Residual Equilibrium Saturation of Porous Media

Dombrowski, H.; Brownell, L.E.

doi:10.1021/ie50534a037

Cited by 110 publications

(31 citation statements)

References 1 publication

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“…The saturation of wetting fluid in the nooks and crannies of the pore-space is determined from the irreducible wetting phase saturation, Swr. Here we have assumed 0.18 for Berea , although we have recently come to believe that this number is somewhat too high, and 0.075 for sphere-pack (Dombrowski and Brownell, 1954). Micromodel studies indicate that, even excluding the nooks and crannies, the nonwetting fluid does not occupy whole pore-bodies.…”

Section: Saturation Determinationmentioning

confidence: 99%

The effect of pore-structure on hysteresis in relative permeability and capillary pressure: Pore-level modeling

Jerauld¹,

Salter²

1990

Transp Porous Med

390

203

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The effect of pore-structure upon two-phase relative permeability and capillary pressure of strongly-wetting systems at low capillary number is simulated. A pore-level model consisting of a network of pore-bodies interconnected by pore-throats is used to calculate scanning loops of hysteresis between primary drainage, imbibition and secondary drainage. The pore-body to pore-throat aspect ratio strongly influences the pattern of hysteresis. Changes in the patterns of hysteresis often attributed to consolidation can be understood in terms of changes in aspect ratio. Correlation between the sizes of neighboring pore-throats affects the shape of the relative permeability curves, while the width and shape of the pore-size distribution have only a minor influence.

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Section: Saturation Determinationmentioning

confidence: 99%

The effect of pore-structure on hysteresis in relative permeability and capillary pressure: Pore-level modeling

Jerauld¹,

Salter²

1990

Transp Porous Med

390

203

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“…Several authors have performed experiments on capillary porous media using various packing materials (Leverett 1941;Dombrowski and Brownell 1954;El-Genk et al 1983;Dullien et al 1989;Demond and Roberts 1991;Bradford and Leij 1995;Kramer 1998;Lago and Araujo 2001;Ishakoglu and Baytas 2005;Dodds and Srivastava 2006). Results from these experiments are not unambiguous and several differing theories prevail.…”

Section: Review Of Capillary Pressure In Packed Bedsmentioning

confidence: 99%

“…Particle properties, such as size, sphericity, and surface roughness have been found to influence capillary pressure (Dombrowski and Brownell 1954;El-Genk et al 1983;Dullien et al 1989). El-Genk et al (1983) examined how particle size and morphology affect the capillary pressure.…”

Section: Effect Of Bed Propertiesmentioning

confidence: 99%

An Analytical Model for Capillary Pressure–Saturation Relation for Gas–Liquid System in a Packed-Bed of Spherical Particles

Lappalainen¹,

Manninen

Alopaeus³

et al. 2008

Transp Porous Med

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Capillary pressure is considered in packed-beds of spherical particles. In the case of gas-liquid flows in packed-bed reactors, capillary pressure gradients can have a significant influence on liquid distribution and, consequently, on the overall reactor performance. In particular, capillary pressure is important for non-uniform liquid distribution, causing liquid spreading as it flows down the packing. An analytical model for capillary pressure-saturation relation is developed for the pendular and funicular regions and the factors affecting capillary pressure in the capillary region are discussed. The present model is compared to the capillary pressure models of Grosser et al. (AIChE J., 34:1850(AIChE J., 34: -1860(AIChE J., 34: , 1988 and Attou and Ferschneider (Chem. Eng. Sci., 55:491-511, 2000) and to the experiments of Dodds and Srivastava (Part Part Syst. Charact., 23:29-39, 2006) and Dullien et al. (J. Colloid Interface Sci., 127:362-372, 1989). The non-homogeneity of real packings is considered through particle size and porosity distributions. The model is based on the assumption that the particles are covered with a liquid film, which provides hydrodynamic continuity. This makes the model more suitable for porous or rough particles than for non-porous smooth particles. The main improvements of the present model are found in the pendular region, where the liquid dispersion due to capillary pressure gradients is most significant. The model can be used to improve the hydrodynamic models (e.g., CFD and cellular automata models) for packed-bed reactors, such as trickle-bed reactors, where gas, liquid, and solid phases are present. Models for such reactors have become quite common lately (Sáez and Carbonell, AIChE J., 31:52-62, 1985; K. Lappalainen (B) · V. Alopaeus Chemical Engineering and Plant Design, Nomenclatures A c Cross-sectional area (m 2 ) d Half spacing between neighboring microcylinders (m) d p Particle diameter (m) d min As defined in Eq. 5 (m) D H Hydraulic diameter (m) f Wetting efficiency J (S L ) Leverett's J -function k Permeability (m 2 ) N c Number of particle contact points per particle p c Capillary pressure (Pa) p i Pressure of phase i (Pa) r 1,2 Scaled radii of curvature R 1,2 Radii of curvature (m) R Particle radius (m) R * Mean curvature of the meniscus (m) s Perimeter (m) S L Liquid saturation V f Volume of fluid in a pendular ring (m 3 )Greek letters ε Void fraction of the packed-bed ϕ Filling angle (see Fig. 3) (rad) (x) Gamma function θ Liquid-solid contact angle (rad) θ i Holdup of phase i ρ i Density of phase i (kg · m −3 ) σ Surface tension between the wetting and the non-wetting phases (N · m −1 ) X(1 − cos ϕ)

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“…The pH of the buffer mixture produced after the acidbase change was also calculated using Equation (5). The added basic buffer was designated solution 2 and the retained buffer (from the previous liposome acidification) was designated solution 1.…”

Section: Buffer Mixture Ph Produced By Acid-base Changementioning

confidence: 99%