Research Papers: Evaporation, Boiling, and Condensation

Heat Transfer During Near-Critical-Pressure Condensation of Refrigerant Blends

[+] Author and Article Information
Srinivas Garimella

Sustainable Thermal Systems Laboratory,
George W. Woodruff School of
Mechanical Engineering,
Georgia Institute of Technology,
Atlanta, GA 30332
e-mail: sgarimella@gatech.edu

Ulf C. Andresen

Shell Oil Company,
New Orleans, LA 70139

Biswajit Mitra

Carrier Corporation,
Chiller Development Program,
Charlotte, NC 28269

Yirong Jiang

Thermo King,
Minneapolis, MN 55420

Brian M. Fronk

School of Mechanical,
Industrial and Manufacturing Engineering,
Oregon State University,
Corvallis, OR 97331

1Corresponding author.

Contributed by the Heat Transfer Division of ASME for publication in the JOURNAL OF HEAT TRANSFER. Manuscript received December 31, 2014; final manuscript received September 5, 2015; published online February 3, 2016. Assoc. Editor: Amitabh Narain.

J. Heat Transfer 138(5), 051503 (Feb 03, 2016) (16 pages) Paper No: HT-14-1849; doi: 10.1115/1.4032294 History: Received December 31, 2014; Revised September 05, 2015

Heat transfer during condensation of refrigerant blends R404A and R410A flowing through horizontal tubes with 0.76 ≤ D ≤ 9.4 mm at nominal Pr = 0.8–0.9 was investigated. Local heat transfer coefficients were measured for the mass flux range 200 < G < 800 kg m−2 s−1 in small quality increments over the entire vapor–liquid region. Heat transfer coefficients increased with quality and mass flux, while the effect of reduced pressure was not very significant within this range of pressures. The heat transfer coefficients increased with a decrease in diameter. Correlations from the literature were not able to predict the condensation heat transfer coefficient for these fluids at these near-critical pressures over the wide range of tube diameters under consideration. A new flow-regime based model for heat transfer in the wavy, annular, and annular/wavy transition regimes, which predicts 91% of the data within ±25%, is proposed.

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Fig. 1

Schematic of the experimental facility

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Fig. 2

Schematic of the 3.05 mm single tube test section

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Fig. 3

Schematic of the multiport test section

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Fig. 4

Resistance network for test section

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Fig. 7

Experimental R404A and R410A condensation heat transfer coefficient results for D = 6.2 and 9.4 mm

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Fig. 8

Comparison of h for R410A and R404A (9.4 mm tube)

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Fig. 9

Schematic of the wavy flow

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Fig. 6

Experimental R410A condensation heat transfer coefficient results for D = 0.76, 1.52, and 3.05 mm

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Fig. 5

Experimental matrix

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Fig. 11

Overall heat transfer model results

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Fig. 12

Predicted h for 0.76, 1.52, and 3.05 mm diameter tubes

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Fig. 10

Differential element for film condensation

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Fig. 13

Predicted h for 6.2 and 9.4 mm diameter tubes

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Fig. 14

Model trends for annular and wavy flows




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