Prediction of gas holdup in a three-phase fluidized bed from bed pressure drop measurement

Jena, Hara Mohan; Roy, Gour Gopal; Meikap, B.C.

doi:10.1016/j.cherd.2008.05.007

Cited by 32 publications

(17 citation statements)

References 22 publications

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“…1). Using this map, 280 gas holdup measurements reported in seven different studies [18,20,22,23,29,31,32] are 75 classified as corresponding to the dispersed flow regime. These data, notably include…”

Section: Methodsmentioning

confidence: 99%

“…More recent work in this area [16,17,[20][21][22][23][24][25] 30 has focused on correlations of gas hold-up as a function of either individual parameters (superficial gas/liquid velocities, liquid properties, particle diameter, column diameter, etc.) or combinations of them in the form of dimensionless groups.…”

Section: Accepted Manuscriptmentioning

confidence: 99%

“…Functional forms of this kind have been previously fitted to limited experimental data [16,17,[20][21][22][23][24].…”

Section: Accepted Manuscriptmentioning

confidence: 99%

“…Two models, one without γ b (Eqs. (23) and (24)) and one containing all the dimensionless groups (Eqs. (25) and (26)) were developed and are 175 shown in Table (2).…”

mentioning

confidence: 99%

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A meta-analysis of empirical correlations for average gas hold-up in three-phase fluidized beds

Mowla¹,

Treeratanaphitak²,

Budman³

et al. 2016

Powder Technology

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Section: Methodsmentioning

confidence: 99%

Section: Accepted Manuscriptmentioning

confidence: 99%

See 2 more Smart Citations

A meta-analysis of empirical correlations for average gas hold-up in three-phase fluidized beds

Mowla¹,

Treeratanaphitak²,

Budman³

et al. 2016

Powder Technology

View full text Add to dashboard Cite

“…In three phase fluidization, the particles are fluidized by the co-current flow of liquid and gas [2][3][4][5][6] or immiscible liquid-liquid phase. The gas or immiscible liquid form discrete bubbles or droplets phase and the liquid a continuous phase containing the solid particles [7].…”

Section: Introductionmentioning

confidence: 99%

Hydrodynamic Characteristic of Three-Phase (Liquid-Liquid-Solid) Fluidized Beds

Mohammed¹,

Sulaymon²,

Abdul-Rahmun³

2014

J Chem Eng Process Technol

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This work aims to study the hydrodynamic characteristic of three-phase fluidized beds (water, kerosene, spherical plastic or cylindrical PVC particles). The hydrodynamic parameters were investigated ( phase hold-up, droplet diameter, droplet rising velocity, particle types and sizes, holes diameter of the liquid distributor, continuous and dispersed phase velocities. The experimental work was carried out using QVF glass 0.106 m I.D. and 2 m height. Three distributors with whole diameters (2.5, 5, 7 mm) were used. Plastic particles with diameters (8, 15 mm) and PVC particles (3.34 mm) were used as a solid phase. Two methods (quick, closing valves and pressure drop method) were used to measure the continuous, dispersed and solid hold-up. A cine camera was used to measure the droplet diameter and rising velocity. It was found that the droplet diameter and rising velocity increase with increasing superficial continuous and dispersed velocities. A relationships between the dispersed phase hold-up, droplet diameter and rising velocity with continuous and dispersed superficial velocities respectively were obtained Dimensionless correlation for the prediction of the droplet rising velocity was developed. Keywords:

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Modeling of Slurry Bubble‐Column Reactors with Emphasis on the Importance of Bubble Size Estimation

2021

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A mathematical model entitled varying‐bubble model (V‐BM) was adapted to simulate a slurry bubble‐column reactor, operating in a churn‐turbulent regime, based on an axial‐dispersion model. This model was theoretically able to estimate the size of forming bubbles at the sparger, variations of each chemical species and catalyst concentration, pressure drop in both gas and liquid phases, change in size and rising velocity of bubbles, as well as gas holdup and specific gas‐liquid interfacial area along the reactor axis. A comparison between the V‐BM and single‐bubble model (S‐BM) indicates that the V‐BM is better compatible with the experimental data. The results demonstrate that the contribution of mass transfer is much more than the pressure drop in increasing the size of the bubble along the reactor.

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Prediction of gas holdup in a three-phase fluidized bed from bed pressure drop measurement

Cited by 32 publications

References 22 publications

A meta-analysis of empirical correlations for average gas hold-up in three-phase fluidized beds

A meta-analysis of empirical correlations for average gas hold-up in three-phase fluidized beds

Hydrodynamic Characteristic of Three-Phase (Liquid-Liquid-Solid) Fluidized Beds

Modeling of Slurry Bubble‐Column Reactors with Emphasis on the Importance of Bubble Size Estimation

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