. S. Patience calculated from an ex- perimental gas RTD indicate values for the core-to-annulus gas interchange coefficient in the range of 0.015-0.094 m/s. Thus there is agreement between the simulation and the experimental data.
Figure 2. Single pass butane conversion for various butane in air mixtures.
Figure 2. Single pass butane conversion for various butane in air mixtures.
Figure 4. Single pass product yields for 1 mol % butane in air mixture.
Figure 4. Single pass product yields for 1 mol % butane in air mixture.
Figure 5. Single pass product yields for 5 mol % butane in air mixture.
Figure 5. Single pass product yields for 5 mol % butane in air mixture.
Figure 6. Maleic anhydride selectivity for various butane in air mixtures.
Figure 6. Maleic anhydride selectivity for various butane in air mixtures.
Figure 7. Effect of solids circulation rate on butane conversion and solids holdup.
Figure 7. Effect of solids circulation rate on butane conversion and solids holdup.
Figure 9. Effect of catalyst deactivation on single pass butane conversion. Figure 8. Effect of inlet superficial gas velocity on butane conver- sion and solids holdup.
Figure 9. Effect of catalyst deactivation on single pass butane conversion. Figure 8. Effect of inlet superficial gas velocity on butane conver- sion and solids holdup.
Figure 10. Contribution to reaction by the core and annular regions for a 5 mol % butane in air mixture. Acknowledgment profiles begin to separate. At the riser inlet, the catalyst has just been regenerated and exposure to reaction con- ditions does not show a noticeable effect. Reaction occurs rapidly at this level, however, and after 3 m the trans- formation of the catalyst crystalline phases at the expense of the surface oxygen layers becomes significant. The higher degree of deactivation, resulting in reduced con- version, will consequently reduce the yields of both maleic anhydride and CO». The results of this simple catalyst deactivation model indicate that reduction of the catalyst activity as the reaction proceeds has only a slight effect on the reactor performance. However, the results will underpredict the effect of deactivation on conversion due to the assumptions involved in the deactivation model. Further work to include the solids RTD in the simulation will produce more realistic results.
Figure 10. Contribution to reaction by the core and annular regions for a 5 mol % butane in air mixture. Acknowledgment profiles begin to separate. At the riser inlet, the catalyst has just been regenerated and exposure to reaction con- ditions does not show a noticeable effect. Reaction occurs rapidly at this level, however, and after 3 m the trans- formation of the catalyst crystalline phases at the expense of the surface oxygen layers becomes significant. The higher degree of deactivation, resulting in reduced con- version, will consequently reduce the yields of both maleic anhydride and CO». The results of this simple catalyst deactivation model indicate that reduction of the catalyst activity as the reaction proceeds has only a slight effect on the reactor performance. However, the results will underpredict the effect of deactivation on conversion due to the assumptions involved in the deactivation model. Further work to include the solids RTD in the simulation will produce more realistic results.
Related topics:
EngineeringIndustrial EngineeringMaleic AnhydrideFluidized Bed ReactorCirculating Fluidized BedIndustrial Chemistry/Chemical Engineering
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