11-7. Wheeler? has summarized the work on internal diffusion for catalytic cracking of gas-oil. At 500C the rate data for fixed-bed operation, with relatively large (-in.) catalyst particles and that for fluidized-bed reactors (very small particle size) are about the same. This suggests that the effectiveness factor for the large particles is high. Confirm this by estimating n for the g-in. catalyst if the mean pore radius is 30 , the particle diameter is 0.31 cm, and the pore volume is 0.35 cm/g catalyst. Molecular weight of oil is 120. At atmospheric pressure with 30- pores the diffusion will be of the Knudsen type. The rate data, interpreted in terms of a first-order rate equation, indicate (at atmospheric pressure) that (kz)exp = 0.25 cm/(sec)(g catalyst). Assume that the parallel-pore model with a tortuosity factor of 2.0 is applicable. 11-7. Wheeler? has summarized the work on internal diffusion for catalytic cracking of gas-oil. At 500C the rate data for fixed-bed operation, with relatively large (-in.) catalyst particles and that for fluidized-bed reactors (very small particle size) are about the same. This suggests that the effectiveness factor for the large particles is high. Confirm this by estimating n for the g-in. catalyst if the mean pore radius is 30 , the particle diameter is 0.31 cm, and the pore volume is 0.35 cm/g catalyst. Molecular weight of oil is 120. At atmospheric pressure with 30- pores the diffusion will be of the Knudsen type. The rate data, interpreted in terms of a first-order rate equation, indicate (at atmospheric pressure) that (kz)exp = 0.25 cm/(sec)(g catalyst). Assume that the parallel-pore model with a tortuosity factor of 2.0 is applicable