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Research Papers: Heat and Mass Transfer

Thermal and Flow Characteristics of Water–Nitrogen Taylor Flow Inside Vertical Circular Tubes

[+] Author and Article Information
Jingzhi Zhang

School of Energy and Power Engineering,
Shandong University,
Jinan 250061, China;
Department of Energy Engineering,
Zhejiang University,
Hangzhou 310027, China

Wei Li

Department of Energy Engineering,
Zhejiang University,
Hangzhou 310027, China
e-mail: weili96@zju.edu.cn

1Corresponding author.

Contributed by the Heat Transfer Division of ASME for publication in the JOURNAL OF HEAT TRANSFER. Manuscript received June 5, 2017; final manuscript received March 27, 2018; published online May 7, 2018. Assoc. Editor: Debjyoti Banerjee.

J. Heat Transfer 140(8), 082004 (May 07, 2018) (10 pages) Paper No: HT-17-1327; doi: 10.1115/1.4039902 History: Received June 05, 2017; Revised March 27, 2018

Heat transfer and flow characteristics of Taylor flows in vertical capillaries with tube diameters ranging from 0.5 mm to 2 mm were studied numerically with the volume of fluid (VOF) method. Streamlines, bubble shapes, pressure drops, and heat transfer characteristics of the fully developed gas–liquid Taylor flow were investigated in detail. The numerical data fitted well with experimental results and with the predicted values of empirical correlations. The results indicate that the dimensionless liquid film thickness and bubble rising velocity increase with increasing capillary number. Pressure drops in liquid slug region are higher than the single-phase flow because of the Laplace pressure drop. The flow pattern dependent model and modified flow separation model which takes Bond number and Reynolds number into account can predict the numerical pressure drops well. Compared with the single-phase flow, less time is needed for the Taylor flow to reach a thermal fully developed status. The Nusselt number of Taylor flow is about 1.16–3.5 times of the fully developed single-phase flow with a constant wall heat flux. The recirculation regions in the liquid and gas slugs can enhance the heat transfer coefficient and accelerate the development of the thermal boundary layer.

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Figures

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Fig. 1

A sketch map for the VOF method: the regions where αG = 0.0 represents the liquid phase, the regions where αG = 1.0 stand for the liquid phase, and the regions where 0.0 < αG < 1.0 contain the liquid--vapor interfaces [33]

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Fig. 2

Computational geometry and boundary conditions

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Fig. 3

Taylor bubble shapes for different mesh sizes in a 1 mm diameter tube at Re = 300 and ξG = 0.3

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Fig. 4

Streamlines and bubble shapes for Taylor flows at Re = 100 and 500 with d ranging from 0.5 to 2 mm

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Fig. 5

The effects of tube diameter and Re on the Taylor bubble shapes: (a) the effect of tube diameter (Re = 300) and (b) the effect of Re (d = 0.5 mm)

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Fig. 6

Dimensionless bubble velocities express as a function of Ca based on two phase superficial velocities

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Fig. 7

A sketch map for the liquid film thickness in the Taylor flow

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Fig. 8

The effect of Cab on the dimensionless liquid film thickness δ/R

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Fig. 9

Comparison between the values of δ/R obtained by numerical simulations and empirical correlations

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Fig. 10

The wall and axis pressure distribution along the axis direction

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Fig. 11

fsRe versus Ls/d(Ca/Re)0.33

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Fig. 12

Comparison between the numerical and the predicted pressure drop with correlations: (a) correlation of Kreutzer et al [4], (b) correlation of Li and Wu [37], (c) correlation of Kim and Mudawar [38], and (d) correlation of the present work

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Fig. 13

The evolution of average Nu of Taylor flow and single-phase flow

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Fig. 14

The evolution of dimensionless temperature contours (Θ) of the gas–liquid Taylor flow in a round tube with d = 1 mm at Re = 300

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Fig. 15

Temperature contours and streamlines in the liquid and gas slug in a tube with d = 0.5 mm at Re = 300

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Fig. 16

Liquid slug Nu expressed as a function of dimensionless liquid slug length

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Fig. 17

Comparison of numerical Nutp with the predicted results

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