An automated apparatus for equilibrium phase compositions, densities, and interfacial tensions: data for carbon dioxide + decane

Shaver, R.D.; Robinson, Robert L.; Gasem, Khaled A. M.

doi:10.1016/s0378-3812(00)00475-1

Cited by 91 publications

(77 citation statements)

References 18 publications

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“…Figure 2͑a͒ illustrates the P-x phase equilibrium of CO 2 ͑99.99% purity͒ and n-decane ͑with purity of 99.9%͒ binary system. As can be seen in the figure, the experimental data of this setup are in excellent agreement with literature data of Shaver et al 24 and Nagarajan, and Robinson, Jr., 25 which were measured by an analytical method. They sampled the liquid phase from the equilibrium cell and analyzed using a gas chromatograph ͑GC͒ for composition.…”

Section: Apparatus Verificationsupporting

confidence: 90%

“…Figure 3 illustrates the density data of n-decane and CO 2 in the liquid phase. The experimental data have a very good correlation to the literature data of Shaver et al 24 and Nagarajan and Robinson. 25 Their density data were obtained by using a densitometer.…”

Section: Apparatus Verificationsupporting

confidence: 83%

“…The mixture critical point for n-decane and CO 2 at 71.1°C is 127.9 bars and the mole fraction of CO 2 is 95.34%, compared to the literature data ͑127.2 bars and 93.5% CO 2 ͒ at 71.15°C. 24 The difference of CO 2 composition is less than 2%, and the critical pressure difference is less than 1 bar.…”

Section: Apparatus Verificationmentioning

confidence: 95%

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High-pressure phase equilibria with compressed gases

Wei

Scurto

2007

Review of Scientific Instruments

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An apparatus is described that is capable of determining high-pressure vapor-liquid equilibrium, liquid-liquid equilibrium, solid-liquid-vapor equilibrium, vapor-liquid-liquid equilibrium, and mixture critical points and transitions. The device is capable of temperatures to 150°C and pressures to 300bars (higher with slight modifications). The construction and operation are described in detail and do not require the use of mercury. This method requires very low sample volumes and no analytical equipment nor system-specific calibration. The apparatus was verified by comparison with literature data for the decane-CO2 mixture and CO2-ionic liquid [1-hexyl-3-methyl-imidazolium bis(trifyl)imide)] systems. The experimental data have excellent agreement with the literature data that used different experimental methods. A rigorous error analysis of the system is also presented.

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Section: Apparatus Verificationsupporting

confidence: 90%

Section: Apparatus Verificationsupporting

confidence: 83%

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High-pressure phase equilibria with compressed gases

Wei

Scurto

2007

Review of Scientific Instruments

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“…We have used the same apparatus to measure C V for the CO 2 + n-decane mixture. Prior to this work, some thermodynamic properties of CO 2 + n-decane mixtures have been reported by other investigators [20][21][22][23][24][25][26]. However, most of the available PVTx and VLE data cover only limited ranges of temperature, pressure, and concentration.…”

Section: Introductionmentioning

confidence: 94%

Isochoric Heat Capacity of CO2 + n-Decane Mixtures in the Critical Region

et al. 2006

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The isochoric heat capacity of two binary (CO 2 + n-decane) mixtures (0.095 and 0.178 mole fraction of n-decane) have been measured with a hightemperature, high-pressure, nearly constant volume adiabatic calorimeter. Measurements were made at nineteen near-critical liquid and vapor densities between 87 and 658 kg · m −3 for the composition of 0.095 mole fraction n-decane and at nine densities between 83 and 458 kg · m −3 for the composition of 0.178 mole fraction n-decane. The range of temperatures was 295 to 568 K. These temperature and density ranges include near-and supercritical regions. The measurements were performed in both one-and two-phase regions including the vapor + liquid coexistence curve. The uncertainty of the heat-capacity measurements is estimated to be 2% (coverage factor k = 2). The uncertainty in temperature is 15 mK, and that for density measurements is 0.06%. The liquid and vapor one-(C V 1 , C V 1 ) and two-phase (C V 2 , C V 2 ) isochoric heat capacities, temperatures (T S ), and densities (ρ S ) at saturation were measured by using the well-established method of quasi-static thermograms for each filling density. The critical temperatures (T C ), the critical densities (ρ C ), and the critical pressure (P C ) for the CO 2 + n-decane mixtures were extracted from the isochoric heat-capacity measurements on the coexistence curve. The observed isochoric heat capacity along the critical isochore of the CO 2 + n-decane mixture exhibits a renormalization of the critical behavior of C VX typical for mixtures. The values of the characteristic parameters (K 1 , K 2 ), temperatures (τ 1 , τ 2 ), and the characteristic density differences ( ρ 1 , ρ 2 ) were estimated for the CO 2 + n-decane mixture by using the critical-curve data and the theory of critical phenomena in 730 Polikhronidi, Batyrova, Abdulagatov, and Stepanov binary mixtures. The ranges of conditions were defined on the T-x plane for the critical isochore and the ρ-x plane for the critical isotherm, for which we observed renormalization of the critical behavior for the isochoric heat capacity.

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“…Some of the most cited works are the experimental determinations of VLE and IFT reported for Nagarajan Figure 6 shows the extent of the positive deviations from ideal behaviour of this non-azeotropic mixture. As in the previous system, k ij of the SAFT-EoS was optimized using the available experimental information [79,80] and constrained in order to avoid unstable liquid -liquid phase equilibria. The k ij value as well as deviation statistics for VLE predictions are summarized in Table 3.…”

Section: Carbon Dioxide + Decane Mixturementioning

confidence: 99%