Bubble behavior in gas–liquid–solid three-phase circulating fluidized beds

Wang, Tiefeng; Wang, Jinfu; Wei-guo, Yang; Ye, Jin

doi:10.1016/s1385-8947(01)00129-2

Cited by 36 publications

(38 citation statements)

References 14 publications

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“…The measuring principle was based on the different conductivities of the gas and liquid, which gave different output voltage signals when the probe tip was in contact with different phases. The bubble chord length, rise velocity, size distribution and local gas holdup were obtained from the measured signals by the use of a previously published algorithm [39].…”

Section: Bubble Behavior and Local Gas Holdupmentioning

confidence: 99%

Gas holdup, bubble behavior and mass transfer in a 5m high internal-loop airlift reactor with non-Newtonian fluid

Deng

Wang

Zhang

et al. 2010

Chemical Engineering Journal

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Section: Bubble Behavior and Local Gas Holdupmentioning

confidence: 99%

Gas holdup, bubble behavior and mass transfer in a 5m high internal-loop airlift reactor with non-Newtonian fluid

Deng

Wang

Zhang

et al. 2010

Chemical Engineering Journal

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“…Bubble sizes and their distribution as well as the bubble rise velocity are measured experimentally using a fiber optic probe. The measuring principle is based on the difference in the reflection of light in the gas and liquid [13]. The intensity of the reflected signals is low when the probe is in the liquid-phase, and is high when it is in a bubble.…”

Section: Methodsmentioning

confidence: 99%

“…The Sauter average diameter d 32 , viz. the average diameter related to the volumetric surface, can be statistically calculated [13] from the plentiful bubble signals. With the Sauter average diameter of the whole system and the measured gas hold-up, the contact area of the gas-liquid interface can be obtained.…”

Section: Methodsmentioning

confidence: 99%

Gas–liquid mass transfer in slurry bubble systems

Wei-guo

Wang

Zhao

et al. 2003

Chemical Engineering Journal

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Bubble sizes, interfacial areas and volumetric mass transfer coefficients in a slurry bubble column are measured experimentally and used to determine the two parameters of a mass transfer model. The mass transfer coefficients k L between the gas and liquid phases in a slurry bubble column under different operating conditions are simulated. Calculated results show very good agreement with experimental measurements. The mass transfer model proposed can predict well the mass transfer rate in slurry bubble systems.

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“…where, since the bubble shape is not a regular sphere, the shape factor of the bubble a is introduced; and a=0.8 according to Wang et al (2001). Bubble number density can be defined as:…”

Section: The Interfacial Area Concentration (Iac) Transport Equationmentioning

confidence: 99%

Numerical Prediction of Bubble Size and Interfacial Area Concentration in the Liquid Bath of an Entrained-Flow Coal Gasifier

et al. 2016

Braz. J. Chem. Eng.

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-A CFD-ABND coupling model was used to study the flow characteristic of gas-liquid two-phase flow in the process of gas passing through the liquid bath of a water-coal-slurry entrained-flow gasifier. In this model, an average bubble number density (ABND) approach was employed and merged with the two-fluid model. A two-phase version of the RNG k-ε turbulence model was used for the liquid and gas, respectively. Comparisons of computational results with experimental data are done. The results show that the gas gathers along the outer wall of the cooling pipe and rises. The higher turbulent kinetic energy of gas and liquid, the larger bubble and the higher interfacial area concentration exist mainly near the exit and outer wall of the cooling pipe. The existence of a separator inserter is very helpful to strengthen the turbulence between gas and liquid; this can reduce the bubble diameter and increase the interfacial area effectively.

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Bubble behavior in gas–liquid–solid three-phase circulating fluidized beds

Cited by 36 publications

References 14 publications

Gas holdup, bubble behavior and mass transfer in a 5m high internal-loop airlift reactor with non-Newtonian fluid

Gas holdup, bubble behavior and mass transfer in a 5m high internal-loop airlift reactor with non-Newtonian fluid

Gas–liquid mass transfer in slurry bubble systems

Numerical Prediction of Bubble Size and Interfacial Area Concentration in the Liquid Bath of an Entrained-Flow Coal Gasifier

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