Dynamic simulation of gas-liquid two-phase flow: effect of column aspect ratio on the flow structure

Delnoij, E; Kuipers, J.A.M.; Swaaij, van Wpm Wim

doi:10.1016/s0009-2509(97)00222-4

Cited by 134 publications

(111 citation statements)

References 12 publications

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“…In the literature, there is no universal agreement that indicates that the CFD models are capable of predicting the experimental results of multiphase flow regimes [10]. For instance, Delnoij et al [11,12,13] have used Eulerian-Lagrangian approach in 119-2 a flat bubble column to model two-phase flow by using laminar flow model, as well as drag, lift, virtual-mass, and hydrodynamic-interaction forces [14]. Sokolichin and Eigenberger [15] have obtained same results by using finer grid size and neglecting the effects of virtual-mass and lift forces, as well as bubble-bubble interactions.…”

Section: Introductionmentioning

confidence: 99%

CFD Analysis of Temperature Distributions in a Slurry Bubble Column with Direct Contact Heat Transfer

Abdulrahman

2016

International Conference of Fluid Flow, Heat and Mass Transfer

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-Slurry bubble column reactors have different applications in the industry due to their advantages. In spite of the simple construction of the slurry bubble column reactors, their scale up analyses are complex due to the effect of various parameters on the hydrodynamic and heat transfer rates in these reactors. Direct-contact heat transfer in slurry bubble columns involves a complex phenomenon of bubble formation and gas motion through the slurry. In this paper, Computational Fluid Dynamics (CFD) simulations are used to investigate the temperature distributions for a direct contact heat transfer in a helium-water-alumina slurry bubble column, where helium gas is injected at 90 o C through a slurry of water at 22 o C and alumina solid particles. This paper studies the effects of superficial gas velocity, static liquid height, and solid particles concentration, on the average temperature of the slurry. In this study, it is assumed that the slurry inside the slurry bubble column is perfectly mixed, and the approaches used to model the slurry bubble column by CFD is 2D plane. From the CFD results, it is found that the average slurry temperature increases by increasing the superficial gas velocity and decreases by increasing the static liquid height and/or the solid concentration at any given superficial gas velocity, but the decrease with the solid concentration is negligible. The results of CFD simulations were compared with experimental data from the literature and show that the profiles of the slurry temperature calculated from CFD models, generally under-predicts the experimental data. The CFD model correctly predicts the experimental effects of static liquid height and solid concentration on average slurry temperature.

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Section: Introductionmentioning

confidence: 99%

CFD Analysis of Temperature Distributions in a Slurry Bubble Column with Direct Contact Heat Transfer

Abdulrahman

2016

International Conference of Fluid Flow, Heat and Mass Transfer

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“…15,16 There are numerous studies that have applied either the Euler-Euler or the Euler-Lagrange approach within 2D or 3D two-fluid turbulent models. [17][18][19][20][21][22][23][24][25][26][27][28][29][30][31][32] Large-eddy simulation (LES) studies have also been reported in the literature. 33,34 Additionally, several researchers have reported on the prediction of flow-regime transitions using either numerical simulations 35 or linear stability analysis of various model equations.…”

Section: Introductionmentioning

confidence: 99%

Validation of Two-Fluid Simulations of a Pseudo-Two-Dimensional Bubble Column with Uniform and Nonuniform Aeration

Monahan

Fox

2009

Ind. Eng. Chem. Res.

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The multiphase flow simulated in this work corresponds to the pseudo-2D bubble-column experiments at Delft University of Technology (Harteveld et al. Can. J. Chem. Eng. 2003, 81, 389-394). As in the work of Monahan and Fox (AIChE J. 2007, 53, 9-18), the complete set of interphase force models includes drag, added-mass, lift, rotation, and strain. The simulation results are presented in the form of comparisons with the experimental data for the time-averaged gas holdup and the instantaneous and time-averaged air and liquid velocity fields. Overall, the qualitative and quantitative comparisons between experiments and simulations are satisfactory for both uniform and nonuniform aeration. In particular, the model predicts the flow patterns observed in the experiments, but in some cases at slightly different values of the amount of aeration. In the latter cases, it is shown that changing the model parameters does not improve the agreement with experiments. However, changing the liquid-velocity boundary condition from zero stress to zero slip leads to a small improvement. The multiphase flow simulated in this work corresponds to the pseudo-2D bubble-column experiments at Delft University of Technology (Harteveld et al. Can. J. Chem. Eng. 2003, 81, 389-394). As in the work of Monahan and Fox (AIChE J. 2007, 53, 9-18), the complete set of interphase force models includes drag, added-mass, lift, rotation, and strain. The simulation results are presented in the form of comparisons with the experimental data for the time-averaged gas holdup and the instantaneous and time-averaged air and liquid velocity fields. Overall, the qualitative and quantitative comparisons between experiments and simulations are satisfactory for both uniform and nonuniform aeration. In particular, the model predicts the flow patterns observed in the experiments, but in some cases at slightly different values of the amount of aeration. In the latter cases, it is shown that changing the model parameters does not improve the agreement with experiments. However, changing the liquid-velocity boundary condition from zero stress to zero slip leads to a small improvement. Disciplines Biological Engineering | Chemical Engineering

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“…Numerical simulations of bubble columns either employing Eulerian-Eulerian models [ [1][2][3][4][5], Euleri an-Lagrang ian mode ls [6][7][8] , or Volume of Fluid (VOF) [9] methods were surveyed. The Eulerian-Eulerian model treats di spersed (gas bubb les) and continuous (liquid) phases as interpenetrating continua, and describes the motion for gas and liquid phases Ill an Eulenan frame of reference.…”

Section: Introductionmentioning

confidence: 99%

“…[6][7][8] applied an ulen an-LagrangJan method to imula~e detai led bubble-bub ble interacti ons along With interfacial force in the laminar bubb ly flow regJme. Lm et at.…”

Section: Introductionmentioning

confidence: 99%

Numerical Simulations of Gas-Liquid Flow Dynamics in Bubble Columns

2006

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There is great potential for using computational fluid dynamics (CFD) as a tool in scale-up and design of bubble columns. Full-scale experimentation in bubble columns is expensive and CFD is an alternative approach to study bubble column hydrodynamics. However, CFD can be computationally intensive as a predictive tool for a full three-dimensional geometry. In this paper, a 0.2 m diameter semi-batch bubble column is numerically simulated and the results are compared to experimental measurements performed by Rampure et al. [1]. The objectives are to examine and determine an appropriate set of numerical parameters and to determine if two-dimensional simulations are able to accurately predict observed bubble phenomena so that the computational cost can be reduced. A two-fluid Eulerian-Eulerian model is employed to represent each phase as interpenetrating continua and the conservation equations for mass and momentum for each phase are ensemble-averaged. Time-averaged gas holdup is mainly examined due to its significant role in gasliquid mass transfer and to compare to available data. Numerical predictions are presented for gas holdup at various axial heights as a function of radial position for a superficial gas velocity of 0.1 m/s. The numerical predictions exhibit the axial development of the gas holdup profile phenomena; that is, the gas holdup at the center of the column increases with increasing axial height. The effects of grid resolution and convergence criteria on the numerical predictions are also demonstrated. However, FD ca n be computationally inten ive a a predict ive too l fo r a full th reedimensional geo metry. In th i paper, a 0.2 m diameter semibatch bubble column is numerica ll y imul ated and the res ults are compared to ex perimental meas urements performed by R ampure et al. [ !] . The objecti ve are to exa mine and determine an appropriate set of numerica l parameters and to determine if two-dimensional simul ations are abl e to accuratel y predtct observed bubble phenomena so that the computational cost can be reduced. A two-fluid Euleri an-Eul eri an model is employed to represent each phase as interpenetrating continua and the conservation equations fo r mass and momentum for each phase are ensemble-averaged. Time-averaged gas holdup ts mamly examined due to its significant role in gas-liquid mass transfer and to compare to available data. Numerical predictions are presented for gas holdup at various ax ial heights as a function of radial position for a superfi cial gas velocity of ~· 1 mls. The numerical predictions exhibit the axial evelopment of the gas holdup profile phenomena · that is the gas h ld ' '. 0 up at the center of the column increases with Increasing axial height. The effects of grid resolution and convergence .t . d en ena on the numerical predictions are also emonstrated.

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Dynamic simulation of gas-liquid two-phase flow: effect of column aspect ratio on the flow structure

Cited by 134 publications

References 12 publications

CFD Analysis of Temperature Distributions in a Slurry Bubble Column with Direct Contact Heat Transfer

CFD Analysis of Temperature Distributions in a Slurry Bubble Column with Direct Contact Heat Transfer

Validation of Two-Fluid Simulations of a Pseudo-Two-Dimensional Bubble Column with Uniform and Nonuniform Aeration

Numerical Simulations of Gas-Liquid Flow Dynamics in Bubble Columns

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