Three‐phase equilibria using equations of state

Heidemann, Robert A.

doi:10.1002/aic.690200504

Cited by 56 publications

(26 citation statements)

References 4 publications

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“…Hence, Equation (4) is not recommended for applications in which quantitative predictions of x hcW are important. It is a known limitation that a single cubic EOS with the van der Waals mixing rules cannot model x wL and x hcW simultaneously over a wide temperature range (Nasrifar and Moshfeghian, 2002;Heidemann, 1974;Daridon et al, 1993;Satyro et al, 2013). Furthermore, the W-phase density is underestimated with the PR EOS, but can be corrected by volume shift, or simply by using the saturated liquid density of water at the temperature of interest.…”

Section: Tablementioning

confidence: 96%

“…The primary purpose of the development of the BIP correlation (Equation (4)) was the quantitative prediction of x wL for water with n-alkanes. The solubilities of hydrocarbons in the W phase (x hcW ) are orders of magnitude lower than x wL (Heidemann, 1974). They may be negligible for most reservoir engineering applications even at elevated temperatures (Luo and Barrufet, 2005).…”

Section: Tablementioning

confidence: 99%

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Characterization of water-containing reservoir oil using an EOS for steam injection processes

Venkatramani

Okuno

2015

Journal of Natural Gas Science and Engineering

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Section: Tablementioning

confidence: 96%

Section: Tablementioning

confidence: 99%

Characterization of water-containing reservoir oil using an EOS for steam injection processes

Venkatramani

Okuno

2015

Journal of Natural Gas Science and Engineering

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“…For both cases, the dissolution of hydrocarbons in the W phase (x hcW ) is disregarded. This assumption is considered reasonable in view of low values for x hcW (Ͻ 1 mol%) indicated by experimental measurements (e.g., Heidemann, 1974). (Keshavarz et al, 2014) 2600 kJ/m 3°C Rock thermal conductivity (Keshavarz et al, 2014) 660 kJ/m day°C Over/underburden heat capacity (Keshavarz et al, 2014) 2600 kJ/m 3°C Over/underburden thermal conductivity (Keshavarz et al, 2014) 660 kJ/m day°C Bitumen thermal conductivity 11.5 kJ/m day°C Gas thermal conductivity 2.89 kJ/m day°C Producer bottom-hole pressure (minimum) 15 bars Steam quality 0.9…”

Section: Fluid Modelmentioning

confidence: 77%

Compositional Mechanisms in SAGD and ES-SAGD With Consideration of Water Solubility in Oil

Venkatramani

Okuno

2016

Day 2 Wed, June 08, 2016

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Experimental data have shown that the solubility of water in the oleic (L) phase (x wL ) can be significant at elevated temperatures. However, x wL was not properly considered in prior studies of SAGD and ES-SAGD. The main objective of this research is to present a detailed study of compositional mechanisms in SAGD and ES-SAGD simulation by considering x wL . The importance of properly considering x wL is shown in economic evaluation of these bitumen-recovery processes.The phase-behavior models used in this research are carefully created on the basis of experimental studies presented in the literature. Mechanistic simulation studies are then conducted for SAGD and ES-SAGD. Co-injectants used in ES-SAGD simulations range from propane through n-decane.Results show that x wL enhances bitumen production in both SAGD and ES-SAGD mainly because x wL results in reduction of L-phase viscosity. The enhancement is more significant when the chamber-edge temperature is higher, because x wL increases with temperature. The enhancement of bitumen production observed in the case studies is 7.66% for SAGD, 4.08% for C 6 -SAGD, and 4.85% for C 8 -SAGD for a fixed period of operation at 35 bars. It is important to consider x wL in SAGD and ES-SAGD simulations, because the relative performance of ES-SAGD to SAGD tends to be overestimated without considering x wL .On the basis of a sensitivity analysis for economic performance of ES-SAGD, a guideline is presented to leverage x wL to improve bitumen production in ES-SAGD. As discussed in our prior research, solvent becomes effective in diluting bitumen and reducing steam requirement, only when it sufficiently accumulates near the chamber edge. New results show that water can act as a diluting agent until solvent sufficiently accumulates near the chamber edge.

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“…Extra, or trivial, phases are detected when two phases tend toward exactly the same composition and molar volume. This multiphase calculation algorithm has been validated in publications by Michelsen (9) and Heidemann (11) . Table 1 summarizes the composition (mass%) of the Swan Hills oil as determined using a simulated distillation gas chromatograph.…”

Section: Outer Loopmentioning

confidence: 99%

Phase Behaviour and Compositional Changes Associated With Residual Oxygen in a Miscible CO/Light Oil Reservoir

Jia

Moore

Mehta

et al. 2007

Journal of Canadian Petroleum Technology

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Concern about the effects of global greenhouse gases has made people aware of the need to reduce the atmospheric concentration of industrial waste gas. Alberta, as the centre of Canada's petroleum industry, is strongly impacted by the politics of greenhouse gases. One way Alberta can achieve the goals of the Kyoto Protocol is to capture CO2 from stack gases and to inject it into oil reservoirs to enhance recovery while sequestering at least a portion of the CO2. This paper will concentrate on oil from the Swan Hills Formation reservoir operated by Devon Oil Corporation. The phase behaviour of different concentrations of CO2/O2 mixtures injected into the Swan Hills reservoir was investigated. Two PVT (Pressure-Volume-Temperature) apparatus were used to visually observe phases and to determine bubble points and swelling of the oil rich phase. The PVT measurements were performed to develop a basic understanding of the phase behaviour for the CO2 / O2 /oil system. The composition of oxidized oil was predicted using a previously developed low temperature oxidation model coupled with phase equilibrium calculations. Introduction Carbon dioxide flooding is a well established enhanced oil recovery process in regions where CO2 is available. Canada has been slow to implement CO2 floods due to the lack of natural sources. However, the public's concern with greenhouse gas emissions and Canada's support for the Kyoto Protocol provide sufficient environmental incentives to allow for the application of CO2 floodingas a combined EOR/sequestration process. Capturing the CO2 from stack gas is an expensive process and the actual cost will depend on the purity of the CO2 stream that is required. Oxygen is an important factor as its impurity can modify the native oil properties through low temperature oxidation reactions, promotion of corrosion in the injection and production piping and alter the phase behaviour of the reservoir fluids. The study described in this paper will examine how oxygen is consumed in the reservoir, and it will concentrate on the impact of oxidation reactions with regard to the composition and emulsification characteristics of the oil. Lee(1) studied the phase behaviour and displacement efficiency of a carbon dioxide-hydrocarbon system which consisted of various mixtures of n-pentane/n-hexane. The results demonstrated that multiple phase behaviour involving two liquids with and without a vapour phase occurred during carbon dioxide injection in low temperature reservoirs. A number of studies on the effectiveness of carbon dioxide displacement under miscible and immiscible conditions have been reported by Wilburn et al.(2), Dyer et al.(3), Srivastava and Huang(4, 5) and Srivastava et.al.(6). The results showed that CO2 /oil miscibility could be developed and that the swelling behaviour depended on the chemical composition of the oil. Wilburn et al.(2) also found that miscibility is strongly dependent on the volatility or boiling point distribution of the oil. Dyer et al.(3) investigated the phase behaviour of typical Saskatchewan heavy oils with carbon dioxide. Their study was divided into two categories: stock tank oil and reservoir oil, which were mixed with CO2 in different ratios. Parameters studied included viscosity, density, swelling factor and gas-oil ratio (GOR).

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Three‐phase equilibria using equations of state

Cited by 56 publications

References 4 publications

Characterization of water-containing reservoir oil using an EOS for steam injection processes

Characterization of water-containing reservoir oil using an EOS for steam injection processes

Compositional Mechanisms in SAGD and ES-SAGD With Consideration of Water Solubility in Oil

Phase Behaviour and Compositional Changes Associated With Residual Oxygen in a Miscible CO/Light Oil Reservoir

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