Gas hold-up in a bi-dimensional three-phase spouted bed

Anabtawi, Mohammed Zohdi; Uysal, Bekir Zühtü

doi:10.1016/0300-9467(92)80021-2

Cited by 7 publications

(4 citation statements)

References 17 publications

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“…The behavior of the gas-liquid spouted bed for viscous and non-viscous fluids was studied and it was found that there is some similarity between the hydrodynamics of spouted beds and bubble columns [27,30]. However, only a few attempts have been made to extend this similarity to highly viscous nonNewtonian fluids.…”

Section: Resultsmentioning

confidence: 93%

“…The behavior of a gas-liquid spouted bed for Newtonian non-viscous fluids was studied by the same author [30] and it was reported that there is some similarity in the hydrodynamics between spouted beds and bubble columns. In a further study Anabtawi [27] studied the behavior of gas-liquid spouted beds for Newtonian viscous fluids and reached a similar qualitative conclusion.…”

Section: Effect Of Effective Liquid Viscositymentioning

confidence: 98%

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Volumetric Mass Transfer Coefficient in non‐Newtonian Fluids in Spout Fluid Beds

Anabtawi

Hilal²,

Muftah³

2003

Chem Eng & Technol

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The volumetric liquid-phase mass transfer coefficient, k L a, was determined by absorption of oxygen in air using six different carboxy-methyl cellulose (CMC) solutions with different rheological values in three phase spout-fluid beds operated continuously with respect to both gas and liquid. Three cylindrical columns of 7.4 cm, 11.4 cm, and 14.4 cm diameters were used. Gas velocity was varied between 0.00154±0.00563 m/s, liquid velocity between 0.0116±0.0387 m/s, surface tension between 0.00416±0.0189 N/m, static bed height between 6.0±10.8 cm, and spherical glass particles of 1.75 mm diameter were used as packing material. A single nozzle sparger of 1.0 cm diameter was used in the spouting line. The volumetric mass transfer coefficient was found to increase with gas velocity, liquid velocity, and static bed height and to decrease with the increase of the effective liquid viscosity of the CMC solution. A dimensionless correlation was developed and compared with those listed in the literature.

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Section: Resultsmentioning

confidence: 93%

Section: Effect Of Effective Liquid Viscositymentioning

confidence: 98%

Volumetric Mass Transfer Coefficient in non‐Newtonian Fluids in Spout Fluid Beds

Anabtawi

Hilal²,

Muftah³

2003

Chem Eng & Technol

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“…Spout-fluidized beds are widely used in chemical industry contactors, absorbers, and reactors (Anabtawi et al, 1991(Anabtawi et al, , 2003Anabtawi & Ebrahim, 1996;Anabtawi & Uysal, 1992;Anabtawi, 1993Anabtawi, , 1995. The present study is closely related to an experimental study on the determination of the volumetric liquid-phase mass transfer coefficient, k L a, in nonNewtonian fluids in spouted beds at high Reynolds numbers (Anabtawi et al, 2003) and together with the results of those studies will provide basic information for design of three-phase spout-fluid beds.…”

mentioning

confidence: 92%

Non-Newtonian Fluids in Spout-Fluid Beds: Mass Transfer Coefficient at Low Reynolds Numbers

Anabtawi

Hilal²,

Muftah³

et al. 2004

Particulate Science and Technology

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Following on from the work of Anabtawi et al. (2003), this study examined how the volumetric liquid-phase mass transfer coefficient, k L a, of oxygen in air in threephase spout-fluid beds was affected by varying the system parameters of bed height, bed diameter, gas velocity, and liquid velocity. The liquid used was 0.1% CMC solution, displaying a pseudo-plastic rheology, with 1.75 mm glass spheres as packing. The values of the Sherwood number were lower than in previous studies (Anabtawi et al., 2003), in the range 9,000-186,000. Gas velocity had a similar effect on k L a as in a bubble column, with results also giving good agreement with previous work on two-phase and three-phase spouted bed systems. The correlation obtained for the effect of liquid velocity on k L a compared well with that of Schumpe et al. (1989). An increase in the height of packing increased k L a to the power of 0.319, with an increase in column diameter also causing an increase in k L a, which is in agreement with the results of Akita and Yoshida (1973).

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“…Employing a two-dimensional column and 1 mm sand particles, Anabtawi and Uysal [14] have shown that the gas holdup increases with the gas flow rate but decreases with the solid concentration in the range from 5-20 %. Similar findings have also been reported by other investigators [2,9,24].…”

Section: Introductionmentioning

confidence: 97%

A Simple Approach to Measuring the Gas Phase Heat and Mass Transfer Coefficients in a Bubble Column

Daous

Al-Zahrani

2006

Chem Eng & Technol

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A simple experimental approach was developed to measure the gas phase volumetric heat and mass transfer coefficients in a bubble column and a slurry bubble column employing a single gas nozzle. The experimental technique was based on a transfer model that simulates humidification and direct contact evaporation models in the case of a gas bubble rising in a liquid of uniform temperature. The temperature and relative humidity of the inlet and outlet gas in the column are the only measurements required in this technique. Experiments were carried out in a 0.15 m inner diameter column using water as the liquid phase, air as the gas phase, and cation resins of 0.1 mm diameter and a specific gravity of 1.2, as the solid phase. The results showed that, when using solid concentrations in the range of 7-10 wt %, both the volumetric gas-phase heat and mass transfer coefficients increased with an increase in the gas superficial velocity and were further enhanced by increasing the solid load after a certain minimum superficial velocity had been reached in the column (0.044 m/s in the system used). Increasing the solid load beyond 10 wt %, did not contribute to a further increase in these coefficients. Furthermore, the gas holdup in the column increased with the superficial gas velocity and was further enhanced when the solid-phase load was in the range of 7-10 wt %. These observations agree well with previously reported findings by other investigators.

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Gas hold-up in a bi-dimensional three-phase spouted bed

Cited by 7 publications

References 17 publications

Volumetric Mass Transfer Coefficient in non‐Newtonian Fluids in Spout Fluid Beds

Volumetric Mass Transfer Coefficient in non‐Newtonian Fluids in Spout Fluid Beds

Non-Newtonian Fluids in Spout-Fluid Beds: Mass Transfer Coefficient at Low Reynolds Numbers

A Simple Approach to Measuring the Gas Phase Heat and Mass Transfer Coefficients in a Bubble Column

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