By F. B. Petlyuk
Writing for designers and operators of separation devices within the chemical, pharmaceutical, foodstuff, and similar industries in addition to software program designers, F.B. Petlyuk offers a transparent, multidimensional geometric illustration of distillation conception legitimate for all sorts of distillation column varieties, splits, and combinations. DistillDesigner software program permits refinement and affirmation of the algorithms of optimum layout. equipment of the overall geometric conception of distillation, encoded in DistillDesigner, supply quickly and trustworthy strategies to difficulties of flowsheet synthesis and to optimum layout calculations.
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Additional info for Distillation Theory And Its Application To Optimal Design Of Separation Units
1940b). Vapour–Liquid Equilibria in Ternary Systems. 2. The Course of the Distillation Lines in the System Acetone– Chloroform–Benzene. Rec. Trav. Chim. , 59, 401–406. Schreinemakers, F. A. H. (1901). Dampfdrucke ternarer Gemische. J. Phys. ). Serafimov, L. A. (1969). The Azeotropic Rule and the Classification of Multicomponent Mixtures. 4. N-Component Mixtures. J. Phys. ). Walas, S. M. (1985). Phase Equilibria in Chemical Engineering. Boston: Butterworth. Zharov, V. T. (1967). Free Evaporation of Homogeneous Multicomponent Solutions.
A. (1975b). Thermodynamic and Topological Analysis of Phase Diagrams of Polyazeotropic Mixtures. 2. Algorithm for Construction of Structural Graphs for Azeotropic Ternary Mixtures. J. Phys. ). Petlyuk, F. , Kievskii, V. , & Serafimov, L. A. (1977). Method for Isolation of Regions of Rectification Polyazeotropic Mixtures Using an Electronic Computer. Theor. Found. Chem. , 11, 1–7. Petlyuk, F. , Kievskii, V. , & Serafimov, L. A. (1979). Determination of Product Compositions for Polyazeotropic Mixtures Distillation.
The operating line of rectifying section has two ultimate positions: it may coincide with the diagonal line when R = ∞; it may be in a point xj = xF reach the equilibrium curve as it is shown in Fig. 2a (line 3 corresponds to minimum reflux R = Rmin ). , n = nmin (the steps between the equilibrium curve and the diagonal line are the largest ones). When R = Rmin (minimum reflux mode), the number of stages is infinite (in the feed point, the step between stages becomes equal to zero − this is an area of constant concentrations or pinch).
Distillation Theory And Its Application To Optimal Design Of Separation Units by F. B. Petlyuk