Abstract
Mixtures of carbon dioxide and secondary butyl alcohol at high pressures are interesting for a range of industrial applications. Therefore, it is important to have trustworthy experimental data on the high-pressure phase behavior of this mixture over a wide range of temperatures. In addition, an accurate thermodynamic model is necessary for the optimal design and operation of processes. In this study, bubble points of binary mixtures of CO2 + secondary butyl alcohol were measured using a synthetic method. Measurements covered a CO2 molar concentration range of (0.10–0.57) % and temperatures from (293 to 370) K, with pressures reaching up to 11 MPa. The experimental data were modelled by the cubic plus association (CPA) equation of state (EoS), as well as the more simple Soave–Redlich–Kwong (SRK) EoS. Predictive and correlative modes were considered for both models. In the predictive mode, the CPA performs better than the SRK because it also considers associations.
Highlights
Vapor–liquid equilibrium (VLE) data and accurate thermodynamic models for mixtures are basic requirements for the design, simulation, operation, and optimization of industrial processes
Mixtures of carbon dioxide and secondary butyl alcohol at high pressures are interesting for a range of industrial applications
The present study aims to investigate the solubility of carbon dioxide in secondary butyl alcohol from an experimental, as well as a modeling perspective, since in addition to experimental data, modeling of the system is vital for investigations of the phase behavior
Summary
Vapor–liquid equilibrium (VLE) data and accurate thermodynamic models for mixtures are basic requirements for the design, simulation, operation, and optimization of industrial processes. Because of the interest in the phase behavior of the components involved, the solubility of carbon dioxide in secondary butyl alcohol has been determined previously by other researchers [2,3,4,5,6,7] Some of these studies are limited to only one or two specific temperatures. The uncertainty of pressure, temperature, density, and liquid and vapor molar compositions are 0.008 MPa, 0.05 K, 0.17 kgÁm3, 1 and 2 %, respectively [6] They correlated their experimental vapor–liquid equilibrium data using the Peng–Robinson EoS coupled with the Wong–Sandler mixing rules and succeeded in obtaining good agreement [6]. Stevens et al developed a new apparatus for the experimental determination of vapor– liquid equilibria in systems containing low-volatility compounds and near-critical carbon dioxide Their apparatus was tested by measuring the VLE of the system CO2 ? Both models are investigated in the predictive and correlative modes
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