Vapor-liquid equilibrium data acetone/water

VER chart, 372 Vapor-liquid equilibrium data acetone/methanol, 416 acetone/water, 416,423 butadiene, 420... 

Gmehhng and Onken (op. cit.) give the activity coefficient of acetone in water at infinite dilution as 6.74 at 25 C, depending on which set of vapor-liquid equilibrium data is correlated. From Eqs. (15-1) and (15-7) the partition ratio at infinite dilution of solute can he calculated as follows ... 

Consider the accuracy of the equilibrium data required to calculate the number of equilibrium stages needed for the separation of a mixture of acetone and water by distillation (see Chapter II, Example 11.2). Several investigators have published vapor-liquid equilibrium data for this system Othmer et al. (1952), York and Holmes (1942), Kojima et al. (1968), Reinders and De Minjer (1947). 

Use the UNIFAC model to predict the vapor-liquid equilibria for the acetone + water system at 25 C, and compare the results with the experimental data that can be found in the DECHEMA data series. -39 The following vapor-liquid equilibrium data have been reported for the system water (1) + 1,4-dioxane (2) at 323.15 K. 

One can use the model in a completely correlative manner to fit. vapor-liquid equilibrium data over a large range of temperatures and pressures using the parameters in the G expression and Ly of Eq. 9.9-lOas adjustable parameters. This is demonstrated in Fig. I0.3-9 for the water-acetone mixture using the NRTL expression (Eqs. 9.5-13 and 9.5-14) for G , setting a = 0.35, and fitting t 2, T2i, and ki2 to each isothermal data set. 

Vapor-liquid equilibrium data for the system acetone-air-water at 1 atm (101.3 kPa) are given as ... 

Vapor-liquid equilibrium data at 1 std atm abs, heats of solution, heat capacities, and latent heats of vaporization for the system acetone-water are as follows ... 

Table 8.1 Vapor-liquid Equilibrium Data for Acetone and Water at 1.00 Atm...

The following vapor-liquid equilibrium data have been reported for a binary mixture of acetone (1) in water (2) at 1 atm. Test these data for thermodynamic consistency. 

Fig. 8. Vapor-liquid equilibrium diagram for acetone (1) + water (2). UNIQUAC and Wilson parameters from ab initio calculations. Experimental data from Gmehling et al. (1977 onward).

Comparison with experimental data shows that the complete local-composition equation preserves the quality of Wilson s equation in describing vapor-liquid equilibrium of completely miscible systems. There are no more than slight differences between the complete equation and Wilson s equation in the fitting of data. But the complete local-composition (CLC) equation extends Wilson s local-composition equation to partially miscible solutions. Good predictions of the coexistent liquid compositions of ternary mixtures based on the binary parameters have been found for water + ethyl acetate + ethanol, for water + methyl acetate + acetone, and for water + acrylonitrile + acetonitrile. 

It is required to design a fractionation tower to operate at 101.3 kPa to obtain a distillate consisting of 95 mole% acetone (A) and 5 mole% water, and a residue containing 1 mole% A. The feed liquid is at 125°C and 687 kPa and contains 57 mole% A. The feed is introduced to the column through an expansion valve so that it enters the column partially vaporized at 60°C. Construct an H-x-y diagram and determine the molar ratio of liquid to vapor in the partially vaporized feed. Enthalpy and equilibrium data are as follows. 

D. The LLE correlations in AspenPlus are not always as accurate as possible. If data are available, AspenPlus will find values of the parameters for any of the T.T.F. correlations by doing a regression against the data you input. The purpose of this part is to obtain an improved fit for the NRTL correlation for the ternary system water, chloroform, acetone. Open a new AspenPlus file, draw an extractor with feed, solvent and two products, in Setup list valid phases as Liquid-Liquid-Vapor, and input these 3 conponents. Then use NRTL as LLE correlation and give any values for the feed and solvent and extractor conditions. Go to Analysis, list ternary and valid phases as liquid-liquid to obtain the predicted equilibrium results - save these for later conparison. 

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