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RESEARCH PAPERS: Forced Convection

Heat Transfer in a Surfactant Drag-Reducing Solution—A Comparison With Predictions for Laminar Flow

[+] Author and Article Information
Paul L. Sears

 Natural Resources Canada, CANMET Energy Technology Centre-Ottawa, 1 Haanel Drive, Nepean, ON K1A 1M1, Canadapsears@nrcan.gc.ca

Libing Yang

 Natural Resources Canada, CANMET Energy Technology Centre-Ottawa, 1 Haanel Drive, Nepean, ON K1A 1M1, Canada

J. Heat Transfer 128(6), 557-563 (Dec 22, 2005) (7 pages) doi:10.1115/1.2188462 History: Received November 30, 2004; Revised December 22, 2005

Heat transfer coefficients were measured for a solution of surfactant drag-reducing additive in the entrance region of a uniformly heated horizontal cylindrical pipe with Reynolds numbers from 25,000 to 140,000 and temperatures from 30to70°C. In the absence of circumferential buoyancy effects, the measured Nusselt numbers were found to be in good agreement with theoretical results for laminar flow. Buoyancy effects, manifested as substantially higher Nusselt numbers, were seen in experiments carried out at high heat flux.

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Copyright © 2006 by American Society of Mechanical Engineers
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Figures

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Figure 1

Schematic diagram of experimental test loop

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Figure 2

Schematic diagram of experimental test section

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Figure 3

Fanning friction factor versus solvent Reynolds number at various fluid temperatures for Ethoquad O∕12 PG (2000ppm)

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Figure 4

Drag reduction as a function of solvent Reynolds number at various fluid temperatures

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Figure 5

Heat transfer reduction as a function of solvent Reynolds number at various fluid inlet temperatures. The heat flux was constant at 23.6kW∕m2.

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Figure 6

Experimental Nusselt number as a function of axial distance at various fluid inlet temperatures and velocities in turbulence-suppressed region. The heat flux was constant at 23.6kW∕m2.

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Figure 7

Measured outer-wall surface temperatures along the test section at various fluid inlet temperatures and velocities in turbulence-suppressed region. The heat flux was constant at 23.6kW∕m2.

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Figure 8

Nusselt number as a function of axial distance at a fluid inlet temperature of 30°C and velocity of 1.5m∕s at various heat fluxes. Dashed lines are theoretical values.

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