Mass Transfer in Packed Beds with Two-Phase Flow

Goto, Shunsaku; Levec, Janez; Smith, J. M.

doi:10.1021/i260056a021

Cited by 75 publications

(38 citation statements)

References 6 publications

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“…= (uL/zt)(Cin -Cout)/C^(9) If the concentration at the outlet, Cout, is greater than Cin/2, the difference between (ka)s from Eq. (8) and that from Eq. (9) is within 4%.…”

Section: Evaluation Of Mass Transfer Coefficientsmentioning

confidence: 99%

“…(4) as (ka)s=uL£/zt=(uL/zt) ln (Cin/Cout); 0<t<ts (8) On the other hand, when resin particles are packed in the shallow bed, the average concentration Cav= (Cin+Cout)/2 may be used in mass balance equations, and then the coefficient (ka)s can be given as (ka). = (uL/zt)(Cin -Cout)/C^(9) If the concentration at the outlet, Cout, is greater than Cin/2, the difference between (ka)s from Eq.…”

Section: Evaluation Of Mass Transfer Coefficientsmentioning

confidence: 99%

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Liquid-solid mass transfer in gas-liquid cocurrent flows through beds of small packings.

Yoshikawa

Iwai

Goto

et al. 1981

J. Chem. Eng. Japan

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to be zero d at Hin Fig. 2, waiting time for homogeneousnucleation surface energy Literature Cited [sec] [sec] [erg/ cm2] 1) Harano, Y., K. Nakano, M. Saito and T. Imoto: /. Chem. Eng. Japan, 9, 373 (1976).2) Harano, Y. andK. Oota: ibid., ll, 119 (1978 Rates of mass transfer from liquid phase to small particles (average diameter, 0.46-1.3 mm) were measured by use of ion-exchange reaction followed by instantaneous irreversible reaction at 30°C. Nitrogen gas and dilute aqueous solution of sodium hydroxide were fed into a shallow bed packed with a strong cation exchange resin. Volumetric mass transfer coefficients for gasliquid cocurrent up flow and downflow were almost identical at the same gas and liquid flowrates but became somewhat greater than those in liquid-full single phase flow. A unified correlation could be derived by arranging experimental data for three arrangements : liquid-full single phase flow, gas-liquid cocurrent up flow and down flow (trickle-bed).

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“…= (uL/zt)(Cin -Cout)/C^(9) If the concentration at the outlet, Cout, is greater than Cin/2, the difference between (ka)s from Eq. (8) and that from Eq. (9) is within 4%.…”

Section: Evaluation Of Mass Transfer Coefficientsmentioning

confidence: 99%

Section: Evaluation Of Mass Transfer Coefficientsmentioning

confidence: 99%

Liquid-solid mass transfer in gas-liquid cocurrent flows through beds of small packings.

Yoshikawa

Iwai

Goto

et al. 1981

J. Chem. Eng. Japan

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“…Firstly, the new reactor separates crystal nucleation and growth steps by the two-stage reaction chamber (nucleation stage occurs mainly in reaction chamber I, and growth stage mainly performed in the reaction chamber II). Secondly, N 2 from the feeding hole (1) helps to form a great deal of gas eddy which further promotes mass transfer [14,15,21] and uniform particles [22]. Finally, the protective agent, polyethylene glycol 2000, prevents Mg-Al-CO 3 LDH nanosheets from congregating in the aging stage [23][24][25].…”

Section: Resultsmentioning

confidence: 99%

Kilogram-scale synthesis of Mg–Al–CO3 LDHs nanosheets using a new two-stage reactor

Liu

Que

Yang³

et al. 2010

Powder Technology

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“…On differentiation, axial profile of solid phase concentration may be given by, The liquid to biofilm mass transfer coefficient k s a s can be determined from the relation given by Goto and Smith [22] and Goto et al [23]. It may be mentioned that although the gas film and liquid film resistances to mass transfer are neglected, the diffusional resistance in solid biofilm cannot be neglected and thus a suitable effectiveness factors appears in Eq.…”

Section: Theoretical Analysismentioning

confidence: 99%

Experiments and three phase modelling of a biofilter for the removal of toluene and trichloroethylene

Das

Chowdhury

Bhattacharya

2010

Bioprocess Biosyst Eng

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Volatile organic compounds, namely, toluene, trichloroethylene, styrene, etc., disposed off by electronics and polymer industries, are very harmful. The treatment of VOC laden air through biochemical route is one of the potential options for reduction of their concentration in parts per million or parts per billion level. Under the present investigation, a 0.05-m diameter and 0.58-m high trickle bed biofilter has been studied for the removal of VOCs namely toluene and trichloroethylene from a simulated air-VOC mixture using pure strain of Pseudomonas putida (NCIM2650) in immobilized form. Inlet concentrations of VOCs have been varied in two ranges, the lower being 0.20-2.00 g/m(3) and higher being 10-20 g/m(3), respectively. The Monod type rate kinetics of removal of VOCs has been determined. A three-phase deterministic mathematical model has been developed taking the simultaneous reaction kinetics and interphase (gas to liquid to biofilm) mass transfer rate of VOCs into consideration. Experimentally determined kinetic parameters and mass transfer coefficients calculated using standard correlations have been used. Concentrations have been simulated for all the three phases. Simulated results based on the model have been compared with the experimental ones for both gas and liquid phases satisfactorily. The mathematical model validated through the successful comparison with experimental data may be utilized for the prediction of performance of biofilters undergoing removal of different VOCs in any further investigation and may be utilized for the scale-up of the system to industrial scale.

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Mass Transfer in Packed Beds with Two-Phase Flow

Cited by 75 publications

References 6 publications

Liquid-solid mass transfer in gas-liquid cocurrent flows through beds of small packings.

Liquid-solid mass transfer in gas-liquid cocurrent flows through beds of small packings.

Kilogram-scale synthesis of Mg–Al–CO3 LDHs nanosheets using a new two-stage reactor

Experiments and three phase modelling of a biofilter for the removal of toluene and trichloroethylene

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