Flow of Viscoelastic Fluids through Porous Media

Marshall, R. J.; Metzner, A. B.

doi:10.1021/i160023a012

Cited by 239 publications

(144 citation statements)

References 19 publications

(34 reference statements)

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“…As a consequence, the relationship between the pressure drop and flow rate very often do not follow the observed Newtonian and inelastic non-Newtonian trend. Further complications arise from the fact that for complex fluids the stress depends not only on whether the flow is a shearing, extensional, or mixed type, but also on the whole history of the velocity gradient [15,42,102,103,104,105].…”

Section: Viscoelasticitymentioning

confidence: 99%

“…Various corrugated tube models with different simple geometries have been used as a first step to model the effect of converging-diverging geometry on the flow of viscoelastic fluids in porous media (e.g. [63,102,110]). Those geometries include conically shaped sections, sinusoidal corrugation and abrupt expansions and contractions.…”

Section: Converging-diverging Geometrymentioning

confidence: 99%

“…The particular response in a given process depends on the time scale of the process in relation to a natural time of the material. With regard to this time scale dependency of viscoelastic flow process at pore level, the fluid relaxation time and the rate of elongation or contraction that occurs as the fluid flows through a channel or pore with varying cross sectional area should be used to characterize and quantify viscoelastic behavior [6,45,102,113]. Sadowski and Bird [9] analyzed the viscometric flow problem in a long straight circular tube and argued that in such a flow no time-dependent elastic effects are expected.…”

Section: Steady-state Time-dependencementioning

confidence: 99%

“…Since the process time is very short, no overshoot will occur at the tube constriction as a measurable finite time is needed for the overshoot to take place. The result is that no increase in the pressure drop will be observed in this flow regime and the normal shear-thinning behavior is resumed with the eventual high flow rate plateau [102,114].…”

Section: Steady-state Time-dependencementioning

confidence: 99%

“…• Marshall and Metzner [102] used three polymeric non-Newtonian solutions (Carbopol 934, polyisobutylene L100 and ET-597) to investigate the flow of viscoelastic fluids through porous media and determine a Deborah number at which viscoelastic effects first become measurable. The porous medium which they used was a sintered bronze porous disk.…”

Section: Experimental Work On Non-newtonian Flow In Porous Mediamentioning

confidence: 99%

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Flow of non‐newtonian fluids in porous media

Sochi

2010

J Polym Sci B Polym Phys

112

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The study of flow of non‐Newtonian fluids in porous media is very important and serves a wide variety of practical applications in processes such as enhanced oil recovery from underground reservoirs, filtration of polymer solutions and soil remediation through the removal of liquid pollutants. These fluids occur in diverse natural and synthetic forms and can be regarded as the rule rather than the exception. They show very complex strain and time dependent behavior and may have initial yield‐stress. Their common feature is that they do not obey the simple Newtonian relation of proportionality between stress and rate of deformation. Non‐Newtonian fluids are generally classified into three main categories: time‐independent whose strain rate solely depends on the instantaneous stress, time‐dependent whose strain rate is a function of both magnitude and duration of the applied stress and viscoelastic which shows partial elastic recovery on removal of the deforming stress and usually demonstrates both time and strain dependency. In this article, the key aspects of these fluids are reviewed with particular emphasis on single‐phase flow through porous media. The four main approaches for describing the flow in porous media are examined and assessed. These are: continuum models, bundle of tubes models, numerical methods and pore‐scale network modeling. © 2010 Wiley Periodicals, Inc. J Polym Sci Part B: Polym Phys, 2010

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Section: Viscoelasticitymentioning

confidence: 99%

Section: Converging-diverging Geometrymentioning

confidence: 99%

Section: Steady-state Time-dependencementioning

confidence: 99%

Section: Steady-state Time-dependencementioning

confidence: 99%

Section: Experimental Work On Non-newtonian Flow In Porous Mediamentioning

confidence: 99%

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Flow of non‐newtonian fluids in porous media

Sochi

2010

J Polym Sci B Polym Phys

112

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Pressure drop in a split‐and‐recombine caterpillar micromixer in case of newtonian and non‐newtonian fluids

et al. 2013

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Microreactors are very promising tools for the design of future chemical processes. For example, emulsions of very narrow size distribution are obtained at much lower energy consumption than the one spent with usual processes. Micromixers play thereby an eminent role. The goal of this study is to better understand the hydrodynamic properties of a split-and-recombine Caterpillar micromixer (CPMM) specially with regard to handling viscoelastic fluids, a topic hardly addressed so far in the context of micromixers in general, although industrial fluids like detergent, cosmetic, or food emulsions are non-Newtonian. Friction factor was measured in a CPMM for both Newtonian and non-Newtonian fluids. For Newtonian fluids, the friction factor in the laminar regime is f/2 = 24/Re. The laminar regime exists up to Reynolds numbers of 15. For shear-thinning fluids like Carbopol 940 or viscoelastic fluids like Poly Acryl Amide (PAAm) aqueous solutions, the friction factor scales identically within statistical errors up to a generalized Reynolds number of 10 and 0.01, respectively. Above that limit, there is an excess pressure drop for the viscoelastic PAAm solution. This excess pressure drop multiplies the friction factor by more than a decade over a decade of Reynolds numbers. The origin of this excess pressure drop is the high elongational flow present in the Caterpillar static mixer applied to a highly viscoelastic fluid. This result can be extended to almost all static mixers, because their flows are generally highly elongational

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Turbulence phenomena in drag reducing systems

1969

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An analysis based on the Townsend-Bakewell model of the eddies in the wall regions of turbulent shear flows shows that viscoelastic fluid properties must lead to significant reductions in the rate of production of turbulent energy. This analysis in turn leads to the proper form of the similarity laws for drag reducing fluids, heretofore deduced empirically.Measurements of the axial and radial turbulence intensities for flow through smooth round tubes are reported, as are measurements o f the time-averaged velocity profiles and the drag coefficients. These indicate that for solutions exhibiting drag reduction a t all Reynolds numbers the flow may be transitional to Reynolds numbers of the order of 105. This Design calculations based upon the present results suggest that in large diameter pipelines, or in boundary layers on large objects, drag reduction may not be attainable under conditions of practical interest until fluids having relaxation times an order of magnitude larger than those presently available, but with comparable viscosity levels, are developed or, alternately, until fluids exhibiting Weissenberg numbers which do not change with deformation rate, can be found.A growing number of studies have been undertaken cesses there. A recent detailed study of the Newtonian which aim to characterize or elucidate the physical asflow wit,hin this wall region (3) has shown that the large pects of drag reduction. Several of these (7, 14, 20, 24, eddies exist as counter-rotating pairs with their axes 35, 39, 46) include sufficient ranges of the primary varialong the mean flow direction. In the lateral direction a ables such as tube size, the polymeric additive used and diffuse influx of material occurs which is concentrated its concentration to illustrate the varied nature and extent between the two eddies and rapidly ejected from the of drag reduction and t,he difficulty of obtaining a genboundary layer region owing to the counter-rotation of era1 and quantitative understanding of the phenomenon. the eddy pair. The eddy pattern remains defined to the Although in several instances (10, 22, 24, 28, 39) drag outer edge of the sublayer and as these patterns may be reduction data have been correlated empirically and associated with about 50% of the total turbulent energy several theoretical analysis have been presented (11, 16, they must control to a large extent the radial momentum 41, 42) little consistent information, pertinent to the transport rates which exist in the wall region. From the processes involved in drag reduction, has evolved. Comstreamline patterns presented by Bakewell a graphical pounding this problem is the utility of measurements using analysis has shown (38) that the streamlines are adethe usual tools of research in turbulence, impact, and hotquately described by: wire probes, which has been severely questioned ( 2 , 15, 23, 25, 36) and remains in doubt for viscoelastic fluids. Thus the several experimental investigations in which such tools were employed ( 2 , 12, 13, 28, 44, 4 6 ) , though clea...

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Flow of Viscoelastic Fluids through Porous Media

Cited by 239 publications

References 19 publications

Flow of non‐newtonian fluids in porous media

Flow of non‐newtonian fluids in porous media

Pressure drop in a split‐and‐recombine caterpillar micromixer in case of newtonian and non‐newtonian fluids

Turbulence phenomena in drag reducing systems

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