Modelling phase equilibria for acid gas mixtures using the CPA equation of state. Part VI. Multicomponent mixtures with glycols relevant to oil and gas and to liquid or supercritical CO 2 transport applications

Tsivintzelis, Ioannis; Kontogeorgis, Georgios M.

doi:10.1016/j.jct.2015.07.003

Cited by 19 publications

(22 citation statements)

References 42 publications

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“…non-associating, solvation and self-association. [38][39][40][41][42][43] Other studies 44,46 have considered the incorporation of additional model terms to account for polar and quadrupolar interactions. In the present study we considered only the non-associating and solvation approaches.…”

Section: Measurementmentioning

confidence: 99%

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Multicomponent Vapor–Liquid Equilibrium Measurement and Modeling of Ethylene Glycol, Water, and Natural Gas Mixtures at 6 and 12.5 MPa

et al. 2018

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Section: Measurementmentioning

confidence: 99%

“…3, with bij given as (bi+bj)/2) must be defined. The following parameters from Tsivintzelis et al 39,43,51 have been used.…”

Section: Eqmentioning

confidence: 99%

Multicomponent Vapor–Liquid Equilibrium Measurement and Modeling of Ethylene Glycol, Water, and Natural Gas Mixtures at 6 and 12.5 MPa

et al. 2018

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“…In the context of CPA, we have previously carried out several studies with polar systems (acetates, ketones, esters, ethers …..) in mixtures with water, inert compounds, etc. where multicomponent and multiphase equilibria have been considered [76][77][78]. In all cases the predictions have been satisfactory without additional polar terms.…”

Section: Discussion and Concluding Remarksmentioning

confidence: 81%

Recent advances with association models for practical applications

2018

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Association models like CPA and other SAFT variants have found widespread use, especially over the recent 30 or so years, and this is not limited any more to universities and researchers. Industry is beginning slowly to adopt such models for some applications and a few of the association models are now provided by commercial simulators. Association models account explicitly for hydrogen bonding (and other complex) phenomena and for this reason they are potentially more useful and more successful than traditional models like cubic equations of state and activity coefficient models. Still, for practical applications all models are judged by their results and these depend on availability of experimental data, the number and type of adjustable parameters and the performance of the models for phase equilibria and occasionally also for other properties. We will consider four case studies in this work which will illustrate some of the capabilities and limitations of these association models in different applications. We will offer a "model developer's" point of view showing in several cases all stages of model development in order to illustrate what worked, what didn't and how it was corrected (when possible). The "physics" and "application" aspects of the models will be in all cases discussed. All results will be shown with the CPA equation of state, although we expect that the overall conclusions will be the same for a wide range of association models.

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“…As previously mentioned, the CPA approach has been successfully applied by several authors for systems involving glycols. ,,,,,, The version of sCPA presented here has been developed over the past decade at the Hydrates, Flow Assurance & Phase Equilibria Research Group at Heriot-Watt University. Predictions for water/TEG were presented by Chapoy et al, while predictions for CH 4 /H 2 O are discussed in Chapoy et al Parameters for TEG are reproduced in Table , and an adjusted expression for parameter c 1 in eq is given by eq .…”

Section: Resultsmentioning

confidence: 99%

Phase Behavior in Natural Gas + Glycol Systems, Part 1: Tri(ethylene glycol) (TEG) and Its Aqueous Solutions

2021

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Glycols and their aqueous solutions are extensively utilized in the natural gas industry as hydrate inhibitors and desiccant agents. An increasing interest in new applications, such as subsea processing and carbon capture and storage (CCS) gas dehydration, requires evaluations for operations at high pressure. New measurements are presented for methane and a natural gas mixture (methane−ethane−propane− carbon dioxide) in tri(ethylene glycol) (TEG) and TEG aqueous solutions. Solubility measurements were carried out at pressures up to 40 MPa for temperatures T = (273.15 and 353.65) K. Water content data covers temperatures between (278.15 and 313.15) K at p = (6 and 12.5) MPa. In addition, water activities in such solutions are also reported. The experimental data were modeled with three different approaches: the simplified cubic-plus-association (sCPA), a Huron−Vidal Soave−Redlich−Kwong (SRK) equation coupled with the Non-Random Two-Liquid (NRTL) Gibbs energy (g ex ) expression (SRK/HV/NRTL), and the non-density-dependent approach to Peng− Robinson (PR/NDD). The SRK/HV/NRTL model was found wanting for correlating experimental methane solubility data, while the PR/NDD and sCPA were successful in describing the methane/TEG phase behavior but not TEG aqueous solutions. An alternative approach that includes a binary interaction parameter dependent on the liquid phase composition (xk ij ) gave fair to satisfactorily results, particularly in the case of sCPA. For the multicomponent system, sCPA-xk ij has yielded more consistent predictions than PR/NDD-xk ij , especially for total gas solubility. Overall, all the models have failed to give satisfactory results based only on binary parameters.

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Modelling phase equilibria for acid gas mixtures using the CPA equation of state. Part VI. Multicomponent mixtures with glycols relevant to oil and gas and to liquid or supercritical CO 2 transport applications

Cited by 19 publications

References 42 publications

Multicomponent Vapor–Liquid Equilibrium Measurement and Modeling of Ethylene Glycol, Water, and Natural Gas Mixtures at 6 and 12.5 MPa

Multicomponent Vapor–Liquid Equilibrium Measurement and Modeling of Ethylene Glycol, Water, and Natural Gas Mixtures at 6 and 12.5 MPa

Recent advances with association models for practical applications

Phase Behavior in Natural Gas + Glycol Systems, Part 1: Tri(ethylene glycol) (TEG) and Its Aqueous Solutions

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