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Research Papers: Multiphase Flows

Centrifugal Pump Derating for Non-Newtonian Slurries

[+] Author and Article Information
J. J. N. Kalombo

Flow Process and Rheology Centre,
Cape Peninsula University of Technology,
P.O. Box 652,
Cape Town, 8000, South Africa
e-mail: kalomboj@cput.ac.za

R. Haldenwang

Flow Process and Rheology Centre,
Cape Peninsula University of Technology,
P.O. Box 652,
Cape Town, 8000, South Africa
e-mail: haldenwangr@cput.ac.za

R. P. Chhabra

Department of Chemical Engineering,
Indian Institute of Technology,
Kanpur, India;
Adjunct Professor
Flow Process and Rheology Centre,
Cape Peninsula University of Technology,
P.O. Box 652,
Cape Town, 8000, South Africa
e-mail: chhabra@iitk.ac.in

V. G. Fester

Flow Process and Rheology Centre,
Cape Peninsula University of Technology,
P.O. Box 652,
Cape Town, 8000, South Africa
e-mail: festerv@cput.ac.za

Contributed by the Fluids Engineering Division of ASME for publication in the JOURNAL OF FLUIDS ENGINEERING. Manuscript received March 22, 2013; final manuscript received November 5, 2013; published online January 20, 2014. Assoc. Editor: Bart van Esch.

J. Fluids Eng 136(3), 031302 (Jan 20, 2014) (11 pages) Paper No: FE-13-1184; doi: 10.1115/1.4025989 History: Received March 22, 2013; Revised November 05, 2013

The Hydraulic Institute method, developed for predicting centrifugal pump performance of viscous Newtonian fluids, is used by some for non-Newtonian fluids. This requires an average value of viscosity representing the variable non-Newtonian viscosities. To determine such an average viscosity, two approaches exist in the literature: the use of a Bingham plastic viscosity and the use of the apparent viscosity. Results from these two approaches are not in agreement. This study evaluates the two approaches using two independent datasets, obtained from three pumps and three fluids. Results indicate that using the apparent viscosity approach gave better head prediction and using the Bingham plastic viscosity resulted in better efficiency prediction.

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References

Pullum, L., Graham, L. J. W., and Rudman, M., 2007, “Centrifugal Pump Performance Calculation for Homogeneous and Complex Heterogeneous Suspensions,” Journal of the Southern African Institute of Mining and Metallurgy, 107, pp. 373–379.
Abulnaga, B. E., 2002, Slurry Systems Handbook, McGraw-Hill, New York.
Roco, M. C., Marsh, M., Addie, G. R., and Maffett, J. R., 1986, “Dredge Pump Performance Prediction,” J. Pipelines, 5, pp. 171–190.
Angel, T., and Crisswell, J., 1997, Slurry Pump Manual, Envirotech Pumpsystems, Salt Lake City, UT.
Engin, T., and Gur, M., 2003, “Comparative Evaluation of Some Existing Correlations to Predict Head Degradation of Centrifugal Slurry Pumps,” ASME J. Fluids Eng., 125(1), pp. 149–157. [CrossRef]
Walker, C. I., and Goulas, A., 1984, “Performance Characteristics of Centrifugal Pumps When Handling Non-Newtonian Homogeneous Slurries,” Proc. Inst. Mech. Eng., Part A, 198(A), pp. 41–49. [CrossRef]
Sery, G., and Slatter, P. T., 2002, “Centrifugal Pump Derating for Non-Newtonian Slurries,” Proc. 15th International Conference on Slurry Handling and Pipeline Transport: Hydrotransport, N.Heywood, ed., BHR Group, Banff, Cranfield, Canada, 2, pp. 679–692.
Kabamba, B. M., 2006, “Evolution of Centrifugal Pump Performance Derating Procedures for Non-Newtonian Slurries,” MTech thesis, Cape Peninsula University of Technology, Cape Town, South Africa.
Engin, T., and Gur, M., 2001, “Performance Characteristics of a Centrifugal Pump Impeller With Running Tip Clearance Pumping Solid-Liquid Mixtures,” ASME J. Fluids Eng., 123, pp. 532–538. [CrossRef]
Wilson, K. C., Addie, G. R., Sellgren, A., and Clift, R., 2006, Slurry Transport Using Centrifugal Pumps, 3rd ed., Springer, New York.
Kazim, K. A., Maiti, B., and Chand, P., 1997, “A Correlation to Predict the Performance Characteristics of Centrifugal Pumps Handling Slurries,” Proc. Inst. Mech. Eng., Part A, 211(A), pp. 147–157. [CrossRef]
Stepanoff, A. J., 1940, “Pumping Viscous Oils With Centrifugal Pumps,” Oil & Gas J., 4, pp. 78–82.
Hydraulic Institute, 1983, Hydraulic Institute Standards for Centrifugal, Rotary and Reciprocating Pumps, 14th ed., Hydraulic Institute, Cleveland, OH.
ANSI/HI 9.6.7, 2004, Effects of Liquid Viscosity on Rotodynamic (Centrifugal and Vertical) Pump Performance, Hydraulic Institute, Parsippany, NJ.
Graham, L. J. W., Pullum, L., Slatter, P., Sery, G., and Rudman, M., 2009, “Centrifugal Pump Performance Calculation for Homogeneous Suspensions,” Can. J. Chem. Eng., 87(4), pp. 526–533. [CrossRef]
Pullum, L., Graham, L. J. W., and Wu, J., 2011, “Centrifugal Pump Performance With Non-Newtonian Slurries,” Proc. 15th International Conference on Transport and Sedimentation of Solid Particles, Wroclaw, Poland.
International Organization for Standardization, 1999, Rotodynamic Pumps, ISO 9906, ISO, Geneva, Switzerland.

Figures

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Fig. 1

Comparison between predicted and experimental pump efficiency for a 17% kaolin slurry [17]

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Fig. 2

Layout of the pump test rig (top view of the rig)

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Fig. 3

Warman 4/3 pump head curves compared to Pullum et al. and Walker and Goulas models

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Fig. 4

Warman 4/3 pump efficiency curves compared to Pullum et al. and Walker and Goulas models

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Fig. 5

Experimental head (efficiency) versus calculated head (efficiency) for the Warman 4/3 pump using the Walker and Goulas [6] approach

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Fig. 6

Experimental head (efficiency) versus calculated head (efficiency) for the GIW 4/3 using the Walker and Goulas [6] approach

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Fig. 7

Experimental head (efficiency) versus calculated head (efficiency) for the Warman 6/4 using the Walker and Goulas [6] approach

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Fig. 8

Experimental head (efficiency) versus calculated head (efficiency) for the Warman 4/3 pump using the Pullum et al. [1] approach

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Fig. 9

Experimental head (efficiency) versus calculated head (efficiency) for the GIW 4/3 using the Pullum et al. [1] approach

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Fig. 10

Experimental head (efficiency) versus calculated head (efficiency) for the Warman 6/4 using the Pullum et al. [1] approach

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Fig. 11

Comparison between the results obtained using w = 0.059 and w = 0.023 for the pump head prediction

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Fig. 12

Sensitivity of the pump performance prediction procedures to a change in viscosity for the Warman 4/3 pump

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