Heat transfer in three-phase fluidized beds

Baker, C. G. J.; Armstrong, E.R.; Bergougnou, M.A.

doi:10.1016/0032-5910(78)80089-8

Cited by 65 publications

(39 citation statements)

References 8 publications

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“…Further increase of u, would not produce more micro-scale liquid eddies which would promote heat transfer (Deckwer, 1980b(Deckwer, , 1985Joshi, 1980). These results are in good agreement with previous investigations in both Newtonian (Baker et al, 1978;Ziegler, 1983, 1985) and non-Newtonian CMC solutions (Kato et al, 1981;Kang et al, 1985).…”

Section: Resultssupporting

confidence: 94%

Heat Transfer in Three-Phase Fluidized Beds With Non-Newtonian Pseudoplastic Solutions

Zaidi

Benchekchou

Karioun

et al. 1990

Chemical Engineering Communications

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Section: Resultssupporting

confidence: 94%

Heat Transfer in Three-Phase Fluidized Beds With Non-Newtonian Pseudoplastic Solutions

Zaidi

Benchekchou

Karioun

et al. 1990

Chemical Engineering Communications

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“…Baker et al (1978) used a coaxially inserted cylindrical heater to investigate the effect of individual operating variables on the surface-to-bed heat transfer coefficient. Baker et al (1978) used a coaxially inserted cylindrical heater to investigate the effect of individual operating variables on the surface-to-bed heat transfer coefficient.…”

mentioning

confidence: 99%

Wall‐to‐bed heat transfer in liquid—solid and gas—liquid—solid fluidized beds part II: Gas—liquid—solid fluidized beds

1986

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Wall-to-bed heat transfer in gas-liquid-solid fluidized beds with a cocurrent upflow was analyzed on the basis of a series thermal resistance model. The effective radial thermal conductivity and the apparent wall heat transfer coefficient were determined over a wide range of experimental conditions. The behavior of the effective thermal conductivity strongly depends on the flow mode for the three-phase fluidized bed, directly indicating the trend of the radial liquid mixing. The modified Peclet number for the radial thermal diffusivity takes on a minimum with respect to the liquid velocity in a manner similar to that in a liquid-solid fluidized bed, but the value of the modified Peclet number decreases significantly with gas velocity. The apparent wall heat transfer coefficient can be correlated well with a Colburn type equation which at zero gas velocity reduces to the same equation as that proposed for liquid-solid fluidization, as follows:Le transfert de chaleur lit-paroi dans les lits fluidises gaz-liquide-solides avec un Ccoulement ascendant cocourant a CtC analysk a I'aide d'un modkle de resistances thermiques en sCrie. La conductivitk thermique radiale effective et le coefficient de transfert de chaleur apparent a la paroi ont CtC dCterminCs pour des conditions exp5rimentales trks variCes.Le comportement de la conductivitk thermique effective dtpend fortement du mode d'tcoulement dans le lit fluidist trois phases, ce qui indique directement la tendance du mklangeage radial du liquide. Le nombre de Peclet modifiC pour la diffusivitt thermique radiale atteint un minimum avec une augmentation de la vitesse du liquide de la m&me manikre que dans un lit fluidisk solides-liquide, mais la valeur du nombre de Peclet modifiC diminue de manikre significative avec la vitesse des gaz. Le coefficient de transfert de chaleur apparent ti la paroi peut &tre corrClC a I'aide d'une Cquation de type Colburn qui, lorsque la vitesse des gaz est nulle, devient identique a celle proposCe pour la fluidisation solides-liquide, a savoir: j b = 0,137 Re;,,-"."' hree-phase fluidized beds with cocurrent upflow of gas

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“…Systems (gas/liquid/solid) air/water/glass beads air/water/glass beads air/water-CMC/porous alumina air/water/glass beads air/water-CMC/ porous alumina (U, = 1 ~ 15.6 mPa»s) air/water/glass beads air/water-CMC/glass beads (U£ = 1 " 39 mPa»s) also data taken from Kato et al (1981) Chiu and Ziegler (1983) Baker et al (1978) Source data from Kato et al (1981) Chiu and Ziegler (1983) Baker et al (1978) Kang et al (1985 air/0.5% tert-pentyl alcohol aqueous where Cj and c 2 are empirical constants (e.g., see Table 3.6 for immersed vertical cylinder to bed heat transfer). In Eqn.…”

Section: " = [( U G + U £ )(E G P G + € I P I + E S P S ) -U J G P I mentioning

confidence: 86%

“…In these studies, a uniform radial temperature distribution is usually imposed to permit an expedient analysis of heat transfer; for example for heat transfer between the bed and the column wall (e.g., Viswanathan et al, 1964;Kato et al, 1980) or between the bed and an immersed heater (e.g., Baker et al, 1978). While there are no reported particle-liquid or liquid-gas heat transfer studies under three-phase fluidization conditions, the corresponding two-phase information (i.e., for liquid-solid fluidization and gas-liquid bubble columns, respectively) could serve as a good approximation for the three-phase situation.…”

Section: Heat Transfermentioning

confidence: 99%

“…An increase in particle size (or Figure 3.23 Relationship between the heat transfer coefficient and particle size in an immersed vertical cylinder to bed heat transfer in an air-water-glass bead fluidized bed (from Baker et al, 1978). introducing solid particles in a gas-liquid column) generally increases the heat transfer coefficient, except for small particles with diameters of about 1 mm at high gas velocities.…”

Section: Immersed Vertical Cylinder-to-bed Heat Transfermentioning

confidence: 99%

See 1 more Smart Citation

Mass Transfer, Mixing and Heat Transfer of Cocurrent Upward Fluidized Bed Systems (Mode E-I-a-1; Figure 1.3)

Fan¹,

Muroyama²

1989

Gas–Liquid–Solid Fluidization Engineering

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Heat transfer in three-phase fluidized beds

Cited by 65 publications

References 8 publications

Heat Transfer in Three-Phase Fluidized Beds With Non-Newtonian Pseudoplastic Solutions

Heat Transfer in Three-Phase Fluidized Beds With Non-Newtonian Pseudoplastic Solutions

Wall‐to‐bed heat transfer in liquid—solid and gas—liquid—solid fluidized beds part II: Gas—liquid—solid fluidized beds

Mass Transfer, Mixing and Heat Transfer of Cocurrent Upward Fluidized Bed Systems (Mode E-I-a-1; Figure 1.3)

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