Measurement of total pressures for ethylene — propane mixtures

Elshayal, I. M.; Lu, Benjamin C.‐Y.

doi:10.1002/cjce.5450530114

Cited by 21 publications

(8 citation statements)

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“…Compared to the literature data, our data does not scatter and yields smooth boiling and dew point curves. [11] (◯), from Mastera [12] (▽) and from Xiao and Liu [13] (△) at 100.0 K, and data from Hiza et al [14] ( ) at 99.9 K.…”

Section: Resultsmentioning

confidence: 99%

Vapor-liquid equilibrium of the nitrogen-argon system at 100 K

Tamson

Mair

Grohmann

2022

IOP Conf. Ser.: Mater. Sci. Eng.

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Mixed-refrigerant cycles (MRC) are state-of-the-art for efficient LNG production. The development of cryogenic mixed-refrigerant cycles (CMRC) at temperatures below 100 K relies on physical property data of cryogenic mixtures such as vapor-liquid equilibria and enthalpies. This data is insufficient for some binary mixtures and unavailable for most multi-component systems. The cryogenic phase equilibria test stand CryoPHAEQTS provides precise physical property data of cryogenic fluid mixtures at temperatures from 15 K to 300K and at pressures up to 150 bar. Contrary to previous apparatus in the literature, CryoPHAEQTS uses cooling of the equilibrium cell by a pulse-tube cryocooler. Temperature is measured by two CERNOX® sensors directly immersed in the liquid/vapor phase. Pressure is measured through a capillary and a differential pressure sensor connected to a secondary system containing three high precision sensors. Up to three occurring phases can be sampled directly from the cell and analyzed by gas chromatography. Measurement uncertainties are ±13mK in temperature, ±1 mbar in pressure and ±1% in composition. Prior to publishing new phase equilibrium data, the test stand is benchmarked against available vapor-liquid equilibrium data of the widely investigated nitrogen-argon system. In this paper, we report on the first measurement results of cryogenic mixtures in CryoPHAEQTS and compare them against the literature data.

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Section: Resultsmentioning

confidence: 99%

Vapor-liquid equilibrium of the nitrogen-argon system at 100 K

Tamson

Mair

Grohmann

2022

IOP Conf. Ser.: Mater. Sci. Eng.

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“…In more detail, the observation of Figure leads to the following considerations: the increased number of experimental data used to perform the optimization reduces the uncertainty region of the optimal parameters (see the red contour versus the black one), as anticipated in section ; the use of a more restrictive objective function, with respect to the least-squares objective function (eq ) obtained by multiplying it by 10 6 , increases the sensitivity of the optimal solution to the order of magnitude of the applied objective function (see the red/black circle versus the red/black cross); the application of MLM on the entire sample of 32 ( P , T , x , y ) data points leads to a confidence region of optimal parameters, which is as extended as the one resulting from the use of the least-squares objective function (eq ); however, the two regions do not overlap. Experimental uncertainties of ( P , T , x , y ) data points from refs and are reported in Appendix III in the Supporting Information. …”

Section: The Optimization Of the Pr+eos/a Res Eγ‑wilson Mixing Rules ...mentioning

confidence: 99%

“…the application of MLM on the entire sample of 32 ( P , T , x , y ) data points leads to a confidence region of optimal parameters, which is as extended as the one resulting from the use of the least-squares objective function (eq ); however, the two regions do not overlap. Experimental uncertainties of ( P , T , x , y ) data points from refs and are reported in Appendix III in the Supporting Information.…”

Section: The Optimization Of the Pr+eos/a Res Eγ‑wilson Mixing Rules ...mentioning

confidence: 99%

“…Optimal parameters A 12 , A 21 , and their 95% joint confidence regions, for the N 2 (1)–Ar(2) system at 100 K with different optimization methods. Legend of data points: (solid black circle, ●) optimal couple of parameters obtained with OF (eq ) and 32 experimental points ( P , T , x , y ) by refs and ; (solid red circle, ●) optimal couple of parameters obtained with OF (eq ) and 7 experimental points ( P , T , x , y ) by ref ; (black cross symbol, × ) optimal couple of parameters obtained with OF (eq ) × 10 6 and 32 experimental points ( P , T , x , y ) by refs and ; (red cross symbol, × ) optimal couple of parameters obtained with OF (eq ) × 10 6 and 7 experimental points ( P , T , x , y ) by ref ; (blue cross symbol, × ) optimal couple of parameters obtained with OF (eq ) and 32 experimental points ( P , T , x , y ) by refs and . Legend of lines: (dotted black line) 95% joint confidence region of parameters identified by black circles (●) and crosses ( × ), (dotted red line) 95% joint confidence region of parameters identified by red circles (●) and crosses ( × ), (continuous blue line) 95% joint confidence region of parameters identified by a blue cross symbol ( × ).…”

Section: The Optimization Of the Pr+eos/a Res Eγ‑wilson Mixing Rules ...mentioning

confidence: 99%

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Modeling the Thermodynamics of Fluids Treated by CO₂ Capture Processes with Peng–Robinson + Residual Helmholtz Energy-Based Mixing Rules

Lasala

Chiesa

Privat

et al. 2017

Ind. Eng. Chem. Res.

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It is currently acknowledged that thermodynamic models routinely used to model the behavior of fluids involved in CO 2 capture and storage processes are not sufficiently accurate. Such a deficiency is one of the main sources of uncertainty for estimating the costs associated with these technologies and, as a direct consequence, engineers largely oversize the equipment. In order to reduce the uncertainty related to the calculation of thermodynamic properties, this work aims at providing the optimal parameters of the model Peng−Robinson + equation of state (EoS)/ a res E,γ-Wilson mixing rules that are currently able to accurately correlate the phase behavior of systems encountered in CCS technologies. In particular, this model is optimized in this work over the experimental vapor−liquid equilibria (VLE) data of 23 binary systems, resulting from the binary combination of CO 2 , H 2 , N 2 , O 2 , Ar, CO, CH 4 , H 2 S, and H 2 O, for which data have been found in the literature. The paper shows that this equation of state is reliably applicable to calculate VLE properties of these binary mixtures and suggests the application of this model to represent the thermodynamics of multicomponent fluids treated by CO 2 capture processes. Another outcome of this work is the conceptual framework outlined to enable the optimization of thermodynamic models based on the Maximum Likelihood Method, accounting for the correlation and joint uncertainty of model parameters.

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“…Wflson (1964) TP-4 (1974) Parrish and Him (1974) Parrish and Him (1974) TP-4 (1974) Stryjek et al (1972) Wilson ( TP-4 (1974) Elshayal and Lu (1975) Elshayal and Lu (1975) Elshayal and Lu (1975) Elshayal and Lu (1975) Sage and Lacey (1955) Sage and Lacey (1955) Sage and Lacey (1955) Sage and Lacey (1955) Sage and Lacey (1955) Besserer and Robinson (1973) Besserer and Robinson (1973) McKay et d. (1951) McKay et d. (1951) McKay et d. (1951) McKay et d.…”

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confidence: 99%

A cubic perturbed, hard sphere equation of state for thermodynamic properties and vapor‐liquid equilibrium calculations

Ishikawa

Chung

1980

AIChE Journal

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A cubic perturbed, hard sphere equation of state which combines the hard sphere expression of Scott and the empirical attractive term of Redlich and Kwong with two temperature dependent parameters has been successfully applied to the calculation of pure component properties and vapor-liquid equilibrium values. SCOPEA well-behaved equation of state can represent and predict thermodynamic properties of pure components and mixtures, including vapor-liquid equilibrium values which are important in equipment design for separation processes. Many attempts have been made in recent years to improve the applicability of simple analytical equations of state such as those proposed by van der Waals and by Redlich and Kwong for chemical engi-neering applications. Special attention has been given to the modification of the repulsive term RT/(V-h). The objective of this study is to apply a new and simple perturbed, hard sphere equation of state to thermodynamic properties and vaporliquid equilibrium calculations and to compare the calculated results with those obtained from other equations of state recently proposed in the literature. CONCLUSIONS AND SIGNIFICANCEThe new perturbed, hard sphere equation used in this studycombines the analytical expression of Scott for the hard sphere compressibility factor and the empirical attractive term of the Redlich-Kwong (RK) equation of state. This equation possesses the qualities of realism and simplicity of the RK equation, contains only two temperature dependent parameters and remains a cubic one in terms of density (or volume). It is much simpler to use than the equations proposed by De Santis et al. (1976) and Oellrich et al. (1978). The calculated results obtained for five pure component properties (vapor pressure, saturated liquid and vapor volumes, latent heat of vaporization and second virial coefficient) indicate that the new equation vields lower deviatians from the literature values than the two more complicated equations mentioned above. Comparisons made on vapor-liquid equilibrium (VLE) values for five binary systems at thirty-two isothermal conditions indicate that the new equation yields better representation of the data than the methods of Soave (1972) and Peng-Robinson (PR) (1976). Some of the binary data w e d by De Santis et al. (1976) for testing their equation were also used in this study. The calculated results indicate that the new equation yields lower deviation in the calculated values of pressure. Comparisons were also made on VLE values for a ternary system at two isothermal conditions between the calculated results obtained by the new equation and the method of Soave (1972). The new equation again yields better results.Ever since van der Waals (1873) proposed his equation, the v d w equation, many modifications have been made in the literature to improve his model. One of the most successful ones was the two-parameter empirical equation proposed by Redlich and Kwong (1949):

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Measurement of total pressures for ethylene — propane mixtures

Cited by 21 publications

References 5 publications

Vapor-liquid equilibrium of the nitrogen-argon system at 100 K

Vapor-liquid equilibrium of the nitrogen-argon system at 100 K

Modeling the Thermodynamics of Fluids Treated by CO₂ Capture Processes with Peng–Robinson + Residual Helmholtz Energy-Based Mixing Rules

A cubic perturbed, hard sphere equation of state for thermodynamic properties and vapor‐liquid equilibrium calculations

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Measurement of total pressures for ethylene — propane mixtures

Cited by 21 publications

References 5 publications

Vapor-liquid equilibrium of the nitrogen-argon system at 100 K

Vapor-liquid equilibrium of the nitrogen-argon system at 100 K

Modeling the Thermodynamics of Fluids Treated by CO2 Capture Processes with Peng–Robinson + Residual Helmholtz Energy-Based Mixing Rules

A cubic perturbed, hard sphere equation of state for thermodynamic properties and vapor‐liquid equilibrium calculations

Contact Info

Product

Resources

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Modeling the Thermodynamics of Fluids Treated by CO₂ Capture Processes with Peng–Robinson + Residual Helmholtz Energy-Based Mixing Rules