The virtual mass and lift force on a sphere in rotating and straining inviscid flow

Drew, Donald A.; Lahey, R.T.

doi:10.1016/0301-9322(87)90011-5

Cited by 394 publications

(125 citation statements)

References 2 publications

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“…Turbulent dispersion was found to be significant at low dispersed phase holdups but is practically negligible at dispersed phase ratio larger than 25%. Similar conclusions apply for the dispersion model proposed by Lopez de Bertodano 32) . (5) At lower holdup range (≤5%) positive lift coefficient with a turbulent dispersion constant CTD of 0.9 base on Favre 41) yields a better match with the data whereas in the case of higher holdups a constant lift coefficient of -0.003 without the turbulent dispersion produces a good agreement with the experimental data.…”

Section: Discussionsupporting

confidence: 82%

“…(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%

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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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Section: Discussionsupporting

confidence: 82%

Section: Conservation Of Momentummentioning

confidence: 99%

Numerical Simulation of Oil Dispersions in Vertical Pipe Flow

Parvini¹,

Dabir²,

Mohtashami³

2010

J. Jpn. Petrol. Inst.

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“…The present work concentrates on bubbly flow regime with 2.88 mm small spherical bubbles, where only positive lift force coefficient is sufficient which can be in the range of 0.1 to 0.5. Drew and Lahey 25) proposed CL = 0.5 based on objectivity arguments. So CL is set to 0.5.…”

Section: Interfacial Forcesmentioning

confidence: 99%

Modeling of Transient Two-Phase Flow in a Continuous Casting Mold Using Euler-Euler Large Eddy Simulation Scheme

Liu

Jiang

et al. 2013

ISIJ Int.

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Euler-Euler Large Eddy Simulation (EELES) scheme has been developed to simulate the two-phase flow of argon gas and molten steel in slab continuous casting mold. The Euler-Euler approach is used to describe the equations of motion of the two-phase flow. The drag force, lift force and virtual mass force are incorporated in this model. Both turbulence of argon gas and molten steel are simulated using large eddy simulation (LES). Simulation results agree acceptably well with the water model experimental measurements of instantaneous flow structures. The flow pattern in the lower recirculation zone is expected to be asymmetrical between the left and right sides of the mold. The flow pattern is changeover; the direction of flow deviation is different from time to time. The time intervals for changeover appeared to vary randomly. The long-term asymmetry in the lower roll is due to the turbulent nature instead of the variation of other operating parameters. The turbulent flow in the mold includes multiple vortices. Those vortexes make the flow field to be more complex. Two typical transient flow structures, consisting of clockwise or counterclockwise rotational direction vortices, are found in the upper roll.

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“…Then, it follows from equation (7-4) that We shall observe that for range of parameters considered, the roots of the quadratic equation (6)(7)(8)(9)(10)(11)(12)(13)(14)(15)(16)(17)(18)(19)(20)(21)(22) always have negative real parts. We also observe that the constraint _:quation (6)(7)(8)(9)(10)(11)(12)(13)(14)(15)(16)(17)(18)(19) is always satisfied for the range of parameters.…”

Section: I_1mentioning

confidence: 97%

“…where the C's in equations (6)(7)(8)(9)(10)(11)(12)(13)(14)(15)(16) are given by, (6)(7)(8)(9)(10)(11)(12)(13)(14)(15)(16)(17)(18) where, A caref_al investigation in these equations (6-21)- (6)(7)(8)(9)(10)(11)(12)(13)(14)(15)(16)(17)(18)(19)(20)(21)(22) Anderson and Jackson, we use a procedure similar to theirs to obtain a quadratic equation in the growth number. We set parameters 0_1°,0_2°and 0_4°to be zero.…”

Section: I_1mentioning

confidence: 99%

Stability of flows in fluidized beds

Rajagopal¹

1992

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DE92 017669 DISCLAIMERThis report was prepared as an account of work sponsored by an agency of the United Stat_,s Government.Neither the Unit¢_t States Government nor any agency th,;r¢of, nor any of their cmp[oy_s, makes any warrant)', express or implied, or assum¢:s any legal liability or r_sponsi-bility for the accuracy, completeness, or usef'ulne.ss of' any information, apparatus, product, or process disclo_d, or rcpr¢_nts that ks use would not infringe privately own_ rights. Reference: herein to any specific _mmercial product, proc,css, or service by trade name, trademark, rna)_ufacturer, or otherwise does not r_e,_saril), constitute or imply its endorsement, r¢com-mc)_dation, or favoring by th.¢ United States Government or any agency thereof. The q¢ws an, d opinions of authors exprcss_ herein do not r_c_,_.ssarily state or rcfl_t tho_ of the United States Oov©rnmcnt or any agency thc,rc_f.

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The virtual mass and lift force on a sphere in rotating and straining inviscid flow

Cited by 394 publications

References 2 publications

Numerical Simulation of Oil Dispersions in Vertical Pipe Flow

Numerical Simulation of Oil Dispersions in Vertical Pipe Flow

Modeling of Transient Two-Phase Flow in a Continuous Casting Mold Using Euler-Euler Large Eddy Simulation Scheme

Stability of flows in fluidized beds

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