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Research Papers

Low Mass Quality Flow Boiling in Microtubes at High Mass Fluxes

[+] Author and Article Information
Mehmed Rafet Özdemir, Alihan Kaya

Mechatronics Engineering Program,  Sabancı University, Tuzla, Istanbul 34956, Turkey

Ali Koşar1

Mechatronics Engineering Program,  Sabancı University, Tuzla, Istanbul 34956, Turkeykosara@sabanciuniv.edu

1

Corresponding author.

J. Thermal Sci. Eng. Appl 3(4), 041001 (Oct 13, 2011) (9 pages) doi:10.1115/1.4005053 History: Received January 28, 2011; Revised August 12, 2011; Published October 13, 2011; Online October 13, 2011

In this article, an experimental study on boiling heat transfer and fluid flow in microtubes at high mass fluxes is presented. De-ionized water flow was investigated over a broad range of mass flux (1000 kg/m2 s–7500 kg/m2 s) in microtubes with inner diameters of  ∼ 250 μm and ∼685 μm. The reason for using two different capillary diameters was to investigate the size effect on flow boiling. De-ionized water was used as working fluid, and the test section was heated by Joule heating. Heat transfer coefficients and qualities were deduced from local temperature measurements. It was found that high heat removal rates could be achieved at high flow rates under subcooled boiling conditions. It was also observed that heat transfer coefficients increased with mass flux, whereas they decreased with local quality and heat flux. Moreover, experimental heat flux data were compared with partial boiling correlations and fully developed boiling correlations. It was observed that at low wall superheat values, there was only a small inconsistency between the experimental data and the conventional partial boiling prediction method of Bergles, while the subcooled and low quality fully developed boiling heat transfer correlation of Kandlikar could fairly predict experimental results at high wall superheat values.

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Copyright © 2011 by American Society of Mechanical Engineers
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Figures

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Figure 1

Experimental test setup (V = voltage, I = current, AC = alligator clip, T = temperature, P = pressure, Q = flow rate, and R = resistance)

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Figure 2

Schematic of the test section (TC = thermocouple)

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Figure 3

(a) Heat flux-local ΔTw , i at saturation for thermocouple 2 location (xth 2 ) at different mass fluxes (254 μm tube), (b) heat flux-local ΔTw , i at saturation for thermocouple 3 location (xth 3 ) at different mass fluxes (254 μm tube), and (c) heat flux-local ΔTw , i at saturation for thermocouple 3 location (xth 3 ) at different mass fluxes (685 μm tube)

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Figure 4

(a) Local two-phase heat transfer coefficient—heat flux for thermocouple 2 locations (xth 2 ) at different mass fluxes for (254 μm tube), (b) local two-phase heat transfer coefficient—heat flux for thermocouple 3 locations (xth 3 ) at different mass fluxes for (254 μm tube), and (c) local two-phase heat transfer coefficient—heat flux for thermocouple 3 locations (xth 3 ) at different mass fluxes for (685 μm tube)

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Figure 5

(a) Local two-phase heat transfer coefficient—local qualities for thermocouple 2 location (xth 2 ) at different mass fluxes (254 μm tube) (b) Local two-phase heat transfer coefficient—local qualities for thermocouple 3 location (xth 3 ) at different mass fluxes (254 μm tube) (c) Local two-phase heat transfer coefficient—local qualities for thermocouple 3 location (xth 3 ) at different mass fluxes (685 μm tube)

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Figure 6

(a) q″experimental /q″predicted - ΔTsaturation at different mass fluxes (254 μm tube) and (b) q″experimental /q″predicted - ΔTsaturation at different mass fluxes (685 μm tube) (partial boiling correlation was used)

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Figure 7

(a) Local two-phase heat transfer coefficient—local qualities for thermocouple 3 location (xth 3 ) at different diameters (G = 3000 kg/m2 s) and (b) Local two-phase heat transfer coefficient—local qualities for thermocouple 3 location (xth 3 ) at different diameters (G = 5000 kg/m2 s)

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