By K. C. Wilson, G. R. Addie, A. Sellgren, R. Clift
Sizeable tonnages of solid-liquid combinations are pumped each year in dredging operations, mining and waste-disposal functions. each one of these platforms are centrifugal pumps, and the answer of difficulties encountered in slurry pumping calls for either targeted medical wisdom and judgment derived from functional event. for a few years the mix of up to date research and hands-on experimentation has been supplied to engineers in a quick direction established on the GIW Hydraulic Laboratory. the teachers during this direction, who symbolize a huge history of foreign services, have ready this widely-recognized textual content, Slurry shipping utilizing Centrifugal Pumps, 3rd version. This special textual content is logically divided into sections: the 1st a part of the e-book concentrates at the behaviors of varied varieties of slurry circulate, and the second one half bargains with the habit of centrifugal pumps dealing with slurries, and with how pumps and pipelines engage as a approach. Slurry delivery utilizing Centrifugal Pumps, 3rd version additionally comprises: New fabric on either non-Newtonian flows and slurries of granular debris. New info on pump put on, solids impression, and method operation. up to date and entirely new fabric on pump choice and environmental elements labored examples and case stories that pressure functional functions Slurry shipping utilizing Centrifugal Pumps, 3rd version, can be of curiosity to all engineers and technologists desirous about the large-scale transportation of slurries. .
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As a result, the slurry can be treated for most purposes as a single-phase fluid. The particles move at the local fluid velocity. Therefore the delivered and in situ concentrations are identical (cf. 4) and, provided that the line is not left full of stagnant slurry for an extended period, a stationary bed of solids does not form. Set against these simplifications is the fact that the slurry usually shows non-Newtonian behaviour. 1. The friction gradient, jm, is given in terms of the head loss of mixture.
Dealt with in Chapter 7) difficulties arise because the viscosity is included in both dimensionless variables. To cover both Newtonian and non-Newtonian cases, an alternative method has been worked out, as described by Wilson et al. (2003) and Wilson & Horsley (2004). This method is based on a pair of dimensionless variables that employ concepts developed in the pipe-flow analysis of Prandtl (1933) and Colebrook(1939). The method expresses the velocity ratio (mean velocity to shear velocity) as a function of the shear Reynolds number (based on shear velocity rather than mean velocity).
81J with d in metres. 3 shows the values that were obtained for this quantity for the various particle sizes. e. pfV*d/|Li. This quantity is used to calculate Vts/V*, using Eq. 2 mm particle (for which Re* < 10) and Eq. 65 for the other particles, based on their shear Reynolds numbers. 3. 2 mm particles lie well beyond the Stokes' law range, while the 2 mm particles are not quite into the Newton's law range. (b) Terminal Velocities of Sand Grains To obtain the terminal fall velocity of the sand particles, the values of Vts must be multiplied by the velocity ratio ^, which, in turn, depends on the dimensionless particle size d*, given by Eq.