Liquid–Liquid Equilibria Determination and Prediction for Ternary Systems of Water + 1,6-Hexanediamine + (1-Butanol or 1-Pentanol) at 298.2, 308.2, and 318.2 K

Abstract

Data of liquid–liquid equilibria (LLE) for water + 1,6-hexanediamine + 1-butanol and water + 1,6-hexanediamine + 1-pentanol ternary systems were determined at T = 298.2, 308.2, and 318.2 K under atmospheric pressure. The distribution coefficients and selectivity factors calculated from LLE data were applied to evaluate the feasibility and effectiveness of extracting 1,6-hexanediamine from the aqueous solution. The results showed that the selectivity factors decrease with the amount of 1,6-hexanediamine increasing in the aqueous phase, and the effect of temperature is insignificant in this study. The nonrandom two-liquid and universal quasichemical activity coefficient models were also applied to regress the experimental equilibrium data of the two ternary systems and the root mean square deviation values between the correlated and experimental results were lower than 0.7%. It turned out that these phase equilibrium behaviors can be described by the two models. Meanwhile, the binary model parameters were acquired from the relevant process simulations.

Measurement and Correlation of Liquid–Liquid Equilibria for Extracting Isopropanol from Cyclohexane with Different Solvents

“…The capabilities of the investigated extractants to separate isopropanol from cyclohexane were assessed in terms of the separation factor ( S ), which can be expressed as follows where w 1 α and w 2 α represent the mass concentrations of cyclohexane and isopropanol, respectively, in the raffinate phase, and w 1 β and w 2 β indicate the mass concentrations of cyclohexane and isopropanol, respectively, in the extraction phase.…”

“…Assessment of the Extraction Performance. The capabilities of the investigated extractants to separate isopropanol from cyclohexane were assessed in terms of the separation factor (S), which can be expressed as follows 25…”

Liquid–Liquid Equilibrium for Ternary Systems of Water + 2,2,3,3-Tetrafluoro-1-propanol + Anisole/1-Octanol at 298.2, 308.2, and 318.2 K

“…After preliminary tests, the optimum value of NRTL nonrandomness parameters α was set to 0.3 for all systems. The binary interaction parameters of NRTL and UNIQUAC models were obtained by minimizing the objective function (OF): ,, where w exp and w cal are experimental mass fraction and calculated mass fraction, respectively. Subscripts i , j , k , and M refer to the components, the phases, the tie lines, and the number of tie lines, respectively.…”

Liquid–Liquid Equilibrium Measurement and Correlation for the Ternary Systems (Dimethyl Succinate + 1,4-Butanediol)/(Dimethyl Glutarate + 1,5-Pentanediol)/(Dimethyl Adipate + 1,6-Hexanediol) + Water at Different Temperatures

“…The LLE data for their ternary systems were measured at four different temperatures (293.15, 303.15, 313.15, and 323.15 K) at 101.3 kPa. The reliability of the equipment used in this work has been evaluated in our previous studies in which the details of apparatus and procedures were described. , …”

“…The reliability of the equipment used in this work has been evaluated in our previous studies in which the details of apparatus and procedures were described. 19,20 Experiments were carried out in the double-jacketed glass vessel with a magnetic stirrer to accelerate the two-phase equilibrium, and the temperature was controlled by a thermostatic bath (type, DC4006, Shanghai Bilon Precision Instrument Co., Ltd.). The actual temperature and atmospheric pressure of liquid in the flask were measured by a mercury thermometer [u(T) = 0.2 K calculated from measurement uncertainty u Td = 0.10 K and calibration uncertainty u Tc = 0.17 K] and a manometer [u(p) = 0.62 kPa calculated from measurement uncertainty u pd = 0.36 kPa and calibration uncertainty u pc = 0.5 kPa], respectively.…”