The mechanics of large bubbles rising through extended liquids and through liquids in tubes

Davies, R. M.; TAYLOR, SIR GEOFFREY

doi:10.1016/b978-0-08-092523-3.50041-1

Cited by 91 publications

(140 citation statements)

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“… is the pipe inclination angle Davies and Taylor [9] showed that, the bubble drift velocity in vertical tube is:…”

Section: Slug Velocitymentioning

confidence: 99%

“…Several investigators have developed flow pattern maps and models to characterize the various flow patterns that may be 4 | P a g e adopted by two-phase oil and gas flow mixtures, for instance references [2], [3][4][5][6] and [7][8][9][10][11][12][13][14].…”

Section: Introductionmentioning

confidence: 99%

“…Therefore, the term 1.2UM is approximately equal to the maximum velocity that the liquid in the slug may achieve. The drift velocity, UD, in equation (1) is the relative velocity between the maximum gas velocity in the bubble, UBF, and the maximum velocity of the liquid in the slug, 1.2Us.As reported whilst the drift velocity is clearly non-zero for inclined flows where,and L  is the liquid density, D is the internal pipe diameter,  is liquid surface tension and g is the acceleration due to gravity Bendiksen [8] presented the formula to calculate the bubble drift velocity in inclined pipes:where, is the pipe inclination angle Davies and Taylor [9] showed that, the bubble drift velocity in vertical tube is:For horizontal pipe, [10] proposed the following relation:Equation (2) should be used in place of equation (6) for cases when the Eotvos number is small (i.e. for small diameter pipes or very viscous fluids).…”

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confidence: 99%

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Experimental study of the hydrodynamic behaviour of slug flow in a horizontal pipe

Abdulkadir

Hernández-Pérez

Lowndes

et al. 2016

Chemical Engineering Science

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Abstract:Despite the research efforts in the last decades, the dynamic behaviour of gas-liquid two-phase flows remains a challenging topic. This is due to the growing demand within the petroleum, process and nuclear industries. In particular, data on the behaviour of these flows in more industry relevant fluids are limited. This paper presents a summary of the experimental results on the hydrodynamic behaviour of slug flow using airsilicone oil mixture in a horizontal 67 mm internal diameter pipeline. A series of slug flow regime experiments were performed for a range of injected air superficial velocities (0.29 to 1.4 ms -1 ) and the liquid flows with superficial velocities of between 0.05 to 0.47 ms -1 . The translational Taylor bubble velocity and slug frequency were measured using two pairs of Electrical Capacitance Tomography (ECT) probes. The expected linear dependence of the translational Taylor bubble velocity on the mixture superficial velocity was confirmed.Pressure drop was measured using a differential pressure (dp) transducer cell. The void fractions in the liquid slugs and Taylor bubbles and slug and Taylor bubble lengths parameters were obtained from the processed data.The average total lengths of the observed slugs were of the order of 8 to 46 pipe diameters. The dimensionless Taylor bubble length is concluded to increase as the gas superficial velocity increases. The average slug frequency was observed to increase as the liquid superficial velocity increases but on the other hand was concluded to be fairly weakly dependent on the gas superficial velocity. The measured translational Taylor bubble velocities, void fractions in the liquid, and slug frequencies are presented and compared to data predicted by empirical models available in the literature. A comparative analysis of this and the previously published experimental data sets confirms good agreement.Key words: ECT, Taylor bubble, liquid slug, slug unit, frequency, void fraction 2 | P a g e Introduction:The determination of the multiphase flow regimes that may exist within pipelines is a key factor to the development of efficient oil and gas production systems. As oil and gas reserves are being depleted in developed fields, activity is shifting to harsher and less accessible environments. As offshore production moves into deeper waters farther offshore, the cost of constructing and operating fixed platforms with separation facilities becomes increasingly challenging. An alternative solution is to utilize subsea production systems which entail minimum offshore processing. The adoption of this method requires the simultaneous transport of produced fluids to land-based separation facilities, with minimal offshore treatment to reduce the undesirable effects as corrosion, wax and hydrates formation. Thus, an accurate prediction of the multiphase flow characteristics that may be experienced within these pipelines is therefore required to effect the safe and economic design and operation of these transportation systems.Slug flows are the most preva...

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“… is the pipe inclination angle Davies and Taylor [9] showed that, the bubble drift velocity in vertical tube is:…”

Section: Slug Velocitymentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

mentioning

confidence: 99%

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Experimental study of the hydrodynamic behaviour of slug flow in a horizontal pipe

Abdulkadir

Hernández-Pérez

Lowndes

et al. 2016

Chemical Engineering Science

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“…For potential flow, the drift velocity of an elongated bubble rising in a vertical pipe is (Dumitrescu 1943, Davies andTaylor 1949)…”

Section: Introductionmentioning

confidence: 99%

Movement of Two Consecutive Taylor Bubbles in Vertical Pipes

2007

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Abstract. The development of slug flow along vertical pipes is governed by the interaction between consecutive elongated bubbles. It is generally assumed that the trailing bubble's shape and velocity are affected by the flow field in the liquid phase ahead of it. To examine this assumption, a facility is used that allows controlled injection of pairs of Taylor bubbles into vertical pipes filled with stagnant or flowing liquid. An experimental approach is developed to perform particle image velocimetry measurements of the velocity field in front of the trailing Taylor bubble, simultaneously with video imaging of Taylor bubble pairs, to be able to relate the instantaneous parameters (shape and velocity) of the trailing bubble to the instantaneous velocity distribution in liquid ahead of it. Experiments are performed in pipes of two diameters and for a number of Reynolds numbers based on mean water velocity, corresponding to both laminar and turbulent background flows. A model relating the propagation velocity of the trailing Taylor bubble to the local mean centerline velocity of the leading bubble is suggested and verified experimentally. The effect of the velocity fluctuations in the leading Taylor bubble's wake on the instantaneous propagation velocity of the trailing bubble is studied. 2 SHEMER, GULITSKI and BARNEA

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“…Another group of authors [10][11][12][13] have stated that for a fully developed gas-liquid two-phase upward slug flow, the translational propagating velocity is independent of the length of the Taylor bubble. The intricacies of obtaining fully developed gas-liquid flow relies on bubbles expansion caused by the pressure changes along the tubing as it rises from the bottom, leading to increase in bubble volume thereby affecting its motion.…”

mentioning

confidence: 99%

Effect of length-to-diameter ratio on axial velocity and hydrodynamic entrance length in air-water twophase flow in vertical pipes

Chidamoio¹,

Akanji²,

Rafati

2018

jogps

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The mechanics of large bubbles rising through extended liquids and through liquids in tubes

Cited by 91 publications

References 3 publications

Experimental study of the hydrodynamic behaviour of slug flow in a horizontal pipe

Experimental study of the hydrodynamic behaviour of slug flow in a horizontal pipe

Movement of Two Consecutive Taylor Bubbles in Vertical Pipes

Effect of length-to-diameter ratio on axial velocity and hydrodynamic entrance length in air-water twophase flow in vertical pipes

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