It is found that the minimum absolute average relative deviation (AARD) of 6.7% is obtained by the methodology developed in this work, compared to the AARD of 35.6% obtained by running the commercial simulator.
Subsequently, the comparisons have been performed between this work and a commercial simulator in terms of the overall prediction accuracy of saturation pressures for the quaternary C 3H 8- n-C 4H 10-CO 2-heavy oil systems. The optimal exponents in binary interaction parameter (BIP) correlations are obtained by best matching the measured saturation pressures. The heavy oil which is a complex mixture with unknown molecular structure is characterized as six pseudocomponents by using an exponential distribution splitting function and a logarithm-type lumping method. Theoretically, the volume-translated Peng-Robinson equation of state (PR EOS) coupled with a recently modified alpha function is applied as the primary thermodynamic model to reproduce the experimental measurements. A pressure-volume-temperature (PVT) setup is used to measure vapor-liquid phase boundaries (i.e., saturation pressures) and swelling factors at high pressures up to 11.1 MPa and elevated temperatures up to 373.35 K. Experimentally, a pure substance of CO 2 and a gas mixture consisting of 27.7 mol% C 3H 8, 23.9 mol% n-C 4H 10, and 48.4 mol% CO 2 are respectively introduced to dilute the highly viscous heavy oil. condensate/Volatile oil/Black oil in the comments and the Title1 section depending on the case you are modelling. Double click on Titles/EOS/Units and write Dry gas/Wet gas/Gas. Rather than introducing new concepts on gas condensate thermodynamic modeling, this paper intends to provide new experimental data (and also some simple treatment on them), checking some day-by-day tools to confirm that EOS tuning strategies for gas condensate fluids remain unavoidable.Techniques have been developed to determine vapor-liquid phase boundaries and swelling factors of CO 2-heavy oil systems and C 3H 8- n-C 4H 10-CO 2-heavy oil systems under reservoir conditions. Double click on the WinProp icon in the Launcher and open the WinProp interface. Results were not improved as expected, suggesting that gas condensate thermodynamic properties are very sensitive to heavy ends mole fraction provided by GC. The performance of such tables is compared with the original one proposed in the literature in predicting experimental PVT data using Peng-Robinson EOS in commercial simulators. Using a traditional three-parameter relationship among density, molecular weight and boiling temperature, these parameters, together with the molecular weight and density of the non-paraffinic compound, are estimated for each fraction up to C 40, and used for the other samples to provide local Single Carbon Number (SCN) tables. Once the fraction's n-paraffin is located by its retention time in the chromatogram, the areas of all other peaks after the previous n-paraffin are computed to make up a fake non-paraffinic compound of the fraction, whose mean boiling temperature is related to its area-weighted retention time. In a routine thermodynamic modeling performance test, mean values for pseudocomponents’ critical temperatures and pressures up to C 40 are re-estimated for Brazilian gas condensate fields based on Gas Chromatography (GC) areas and retention times.