2 0 2019 klo gri 0 journal Original Kloc, Amabille Petza Grilla, Eleni Capeletto, Claudia A. Papadaki, Maria Corazza, Marcos L. Fluid Phase Equilib. 2019 2020-09-29 Phase equilibrium measurements and thermodynamic modeling of {CO2 + diethyl succinate + cosolvent} systems This work reports experimental phase equilibrium data for the binary systems {CO2(1) + diethyl succinate(2)} and {CO2(1) + ethyl acetate(2)}, and for the ternary systems {CO2(1) + diethyl succinate(2) + ethanol(3)} and {CO2(1) + diethyl succinate(2) + ethyl acetate(3)}. The experiments for the binary system {CO2(1) + diethyl succinate(2)} were carried out at temperatures ranging from 308 K to 358 K, and temperatures ranging from 303 K to 343 K for {CO2(1) + ethyl acetate(2)} as well as for all ternary systems. Only vapor-liquid equilibria were observed for all systems. The experimental measurements were carried out in a high-pressure variable-volume view cell containing a movable piston, which allows pressure control inside the cell. Binary and ternary systems were modeled with the Peng-Robinson cubic equation of state with the van der Waals quadratic mixing rule (vdW2). The presence of a cosolvent (ethanol and ethyl acetate) decreased the saturation pressures of either bubble or dew points compared to the binary system CO2 + diethyl succinate, increasing the solubility of diethyl succinate in CO2. Diethyl succinate Cubic equation of state Supercritical CO2 High-pressure VLE measurement. 10.1016/j.fluid.2019.112285 502 112285 1 InChI=1S/CO2/c2-1-3 CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide CO2 1 Commercial source 1 99.9 3 Stated by supplier 2 InChI=1S/C2H6O/c1-2-3/h3H,2H2,1H3 LFQSCWFLJHTTHZ-UHFFFAOYSA-N ethanol ethyl alcohol C2H6O 1 Commercial source 1 99.8 3 Stated by supplier 3 InChI=1S/C4H8O2/c1-3-6-4(2)5/h3H2,1-2H3 XEKOWRVHYACXOJ-UHFFFAOYSA-N ethyl acetate ethyl ethanoate C4H8O2 1 Commercial source 1 99.95 4 Stated by supplier 4 InChI=1S/C8H14O4/c1-3-11-7(9)5-6-8(10)12-4-2/h3-6H2,1-2H3 DKMROQRQHGEIOW-UHFFFAOYSA-N diethyl butanedioate butanedioic acid, diethyl ester diethyl succinate ethyl succinate succinic acid, diethyl ester C8H14O4 1 Commercial source 1 99 2 Stated by supplier 1 1 1 3 1 Principal objective of the work JWM JWM 1/8/2020 1 Vapor or sublimation pressure, kPa Phase Equilibration Liquid Direct value, X 1 Data file compiler Propagation of evaluated standard uncertainties 95 Liquid Gas 1 Temperature, K Liquid 2 Mole fraction 1 Liquid 1 303.55 5 2 0.4065 4 1 2360 3 1 440 1 303.55 5 2 0.4841 4 1 2870 3 1 460 1 303.55 5 2 0.6092 4 1 3530 3 1 480 1 313.18 5 2 0.4065 4 1 2650 3 1 450 1 313.18 5 2 0.4841 4 1 3350 3 1 470 1 313.18 5 2 0.6092 4 1 4160 3 1 510 1 323.21 5 2 0.4065 4 1 3030 3 1 470 1 323.21 5 2 0.4841 4 1 3840 3 1 500 1 323.21 5 2 0.6092 4 1 4940 3 1 540 1 333.23 5 2 0.4065 4 1 3540 3 1 490 1 333.23 5 2 0.4841 4 1 4410 3 1 520 1 333.23 5 2 0.6092 4 1 5750 3 1 590 1 353.43 5 2 0.4065 4 1 4550 3 1 540 1 353.43 5 2 0.4841 4 1 5690 3 1 590 1 353.43 5 2 0.6092 4 1 7470 3 1 680 1 303.55 5 2 0.7018 4 1 4380 3 1 520 1 303.55 5 2 0.8221 4 1 5020 3 1 550 1 313.18 5 2 0.7018 4 1 5080 3 1 550 1 313.18 5 2 0.8221 4 1 6080 3 1 600 1 323.21 5 2 0.7018 4 1 5720 3 1 580 1 323.21 5 2 0.8221 4 1 7160 3 1 670 1 333.23 5 2 0.7018 4 1 6680 3 1 640 1 333.23 5 2 0.8221 4 1 8290 3 1 730 1 353.43 5 2 0.7018 4 1 8590 3 1 750 1 353.43 5 2 0.8221 4 1 10530 4 1 870 2 1 1 4 1 Principal objective of the work JWM JWM 1/8/2020 1 Vapor or sublimation pressure, kPa Phase Equilibration Liquid Direct value, X 1 Data file compiler Propagation of evaluated standard uncertainties 95 Liquid Gas 1 Temperature, K Liquid 2 Mole fraction 1 Liquid 1 308.21 5 2 0.4246 4 1 2460 3 1 450 1 308.21 5 2 0.5484 4 1 3440 3 1 490 1 308.21 5 2 0.7024 4 1 4950 3 1 550 1 308.21 5 2 0.8052 4 1 6060 3 1 610 1 308.21 5 2 0.9008 4 1 6900 3 1 650 1 308.21 5 2 0.9483 4 1 7380 3 1 680 1 308.21 5 2 0.9925 4 1 7690 3 1 690 1 318.24 5 2 0.4246 4 1 2880 3 1 470 1 318.24 5 2 0.5484 4 1 4480 3 1 530 1 318.24 5 2 0.7024 4 1 6070 3 1 610 1 318.24 5 2 0.8052 4 1 7360 3 1 680 1 318.24 5 2 0.9008 4 1 8240 3 1 730 1 318.24 5 2 0.9483 4 1 8910 3 1 780 1 328.23 5 2 0.4246 4 1 3400 3 1 490 1 328.23 5 2 0.5484 4 1 5030 3 1 550 1 328.23 5 2 0.7024 4 1 7230 3 1 670 1 328.23 5 2 0.8052 4 1 8530 3 1 750 1 328.23 5 2 0.9008 4 1 9930 3 1 840 1 328.23 5 2 0.9483 4 1 10720 4 1 890 1 337.91 5 2 0.4246 4 1 3810 3 1 500 1 337.91 5 2 0.5484 4 1 5340 3 1 580 1 337.91 5 2 0.7024 4 1 8220 3 1 740 1 337.91 5 2 0.8052 4 1 10150 4 1 850 1 337.91 5 2 0.9008 4 1 11620 4 1 950 1 337.91 5 2 0.9483 4 1 12570 4 1 1010 1 348.13 5 2 0.4246 4 1 4530 3 1 540 1 348.13 5 2 0.5484 4 1 6250 3 1 630 1 348.13 5 2 0.7024 4 1 9520 3 1 820 1 348.13 5 2 0.8052 4 1 11610 4 1 950 1 348.13 5 2 0.9008 4 1 13570 4 1 1080 1 348.13 5 2 0.9483 4 1 14450 4 1 1140 1 358.09 5 2 0.4246 4 1 5140 3 1 570 1 358.09 5 2 0.5484 4 1 7060 3 1 680 1 358.09 5 2 0.7024 4 1 10750 4 1 900 1 358.09 5 2 0.8052 4 1 13200 4 1 1060 1 358.09 5 2 0.9008 4 1 15210 4 1 1210 1 358.09 5 2 0.9483 4 1 16020 4 1 1260 3 1 1 4 1 Principal objective of the work JWM JWM 1/8/2020 1 Vapor or sublimation pressure, kPa Phase Equilibration Gas Direct value, X 1 Data file compiler Propagation of evaluated standard uncertainties 95 Gas Liquid 1 Mole fraction 1 Gas 0.9925 4 1 Temperature, K Gas 1 318.24 5 1 8990 3 1 760 1 328.23 5 1 10390 4 1 850 1 337.91 5 1 11670 4 1 930 1 348.13 5 1 12820 4 1 1000 1 358.09 5 1 13740 4 1 1070 4 1 1 4 1 2 1 Principal objective of the work JWM JWM 1/8/2020 1 Vapor or sublimation pressure, kPa Phase Equilibration Liquid Direct value, X 4 2 1 Data file compiler Propagation of evaluated standard uncertainties 95 Liquid Gas 1 Solvent: Mole fraction 4 Liquid 2 Temperature, K Liquid 3 Mole fraction 1 Liquid 1 0.496 4 2 303.28 5 3 0.4475 4 1 3480 3 1 480 1 0.496 4 2 303.28 5 3 0.5547 4 1 4020 3 1 500 1 0.496 4 2 303.28 5 3 0.6529 4 1 4470 3 1 520 1 0.496 4 2 313.17 5 3 0.4475 4 1 4100 3 1 500 1 0.496 4 2 313.17 5 3 0.5547 4 1 4810 3 1 540 1 0.496 4 2 313.17 5 3 0.6529 4 1 5500 3 1 570 1 0.496 4 2 323.21 5 3 0.4475 4 1 4700 3 1 530 1 0.496 4 2 323.21 5 3 0.5547 4 1 5600 3 1 580 1 0.496 4 2 323.21 5 3 0.6529 4 1 6220 3 1 600 1 0.496 4 2 333.17 5 3 0.4475 4 1 5290 3 1 570 1 0.496 4 2 333.17 5 3 0.5547 4 1 6830 3 1 640 1 0.496 4 2 333.17 5 3 0.6529 4 1 7270 3 1 660 1 0.496 4 2 343.16 5 3 0.4475 4 1 5930 3 1 600 1 0.496 4 2 343.16 5 3 0.5547 4 1 7630 3 1 690 1 0.496 4 2 343.16 5 3 0.6529 4 1 8520 3 1 740 1 0.324 4 2 303.28 5 3 0.4506 4 1 3860 3 1 490 1 0.324 4 2 303.28 5 3 0.5505 4 1 4440 3 1 520 1 0.324 4 2 313.15 5 3 0.4506 4 1 4460 3 1 520 1 0.324 4 2 313.15 5 3 0.5505 4 1 5320 3 1 560 1 0.324 4 2 323.13 5 3 0.4506 4 1 5250 3 1 560 1 0.324 4 2 323.13 5 3 0.5505 4 1 6230 3 1 610 1 0.324 4 2 333.15 5 3 0.4506 4 1 6020 3 1 600 1 0.324 4 2 333.15 5 3 0.5505 4 1 7330 3 1 670 1 0.324 4 2 343.14 5 3 0.4506 4 1 6850 3 1 640 1 0.324 4 2 343.14 5 3 0.5505 4 1 8010 3 1 710 1 0.496 4 2 303.28 5 3 0.7594 4 1 5160 3 1 560 1 0.496 4 2 303.28 5 3 0.8501 4 1 6020 3 1 600 1 0.496 4 2 303.28 5 3 0.9509 4 1 6520 3 1 630 1 0.496 4 2 313.17 5 3 0.7594 4 1 6400 3 1 620 1 0.496 4 2 313.17 5 3 0.8501 4 1 7180 3 1 660 1 0.496 4 2 313.17 5 3 0.9509 4 1 7870 3 1 700 1 0.496 4 2 323.21 5 3 0.7594 4 1 7430 3 1 670 1 0.496 4 2 323.21 5 3 0.8501 4 1 8520 3 1 740 1 0.496 4 2 323.21 5 3 0.9509 4 1 9400 3 1 800 1 0.496 4 2 333.17 5 3 0.7594 4 1 8880 3 1 760 1 0.496 4 2 333.17 5 3 0.8501 4 1 10090 4 1 830 1 0.496 4 2 333.17 5 3 0.9509 4 1 11450 4 1 920 1 0.496 4 2 343.16 5 3 0.7594 4 1 10280 4 1 840 1 0.496 4 2 343.16 5 3 0.8501 4 1 11660 4 1 930 1 0.496 4 2 343.16 5 3 0.9509 4 1 12840 4 1 1010 1 0.324 4 2 303.28 5 3 0.7506 4 1 5590 3 1 580 1 0.324 4 2 303.28 5 3 0.9011 4 1 5960 3 1 600 1 0.324 4 2 313.15 5 3 0.7506 4 1 6690 3 1 630 1 0.324 4 2 313.15 5 3 0.9011 4 1 7370 3 1 680 1 0.324 4 2 323.13 5 3 0.7506 4 1 7890 3 1 700 1 0.324 4 2 323.13 5 3 0.9011 4 1 8950 3 1 770 1 0.324 4 2 333.15 5 3 0.7506 4 1 9330 3 1 780 1 0.324 4 2 333.15 5 3 0.9011 4 1 10570 4 1 860 1 0.324 4 2 343.14 5 3 0.7506 4 1 10820 4 1 870 1 0.324 4 2 343.14 5 3 0.9011 4 1 12240 4 1 960 5 1 1 4 1 3 1 Principal objective of the work JWM JWM 1/8/2020 1 Vapor or sublimation pressure, kPa Phase Equilibration Liquid Direct value, X 4 3 1 Data file compiler Propagation of evaluated standard uncertainties 95 Liquid Gas 1 Solvent: Mole fraction 4 Liquid 0.497 4 1 Temperature, K Liquid 2 Mole fraction 1 Liquid 1 303.25 5 2 0.4655 4 1 2750 3 1 450 1 303.25 5 2 0.8047 4 1 5150 3 1 550 1 313.21 5 2 0.4655 4 1 3230 3 1 470 1 313.21 5 2 0.8047 4 1 6050 3 1 600 1 323.06 5 2 0.4655 4 1 3880 3 1 500 1 323.06 5 2 0.8047 4 1 7060 3 1 660 1 333.15 5 2 0.4655 4 1 4390 3 1 520 1 333.15 5 2 0.8047 4 1 8330 3 1 740 1 343.11 5 2 0.4655 4 1 4990 3 1 550 1 343.11 5 2 0.8047 4 1 9750 3 1 830 1 303.25 5 2 0.9006 4 1 5990 3 1 600 1 303.25 5 2 0.9466 4 1 6450 3 1 630 1 313.21 5 2 0.9006 4 1 7070 3 1 660 1 313.21 5 2 0.9466 4 1 7790 3 1 720 1 323.06 5 2 0.9006 4 1 8480 3 1 750 1 323.06 5 2 0.9466 4 1 9290 3 1 800 1 333.15 5 2 0.9006 4 1 10040 4 1 850 1 333.15 5 2 0.9466 4 1 10770 4 1 890 1 343.11 5 2 0.9006 4 1 11700 4 1 950 1 343.11 5 2 0.9466 4 1 12230 4 1 970