Gas Mixing Characteristics of a Fluid Bed Regenerator

Handlos, A. E.; Kunstman, R. W.; Schissler, D. O.

doi:10.1021/ie50565a019

Cited by 22 publications

(5 citation statements)

References 1 publication

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“…Expressions for residence time distribution have been developed (7, 6, 7 7, 72, 15) and applied to various systems. In the following brief review, the nomenclature adopted by Danckwerts (7) will be used.…”

Section: Representation and Measurement Of Residence Time Distributionmentioning

confidence: 99%

Residence Time Distribution in Real Systems

Wolf¹,

Resnick²

1963

Ind. Eng. Chem. Fund.

129

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Section: Representation and Measurement Of Residence Time Distributionmentioning

confidence: 99%

Residence Time Distribution in Real Systems

Wolf¹,

Resnick²

1963

Ind. Eng. Chem. Fund.

129

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“…For example Danckwerts (10) concluded that the distribution of residence times for the gas flowing through a commercial fluidized-catalyst regenerator is much closer to piston flow than to complete mixing. Handlos et al (11) on the other hand are convinced that the distribution of residence times for the gas in a similar regenerator follows the complete mixing distribution more closely. Finally there are a number of investigators who characterize the gas flow by models between these extremes.…”

Section: ( 7 )mentioning

confidence: 96%

Kinetics of reduction of ferrous oxide with hydrogen in a fluidized bed at steady state

Feinman¹,

Drexler²

1961

AIChE Journal

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The kinetics of the reduction of ferrous oxide with hydrogen in a steady state fluidized bed have been correlated with a rate equation based on n reaction controlled at the oxide-metal interface and on a differential material balance which assumes that a close approach to piston flow prevails. The correlation gives an enthalpy of activation of 29,500 b.t.u./lb. mole for the reaction, which is in good agreement with McKewan's reported value of 27,500 b.t.u./lb. mole. The relationships developed are used to predict the effect of the important independent variables on the over-all kinetics of the system.

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“…For the dilute phase, the diffusion model approach for axial mixing may be more general (Handlos et al, 1957). However, the usual piston flow assumption is taken here for simplicity, since catalyst particles in the dilute phase are seemingly suspended rather uniformly in small scale fluid beds.…”

Section: Overall Conversion Of a Fluid Bedmentioning

confidence: 99%

Relative contribution of variables affecting the reaction in fluid bed contactors

Miyauchi

Furusaki

1974

AIChE Journal

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Simplified expressions to calculate the extent of reaction in a fluid bed show good agreement with the experimental data of Lewis et al.(1959) and Swaay and Zuiderweg (1972). The contribution of the dilute phase seems more important than that of the jetting zone or reaction factor (Hatta number) in usual fluid bed operations. The effect of the dilute phase is discussed. It is profitable to use the dilute phase for the consecutive isothermal and endothermic reaction, but unprofitable for the exothermic reaction. These characteristics depend upon the nature of reactions and careful considerations as to the choice of the gas velocity, particle characteristics, and reactor design will be necessary.

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Gas Mixing Characteristics of a Fluid Bed Regenerator

Cited by 22 publications

References 1 publication

Residence Time Distribution in Real Systems

Residence Time Distribution in Real Systems

Kinetics of reduction of ferrous oxide with hydrogen in a fluidized bed at steady state

Relative contribution of variables affecting the reaction in fluid bed contactors

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