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본 연구는 298.2 K에서 acetone-ethanol, acetone-water, 그리고 ethanol-water 이성분계의 혼합엔탈피와 acetone-ethanol-water 삼성분계의 혼합엔탈피를 실험에 의하여 측정하였다. 또한 Wilson식과 NRTL식을 이용하여 이성분계 혼합엔탈피 데이터로부터 얻은 매개변수를 이용하여 삼성분계 혼합엔탈피를 예측하였다. 본 실험에서 얻은 실험치와 각 모델로부터 예측된 추산치를 서로 비교하여 본 결과 2개의 매개변수를 갖은 용액모델로서 혼합엔탈피를 잘 예측할 수 있음을 알았다. The enthalpies of mixing for the binary systems of acetone-ethanol, acetone-water and ethanol-water and for the corresponding ternary liquid system of acetone-ethanol-water were measured at 298.2 K. The ternary enthalpies of mixing were estimated from the results of three binary systems by the Wilson equation and the NRTL equation, and the predicted values were found to be in a good agreement with the experimental data.
Phase equilibria and density of polymer in supercritical fluid are fundamental information for chemical process design and molecular structure analysis in polymer science. In this study, we measured high pressure phase equilibria and densities of poly(ethylene-co-butene)_10 and poly(ethylene-co-butene)_47 in two supercritical solvents; dimethyl ether (DME) and dimethyl ether-d (DME-d). A high-pressure moving-volume cell was used to measure the equilibrium properties. High pressure phase equlibria of poly(ethylene-co-butene)_(10)-dimethyl ether were measured at 106∼185 ℃ and pressure range of 486∼1,100 bar. The similar system, polyethylene-dimethyl ether showed higher equilibrium line by 100∼350 bar. The liquid-liquid equilibrium line of poly(ethylene-co-butene)_(10)-dimethyl ether and poly(ethylene-co-butene)_(10)-dimethyl ether-d existed within 110∼150 ℃ below 1,000 bar. Phase behavior of poly(ethylene-co-butene)_(10) and poly(ethylene-co-butene)_(47) in dimethyl ether were also measured.
Tetralin과 이산화탄소 그리고 α-tetralone과 이산화탄소의 이성분계들에 대해 3차 상태방정식인 Redlich-Kwong식, Soave-Redlich-Kwong식 그리고 Peng-Robinson식을 사용하여 기액평형 값을 예측하였다. 추산된 값과 실험값을 비교, 검토한 결과 Peng-Robinson 상태방정식이 다른 방정식에 비해 좋은 접근을 보였다. 또한 이때의 이성분계의 최적 상호작용 파라미터를 온도의 함수로 나타내었다. The vapor-liquid phase equilibria of tetralin and a-tetralone with carbon dioxide were predicted to take advantage of Redlich-Kwong equation, Soave-Redlich-Kwong equation and Peng-Robinson equation in cubic equation of states. The results from comparison predicted values with experimental values have shown that Peng-Robinson equation have better approach than other equations. Also, the optimum interaction parameters kij of the binary systems were presented as the function of temperature.
Pressure-composition isotherms were obtained for the carbon dioxide+1-hexene system at 40, 60, 80, 100 and 120 oC and pressure up to 120 bar and for carbon dioxide+2-ethyl-1-butene system at 40, 75 and 100 oC and pressure up to 115 bar. The accuracy of the experimental apparatus was tested by comparing the measured phase equilibrium data of the carbon dioxide+1-hexene system at 40 oC and 60 oC with those of Wagner and Wichterle , and Jennings and Teja . The solubility of 1-hexene and 2-ethyl-1-butene for the carbon dioxide+1-hexene and carbon dioxide+2-ethyl-1-butene systems increases as the temperatures increases at constant pressure. These two carbon dioxide-polar solute systems exhibit type-I phase behavior, which is characterized by an uninterrupted critical mixture curve that has a maximum in pressure. The experimental data are modeled by using the Peng-Robinson equation of state. A good fit of the data is obtained with Peng-Robinson equation of state using two adjustable parameters for carbon dioxide+1-hexene and carbon dioxide+2-ethyl-1-butene systems.
data of high pressure phase behavior betwen 35oC and 105oC and pressures up to 2,20bar is presented for poly(d,l-lactic acid)(d,l-PLA) and poly(lactide-co-glycolide)15 (PLGA15), PLGA25, and PLGA50 insupercritical carbon dioxide, trifluoromethane (CHF3), chlorodifluoromethane (CHClF2), dichloromethane (CH2Cl2),and chloroform (CHCl3). d,l-PLA dissolves in carbon dioxide at pressures of 1,250 bar, in CHF3 at pressures of 500to 750 bar, and in CHClF2 at pressures of 30-145 bar. As glycolic acid (glycolide) is added to the backbone of PLGA,the cloud point pressure increases by 36 bar/(mol GA) in carbon dioxide, 27 bar/(mol GA) in CHF3, and by only 3.9bar/(mol GA) in CHClF2. PLGA50 does not dissolve in carbon dioxide at pressures of 2,800 bar, whereas it is readilysoluble in CHClF2 at pressures as low as 95 bar at 40oC. Cloud point behavior of d,l-PLA, PLGA15, and PLGA25 insupercritical carbon dioxide shows the effect of glycolide content between 35oC and 108oC. Also, the phase behaviorfor poly(lactic acid) - carbon dioxide-CHClF2 mixture shows the changes of presure-temperature slope, and with CHClF2concentration of 6 wt% , 19 wt% , 36 wt% and 65 wt% . The cloud-point behavior shows the impact of glycolide contenton the phase behavior of PLA, PLGA15, PLGA25 and PLGA50 in supercritical CHClF2. A comparison was made betweenthe phase behaviors of d,l-PLA and poly(l-lactide)(l-PLA) in supercritical CHF3. The phase behavior of CHF3 as acosolvent for 5 wt% d,l-PLA-supercritical carbon dioxide system is presented for the effect being added 10 wt% and29 wt% to CHF3 content.