The vapour pressure and liquid heat capacity of seven biodiesel fuels and its components (fatty a... more The vapour pressure and liquid heat capacity of seven biodiesel fuels and its components (fatty acid methyl esters -FAMEs) were modeled using the Advance Peng Robinson equation of state. The dataset used for the modeling was obtained from the literature and included FAME properties and the composition, vapour pressure, and liquid heat capacity of the biodiesel fuels from different sources at temperatures from 50 to 130ºC and -30 to 75ºC, respectively. New values for the critical properties and acentric factor of FAMEs are introduced as well as new models for the ideal gas heat capacity for the FAMEs. The average AARD is 12% for vapour pressure and 3% for liquid heat capacity.
The design and optimization of solvent assisted thermal recovery processes for heavy oil and bitu... more The design and optimization of solvent assisted thermal recovery processes for heavy oil and bitumen require accurate predictions of viscosity as a function of temperature, pressure, and composition. In this case study, the performance of the Expanded Fluid (EF) viscosity model is tested on viscosity data for an Alberta bitumen diluted with carbon dioxide (5.2 wt%), ethane (5.1 wt%), propane (7.6 and 16 wt%), n-butane (14.5 wt%), n-pentane (15 and 30 wt%) and n-heptane (15 and 30 wt%) at temperatures from 20 to 175°C and pressures up to 10 MPa. The main input to the EF model is the density of the fluid and densities were measured at the same conditions as the viscosity measurements.The viscosity of the bitumen was fitted with average absolute relative deviation (AARD) of 8%. The viscosities of the diluted bitumen mixtures were predicted without tuning with an overall AARD of 17% when using measured densities as an input. The viscosity predictions were improved to an AARD of 7% using...
Canadian Unconventional Resources Conference, 2011
The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate p... more The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate predictions of phase behavior as straightforward as saturation pressures and as potentially complex as vapour-liquid-liquid equilibria and asphaltene precipitation. In this case study, saturation pressures of dead and live bitumen were measured in a Jefri PVT cell at different concentrations of a multi-component solvent at temperatures from 20 to 180°C. Saturation pressures and the onset of asphaltene precipitation were also measured for the bitumen diluted with n-pentane. The onset of precipitation was determined by titrating the bitumen with pentane and periodically circulating the mixture past a high pressure microscope. The data were modeled with the Advanced Peng-Robinson equation of state (APR EoS). The maltene fraction of the bitumen was characterized into pseudo-components based on extrapolated distillation data. The asphaltenes were characterized based on a Gamma distribution of the molecular weights of selfassociated asphaltenes. The APR EoS was tuned to match the saturation pressures by adjusting the binary interaction parameter between the solvent and the pseudo-components via a correlation based on critical temperatures. Rather than adjusting the interaction parameters for each pair of components, only the exponent in the correlation was adjusted. The role of mixing rules in correctly predicting the onset and amount of asphaltene precipitation is discussed.
Accurate phase equilibrium modeling for complex mixtures such as hydrocarbon and organic compound... more Accurate phase equilibrium modeling for complex mixtures such as hydrocarbon and organic compounds such as alcohols and ethers is necessary for the design and optimization of processes as well as for the development of new fuels and fuel blends. A straightforward methodology is proposed to tune a phase equilibrium model based on a relatively small amount of data. The data are collected using the Advanced Distillation Curve method developed by Bruno (2006) where boiling points are measured in the boiling liquid and are therefore thermodynamic state points. The data are modeled using the trajectory optimization method developed by Satyro and Yarranton (2009). The approach was first tested on methanol/water, iso-propanol/water and triethylene glycol/water mixtures. Each mixture was distilled at atmospheric pressure. The NRTL model was used to describe the phase behaviour, and the interaction parameters (interaction energies and randomness factor) were adjusted to fit the model to the distillation data. The tuned model was tested on literature vapour-liquid equilibrium data for each mixture and predicted the bubble and dew saturation temperatures with less than ±2 o C deviation. The approach was then tested on more complex hydrocarbon mixtures such as gasoline, gasoline with methanol and gasoline with ethanol. The Peng Robinson equation of state was used to describe the phase behaviour. The methodology correctly described the phase behaviour including azeotropism of these complex mixtures by tuning the interaction parameters between the gasoline pseudo-components and the organic compounds. The combination of the Bruno distillation method with the trajectory optimization technique provides a useful tool for the characterization of ill defined fluids such as petroleum and for the prediction of basic phase behaviour, including saturation temperatures, azeotropes, and vapour-liquid equilibria.
In natural gas dehydration units, rich TEG solutions are decompressed before the TEG regeneration... more In natural gas dehydration units, rich TEG solutions are decompressed before the TEG regeneration stage and the direction of the temperature change during the decompression has been debated. The temperature change from an isenthalpic expansion from (7000kPa to 440kPa was measured for the following aqueous mixtures: pure water, 99% pure triethylene glycol (TEG), aqueous TEG (99wt% TEG+1% water), aqueous TEG saturated with methane, aqueous TEG saturated with n-pentane, and aqueous TEG saturated with n-heptane. In all cases, the temperature increased upon expansion with the magnitude of the temperature change ranging from 1.4K for pure water to 2.4K for TEG. A simple equation of state model predicted the correct direction for the temperature change and the predicted values were within ±1K of the experimental data.
The Expanded Fluid (EF) viscosity correlation was used to model the viscosity of mixtures commonl... more The Expanded Fluid (EF) viscosity correlation was used to model the viscosity of mixtures commonly encountered in natural gas processing. This correlation provides viscosity values as a function of fluid density and characterizes each pure compound with three fluid-specific parameters: c 2 , o s and c 3 , when using experimental densities (Version 1) and two parameters, c 2 and o s , when using a cubic equation of state (Version 2). In particular, the original EF correlation for hydrocarbons was adapted for non-hydrocarbon components, including: carbon dioxide, hydrogen sulfide, nitrogen, helium, water, methanol, ethylene glycol, diethylene glycol and triethylene glycol. A temperature dependency was introduced for parameter c 2 for components with significant hydrogen bonding such as water and methanol. For all other components, a fixed c 2 was found to be adequate. Both versions of the correlation were fit to experimental data for the non-hydrocarbon components with overall average absolute relative deviation (AARD) below 6%. The viscosities of several sweet and sour natural gas mixtures were predicted with overall AARDs of 6.3% and 5.1% for Versions 1 and 2, respectively. The viscosities of aqueous solutions both of methanol and of glycols were also modeled. A binary interaction parameter was required to fit the data for all aqueous mixtures in Version 2 but only for mixtures of water and methanol in Version 1. The overall AARDs of the calculated viscosities of the aqueous solutions of methanol and glycols by Versions 1 and 2 were 6% and 8.7%, respectively.
The viscosity of pure hydrocarbons was correlated using a simple function based on the fluid dens... more The viscosity of pure hydrocarbons was correlated using a simple function based on the fluid density. The correlation has three adjustable parameters, a compressed state density, F s °, an empirical parameter, c 2 , that scales the viscosity response to fluid expansion, and another empirical parameter, c 3 , used to tune at pressures above 10 MPa. The inputs to the correlation are the fluid density, pressure, and low-pressure gas viscosity. The correlation fit experimental viscosities for 39 pure hydrocarbons including n-alkanes, branched alkanes, alkenes, cyclics, and aromatics, within experimental error over a broad range of temperatures and pressures. Heavy hydrocarbons such as mineral oils were also fit with an AAPRD of 2.7%. Binary mixture viscosities were predicted to within 10% using simple volumetric mixing rules. The method provides a single framework for liquid and vapor phases, is simple to implement, and is very fast computationally, making it ideal for incorporation into process and reservoir simulators.
ABSTRACT An enhanced form of the temperature-dependent attractive pressure term of the Peng−Robin... more ABSTRACT An enhanced form of the temperature-dependent attractive pressure term of the Peng−Robinson equation of state (PR EOS) was developed. The function was developed using experimental vapor pressures from the NIST Standard Reference Data Base #103 as well as vapor pressures estimated based on the Nji et al. (2008) vapor pressure prediction correlation. 6000 vapor pressure data points from 237 diverse hydrocarbons were used in this study to develop the new attractive term. The quality of predicted vapor pressures using the modified PR EOS for heavy hydrocarbons showed a significant improvement when compared against the standard equation of state. Between reduced temperatures of 0.3 and 0.8, the average and maximum absolute percentage deviations for the predicted vapor pressures for the modified PR EOS are 4.9% and 78.0%, respectively, as compared to 10.4% and 230% for the standard PR EOS. For hydrocarbons from methane to tetralin corresponding to C1−C10, the average and maximum absolute percentage deviations in the vapor pressures using the standard Peng−Robinson are 5.7% and 70.7%, respectively. Using the modified PR EOS, the average and maximum percentage deviations in the calculated vapor pressures are 4.6% and 35.6%, respectively. This enhanced attractive pressure term combined with the critical property estimation method presented by Nji et al. (2008) provides a simple and self-consistent method for the prediction of thermodynamic properties of heavy hydrocarbons.
The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate p... more The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate predictions of phase behaviour as straightforward as saturation pressures and as potentially complex as vapour-liquid-liquid equilibria and asphaltene precipitation. Among the various methods of predicting the phase behaviour of crude oils, the equation of state (EoS) is the most commonly used. To use an EoS, the amounts, critical properties, acentric factor, molecular weight and binary interaction parameters of the constituent components are required to characterize the fluid. For conventional oils, techniques such as distillation are used to obtain a normal boiling point curve which can be divided into pseudo-components. The boiling point curve is extrapolated over the relatively small heavy residue fraction and then correlations are used to determine the properties of each pseudo-component. However, for heavy oils, only about 30 to 50% of the oil can be distilled even with vacuum distillation. Hence, there is a need for a methodology to characterize the large residue fraction of heavy oils for EoS models. The objective of this thesis is to adapt a heavy oil characterization method for an equation of state model for not only conventional vapour-liquid and liquid-liquid equilibria but also asphaltene precipitation for mixtures of heavy oil and solvents. Literature data on saturation pressures and liquid-liquid phase boundaries were collected for pseudobinaries of bitumen and carbon dioxide, methane, ethane, and propane. Saturation pressures and the onset of asphaltene precipitation were measured for a pseudo-binary of bitumen and n-pentane. Saturation pressures were measured in a Jefri PVT cell at temperatures from 20 to 180°C. The onset of precipitation was determined at 20 and 180°C by titrating the bitumen with n-pentane and periodically circulating the mixture past a high pressure microscope. Saturation pressures were also measured for a live bitumen diluted with a multi-component solvent also at temperatures from 20 to 180°C. The data were modeled with the Advanced Peng-Robinson equation of state. The maltene fraction of the bitumen was characterized into pseudo-components based on extrapolated distillation data. The asphaltenes were characterized based on a Gamma distribution of iv the molecular weights of self-associated asphaltenes. The APR EoS was tuned to fit the saturation pressure and asphaltene onset data of the pseudo-binaries by adjusting the binary interaction parameter between the solvent and the bitumen pseudo-components. A temperature dependent binary interaction parameter correlation was developed for the interaction parameters. The model with temperature dependent binary interaction parameters fit the saturation pressures, liquid-liquid boundaries, asphaltene onset over a wide range of temperatures. The model predicted saturation pressures of live oil and live oil diluted with condensate solvent generally within experimental error. The model also predicted the asphaltene onset in propane diluted bitumen although the asphaltene yield at higher dilution was underestimated. The model extends the capability for modeling the phase behaviour of solvent based heavy oil processes to a broad range of operating conditions.
this paper is invited and may be presented at the meeting if filed in writing with the technical ... more this paper is invited and may be presented at the meeting if filed in writing with the technical program chairman prior to the conclusion of the meeting. This paper and any discussion filed will be considered for publication in Petroleum Society journals. Publication rights are reserved. This is a pre-print and subject to correction.
this paper is invited and may be presented at the meeting if filed in writing with the technical ... more this paper is invited and may be presented at the meeting if filed in writing with the technical program chairman prior to the conclusion of the meeting. This paper and any discussion filed will be considered for publication in Petroleum Society journals. Publication rights are reserved. This is a pre-print and subject to correction.
... 5. Thomas, FB, Bennion, DB, Bennion, DW, and Hunter, BE, "Experimental and Theoretical S... more ... 5. Thomas, FB, Bennion, DB, Bennion, DW, and Hunter, BE, "Experimental and Theoretical Studies of solid Precipitation From Reservoir Fluid," J. of Canadian Petroleum Technology, 31 (1), Jan. 1992. 6. Fotland, P., Anfindsen, H., and Fadnes, FH, "Detection of Asphaltene ...
The vapour pressure and liquid heat capacity of seven biodiesel fuels and its components (fatty a... more The vapour pressure and liquid heat capacity of seven biodiesel fuels and its components (fatty acid methyl esters -FAMEs) were modeled using the Advance Peng Robinson equation of state. The dataset used for the modeling was obtained from the literature and included FAME properties and the composition, vapour pressure, and liquid heat capacity of the biodiesel fuels from different sources at temperatures from 50 to 130ºC and -30 to 75ºC, respectively. New values for the critical properties and acentric factor of FAMEs are introduced as well as new models for the ideal gas heat capacity for the FAMEs. The average AARD is 12% for vapour pressure and 3% for liquid heat capacity.
The design and optimization of solvent assisted thermal recovery processes for heavy oil and bitu... more The design and optimization of solvent assisted thermal recovery processes for heavy oil and bitumen require accurate predictions of viscosity as a function of temperature, pressure, and composition. In this case study, the performance of the Expanded Fluid (EF) viscosity model is tested on viscosity data for an Alberta bitumen diluted with carbon dioxide (5.2 wt%), ethane (5.1 wt%), propane (7.6 and 16 wt%), n-butane (14.5 wt%), n-pentane (15 and 30 wt%) and n-heptane (15 and 30 wt%) at temperatures from 20 to 175°C and pressures up to 10 MPa. The main input to the EF model is the density of the fluid and densities were measured at the same conditions as the viscosity measurements.The viscosity of the bitumen was fitted with average absolute relative deviation (AARD) of 8%. The viscosities of the diluted bitumen mixtures were predicted without tuning with an overall AARD of 17% when using measured densities as an input. The viscosity predictions were improved to an AARD of 7% using...
Canadian Unconventional Resources Conference, 2011
The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate p... more The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate predictions of phase behavior as straightforward as saturation pressures and as potentially complex as vapour-liquid-liquid equilibria and asphaltene precipitation. In this case study, saturation pressures of dead and live bitumen were measured in a Jefri PVT cell at different concentrations of a multi-component solvent at temperatures from 20 to 180°C. Saturation pressures and the onset of asphaltene precipitation were also measured for the bitumen diluted with n-pentane. The onset of precipitation was determined by titrating the bitumen with pentane and periodically circulating the mixture past a high pressure microscope. The data were modeled with the Advanced Peng-Robinson equation of state (APR EoS). The maltene fraction of the bitumen was characterized into pseudo-components based on extrapolated distillation data. The asphaltenes were characterized based on a Gamma distribution of the molecular weights of selfassociated asphaltenes. The APR EoS was tuned to match the saturation pressures by adjusting the binary interaction parameter between the solvent and the pseudo-components via a correlation based on critical temperatures. Rather than adjusting the interaction parameters for each pair of components, only the exponent in the correlation was adjusted. The role of mixing rules in correctly predicting the onset and amount of asphaltene precipitation is discussed.
Accurate phase equilibrium modeling for complex mixtures such as hydrocarbon and organic compound... more Accurate phase equilibrium modeling for complex mixtures such as hydrocarbon and organic compounds such as alcohols and ethers is necessary for the design and optimization of processes as well as for the development of new fuels and fuel blends. A straightforward methodology is proposed to tune a phase equilibrium model based on a relatively small amount of data. The data are collected using the Advanced Distillation Curve method developed by Bruno (2006) where boiling points are measured in the boiling liquid and are therefore thermodynamic state points. The data are modeled using the trajectory optimization method developed by Satyro and Yarranton (2009). The approach was first tested on methanol/water, iso-propanol/water and triethylene glycol/water mixtures. Each mixture was distilled at atmospheric pressure. The NRTL model was used to describe the phase behaviour, and the interaction parameters (interaction energies and randomness factor) were adjusted to fit the model to the distillation data. The tuned model was tested on literature vapour-liquid equilibrium data for each mixture and predicted the bubble and dew saturation temperatures with less than ±2 o C deviation. The approach was then tested on more complex hydrocarbon mixtures such as gasoline, gasoline with methanol and gasoline with ethanol. The Peng Robinson equation of state was used to describe the phase behaviour. The methodology correctly described the phase behaviour including azeotropism of these complex mixtures by tuning the interaction parameters between the gasoline pseudo-components and the organic compounds. The combination of the Bruno distillation method with the trajectory optimization technique provides a useful tool for the characterization of ill defined fluids such as petroleum and for the prediction of basic phase behaviour, including saturation temperatures, azeotropes, and vapour-liquid equilibria.
In natural gas dehydration units, rich TEG solutions are decompressed before the TEG regeneration... more In natural gas dehydration units, rich TEG solutions are decompressed before the TEG regeneration stage and the direction of the temperature change during the decompression has been debated. The temperature change from an isenthalpic expansion from (7000kPa to 440kPa was measured for the following aqueous mixtures: pure water, 99% pure triethylene glycol (TEG), aqueous TEG (99wt% TEG+1% water), aqueous TEG saturated with methane, aqueous TEG saturated with n-pentane, and aqueous TEG saturated with n-heptane. In all cases, the temperature increased upon expansion with the magnitude of the temperature change ranging from 1.4K for pure water to 2.4K for TEG. A simple equation of state model predicted the correct direction for the temperature change and the predicted values were within ±1K of the experimental data.
The Expanded Fluid (EF) viscosity correlation was used to model the viscosity of mixtures commonl... more The Expanded Fluid (EF) viscosity correlation was used to model the viscosity of mixtures commonly encountered in natural gas processing. This correlation provides viscosity values as a function of fluid density and characterizes each pure compound with three fluid-specific parameters: c 2 , o s and c 3 , when using experimental densities (Version 1) and two parameters, c 2 and o s , when using a cubic equation of state (Version 2). In particular, the original EF correlation for hydrocarbons was adapted for non-hydrocarbon components, including: carbon dioxide, hydrogen sulfide, nitrogen, helium, water, methanol, ethylene glycol, diethylene glycol and triethylene glycol. A temperature dependency was introduced for parameter c 2 for components with significant hydrogen bonding such as water and methanol. For all other components, a fixed c 2 was found to be adequate. Both versions of the correlation were fit to experimental data for the non-hydrocarbon components with overall average absolute relative deviation (AARD) below 6%. The viscosities of several sweet and sour natural gas mixtures were predicted with overall AARDs of 6.3% and 5.1% for Versions 1 and 2, respectively. The viscosities of aqueous solutions both of methanol and of glycols were also modeled. A binary interaction parameter was required to fit the data for all aqueous mixtures in Version 2 but only for mixtures of water and methanol in Version 1. The overall AARDs of the calculated viscosities of the aqueous solutions of methanol and glycols by Versions 1 and 2 were 6% and 8.7%, respectively.
The viscosity of pure hydrocarbons was correlated using a simple function based on the fluid dens... more The viscosity of pure hydrocarbons was correlated using a simple function based on the fluid density. The correlation has three adjustable parameters, a compressed state density, F s °, an empirical parameter, c 2 , that scales the viscosity response to fluid expansion, and another empirical parameter, c 3 , used to tune at pressures above 10 MPa. The inputs to the correlation are the fluid density, pressure, and low-pressure gas viscosity. The correlation fit experimental viscosities for 39 pure hydrocarbons including n-alkanes, branched alkanes, alkenes, cyclics, and aromatics, within experimental error over a broad range of temperatures and pressures. Heavy hydrocarbons such as mineral oils were also fit with an AAPRD of 2.7%. Binary mixture viscosities were predicted to within 10% using simple volumetric mixing rules. The method provides a single framework for liquid and vapor phases, is simple to implement, and is very fast computationally, making it ideal for incorporation into process and reservoir simulators.
ABSTRACT An enhanced form of the temperature-dependent attractive pressure term of the Peng−Robin... more ABSTRACT An enhanced form of the temperature-dependent attractive pressure term of the Peng−Robinson equation of state (PR EOS) was developed. The function was developed using experimental vapor pressures from the NIST Standard Reference Data Base #103 as well as vapor pressures estimated based on the Nji et al. (2008) vapor pressure prediction correlation. 6000 vapor pressure data points from 237 diverse hydrocarbons were used in this study to develop the new attractive term. The quality of predicted vapor pressures using the modified PR EOS for heavy hydrocarbons showed a significant improvement when compared against the standard equation of state. Between reduced temperatures of 0.3 and 0.8, the average and maximum absolute percentage deviations for the predicted vapor pressures for the modified PR EOS are 4.9% and 78.0%, respectively, as compared to 10.4% and 230% for the standard PR EOS. For hydrocarbons from methane to tetralin corresponding to C1−C10, the average and maximum absolute percentage deviations in the vapor pressures using the standard Peng−Robinson are 5.7% and 70.7%, respectively. Using the modified PR EOS, the average and maximum percentage deviations in the calculated vapor pressures are 4.6% and 35.6%, respectively. This enhanced attractive pressure term combined with the critical property estimation method presented by Nji et al. (2008) provides a simple and self-consistent method for the prediction of thermodynamic properties of heavy hydrocarbons.
The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate p... more The design of solvent-based and solvent assisted heavy oil recovery processes requires accurate predictions of phase behaviour as straightforward as saturation pressures and as potentially complex as vapour-liquid-liquid equilibria and asphaltene precipitation. Among the various methods of predicting the phase behaviour of crude oils, the equation of state (EoS) is the most commonly used. To use an EoS, the amounts, critical properties, acentric factor, molecular weight and binary interaction parameters of the constituent components are required to characterize the fluid. For conventional oils, techniques such as distillation are used to obtain a normal boiling point curve which can be divided into pseudo-components. The boiling point curve is extrapolated over the relatively small heavy residue fraction and then correlations are used to determine the properties of each pseudo-component. However, for heavy oils, only about 30 to 50% of the oil can be distilled even with vacuum distillation. Hence, there is a need for a methodology to characterize the large residue fraction of heavy oils for EoS models. The objective of this thesis is to adapt a heavy oil characterization method for an equation of state model for not only conventional vapour-liquid and liquid-liquid equilibria but also asphaltene precipitation for mixtures of heavy oil and solvents. Literature data on saturation pressures and liquid-liquid phase boundaries were collected for pseudobinaries of bitumen and carbon dioxide, methane, ethane, and propane. Saturation pressures and the onset of asphaltene precipitation were measured for a pseudo-binary of bitumen and n-pentane. Saturation pressures were measured in a Jefri PVT cell at temperatures from 20 to 180°C. The onset of precipitation was determined at 20 and 180°C by titrating the bitumen with n-pentane and periodically circulating the mixture past a high pressure microscope. Saturation pressures were also measured for a live bitumen diluted with a multi-component solvent also at temperatures from 20 to 180°C. The data were modeled with the Advanced Peng-Robinson equation of state. The maltene fraction of the bitumen was characterized into pseudo-components based on extrapolated distillation data. The asphaltenes were characterized based on a Gamma distribution of iv the molecular weights of self-associated asphaltenes. The APR EoS was tuned to fit the saturation pressure and asphaltene onset data of the pseudo-binaries by adjusting the binary interaction parameter between the solvent and the bitumen pseudo-components. A temperature dependent binary interaction parameter correlation was developed for the interaction parameters. The model with temperature dependent binary interaction parameters fit the saturation pressures, liquid-liquid boundaries, asphaltene onset over a wide range of temperatures. The model predicted saturation pressures of live oil and live oil diluted with condensate solvent generally within experimental error. The model also predicted the asphaltene onset in propane diluted bitumen although the asphaltene yield at higher dilution was underestimated. The model extends the capability for modeling the phase behaviour of solvent based heavy oil processes to a broad range of operating conditions.
this paper is invited and may be presented at the meeting if filed in writing with the technical ... more this paper is invited and may be presented at the meeting if filed in writing with the technical program chairman prior to the conclusion of the meeting. This paper and any discussion filed will be considered for publication in Petroleum Society journals. Publication rights are reserved. This is a pre-print and subject to correction.
this paper is invited and may be presented at the meeting if filed in writing with the technical ... more this paper is invited and may be presented at the meeting if filed in writing with the technical program chairman prior to the conclusion of the meeting. This paper and any discussion filed will be considered for publication in Petroleum Society journals. Publication rights are reserved. This is a pre-print and subject to correction.
... 5. Thomas, FB, Bennion, DB, Bennion, DW, and Hunter, BE, "Experimental and Theoretical S... more ... 5. Thomas, FB, Bennion, DB, Bennion, DW, and Hunter, BE, "Experimental and Theoretical Studies of solid Precipitation From Reservoir Fluid," J. of Canadian Petroleum Technology, 31 (1), Jan. 1992. 6. Fotland, P., Anfindsen, H., and Fadnes, FH, "Detection of Asphaltene ...
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