This work presents a formalized methodology for salt's separation from three component electrolytic systems. The methodology is based on the multi-variant modelling block of a generalized crystallization process, with options for simulating the boundary conditions of feasible equilibrium processes and the elements of crystallization techniques. The following techniques are considered: cooling crystallization, adiabatic evaporative-cooling crystallization, salt-out crystallization, isothermal crystallization, and a combination of the mentioned techniques. The multi-variant options of the crystallization module are based on different variable sets with assigned values for solving mathematical models of generalized crystallization processes. The first level of the methodology begins with the determination of salt crystallization paths from a hypothetical electrolytic AX-BX-H2O system, following by an examination of salt-cooling crystallization possibilities. The second level determines feasible processes by the communication of a feed-system with the environment through a stream of evaporated water, or introduced water with introduced crystallized BX salt. The third level determines the value intervals of the variables for feasible processes. The methodological logic and possibilities for the created process simulator are demonstrated on examples of sodium sulphate separation from the NaCl-Na2SO4-H2O system, using different salt concentrations within the feed system
The aim of this paper is to define feasible process pathways of fractional crystallization of NaCl and LiClO43H₂0 from LiClO₄-NaCl-H₂O system using the information on the equilibrium of the LiClO₄-NaCl-H₂O system at different temperatures, as well as the information on the composition of the starting solution obtained by electrolysis and double exchange with LiCl. The paper also synthesizes a feasible process structure that can be applied for the process of fractional crystallization, and gives a simulation of the process by calculating the material balance of the process. The parameters of relevant process paths that were obtained prove that the process presented in this paper is feasible in practice and applicable in industry.
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The influence of the fundamental parameters of non-ideal phase flow and the extraction parameters on the number of equilibrium stages - ND, theoretical stages - NT, as well as the number of stages (ND - NT), the existence of which is a consequence of the backflow in extractors, was investigated. The calculated number of stages (ND - NT) served as a measure of the influence of the denoted parameters on the extraction efficiency. The results of the investigation indicate that the number of stages (ND - NT) considerably increased with increasing backmixing coefficients and that the dependence was linear. It was established that the increase of the ratio of the flow rate of the heavy and light phase and the decrease of the equilibrium distribution coefficient, as well as the increase of the total separation factor, led to an exponential increase of the number of stages in the extractor, which consequently caused a decrease in the extraction efficiency
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