Technical Brief: Technical Briefs

Modeling the Flow of Non-Newtonian Fluids Through Sharp Orifices

[+] Author and Article Information

Maha Fluid Power Research Center,
1500 Kepner Drive,
Lafayette, IN 47905
e-mail: rituraj@purdue.edu

Andrea Vacca

Maha Fluid Power Research Center,
1500 Kepner Drive,
Lafayette, IN 47905
e-mail: avacca@purdue.edu

1Corresponding author.

Contributed by the Fluids Engineering Division of ASME for publication in the JOURNAL OF FLUIDS ENGINEERING. Manuscript received February 20, 2017; final manuscript received August 24, 2017; published online January 9, 2018. Assoc. Editor: Mhamed Boutaous.

J. Fluids Eng 140(5), 054501 (Jan 09, 2018) (6 pages) Paper No: FE-17-1111; doi: 10.1115/1.4038659 History: Received February 20, 2017; Revised August 24, 2017

This paper proposes a novel orifice flow model for non-Newtonian fluids. The orifice model is developed for sharp orifices with small apertures (orifice to pipe diameter ratio: 0.04 ≤ β ≤ 0.16) for which predictive models are not present in the literature. The orifice flow experiment is conducted with three different orifices and three different fluids. From the experimental data, a correlation is developed that relates Euler number to Reynolds number and orifice diameter ratio. It also accounts for elastic effects of the fluid on orifice flow by including Weissenberg number in the model. The developed model predicts the experimental data within reasonable accuracy.

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Fig. 1

The viscosity-shear rate behavior of a typical shear thinning fluid

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Fig. 2

ISO standard hydraulic circuit of the experimental setup

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Fig. 3

Normalized viscosity shear rate plot for fluid C. The dots indicate the data points obtained from viscometric measurements. The line is obtained from Carreau–Yashuda law (Eq.(6)).

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Fig. 4

Eu versus Re for different orifice diameter ratios for different fluids

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Fig. 5

Comparison of the Euler number predicted by the correlations proposed versus the Euler number from experimental data

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Fig. 6

Eu versus Re comparison between experimental data and those obtained from proposed correlation

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Fig. 7

Eu versus Re for fluid B with error bars. The error bars in x-direction, i.e., for Re are not visible because of very low value of error. The error bars in y-direction, i.e., for Eu are visible at high Eu.



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