Abstract
In this work, we investigate the accuracy of some physical models that are frequently used to describe and interpret dispersive mixing and mass transfer in compositional reservoir simulation. We have designed a quaternary analog fluid system (alcohol–water–hydrocarbon) that mimics the phase behavior of CO2-hydrocarbon mixtures at high pressure and temperature. A porous medium was designed using PolyTetraFlouroEthylene (PTFE) materials to ensure that the analog oil acts as the wetting phase, and the properties of the porous medium were characterized in terms of porosity, permeability and dispersivity. Relative permeability and interfacial tension (IFT) measurements were also performed to delineate interactions between the fluid system and the porous medium. The effluent concentrations from two-component first-contact miscible (FCM) displacement experiments exhibit a tailing behavior that is attributed to imperfect sweep of the porous medium: A feature that is not captured by normal dispersion models. To represent this behavior in displacement calculations, we use dual-porosity (DP) models including mass transfer between flowing and stagnant porosities. Two 4-component two-phase displacement experiments were performed at near-miscible and multicontact miscible (MCM) conditions and the effluent concentrations were interpreted by numerical calculations. We demonstrate that the accuracy of our displacement calculations relative to the experimental observations is sensitive to the selected models for dispersive mixing, mass transfer between flowing and stagnant porosities, and IFT scaling of relative permeability functions. We also demonstrate that numerical calculations substantially agree with the experimental observations for some physical models with limited need for model parameter adjustment. The combined experimental and modeling effort presented in this work identifies and explores the impact of a set of physical mechanisms (dispersion and mass transfer) that must be upscaled adequately for field-scale displacement calculations in DP systems.
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Abbreviations
- d p :
-
Particle diameter
- D o :
-
Molecular diffusion
- f :
-
Flowing fraction
- F :
-
IFT scaling factor
- FF:
-
Formation factor
- K ij :
-
Effective dispersion coefficient of component i in phase j
- K l :
-
Longitudinal dispersion coefficient
- n :
-
Corey exponent
- S :
-
Saturation
- S gc :
-
Critical gas saturation
- S or :
-
Residual oil saturation
- t :
-
Time
- x :
-
Length of tie line (mass fraction)
- x ij :
-
Mole fraction of component i in phase j
- z :
-
Direction along packed column
- α :
-
Longitudinal dispersivity
- β :
-
IFT scaling exponent
- θ i :
-
Mass transfer coefficient of component i
- ρ :
-
Molar density
- σ :
-
Interfacial tension
- σ 0 :
-
Reference interfacial tension
- υ :
-
Average linear velocity
- φ :
-
Porosity
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Reza Rastegar is now with Chevron Energy Technology Company. This work was done when he was a PhD student at USC.
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Shojaei, H., Rastegar, R. & Jessen, K. Mixing and Mass Transfer in Multicontact Miscible Displacements. Transp Porous Med 94, 837–857 (2012). https://doi.org/10.1007/s11242-012-0027-8
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DOI: https://doi.org/10.1007/s11242-012-0027-8