Vapor-liquid equilibrium diagrams

Tables of azeotropes and nonazeotropes compiled by L. H. Horsley and coworkers at the Dow Chemical Co. Included are a formula index, a bibliography, and three articles, "Vapor-Liquid Equilibrium Diagrams of Alcohol-Ketone Azeotropes as a Function of Pressure, ...

Vapor-Liquid Equilibrium Diagrams of Alcohol-Ketone Azeotropes as a Function of Pressure... 

Pressure has a marked effect on the azeotropic composition and vapor-liquid equilibrium diagrams of alcohol-ketone systems (J). This is due to the fact that the slopes of the vapor pressure curves of alcohols are appreciably greater than for ketones it results in an unusually larger change in the relative boiling points of the components of an alcohol-ketone system with change in pressure. 

Figure 2. Vapor-liquid equilibrium diagram of ozone-fluorine system...

Schematic three-dimensional vapor-liquid equilibrium diagram for a two-component system obeying Raoult s law.

As an example, the vapor/liquid equilibrium diagram of the diacetyl/water system is shown in Figure 75. At the high diacetyl concentrations obtained by both the cryogenic crystallization or the polyazeotropic distillation, the water is more volatile than the diacetyl, and there is a low-boiling azeotrope at 63.57 % diacetyl by mole corresponding to 89.29 % by... 

Water in THF is the second most important problem as it makes polymerization impossible. The vapor/liquid equilibrium diagram of the THF/water system at atmospheric pressure is shown in Figure 95. 

Figure 95. The Vapor/Liquid Equilibrium Diagram of the THF/Water System at 1 ATM.

Vapor/liquid equilibrium diagram of the furfiiral/water system at 1 ATM as shown in Figure 105. 

Figure 117. Vapor/Liquid Equilibrium Diagram for the Water/Acetic Acid System...

Figure 7 High-pressure vapor-liquid equilibrium diagram at 60 °C for the system DMSO-CO2 in the presence of Cefonicid...

Fig. 7. Vapor-liquid equilibrium diagram for ethanol (1) + water (2). UNIQUAC and Wilson parameters from ab initio calculations. Experimental data from Gmehling et al. (1977 onward).

Development of Vapor-Liquid Equilibrium Diagrams for a.Mixture That Obeys Raoult s Law... 

Assuming a mixture of n-pentane and n-heptane is ideal, prepare vapor-liquid equilibrium diagrams for this mixture at... 

For a binary (that is, two-component) mixture, if constant-pressure vapor-liquid equilibrium diagrams, such as Fig. 10.1-4 or that of Illustration 10.1-1. have been previously prepared, dewpoint and bubblepoint temperatures can easily be read from these diagrams. For the cases in which such information is not available, or if a multicomponent mixture is of interest, the trial-and-error procedure of Illustration 10.1 -2 is used to estimate these temperatures. 

Plot Vapor-Liquid Equilibrium diagram N = number of points -1... 

Figure 3.2b, an x-y vapor-liquid equilibrium diagram, is an alternative way of presenting some of the information in Fig. 3.2a. Here each point on the x-y equilibrium curve is at a different but undesignated temperature. Figure 3.2b is widely used in calculating equilibrium-stage requirements even though it contains less information than Fig. 3.2a.

Figure 1. Vapor-liquid equilibrium diagrams of alcohol-ketone systems at...

Fig. 2-29. Azeotropic distillation unit for heteroazeotropes (a) with corresponding vapor-liquid equilibrium diagram (b).

Fig. 2-30. 1 vo-pressure distillation unit with corresponding vapor - liquid equilibrium diagram. 

Figure 5.15 Different types of vapor-liquid equilibrium diagrams for the following binary systems (1) benzene (1) -toluene (2) (2) methanol (l)-water (2) (3)...

Figure 7.9 Vapor-liquid equilibrium diagram for the ternary system methyl acetate (l)-methanol (2)-LiN03 (3) at 101.33 kPa. (Experimental data from Vasileva et al. [30] and Topphoff et al. [31].)...

The McCabe-Thiele approach for a binary mixture can be described as follows. First, we take the vapor-liquid equilibrium diagram y/x plot). Then we draw the operating lines based on the mass balance for the liquid and the vapor phase. There is one operating line for the stripping section and one for the top (rectification or enriching) section. The assumption of (in each case) constant molar flows of liquid and vapor ensures strictly straight operating lines. 

---