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The effect of adsorption on mass transfer in fluidized bed catalytic reactors
Author(s) -
Akşahin Inci,
Eroĝlu Inci,
Yücel Hayrettin
Publication year - 2001
Publication title -
the canadian journal of chemical engineering
Language(s) - English
Resource type - Journals
SCImago Journal Rank - 0.404
H-Index - 67
eISSN - 1939-019X
pISSN - 0008-4034
DOI - 10.1002/cjce.5450790108
Subject(s) - mass transfer , residence time distribution , tracer , dispersion (optics) , mass flux , bubble , fluidized bed , mechanics , thermodynamics , flux (metallurgy) , residence time (fluid dynamics) , range (aeronautics) , propane , chemistry , materials science , flow (mathematics) , physics , nuclear physics , optics , geotechnical engineering , organic chemistry , composite material , engineering
Tracer gas residence time distributions (RTD) in a laboratory scale fluidized bed system have been measured for pulses of three different tracer gases (methane, ethane and propane) at different temperatures in the range 323 to 435 K. The fluidized solid was a commercial zeolite based FCC catalyst (CBZ‐2), and measurements were carried out in a superficial air velocity range of 0.01 to 0.04 m/s. The data were interpreted with two‐phase dense phase dispersion models for adsorptive tracers, available in the literature. In addition, modified models were considered by assuming a stationary dense phase and neglecting axial dispersion in this phase. Mean residence time, μ 1 , and the variance of the residence time, σ 2 , of RTD data were calculated for each experimental run. Applying the moment technique in the Laplace domain, the differential equations for all models considered were analytically solved. Mass transfer coefficients obtained from dynamic experiments were compared with the values estimated from the relations available in the literature. It was found that methods considering convective flux alone between the bubble and emulsion phases give closer values to the experimental ones than the methods also including the diffusive flux.