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TECHNICAL PAPERS

An Expermentally Validated Model for Two-Phase Pressure Drop in the Intermittent Flow Regime for Noncircular Microchannels

[+] Author and Article Information
Srinivas Garimella, Jesse D. Killion, John W. Coleman

George W. Woodruff School of Mechanical Engineering, Georgia Institue of Technology, Atlanta, GA 30332-0405

J. Fluids Eng 125(5), 887-894 (Oct 07, 2003) (8 pages) doi:10.1115/1.1601258 History: Received April 02, 2002; Revised April 30, 2003; Online October 07, 2003
Copyright © 2003 by ASME
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References

Coleman,  J. W., and Garimella,  S., 1999, “Characterization of Two-Phase Flow Patterns in Small Diameter Round and Rectangular Tubes,” Int. J. Heat Mass Transfer, 42(15), pp. 2869–2881.
Coleman, J. W., and Garimella, S., 2000, “Visualization of Refrigerant Two-Phase Flow During Condensation,” Proceedings of the 34th National Heat Transfer Conference, ASME, New York.
Coleman, J. W., and Garimella, S., 2000, “Two-Phase Flow Regime Transitions in Microchannel Tubes: The Effect of Hydraulic Diameter,” Proc. ASME Heat Transfer Division—2000, ASME, New York, Orlando, FL, HTD-Vol. 366-4, pp. 71–83.
Mandhane,  J. M., Gregory,  G. A., and Aziz,  K., 1974, “A Flow Pattern Map for Gas-Liquid Flow in Horizontal Pipes,” Int. J. Multiphase Flow, 1, pp. 537–553.
Taitel,  Y., and Dukler,  A. E., 1976, “A Model for Predicting Flow Regime Transitions in Horizontal and Near Horizontal Gas-Liquid Flow,” AIChE J., 22(1), pp. 47–55.
Garimella,  S., Killion,  J. D., and Coleman,  J. W., 2002, “An Experimentally Validated Model for Two-Phase Pressure Drop in the Intermittent Flow Regime for Circular Microchannels,” ASME J. Fluids Eng., 124(1), pp. 205–214.
Suo,  M., and Griffith,  P., 1964, “Two-Phase Flow in Capillary Tubes,” J. Basic Eng., 86, pp. 576–582.
Dukler,  A. E., and Hubbard,  M. G., 1975, “A Model for Gas-Liquid Slug Flow in Horizontal and Near Horizontal Tubes,” Ind. Eng. Chem. Fundam., 14(4), pp. 337–347.
Fukano, T., Kariyasaki, A., and Kagawa, M., 1989, “Flow Patterns and Pressure Drop in Isothermal Gas-Liquid Concurrent Flow in a Horizontal Capillary Tube,” ANS Proceedings 1989 National Heat Transfer Conference, American Nuclear Society, La Grange Park, IL, 4 , pp. 153–161.
Tran,  T. N., Chyu,  M.-C., Wambsganss,  M. W., and France,  D. M., 2000, “Two-Phase Pressure Drop of Refrigerants During Flow Boiling in Small Channels: An Experimental Investigation and Correlation Development,” Int. J. Multiphase Flow, 26(11), pp. 1739–1754.
Churchill,  S. W., 1977, “Friction Factor Equation Spans All Fluid Flow Regimes,” Chem. Eng. (Rugby, U.K.), 84(24), pp. 91–92.
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Berker, A. R., 1963, “Intégration des équations du Mouvement d’un Fluide Visqueux Incompressible,” Encyclopedia of Physics, S. Flügge, ed., Springer, Berlin, pp. 1–384.
Heywood,  N. I., and Richardson,  J. F., 1979, “Slug Flow of Air-Water Mixtures in a Horizontal Pipe: Determination of Liquid Holdup by Γ-Ray Absorption,” Chem. Eng. Sci., 34, p. 17.
Gregory,  G. A., and Scott,  D. S., 1969, “Correlation of Liquid Slug Velocity and Frequency in Horizontal Cocurrent Gas-Liquid Slug Flow,” AIChE J., 15(6), pp. 933–935.
Kago,  T., Saruwatari,  T., Ohno,  S., Morooka,  S., and Kato,  Y., 1987, “Axial Mixing of Liquid in Horizontal Two Phase Slug Flow,” J. Chem. Eng. Jpn., 20, p. 252.
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Figures

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Test facility schematic
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Noncircular tubes investigated in the present study
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Cross section of assumed flow pattern for model unit cell
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Contribution of each pressure drop mechanism to total pressure drop for each test point
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Comparison of total predicted pressure drop based on frequency model of Tronconi 17 with measured data
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Comparison of total predicted pressure drop based on frequency model of Gregory and Scott 15 with measured data
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Comparison of total predicted pressure drop based on frequency model of Garimella et al. 6, Eq. (21), and Eq. (24) with measured data
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Number of unit cells per meter derived from measured data as a function of slug Reynolds number, comparison with model: Eq. (21) and Eq. (24)
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Comparison of Lockhart-Martinelli, Chisholm, and Friedel two-phase pressure drop models, 22, with measured data
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Predicted effect of tube shape for nominal flow area equivalent to 0.75-mm diameter circular tube, L/Dh,nominal=500

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