Three‐dimensional simulation of bubble column flows with bubble coalescence and breakup

Chen, P.; Duduković, Milorad P.; Sanyal, Jay

doi:10.1002/aic.10381

Cited by 181 publications

(119 citation statements)

References 41 publications

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“…For further reference, Strasser [18] offers a study of turbulence interactions between continuous and dispersed phases. Commercial implementations of bubble population balance models for CFX and FLUENT are discussed in Olmos et al [14] and Chen et al [15], respectively; however, application to pX oxidation proved ineffective at matching experimental hold-up and velocity distributions and pressure fluctuations. Therefore, the authors have developed a novel population balance method for realistic industrial pX oxidation conditions.…”

Section: Drag Bubble Size and Other Forcesmentioning

confidence: 99%

Commercial scale slurry bubble column reactor optimization

Strasser¹,

Wonders²

2008

Advances in Fluid Mechanics VII

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An in-depth numerical study has been carried out to investigate a high-pressure commercial scale (2-8 meter diameter) slurry bubble column reactor (SBCR). Typical superficial gas velocities are in the range of 0.5-3 m/s, and overall vapor hold-ups are in the range of 0.45-0.85. The study revealed that steady compartmental reaction models do not match plant data when reaction time constants are very fast. Also, off-the-shelf commercial CFD codes do not produce useful information about a reactive column of this scale and aeration without tuning to reconcile with vapor hold-up and reactant operating data "anchors" from in-plant units. Important measures include both transient and time-averaged profiles, integrals, and extrema of vapor hold-up and reactants. The present study proposes reactor designs that improve productivity and product quality.

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Section: Drag Bubble Size and Other Forcesmentioning

confidence: 99%

Commercial scale slurry bubble column reactor optimization

Strasser¹,

Wonders²

2008

Advances in Fluid Mechanics VII

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“…(Rande 12) ). For steady-state incompressible flow in the absence of mass transfer, external body forces such as the centrifugal forces, and virtual mass effects (which assume significance only when high-frequency fluctuations of the relative velocity are predominant; Drew 32) ; Chen et al 14) ), the momentum conservation equation simplifies to:…”

Section: Conservation Of Momentummentioning

confidence: 99%

“…Multi-fluid Flow It is well known that in dispersed multiphase flows, inter-phase forces play a significant role in determining the local phase distribution (Jakobsen et 14) ; Tabib et al 15) ). Some of the typical interface forces encountered in multi-fluid dispersion are gravitational and buoyancy force, drag force, lift force, virtual/added mass force, Basset force, wall lubrication force and turbulent dispersion.…”

Section: Treatment Of Inter-phase Forces In Dispersedmentioning

confidence: 99%

Numerical Simulation of Oil Dispersions in Vertical Pipe Flow

Parvini¹,

Dabir²,

Mohtashami³

2010

J. Jpn. Petrol. Inst.

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Immiscible liquid dispersions are widely used in chemical process, petroleum industries, polymerization, heterogeneous chemical synthesis, etc. In most of these chemical processes, the rate of inter-phase heat and mass transfer is known to strongly affect the overall performance and depends on the interfacial contact area between the phases. This study at CFD simulations of immiscible liquid dispersion has been performed on a vertical pipe. With specific reference to dispersed liquid-liquid flows, it was seen that the two-fluid approach (Eulerian-Eulerian approach) was extensively used for multiphase modeling, especially when detailed predictions are desirable over a range of holdups in exchange for a reasonable amount of computation power. The results of CFD predictions for water as a continuous and kerosene as a dispersed phase have been compared with the experiments of Farrar and Bruun and Al-Deen and Bruun. These simulations have also been done to understand the effect of various significant forces in turbulent liquid dispersions (drag, lift, turbulent dispersion and added mass). Several expressions for these forces were tested in order to choose the best combination. Further, the problem has been simulated using two different turbulence models. It has been found that lift force is more important than turbulent dispersion and added mass. Inter-phase closure guidelines for liquid-liquid bubbly flows were developed based on simulation results that yielded the best agreement with experimental data.

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“…These will be discussed briefly below in order of increasing complexity. Mixture models (see, for instance Chen et al [2]) are those in which the gas and all particle size classes are combined into a single equivalent fluid. Particulate mixture models (see, for instance, Chen et al [2]) are created by combining all particulate size classes into a single equivalent fluid while allowing the gas to retain a separate identity.…”

Section: Introductionmentioning

confidence: 99%

“…Mixture models (see, for instance Chen et al [2]) are those in which the gas and all particle size classes are combined into a single equivalent fluid. Particulate mixture models (see, for instance, Chen et al [2]) are created by combining all particulate size classes into a single equivalent fluid while allowing the gas to retain a separate identity. Multiple size group (MUSIG) models (see, for instance, Ghaniyari-Benis et al [3]) group the size classes into a smaller number of equivalent fluids which, along with the gas, have separate identities.…”

Section: Introductionmentioning

confidence: 99%

Eulerian Multiphase Population Balance Model of Atomizing, Swirling Flows

Rayapati

Panchagnula

Peddieson

et al. 2011

International Journal of Spray and Combustion Dynamics

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An Eulerian/Eulerian multiphase flow model coupled with a population balance model is used as the basis for numerical simulation of atomization in swirling flows. The objective of this exercise is to develop a methodology capable of predicting the local point-wise drop size distribution in a spray, such as would be measured by the Phase Doppler Particle Analyzer (PDA). Model predictions are compared to experimental measurements of particle size distributions in an airblast atomizer spray to demonstrate good qualitative and quantitative agreement. It is observed that the dependence of velocity on drop size inherent in a multiphase description of the drop cloud appears necessary to capture some features of the experimental data. Using this model, we demonstrate the relative contributions of secondary atomization and transport to the variation observed in the downstream spray drop size distribution.

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Three‐dimensional simulation of bubble column flows with bubble coalescence and breakup

Cited by 181 publications

References 41 publications

Commercial scale slurry bubble column reactor optimization

Commercial scale slurry bubble column reactor optimization

Numerical Simulation of Oil Dispersions in Vertical Pipe Flow

Eulerian Multiphase Population Balance Model of Atomizing, Swirling Flows

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