Publications
266 results found
McBride-Wright M, Maitland GC, Trusler JPM, 2015, Viscosity and Density of Aqueous Solutions of Carbon Dioxide at Temperatures from (274 to 449) K and at Pressures up to 100 MPa, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 60, Pages: 171-180, ISSN: 0021-9568
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- Citations: 49
Schmidt KAG, Pagnutti D, Curran MD, et al., 2015, New Experimental Data and Reference Models for the Viscosity and Density of Squalane, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 60, Pages: 137-150, ISSN: 0021-9568
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- Citations: 43
Cadogan SP, Hallett JP, Maidand GC, et al., 2015, Diffusion Coefficients of Carbon Dioxide in Brines Measured Using <SUP>13</SUP>C Pulsed-Field Gradient Nuclear Magnetic Resonance, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 60, Pages: 181-184, ISSN: 0021-9568
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- Citations: 19
Trusler JPM, 2015, Virial Coefficients, VOLUME PROPERTIES: LIQUIDS, SOLUTIONS AND VAPOURS, Editors: Wilhelm, Letcher, Publisher: ROYAL SOC CHEMISTRY, Pages: 152-162, ISBN: 978-1-84973-899-6
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- Citations: 1
Hou S-X, Maitland GC, Trusler JPM, 2014, Phase equilibria of (CO2 + butylbenzene) and (CO2 + butylcyclohexane) at temperatures between (323.15 and 423.15) K and at pressures up to 21 MPa, Fluid Phase Equilibria, Vol: 387, Pages: 111-116, ISSN: 0378-3812
Experimental measurements of the phase equilibria of (CO2 + butylbenzene) and (CO2 + butylcyclohexane) have been made with an analytical apparatus at temperatures of (323.15, 373.15 and 423.15) K at pressures from 2 MPa to the mixture critical pressure. These are the first results to be published for (CO2 + butylcyclohexane), while for (CO2 + butylbenzene) they are the first at pressures above 6 MPa. To model the data, we use the Peng–Robinson equation of state with Wong–Sandler mixing rules incorporating the NRTL equation. The model describes the measured bubble point curves very well at all temperatures, except close to the mixture critical points at high pressures. The dew point curves are described well only at the lowest temperature; otherwise, deviations increase in the approach to the mixture critical point.
Lin C-W, Trusler JPM, 2014, Speed of Sound in (Carbon Dioxide plus Propane) and Derived Sound Speed of Pure Carbon Dioxide at Temperatures between (248 and 373) K and at Pressures up to 200 MPa, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 59, Pages: 4099-4109, ISSN: 0021-9568
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- Citations: 16
Al Ghafri SZS, Forte E, Maitland GC, et al., 2014, Experimental and Modeling Study of the Phase Behavior of (Methane + CO2 + Water) Mixtures, The Journal of Physical Chemistry B, Vol: 118, Pages: 14461-14478, ISSN: 1520-5207
May EF, Tay WJ, Nania M, et al., 2014, Physical apparatus parameters and model for vibrating tube densimeters at pressures to 140 MPa and temperatures to 473 K, Review of Scientific Instruments, Vol: 85, ISSN: 1089-7623
Cadogan SP, Maitland GC, Trusler JPM, 2014, Diffusion coefficients of CO2 and N-2 in water at temperatures between 298.15 K and 423.15 K at pressures up to 45 MPa, Journal of Chemical and Engineering Data, Vol: 59, Pages: 519-525, ISSN: 1520-5134
We report measurements of the diffusion coefficients of CO2 and N2 in pure water at temperatures between (298.15 and 423.15) K and pressures between (15 and 45) MPa. The measurements were made by the Taylor dispersion method and have a standard relative uncertainty of 2.3 %. The results were found to be essentially independent of pressure over the range investigated and a simple relation, based on the Stokes–Einstein equation, is proposed to correlate the experimental data. Some experimental difficulties arising in the measurement of the diffusivities of slightly soluble acid-gas solutes such as CO2 in water are also discussed.
Vesovic V, Trusler JPM, Assael MJ, et al., 2014, Dense Fluids: Viscosity, EXPERIMENTAL THERMODYNAMICS, VOL IX: ADVANCES IN TRANSPORT PROPERTIES OF FLUIDS, Editors: Assael, Goodwin, Vesovic, Wakeham, Publisher: ROYAL SOC CHEMISTRY, Pages: 253-287, ISBN: 978-1-84973-677-0
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- Citations: 3
Al Ghafri SZ, Maitland GC, Trusler JPM, 2013, Experimental and modeling study of the phase behavior of synthetic crude oil + CO2, Fluid Phase Equilibria, Vol: 365, Pages: 20-40, ISSN: 0378-3812
A full understanding of the phase behavior of CO2–hydrocarbon mixtures at reservoir conditions is essential for the proper design, construction and operation of carbon capture and storage (CCS) and enhanced oil recovery (EOR) processes. While equilibrium data for binary CO2–hydrocarbon mixtures are plentiful, equilibrium data and validated equations of state having reasonable predictive capability for multi-component CO2–hydrocarbon mixtures are limited. In this work, a new synthetic apparatus was constructed to measure the phase behavior of systems containing CO2 and multicomponent hydrocarbons at reservoir temperatures and pressures. The apparatus consisted of a thermostated variable-volume view cell driven by a computer-controlled servo motor system, and equipped with a sapphire window for visual observation. Two calibrated syringe pumps were used for quantitative fluid injection. The maximum operating pressure and temperature were 40 MPa and 473.15 K, respectively. The apparatus was validated by means of isothermal vapor–liquid equilibrium measurement on (CO2 + heptane), the results of which were found to be in good agreement with literature data.In this work, we report experimental measurements of the phase behavior and density of (CO2 + synthetic crude oil) mixtures. The ‘dead’ oil contained a total of 17 components including alkanes, branched-alkanes, cyclo-alkanes, and aromatics. Solution gas (0.81 methane + 0.13 ethane + 0.06 propane) was added to obtain live synthetic crudes with gas-oil ratios of either 58 or 160. Phase equilibrium and density measurements are reported for the ‘dead’ oil and the two ‘live’ oils under the addition of CO2. The measurements were carried out at temperatures of 298.15, 323.15, 373.15 and 423.15 K and at pressures up to 36 MPa, and included vapor–liquid, liquid–liquid and vapor–liquid–liquid equilibrium conditions. The results are qualitatively
Ciotta F, Trusler JPM, Vesovic V, 2013, Extended hard-sphere model for the viscosity of dense fluids, Fluid Phase Equilibria, Vol: 363, Pages: 239-247, ISSN: 0378-3812
An extended hard-sphere model is reported that may be applied to correlate and predict the viscosity of gases, liquids and supercritical fluids. The method is based on the hard-sphere model of Dymond and Assael and uses their roughness factors and molar core volumes to relate reduced viscosity to a universal function of reduced volume. The extended model behaves correctly in the limit of low densities and offers improved accuracy at high densities. The new universal reference function was determined from a large database of experimental viscosities for alkanes extending up to reduced densities of 0.84. It has been tested by correlating the viscosity of two high-viscosity liquids not used in the development of the universal function and has shown to perform satisfactorily up to reduced densities of approximately 0.9.
Peng C, Crawshaw JP, Maitland GC, et al., 2013, The pH of CO2-saturated water at temperatures between 308 K and 423 K at pressures up to 15 MPa, The Journal of Supercritical Fluids, Vol: 82, Pages: 129-137, ISSN: 0896-8446
Abstract We report pH measurements for CO2-saturated water in the pressure range from (0.28 to 15.3) MPa and temperatures from (308.3 to 423.2) K. Commercially available pH and Ag/AgCl electrodes were used together with a high pressure equilibrium vessel operating under conditions of precisely controlled temperature and pressure. The results of the study indicate that pH decreases along an isotherm in proportion to −log10(x), where x is the mole fraction of dissolved CO2 in H2O. The expanded uncertainty of the pH measurements is 0.06 pH units with a coverage factor of 2. The reported results are in good agreement with the literature in pressure ranges up to 16 MPa at temperatures below 343 K. An empirical equation has been developed to represent the present results with an expanded uncertainty of 0.05 pH units. We also compare our results with a chemical equilibrium model and find agreement to within 0.1 pH unit.
Chirico RD, Frenkel M, Magee JW, et al., 2013, Improvement of Quality in Publication of Experimental Thermophysical Property Data: Challenges, Assessment Tools, Global Implementation, and Online Support, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 58, Pages: 2699-2716, ISSN: 0021-9568
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- Citations: 210
Tong D, Trusler JPM, Vega-Maza D, 2013, Solubility of CO<sub>2</sub> in Aqueous Solutions of CaCl<sub>2</sub> or MgCl<sub>2</sub> and in a Synthetic Formation Brine at Temperatures up to 423 K and Pressures up to 40 MPa, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 58, Pages: 2116-2124, ISSN: 0021-9568
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- Citations: 70
Tong D, Maitland GC, Trusler MJP, et al., 2013, Solubility of carbon dioxide in aqueous blends of 2-amino-2-methyl-1-propanol and piperazine, Chemical Engineering Science, Vol: 101, Pages: 851-864, ISSN: 0009-2509
In this work, we report new solubility data for carbon dioxide in aqueous blends of 2-amino-2-methyl-1-propanol (AMP) and piperazine (PZ). A static-analytical apparatus, validated in previous work, was employed to obtain the results at temperatures of (313.2, 333.2, 373.2, 393.2) K, and at total pressures up to 460 kPa. Two different solvent blends were studied, both having a total amine mass fraction of 30%: (25 mass% AMP+5 mass% PZ) and (20 mass% AMP+10 mass% PZ). Comparisons between these PZ activated aqueous AMP systems and 30 mass% aqueous AMP have been made in terms of their cyclic capacities under typical scrubbing conditions of 313 K in the absorber and 393 K in the stripper. The Kent–Eisenberg model was used to correlate the experimental data.
Hou S-X, Maitland GC, Trusler JPM, 2013, Phase equilibria of (CO<sub>2</sub> + H<sub>2</sub>O + NaCl) and (CO<sub>2</sub> + H<sub>2</sub>O + KCl): Measurements and modeling, JOURNAL OF SUPERCRITICAL FLUIDS, Vol: 78, Pages: 78-88, ISSN: 0896-8446
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- Citations: 36
Li X, Ross DA, Trusler JPM, et al., 2013, Molecular Dynamics Simulations of CO<sub>2</sub> and Brine Interfacial Tension at High Temperatures and Pressures, JOURNAL OF PHYSICAL CHEMISTRY B, Vol: 117, Pages: 5647-5652, ISSN: 1520-6106
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- Citations: 68
Forte E, Galindo A, Trusler JPM, 2013, Experimental and molecular modelling study of the three-phase behaviour of (propane plus carbon dioxide plus water) at reservoir conditions, JOURNAL OF SUPERCRITICAL FLUIDS, Vol: 75, Pages: 30-42, ISSN: 0896-8446
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- Citations: 11
Al Ghafri SZ, Maitland GC, Trusler JPM, 2013, Densities of SrCl<sub>2</sub>(aq), Na<sub>2</sub>SO<sub>4</sub>(aq), NaHCO<sub>3</sub>(aq), and Two Synthetic Reservoir Brines at Temperatures between (298 and 473) K, Pressures up to 68.5 MPa, and Molalities up to 3 mol.kg<SUP>-1</SUP>, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 58, Pages: 402-412, ISSN: 0021-9568
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- Citations: 12
Vega-Maza D, Carmen Martin M, Trusler JPM, et al., 2013, Heat capacities and densities of the binary mixtures containing ethanol, cyclohexane or 1-hexene at high pressures, JOURNAL OF CHEMICAL THERMODYNAMICS, Vol: 57, Pages: 550-557, ISSN: 0021-9614
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- Citations: 21
Forte E, Llovell F, Trusler JPM, et al., 2013, Application of the statistical associating fluid theory for potentials of variable range (SAFT-VR) coupled with renormalisation-group (RG) theory to model the phase equilibria and second-derivative properties of pure fluids, FLUID PHASE EQUILIBRIA, Vol: 337, Pages: 274-287, ISSN: 0378-3812
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- Citations: 23
Al Ghafri S, Maitland G, Trusler JPM, 2013, Experimental and modeling study of the phase behavior of (Synthetic Crude Oil + CO<inf>2</inf>), Pages: 527-529
Hou S-X, Maitland GC, Trusler JPM, 2013, Measurement and modeling of the phase behavior of the (carbon dioxide + water) mixture at temperatures from 298.15 K to 448.15 K, The Journal of Supercritical Fluids, Vol: 73, Pages: 87-96
Tong D, Trusler JPM, Maitland GC, et al., 2012, Solubility of carbon dioxide in aqueous solution of monoethanolamine or 2-amino-2-methyl-1-propanol: Experimental measurements and modelling, International Journal of Greenhouse Gas Control, Vol: 6, Pages: 37-47
Despite the importance of the accurate measurement of vapour–liquid equilibria (VLE) data, the reported values, even for well-studied systems such as MEA–H2O–CO2, are scattered. This work centres on the development of an experimental method to measure accurately the VLE of various aqueous amine systems. A static-analytic type of VLE apparatus has been constructed and employed to measure the VLE of CO2 in aqueous monoethanolamine and 2-amino-2-methyl-1-propanol. Gas chromatography was used to analyse the liquid phase compositions. The setup has been validated against literature data for 30 mass% MEA (monoethanolamine) at T = 313 and 393 K and was shown to be capable of generating reliable and repeatable data. New measurements for 30 mass% aqueous AMP (2-amino-2-methyl-1-propanol) solutions are also presented at temperatures between 313 and 393 K and a total pressure range of 23–983 kPa. A quasi-chemical model has been employed to interpret the experimental data for the MEA–H2O–CO2 and AMP–H2O–CO2 systems. The average absolute deviation (ΔAAD) between model prediction and experimental data is within 7%.
Rahman MQ, Chuah K-S, Macdonald ECA, et al., 2012, The effect of pH, dilution, and temperature on the viscosity of ocular lubricants-shift in rheological parameters and potential clinical significance, EYE, Vol: 26, Pages: 1579-1584, ISSN: 0950-222X
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- Citations: 31
Lin C-W, Ramjugernath D, Reddy P, et al., 2012, Speeds of Sound in Liquid and Supercritical Hexafluoropropylene (HFP) and Hexafluoropropylene Oxide (HFPO) at Pressures up to 400 MPa, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 57, Pages: 2568-2575, ISSN: 0021-9568
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- Citations: 3
Trusler JPM, 2012, Equation of State for Solid Phase I of Carbon Dioxide Valid for Temperatures up to 800 K and Pressures up to 12 GPa (vol 40, 043105, 2011), JOURNAL OF PHYSICAL AND CHEMICAL REFERENCE DATA, Vol: 41, ISSN: 0047-2689
Li X, Boek ES, Maitland GC, et al., 2012, Interfacial Tension of (Brines+CO<sub>2</sub>): CaCl<sub>2</sub>(aq), MgCl<sub>2</sub>(aq), and Na<sub>2</sub>SO<sub>4</sub>(aq) at Temperatures between (343 and 423) K, Pressures between (2 and 50) MPa, and Molalities of (0.5 to 5) mol.kg-1, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 57, Pages: 1369-1375, ISSN: 0021-9568
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- Citations: 68
Li X, Boek E, Maitland GC, et al., 2012, Interfacial Tension of (Brines + CO<sub>2</sub>): (0.864 NaCl+0.136 KCl) at Temperatures between (298 and 448) K, Pressures between (2 and 50) MPa, and Total Molalities of (1 to 5) mol.kg<SUP>-1</SUP>, JOURNAL OF CHEMICAL AND ENGINEERING DATA, Vol: 57, Pages: 1078-1088, ISSN: 0021-9568
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- Citations: 125
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