Technical Brief

Eulerian–Eulerian Modeling of Convective Heat Transfer Enhancement in Upward Vertical Channel Flows by Gas Injection

[+] Author and Article Information
Deify Law

Department of Mechanical Engineering,
California State University, Fresno,
2320 E. San Ramon Avenue, M/S EE94,
Fresno, CA 93740-8030
e-mail: dlaw@csufresno.edu

Haden Hinkle

Department of Mechanical Engineering,
California State University,
Fresno, 1320 E. San Ramon Avenue, M/S EE94,
Fresno, CA 93740-8030

1Corresponding author.

Contributed by the Heat Transfer Division of ASME for publication in the JOURNAL OF THERMAL SCIENCE AND ENGINEERING APPLICATIONS. Manuscript received March 29, 2017; final manuscript received July 13, 2017; published online September 13, 2017. Assoc. Editor: Wei Li.

J. Thermal Sci. Eng. Appl 10(2), 024501 (Sep 13, 2017) (5 pages) Paper No: TSEA-17-1097; doi: 10.1115/1.4037650 History: Received March 29, 2017; Revised July 13, 2017

Two-phase bubbly flows by gas injection had been shown to enhance convective heat transfer in channel flows as compared with that of single-phase flows. The present work explores the effect of gas phase distribution such as inlet air volume fraction and bubble size on the convective heat transfer in upward vertical channel flows numerically. A two-dimensional (2D) channel flow of 10 cm wide × 100 cm high at 0.2 and 1.0 m/s inlet water and air superficial velocities in churn-turbulent flow regime, respectively, is simulated. Numerical simulations are performed using the commercial computational fluid dynamics (CFD) code ANSYS fluent. The bubble size is characterized by the Eötvös number. The inlet air volume fraction is fixed at 10%, whereas the Eötvös number is maintained at 1.0 to perform parametric studies, respectively, in order to investigate the effect of gas phase distribution on average Nusselt number of the two-phase flows. All simulations are compared with a single-phase flow condition. To enhance heat transfer, it is determined that the optimum Eötvös number for the channel with a 10% inlet air volume fraction has an Eötvös number of 0.2, which is equivalent to a bubble diameter of 1.219 mm. Likewise, it is determined that the optimum volume fraction peaks at 30% inlet air volume fraction using an Eötvös number of 1.0.

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Howard, J. A. , Walsh, P. A. , and Walsh, E. J. , 2011, “ Prandtl and Capillary Effects on Heat Transfer Performance Within Laminar Liquid-Gas Slug Flows,” Int. J. Heat Mass Transfer, 54(21–22), pp. 4752–4761. [CrossRef]
Betz, A. R. , and Attinger, D. , 2010, “ Bubble Injection to Enhance Heat Transfer in Microchannel Heat Sinks,” ASME Paper No. IMECE2009-11972.
Ma, F. , and Shen, Z. Q. , 2004, “ Convective Heat Transfer Enhancement by Inert Gas Injection,” J. Dalian Univ. Technol., 44(4), pp. 490–494.
Tokuhiro, A. T. , and Lykoudis, P. S. , 1994, “ Natural Convection Heat Transfer From a Vertical Plate-I. Enhancement With Gas Injection,” Int. J. Heat Mass Transfer, 37(6), pp. 997–1003. [CrossRef]
Choo, K. , and Kim, S. J. , 2011, “ Heat Transfer and Fluid Flow Characteristics of Nonboiling Two-Phase Flow in Microchannels,” ASME J. Heat Transfer, 133(10), p. 102901.
Kitagawa, A. , Kosuge, K. , Uchida, K. , and Hagiwara, Y. , 2008, “ Heat Transfer Enhancement for Laminar Natural Convection Along a Vertical Plate Due to Sub-Millimeter-Bubble Injection,” Exp. Fluids, 45(3), pp. 473–484. [CrossRef]
Panahi, D. , 2017, “ Evaluation of Nusselt Number and Effectiveness for a Vertical Shell-Coiled Tube Heat Exchanger With Air Bubble Injection Into Shell Side,” Exp. Heat Transfer, 30(3), pp. 179–191. [CrossRef]
Moosavi, A. , Abbasalizadeh, M. , and Sadighi, D. H. , 2016, “ Optimization of Heat Transfer and Pressure Drop Characteristics Via Air Bubble Injection Inside a Shell and Coiled Tube Heat Exchanger,” Exp. Therm. Fluid Sci., 78, pp. 1–9. [CrossRef]
Nandan, A. , and Sinh, G. , 2016, “ Experimental Study of Heat Transfer Rate in a Shell and Tube Heat Exchanger With Air Bubble Injection,” Int. J. Eng., Trans. B, 29(8), pp. 1160–1166. http://www.ije.ir/abstract/%7BVolume:29-Transactions:B-Number:8%7D/=2309
Li, W. Z. , Zhao, D. Y. , and Chen, G. J. , 2006, “ Numerical Simulation on Effects of Vertical Channel Wide on Deformation and Heat Transfer of a Rising Gas Bubble,” Chin. J. Comput. Mech., 23(2), pp. 196–201.
Dabiri, S. , and Tryggvason, G. , 2015, “ Heat Transfer in Turbulent Bubbly Flow in Vertical Channels,” Chem. Eng. Sci., 122(27), pp. 106–113. [CrossRef]
Willard, J. R. , and Hollingsworth, D. K. , 2016, “ Numerical Investigation of Flow Structure and Heat Transfer Produced by a Single Highly Confined Bubble in a Pressure-Driven Channel Flow,” ASME Paper No. HT2016-1060.
Picardi, R. , Zhao, L. , and Battaglia, F. , 2016, “ On the Ideal Grid Resolution for Two-Dimensional Eulerian Modeling of Gas-Liquid Flows,” ASME J. Fluids Eng., 138(11), p. 114503.
Law, D. , Battaglia, F. , and Heindel, T. J. , 2008, “ Model Validation for Low and High Superficial Gas Velocity Bubble Column Flows,” Chem. Eng. Sci., 63(18), pp. 4605–4616. [CrossRef]
Law, D. , Jones, S. T. , Heindel, T. J. , and Battaglia, F. , 2011, “ A Combined Numerical and Experimental Study of Hydrodynamics for an Air-Water External Loop Airlift Reactor,” ASME J. Fluids Eng., 133(2), p. 021301.
Simonin, Q. , and Viollet, P. L. , 1990, “ Prediction of an Oxygen Droplet Pulverization in a Compressible Subsonic Coflowing Hydrogen Flow,” Numerical Methods for Multiphase Flow, ASME, New York, pp. 73–82.
Leonard, B. P. , 1979, “ A Stable and Accurate Convective Modelling Procedure Based on Quadratic Upstream Interpolation,” Comput. Methods Appl. Mech. Eng., 19(1), pp. 59–98. [CrossRef]
Kulkarni, A. V. , and Joshi, J. B. , 2006, “ Estimation of Hydrodynamic and Heat Transfer Characteristics of Bubble Column by Analysis of Wall Pressure Measurements and CFD Simulations,” Chem. Eng. Res. Des., 84(A7), pp. 601–609. [CrossRef]
Miyahara, T. , Matsuba, Y. , and Takahashi, T. , 1983, “ The Size of Bubbles Generated From Perforated Plates,” Int. Chem. Eng., 23(1), pp. 517–523. https://www.jstage.jst.go.jp/article/kakoronbunshu1975/8/1/8_1_13/_article
Shah, Y. T. , and Deckwer, W. D. , 1985, “ Fluid-Fluid Reactors,” Scale-Up of Chemical Processes: Conversion From Lab-Scale Tests to Successful Commercial-Size Design, Wiley, Hoboken, NJ, pp. 201–274.
Celik, I. B. , Ghia, U. , Roache, P. J. , Freitas, C. J. , Coleman, H. , and Raad, P. E. , 2008, “ Procedure for Estimation and Reporting of Uncertainty Due to Discretization in CFD Applications,” ASME J. Fluids Eng., 130(7), p. 078001. [CrossRef]
Nouri, N. M. , Motlagh, S. Y. , Navidbakhsh, M. , Dalilhaghi, M. , and Moltani, A. A. , 2013, “ Bubble Effect on Pressure Drop Reduction in Upward Pipe Flow,” Exp. Therm. Fluid Sci., 44, pp. 592–598. [CrossRef]


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Fig. 1

Schematic of the 2D channel

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Fig. 2

Comparison of CFD and experimental data [18] for wall heat transfer coefficient of a 0.385 m diameter bubble column at 82.3 cm above the column inlet at several inlet gas superficial velocities

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Fig. 3

Grid-resolution study for space-averaged water axial velocity profile of case 2 between channel heights of 20 and 80 cm at 40 s

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Fig. 4

Grid-resolution study for space-averaged water static temperature profile of case 2 between channel heights of 20 and 80 cm at 40 s

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Fig. 5

Comparison of average Nusselt number at a given Eötvös number with a 10% inlet air volume fraction between channel heights of 20 and 80 cm

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Fig. 6

Comparison of average Nusselt number at a given inlet air volume fraction with Eötvös number of 1.0 between channel heights of 20 and 80 cm



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