Phase equilibrium binary mixtures, distillation

Lamivudine is an example of the effect of hydrates in nonaqueous solvents (Jozwiakowski et al., 1996). In distilled water at 25D, the anhydrate free base (form II) is 1.2 times as soluble as the 0.2 hydrate (form I). In ethanol at 26, the hydrate is 1.6 times as soluble as the anhydrate. The maximum solubility in ethanol-water mixtures was found to be at 40-60% water in ethanol, when form I is the most stable solid phase. The transition composition was with 18-20% water in ethanol in binary mixtures with more than 20% water, only the hydrate was found at equilibrium, and with less than 18% water, only the anhydrate was found at equilibrium. 

This study was undertaken to obtain the necessary vapor-liquid equilibrium data and to determine the distillation requirements for recovering solvent for reuse from the solvent-water mixture obtained from adsorber regeneration. Previous binary vapor-liquid equilibrium data (2, 3) indicated two binary azeotropes (water-THF and water-MEK) and a two phase region (water-MEK). The ternary system was thus expected to be highly nonideal. 

Molar vapour flow-rate of component from stage n Mol fraction of component in liquid phase Mol fraction of component A in binary mixture Mol fraction of component B in binary mixture Mol fraction of component in bottom product Mol fraction of component in distillate Equilibrium concentration Mol fraction of component i... 

In this study, the phase equilibrium in the binary mixtures that are expected to be found in the flash distillation was modeled with the Predictive Soave-Redlich-Kwong (PSRK) equation of state [4], using modified molecular parameters r and q. Five binary ethanol + congener mixtures were considered for new yield values for parameters r and q. The congeners considered were acetic acid, acetaldehyde, furfural, methanol, and 1-pentanol. Subsequently, the model was validated with the water + ethanol binary system, and the 1 -pentanol + ethanol + water, 1-propanol + ethanol + water, and furfural + ethanol + water ternary systems. 

In a countercurrent multistage section, the phases to be contacted enter a series of ideal or equilibrium stages from opposite ends. A contactor of this type is diagramatically represented by Fig. 8.1, which could be a series of stages in an absorption, a distillation, or an extraction column. Here L and V are the molal (or mass) flow rates of the heavier and lighter phases, and x,- and y,- the corresponding mole (or mass) fractions of component /, respectively. This chapter focuses on binary or pseudobinary systems so the subscript / is seldom required. Unless specifically stated, y and x will refer to mole (or mass) fractions of the lighter component in a binary mixture, or the species that is transferred between phases in three-component systems. 

While we have studied the properties of binary mixtures at constant temperature so far we shall now examine the behaviour of these mixtures at constant pressure. The conditions are those found in distillation, which is normally an isobaric process tending to establish equilibrium between the liquid and vapour phases. A boiling point diagram shows the boiling points and the equilibrium compositions of binary mix-... 

An excellent example of the implementation of SCFF to obtain palmitic acid from a plant source is the work of Brunner and Machado [7,72]. They conducted a detailed analysis on the fractionation of fatty acids from palm fatty acid distillates (99 % FFA (mainly palmitic, oleic and linoleic acid), 0.9 % squalene and 0.1 tocopherol) starting with a phase equilibrium analysis through to pilot plant studies and experimental verification of the separation. They postulated, from the phase equilibrium studies, that squalene and palmitie acid would be preferentially extracted and verified their postulation experimentally. They also considered a pseudo-binary mixture separation where palmitic acid is to be separated from oleic and linoleic acid and showed, using separation factors that this is possible. On pilot plant scale they showed that such a separation is feasible and balanced yield and extraet quality. At their optimum conditions (373 K, 29 MPa, extract to raffinate ratio of 1.2) they obtained an extract where the palmitic acid content was enriched from 52.5 % in the feed to 74.4 % in the extract and the oleic and linoleic acid content enriched from 46.3 % in the feed to 59.0 % in the raffinate. Squalene was also enriched in the extraet Irom 0.6 % in the feed to 1.2 % in the... 

The use of a y-x curve in the McCabe-Thiele method for binary distillation calculations brings up the matter of a flash-vaporization representation, in case the feedstream mixture is at saturation. An inspection of the y-x curve relative to a given feed composition shows that the equilibrium mixture varies along the curve over a range from the bubble point (where the liquid phase composition x is equal to that of the feed mixture x ) to the dew point (where the vapor composition y is equal to that of the feed mixture Xj.). Between the two is the region of flash vaporization, where the equilibrium compositions (y, x) respectively of phases V and L must satisfy the flash material balance relation F = V + L, where... 

Figure 13.10 on the next page summarizes the general appearance of some relatively simple temperature-composition phase diagrams of binary systems. If the system does not form an azeotrope (zeotropic behavior), the equilibrated gas phase is richer in one component than the liquid phase at all liquid compositions, and the liquid mixture can be separated into its two components by fractional distillation. The gas in equilibrium with an azeotropic mixture, however, is not enriched in either component. Fractional distillation of a system with an azeotrope leads to separation into one pure component and the azeotropic mixture. 

---