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Research Papers: Evaporation, Boiling, and Condensation

Flow Boiling Heat Transfer Characteristics of a Minichannel up to Dryout Condition

[+] Author and Article Information
Rashid Ali

Applied Thermodynamics and Refrigeration, Department of Energy Technology, Royal Institute of Technology, KTH, Brinellvägen 68, 100 44-SE Stockholm, Swedenrashid.ali@energy.kth.se

Björn Palm

Applied Thermodynamics and Refrigeration, Department of Energy Technology, Royal Institute of Technology, KTH, Brinellvägen 68, 100 44-SE Stockholm, Swedenbpalm@energy.kth.se

Mohammad H. Maqbool

Applied Thermodynamics and Refrigeration, Department of Energy Technology, Royal Institute of Technology, KTH, Brinellvägen 68, 100 44-SE Stockholm, Swedenmaqbool@kth.se

J. Heat Transfer 133(8), 081501 (Apr 26, 2011) (10 pages) doi:10.1115/1.4003669 History: Received May 17, 2010; Revised February 12, 2011; Published April 26, 2011; Online April 26, 2011

In this paper, the experimental flow boiling heat transfer results of a minichannel are presented. A series of experiments was conducted to measure the heat transfer coefficients in a minichannel made of stainless steel (AISI 316) having an internal diameter of 1.70 mm and a uniformly heated length of 220 mm. R134a was used as a working fluid, and experiments were performed at two different system pressures corresponding to saturation temperatures of 27°C and 32°C. Mass flux was varied from 50kg/m2s to 600kg/m2s, and heat flux ranged from 2kW/m2 to 156kW/m2. The test section was heated directly using a dc power supply. The direct heating of the channel ensured uniform heating, which was continued until dryout was reached. The experimental results show that the heat transfer coefficient increases with imposed wall heat flux, while mass flux and vapor quality have no considerable effect. Increasing the system pressure slightly enhances the heat transfer coefficient. The heat transfer coefficient is reduced as dryout is reached. It is observed that the dryout phenomenon is accompanied with fluctuations and a larger standard deviation in outer wall temperatures.

Copyright © 2011 by American Society of Mechanical Engineers
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Figures

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Figure 1

Schematic diagram of microchannel test rig and test section

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Figure 2

Inner surface characterization of test tube, D=1.70 mm

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Figure 3

Boiling curve at Tsat=27°C

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Figure 4

Boiling curve at Tsat=32°C

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Figure 5

Local heat transfer coefficient at G=75 kg/m2 s, Tsat=27°C

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Figure 6

Local heat transfer coefficient at G=200 kg/m2 s, Tsat=32°C

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Figure 7

Local heat transfer coefficient at G=600 kg/m2 s, Tsat=27°C

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Figure 8

Variation in local heat transfer coefficient for different heat and mass fluxes at Tsat=27°C

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Figure 9

Pressure effect on local heat transfer coefficient

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Figure 10

Average heat transfer coefficient at Tsat=27°C

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Figure 11

Continuous recording of outer wall temperatures at high heat fluxes, G=300 kg/m2 s, Tsat=32°C

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Figure 12

SD of wall temperatures and HTCs close to dryout conditions, G=300 kg/m2 s, Tsat=32°C

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Figure 13

Comparison of average heat transfer coefficient with Cooper (25) correlation

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Figure 14

Comparison of average heat transfer coefficient with Gorenflo (26) correlation

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Figure 15

Comparison of average heat transfer coefficient with Lazarek and Black (9) correlation

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Figure 16

Comparison of average heat transfer coefficient with Owhaib (27) correlation

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Figure 17

Comparison of average heat transfer coefficient with Tran (29) correlation

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Figure 18

Comparison of local heat transfer coefficient with Liu and Winterton (12) correlation

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Figure 19

Comparison of local heat transfer coefficient with Chaddock and Brunemann (31) correlation

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Figure 20

Comparison of local heat transfer coefficient with Kandlikar and Balasubramanian (32) correlation

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Figure 21

Comparison of local heat transfer coefficient with Zhang (33) correlation

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