New procedure for vapor-liquid equilibria. Nitrogen + carbon dioxide, methane + Freon 22, and methane + Freon 12

Yorizane, Masahiro; Yoshimura, Shooshin; Masuoka, Hirokatsu; Miyano, Yoshimori; Kakimoto, Yukihiko

doi:10.1021/je00040a012

Cited by 53 publications

(12 citation statements)

References 1 publication

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“…Our liquid and vapor points at 7.41 MPa and our liquid points at 8.15 MPa and the data of Yorizane et al [29] were in good agreement, given their stated composition and pressure uncertainty. The remaining data of Yorizane et al [29] were not in agreement with our measurements, and they predicted a higher critical point, compared to our measurements.…”

Section: Comparison With Literature Datasupporting

confidence: 88%

Vapor–liquid equilibrium data for the carbon dioxide and nitrogen (CO2 + N2) system at the temperatures 223, 270, 298 and 303 K and pressures up to 18 MPa

Westman

Stang

Løvseth

et al. 2016

Fluid Phase Equilibria

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A new setup for the measurement of vapor-liquid phase equilibria of CO 2 -rich mixtures relevant for carbon capture and storage (CCS) transport conditions is presented. An isothermal analytical method with a variable volume cell is used. The apparatus is capable of highly accurate measurements in terms of pressure, temperature and composition, also in the critical region. Vapor-liquid equilibrium (VLE) measurements for the binary system CO 2 +N 2 are reported at 223, 270, 298 and 303 K, with estimated standard uncertainties of maximum 0.006 K in the temperature, maximum 0.003 MPa in the pressure, and maximum 0.0004 in the mole fractions of the phases. These measurements are verified against existing data. Although some data exists, there is little trustworthy data around critical conditions, and our data indicate a need to revise the parameters of existing models. A fit made against our data of the vapor-liquid equilibrium prediction of GERG-2008/EOS-CG for CO 2 +N 2 is presented. At 223 and 298 K, the critical region of the isotherm are fitted using a scaling law, and high accuracy estimates for the critical composition and pressure are found.

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Section: Comparison With Literature Datasupporting

confidence: 88%

Vapor–liquid equilibrium data for the carbon dioxide and nitrogen (CO2 + N2) system at the temperatures 223, 270, 298 and 303 K and pressures up to 18 MPa

Westman

Stang

Løvseth

et al. 2016

Fluid Phase Equilibria

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“…equation of state with recommended binary parameters from Table 6, ---, Eq. (16) with parameters from Table 7 Table 6 for [CO2 (1) + N2 (2)]: , this work, , Brown et al [15,16,23]; , Al-Sahhaf et al [11];  Kaminishi and Toriumi [3]; , Bian and Bian et al [19,22]; , Somait and Kidnay [39]; , Trappehl [14]; , Xu et al [20,21]; , Yang [18]; ; Yorizan et al [5,10,13]; , Yucelen and Kidnay [24]; ▬, Zenner and Dana [9]; , Zhanzhu et al [25]. …”

Section: Discussionmentioning

confidence: 98%

“…The VLE of (CO2 + N2) system has been investigated extensively [3,5,[8][9][10][11][12][13][14][15][16][17][18][19][20][21][22][23][24][25], with most studies utilizing a static or quasi-static analytic method. The available data are summarized in Table 1.…”

Section: Introductionmentioning

confidence: 99%

Phase behavior of (CO2+H2) and (CO2+N2) at temperatures between (218.15 and 303.15)K at pressures up to 15MPa

Fandiño

Trusler

Vega‐Maza

2015

International Journal of Greenhouse Gas Control

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Vapor-liquid equilibrium data are reported for the binary systems (CO2 + H2) and (CO2 + N2) at temperatures between (218.15 and 303.15) K at pressures ranging from the vapor pressure of CO2 to approximately 15 MPa. These data were measured in a new analytical apparatus which is described in detail. The results are supported by a rigorous assessment of uncertainties and careful validation measurements. The new data help to resolve discrepancies between previous studies, especially for the (CO2 + H2) system. Experimental measurements of the three-phase solid-liquid-vapor locus are also reported for both binary systems.The vapor-liquid equilibrium data are modelled with the Peng-Robinson (PR) equation of state with two binary interaction parameters: one, a linear function of inverse temperature, applied to the unlike term in the PR attractive-energy parameter; and the other, taken to be constant, applied to the unlike term in the PR co-volume parameter. This model is able to fit the experimental data in a satisfactory way except in the critical region. We also report alternative binary parameter sets optimized for improved performance at either temperatures below 243 K or temperatures above 273 K. A simple predictive model for the three-phase locus is also presented and compared with the experimental data.

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“…In Figure 2, the calculated results are compared with experimental data [23][24][25] at 273.2 K and 220 K. Along with the increment of pressure, the performance of all equations decreases. Comparatively, RK has the worst accuracy.…”

Section: Selection and Calculation Of The Equations Of Statementioning

confidence: 99%

“…The comparisons between calculated results and experimental data [23][24][25][26] Table 3 summarizes the average relative deviation between calculated results and experimental data on Ps and the N2 vapor fraction of N2/CO2. It can be seen that the same equation of state, combining different mixing rules, could lead to different results.…”

Section: Selection and Calculation Of The Mixing Rulesmentioning

confidence: 99%

Analysis of a New Liquefaction Combined with Desublimation System for CO2 Separation Based on N2/CO2 Phase Equilibrium

Yang

et al. 2015

Energies

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Cryogenic CO2 capture is considered as a promising CO2 capture method due to its energy saving and environmental friendliness. The phase equilibrium analysis of CO2-mixtures at low temperature is crucial for the design and operation of a cryogenic system because it plays an important role in analysis of recovery and purity of the captured CO2. After removal of water and toxic gas, the main components in typical boiler gases are N2/CO2. Therefore, this paper evaluates the reliabilities of different cubic equations of state (EOS) and mixing rules for N2/CO2. The results show that Peng-Robinson (PR) and Soave-Redlich-Kwong (SRK) fit the experimental data well, PR combined with the van der Waals (vdW) mixing rule is more accurate than the other models. With temperature decrease, the accuracy of the model improves and the deviation of the N2 vapor fraction is 0.43% at 220 K. Based on the selected calculation model, the thermodynamic properties of N2/CO2 at low temperature are analyzed. According to the results, a new liquefaction combined with a desublimation system is proposed. The total recovery and purity of CO2 production of the new system are satisfactory enough for engineering applications. Additionally, the total energy required by the new system to capture the CO2 is about 3.108 MJ·kgCO2, which appears to be at least 9% lower than desublimation separation when the initial concentration of CO2 is 40%. OPEN ACCESSEnergies 2015, 8 9496

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New procedure for vapor-liquid equilibria. Nitrogen + carbon dioxide, methane + Freon 22, and methane + Freon 12

Cited by 53 publications

References 1 publication

Vapor–liquid equilibrium data for the carbon dioxide and nitrogen (CO2 + N2) system at the temperatures 223, 270, 298 and 303 K and pressures up to 18 MPa

Vapor–liquid equilibrium data for the carbon dioxide and nitrogen (CO2 + N2) system at the temperatures 223, 270, 298 and 303 K and pressures up to 18 MPa

Phase behavior of (CO2+H2) and (CO2+N2) at temperatures between (218.15 and 303.15)K at pressures up to 15MPa

Analysis of a New Liquefaction Combined with Desublimation System for CO2 Separation Based on N2/CO2 Phase Equilibrium

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