Manifestations of Fouling of Heterogeneous Membranes by Wine Components in the Process of their Tartrate Stabilization by Electrodialysis Method

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Tartrate stabilization of wine components by electrodialysis makes it possible to speed up and automate this process, as well as reduce the loss of valuable components. The widespread introduction of electrodialysis into industrial wine production is hampered due to fouling of ion-exchange membranes with wine components, as well as due to the very limited range of membranes currently used. This study is devoted to a comparative analysis of the properties of relatively inexpensive heterogeneous ion exchange membranes MA-41, MK-40 and AMH-PES, CMH-PES before and after their use in the tartrate stabilization of wine materials by electrodialysis. It has been shown that the mechanisms of fouling and its impact on transport characteristics, as well as on the development of electroconvection and the generation of H+, OH– ions are largely determined by the counterions that are transferred through cation-exchange (transition metal cations) and anion-exchange (carboxylic acid anions) membranes. Membranes MA-41, MK-40 demonstrate higher resistance to fouling during operation in electrodialysis units for less than 15 hours.

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Sobre autores

E. Pasechnaya

Kuban State University

Email: n_pismen@mail.ru
Rússia, Krasnodar, 149, Stavropolskaya St., 350040

M. Ponomar

Kuban State University

Email: n_pismen@mail.ru
Rússia, Krasnodar, 149, Stavropolskaya St., 350040

A. Klevtsova

Kuban State University

Email: n_pismen@mail.ru
Rússia, Krasnodar, 149, Stavropolskaya St., 350040

K. Kirichenko

Kuban State University

Email: n_pismen@mail.ru
Rússia, Krasnodar, 149, Stavropolskaya St., 350040

K. Solonchenko

Kuban State University

Email: n_pismen@mail.ru
Rússia, Krasnodar, 149, Stavropolskaya St., 350040

N. Pismenskaya

Kuban State University

Autor responsável pela correspondência
Email: n_pismen@mail.ru
Rússia, Krasnodar, 149, Stavropolskaya St., 350040

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2. Fig. 1. Optical images of the surfaces of the CMH-PES cation exchange membrane (a, c) and AMH-PES anion exchange membrane (b, d) after their operation in the electrodialysis process of tartrate stabilisation of model wine material in the NEP (a, b) and PEP (c, d) modes. The numbers (1) and (2) denote the surface areas that were not in contact and those that were in contact with the wine material. The light green box limits the polarisable region of the membranes. The inserts in the centre of each figure correspond to enlarged portions of the images.

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3. Fig. 2. Effect of pH on colour changes of optical images of surfaces (1, 2) and slices (3-8) of CMH-PES cation exchange membrane (a) and AMH-PES anion exchange membrane (b) after PEP operation.

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4. Fig. 3. IR spectra of the wine material (a) as well as AMH-PES (b) and MA-41 (c) membranes before and after electrodialysis under NEP and PEP current regimes.

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5. Fig. 4. Specific electrical conductivity of cation-exchange (a) and anion-exchange (b) membranes before and after their operation in the electrodialysis process under NEP and PEP current regimes. The studies were carried out in 0.5 M NaCl solution.

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6. Fig. 5. Voltampere characteristics of cation-exchange membrane CMH-PES (a) and anion-exchange membrane AMH-PES before and after electrodialysis in NEP and PEP modes (b), as well as pH difference at the outlet and inlet of desalting chambers (c, d) formed by the investigated and auxiliary membranes MA-41 (a, c) or MK-40 (b, d), respectively. The studies were carried out in 0.02 M NaCl solution. The values of the theoretical limiting current ilimLev are indicated by the dotted line.

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7. Fig. 6. Voltampere characteristics of cation exchange membrane MK-40 (a) and anion exchange membrane MA-41 (b) before and after electrodialysis in NEP and PEP modes, as well as pH differences at the outlet and inlet of desalting chambers (c, d) formed by the investigated and auxiliary membranes MA-41 (a, c) or MK-40 (b, d), respectively. The studies were carried out in 0.02 M NaCl solution. The values of the theoretical limiting current ilimLev are indicated by the dotted line.

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8. Fig. 7. Ratios of the values of experimental limiting currents found from WACs for cation-exchange (a) and anion-exchange (b) membranes operated in electrodialysis processes and initial cation-exchange (a) and anion-exchange (b) membranes.

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9. Fig. 8. pH difference at the outlet of desalting chambers formed by cation-exchange (a) and anion-exchange (b) membranes used in electrodialysis or original. Data are presented for i/ilimLev = 2.5.

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