Compositional Model Studies - CO2 Oil-Displacement Mechanisms

1981 ◽  
Vol 21 (01) ◽  
pp. 89-97 ◽  
Author(s):  
M.P. Leach ◽  
W.F. Yellig

Abstract This paper presents matches, using a fully compositional model, of the performances of seven laboratory CO2 displacements of a 10-component synthetic oil. The criteria for achieving a match of laboratory performance include (1) comparisons of predicted and experimentally determined oil recovery and (2) effluent compositional profiles for each component as functions of hydrocarbon pore volumes (HCPV) of CO2 injected.An equation of state was tuned to predict single-contact (PVT) phase equilibria for CO2/synthetic-oil mixtures. The model incorporates this equation of state to predict the multiple-contact phase equilibria during a CO2 displacement test. Input to the model were independently determined gas/oil relative permeability characteristics and - for each laboratory displacement - injection rate, effluent pressure, pore volume, and temperature.The experimental displacements were conducted in linear Berea core systems using a synthetic (C1-C14) oil at 120 and 150 degrees F. Three displacements at 120 degrees F have been published by Metcalfe and Yarborough. Previously, it was thought that these displacements were conducted at selected pressures so that oil displacements encompassed immiscible, multiple-contact miscible (MCM), and contact miscible mechanisms. However, the model results show that only contact miscible and MCM displacement mechanisms were involved. To confirm the mechanistic understanding at 120 degrees F, three additional laboratory displacements were conducted at 150 degrees F. These encompassed pressures such that the displacement was controlled by an immiscible, an MCM, and a contact miscible mechanism, respectively. The model results at 150 degrees F match the experimental data and confirm the mechanistic understanding. The experimental and numerical results are in agreement with the minimum miscibility pressure theory of Yellig and Metcalfe.The results of this study confirm the importance of experimentally determined effluent compositional profiles and fully compositional models for CO2 mechanism studies. Introduction A mechanistic understanding of oil displacement by CO2 is basic to establishing the CO2 requirements and predicting performance for field projects. The petroleum engineering community relies heavily on fully compositional models and sophisticated laboratory experiments to acquire this mechanistic understanding.Currently, it is not deemed feasible to use fully compositional models to simulate performance of field-wide miscible floods. However, these models should be capable of predicting performances of laboratory-scale displacements. The results of such predictions will identify important variables that control oil recovery and that must be incorporated in mechanistically simpler field performance simulators. Further, confidence in field models will be enhanced greatly by the demonstrated ability to predict laboratory floods.Studies to improve the effectiveness and efficiency of multicomponent compositional simulators have been reported. A cell-to-cell flash model has been used to study mechanisms in rich-gas drives. However, no investigations have been reported previously that demonstrate that a fully compositional model can predict results of rich gas or CO2 laboratory displacements, including prediction of the phases and compositions developed in situ. SPEJ P. 89^

1978 ◽  
Vol 18 (03) ◽  
pp. 173-182 ◽  
Author(s):  
D.D. Fussell ◽  
J.L. Yanosik

Abstract Phase equilibria equations that incorporate the Redlich-Kwong equation of state are nonlinear and, therefore, must be solved by an iterative method. The method of successive substitutions commonly is used. This method, however, almost always diverges near the critical region for bubble point, dew point, and two-phase calculations. Iterative methods that converge for these calculations are presented. These iterative methods are called presented. These iterative methods are called "minimum variable Newton-Raphson" (MVNR) methods because they try to minimize the number of variable for which simultaneous iteration is required and use the Newton-Raphson method for the correction step. Procedures are given for obtaining starting values for the first iteration and several example problems are discussed. Introduction Reservoir performance predictions for gas condensate and volatile oil reservoirs require a knowledge of the vapor-liquid phase equilbria of the reservoir fluids. A similar knowledge also is required when studying multiple-contact, miscible oil recovery methods that involve injection of hydrocarbons and/or carbon dioxide. Such knowledge is obtained experimentally or calculated from physical properties of the components of the physical properties of the components of the reservoir fluid system. Calculation is desirable because experimental determination is both laborious and expensive. A common basis for calculation of vapor-liquid phase equilibria is the single-stage separation unit. phase equilibria is the single-stage separation unit. This unit represents a PVT cell in which a fluid mixture of known over-all composition is equilibrated at the temperature and pressure of interest. Liquid and vapor compositions and moles of liquid and vapor per mole of fluid mixture are determined. Reliable estimates of other fluid properties (such as phase densities and viscosities) are obtained readily with these properties. The Redlich-Kwong equation of state is used widely in the petroleum industry for phase equilibria calculations. The phase equilibria equations that incorporate this equation of state are nonlinear. As a result, they must be solved by an iterative method. The method of successive substitutions commonly is used. This method, however, almost always diverges for bubble point, dew point, and two-phase calculations near the critical region. This region is extremely important when studying multiple-contact, miscible oil recovery methods involving CO2 or rich-gas injection because the path of the over-all fluid mixture passes through path of the over-all fluid mixture passes through this region. The method of successive substitutions also will diverge for some fluid mixtures near their saturation (bubble point or dew point) pressure at conditions removed from the critical region. This paper presents a reliable iterative sequence that can be used to predict phase equilibria of multiple-contact, miscible oil recovery methods. The method includes sequences for calculation of the saturation pressure and phase equilibria in the two phase region. These MVNR methods rely on minimization of the number of unknowns for which simultaneous iteration is required and use the Newton-Raphson method for the correction step. Minimization is subject to the constraint that all additional unknowns can be calculated by using simple linear equations or, at most, an iteration method applied to one equation in one unknown. MVNR is compared with the method of successive substitutions for a two-phase fluid mixture at various pressures for a fixed temperature. MVNR also is compared with the method of successive substitutions for saturation-envelope calculations near the critical region. DESCRIPTION OF PHYSICAL SYSTEM The single-stage separation unit is the basis for the phase equilibria calculations discussed in this study. This unit represents a PVT cell in which a fluid mixture of known over-all composition is equilibrated at the temperature and pressure of interest. SPEJ P. 173


1982 ◽  
Vol 22 (05) ◽  
pp. 731-742 ◽  
Author(s):  
L.E. Baker ◽  
A.C. Pierce ◽  
K.D. Luks

Abstract Equations of state are used to predict or to match equilibrium fluid phase behavior for systems as diverse as distillation columns and miscible gas floods of oil reservoirs. The success of such simulations depends on correct predictions of the number and the compositions of phases present at a given temperature, pressure, and overall fluid composition. For example, recent research has shown that three or more phases may exist in equilibrium in CO floods. This paper shows why an equation of state can predict the incorrect number of phases or incorrect phase compositions. The incorrect phase descriptions still satisfy the usual restrictions on equality of chemical potentials of components in each phase and conservation of moles in the system. A new method and its mathematical proof are presented for determining when a phase equilibrium solution is incorrect. Examples of instances where incorrect predictions may be made are described. These include a binary system in which a two-phase solution may be predicted for a single-phase fluid and a multicomponent CO /reservoir oil system in which three or more phases may coexist. Introduction Advances in reservoir oil recovery methods have necessitated advances in methods for prediction of phase equilibria associated with those methods. It was long considered sufficient to approximate the reservoir behavior of oil and gas systems with models in which compositions of the phases in equilibrium were unimportant. In such a model, the amounts and properties of the phases are dependent on pressure and temperature only. Later, experience in production from condensate and volatile oil reservoirs showed that models incorporating compositional effects were required to simulate the phase equilibria adequately. This led to the use of convergence pressure correlations and subsequently to the development of more sophisticated equation of state methods for modeling and predicting phase equilibria. For adequate description of the compositional effects that occur in enhanced oil recovery processes such as CO and rich gas flooding, an equation-of-state approach is a virtual necessity. equilibrium The use of equations of state for phase prediction is not limited to the petroleum industry. Such equations also find wide use in basic chemical and physical research, and in the refining and chemical processing industries. Solution techniques for phase equilibrium problems are varied and depend to some extent on the application and equation of state used however, there are three restrictions that all phase equilibrium solutions must satisfy. First, material balance must be preserved. Second, for phases in equilibrium there must be no driving force to cause a net movement of any component from one phase to any other phase. In thermodynamic parlance, the chemical potentials for each component must be the same in all phases. Third, the system of predicted phases at the equilibrium state must have the lowest possible Gibbs energy at the system temperature and pressure. The requirement that the Gibbs energy of a system. at a given temperature and pressure, must be a minimum is a statement of the second law of thermodynamics, equivalent to the more common version requiring the entropy of an isolated system to be a maximum. The equivalence is demonstrated formally in Ref. 1, for example. If the Gibbs energy of a predicted equilibrium state is greater than that of another state that also satisfies Requirements 1 and 2, the state with the greater Gibbs energy is not thermodynamically stable. Requirements 1 and 2, material balance and equality of chemical potentials, are used commonly as the sole criteria for solution of phase equilibrium problems. SPEJ P. 731^


Energies ◽  
2021 ◽  
Vol 14 (4) ◽  
pp. 1055
Author(s):  
Qian Sun ◽  
William Ampomah ◽  
Junyu You ◽  
Martha Cather ◽  
Robert Balch

Machine-learning technologies have exhibited robust competences in solving many petroleum engineering problems. The accurate predictivity and fast computational speed enable a large volume of time-consuming engineering processes such as history-matching and field development optimization. The Southwest Regional Partnership on Carbon Sequestration (SWP) project desires rigorous history-matching and multi-objective optimization processes, which fits the superiorities of the machine-learning approaches. Although the machine-learning proxy models are trained and validated before imposing to solve practical problems, the error margin would essentially introduce uncertainties to the results. In this paper, a hybrid numerical machine-learning workflow solving various optimization problems is presented. By coupling the expert machine-learning proxies with a global optimizer, the workflow successfully solves the history-matching and CO2 water alternative gas (WAG) design problem with low computational overheads. The history-matching work considers the heterogeneities of multiphase relative characteristics, and the CO2-WAG injection design takes multiple techno-economic objective functions into accounts. This work trained an expert response surface, a support vector machine, and a multi-layer neural network as proxy models to effectively learn the high-dimensional nonlinear data structure. The proposed workflow suggests revisiting the high-fidelity numerical simulator for validation purposes. The experience gained from this work would provide valuable guiding insights to similar CO2 enhanced oil recovery (EOR) projects.


RSC Advances ◽  
2017 ◽  
Vol 7 (14) ◽  
pp. 8118-8130 ◽  
Author(s):  
Hongbin Yang ◽  
Wanli Kang ◽  
Hairong Wu ◽  
Yang Yu ◽  
Zhou Zhu ◽  
...  

The dispersed low-elastic microsphere system shows shear-thickening behavior because of the microstructure change and the interaction of internal forces.


1984 ◽  
Vol 24 (06) ◽  
pp. 606-616 ◽  
Author(s):  
Charles P. Thomas ◽  
Paul D. Fleming ◽  
William K. Winter

Abstract A mathematical model describing one-dimensional (1D), isothermal flow of a ternary, two-phase surfactant system in isotropic porous media is presented along with numerical solutions of special cases. These solutions exhibit oil recovery profiles similar to those observed in laboratory tests of oil displacement by surfactant systems in cores. The model includes the effects of surfactant transfer between aqueous and hydrocarbon phases and both reversible and irreversible surfactant adsorption by the porous medium. The effects of capillary pressure and diffusion are ignored, however. The model is based on relative permeability concepts and employs a family of relative permeability curves that incorporate the effects of surfactant concentration on interfacial tension (IFT), the viscosity of the phases, and the volumetric flow rate. A numerical procedure was developed that results in two finite difference equations that are accurate to second order in the timestep size and first order in the spacestep size and allows explicit calculation of phase saturations and surfactant concentrations as a function of space and time variables. Numerical dispersion (truncation error) present in the two equations tends to mimic the neglected present in the two equations tends to mimic the neglected effects of capillary pressure and diffusion. The effective diffusion constants associated with this effect are proportional to the spacestep size. proportional to the spacestep size. Introduction In a previous paper we presented a system of differential equations that can be used to model oil recovery by chemical flooding. The general system allows for an arbitrary number of components as well as an arbitrary number of phases in an isothermal system. For a binary, two-phase system, the equations reduced to those of the Buckley-Leverett theory under the usual assumptions of incompressibility and each phase containing only a single component, as well as in the more general case where both phases have significant concentrations of both components, but the phases are incompressible and the concentration in one phase is a very weak function of the pressure of the other phase at a given temperature. pressure of the other phase at a given temperature. For a ternary, two-phase system a set of three differential equations was obtained. These equations are applicable to chemical flooding with surfactant, polymer, etc. In this paper, we present a numerical solution to these equations paper, we present a numerical solution to these equations for I D flow in the absence of gravity. Our purpose is to develop a model that includes the physical phenomena influencing oil displacement by surfactant systems and bridges the gap between laboratory displacement tests and reservoir simulation. It also should be of value in defining experiments to elucidate the mechanisms involved in oil displacement by surfactant systems and ultimately reduce the number of experiments necessary to optimize a given surfactant system.


The Analyst ◽  
2021 ◽  
Author(s):  
Khashayar R. Bajgiran ◽  
Hannah C. Hymel ◽  
Shayan Sombolestani ◽  
Nathalie Dante ◽  
Nora Safa ◽  
...  

The developed platform offers a simple fluorescent visualization technique to specifically identify the oil and water phases without altering their surface properties which improves on the achievable resolution in EOR applications.


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