Modeling of Two-Phase Slug Flow

Fabre, J.; Liné, Alain

doi:10.1146/annurev.fl.24.010192.000321

Cited by 297 publications

(101 citation statements)

References 64 publications

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“…At the interface between the phases, the mixture properties are determined based on the volume fraction weighted average, and the density and viscosity can be expressed as: (6) where, the phases are represented by the subscripts 1 and 2 and if the volume fraction of the phase 2 is known, the  and  in each cell can be determined.…”

Section: Computational Domainmentioning

confidence: 99%

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Comparison of experimental and Computational Fluid Dynamics (CFD) studies of slug flow in a vertical riser

Abdulkadir

Hernández-Pérez

et al. 2015

Experimental Thermal and Fluid Science

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Section: Computational Domainmentioning

confidence: 99%

“…The important question of when and how these slugs are formed has received much attention from research workers: [1][2][3][4][5] among others. A critical review of this topic is given by Fabre and Line [6]. However, there remains much to be investigated and understand about that flow pattern.…”

Section: Introductionmentioning

confidence: 99%

Comparison of experimental and Computational Fluid Dynamics (CFD) studies of slug flow in a vertical riser

Abdulkadir

Hernández-Pérez

et al. 2015

Experimental Thermal and Fluid Science

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“…Theoretical predictions for F r exist in the range 0.328 − 0.369 [3,2,15,22,25] with Dumitrescu's 0.351 being regarded as the most accurate [4]. The stability of large diameter bubbles is less well understood [5,1,12,14].…”

Section: Introductionmentioning

confidence: 99%

The existence and behaviour of large diameter Taylor bubbles

Pringle

Ambrose

Azzopardi

et al. 2015

International Journal of Multiphase Flow

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Large tube filling bubbles rising up through quiescent fluid in a vertical tube are commonly known as Taylor bubbles. Their apparent simplicity of form and behaviour has led to them being viewed and modelled as a paradigm for both large bubble dynamics, where there is no continuous gas flow, and slug flow for the case of continuous gas flow. Central to this approach is the question: what diameter tubes support stable Taylor bubbles? In this paper we examine the case of low viscosity Taylor bubbles through experiments and theory and show that they exist in much wider diameter tubes than had previously been reported. In order for the bubbles to be stable a settling period is required to allow the column to sufficiently quiesce. This settling period is compared favourably with the classical stability analysis of Batchelor (1987). We also observe such bubbles rising in an oscillatory manner if the gas input is abruptly curtailed. The oscillations match theoretical predictions well.

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“…We do not make this assumption, hence our break with convention. Much of the previous research into the behaviour of Taylor bubbles has been motivated by their importance in industrial and engineering settings, particularly as components of two-phase 'slug flow' (Nicklin et al 1962, Fabré & Liné 1992. This work has included theoretical studies (Dumitrescu 1943;Davies & Taylor 1950;Goldsmith & Mason 1962;Brown 1965;Batchelor 1967), experimental studies (Davies & Taylor 1950;Goldsmith & Mason 1962;White & Beardmore 1962;Campos & Guedes de Carvalho 1988;Viana et al 2003;Nogueira et al 2006) and numerical studies (Taha & Cui 2006;Zheng et al 2007;Feng 2008;Kang et al 2010).…”

Section: Introductionmentioning

confidence: 99%

The thickness of the falling film of liquid around a Taylor bubble

et al. 2011

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We present the results of laboratory experiments that quantify the physical controls on the thickness of the falling film of liquid around a Taylor bubble, when liquid-gas interfacial tension can be neglected. We find that the dimensionless film thickness l (the ratio of the film thickness to the pipe radius) is a function only of the dimensionless parameter N f = r gD 3 /m, where r is the liquid density, g the gravitational acceleration, D the pipe diameter and m the dynamic viscosity of the liquid. For N f 10, the dimensionless film thickness is independent of N f with value l ≈ 0.33; in the interval 10 N f 10 4 , l decreases with increasing N f ; for N f 10 4 film thickness is, again, independent of N f with value l ≈ 0.08. We synthesize existing models for films falling down a plane surface and around a Taylor bubble, and develop a theoretical model for film thickness that encompasses the viscous, inertial and turbulent regimes. Based on our data, we also propose a single empirical correlation for l (N f ), which is valid in the range 10 −1 < N f < 10 5 . Finally, we consider the thickness of the falling film when interfacial tension cannot be neglected, and find that film thickness decreases as interfacial tension becomes more important.

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Modeling of Two-Phase Slug Flow

Cited by 297 publications

References 64 publications

Comparison of experimental and Computational Fluid Dynamics (CFD) studies of slug flow in a vertical riser

Comparison of experimental and Computational Fluid Dynamics (CFD) studies of slug flow in a vertical riser

The existence and behaviour of large diameter Taylor bubbles

The thickness of the falling film of liquid around a Taylor bubble

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