Next Article in Journal
Direct Measurement of Crossover and Interfacial Resistance of Ion-Exchange Membranes in All-Vanadium Redox Flow Batteries
Next Article in Special Issue
Assessment of the Performance of Electrodialysis in the Removal of the Most Potent Odor-Active Compounds of Herring Milt Hydrolysate: Focus on Ion-Exchange Membrane Fouling and Water Dissociation as Limiting Process Conditions
Previous Article in Journal
ZrO2-TiO2 Incorporated PVDF Dual-Layer Hollow Fiber Membrane for Oily Wastewater Treatment: Effect of Air Gap
Previous Article in Special Issue
A 2D Convection-Diffusion Model of Anodic Oxidation of Organic Compounds Mediated by Hydroxyl Radicals Using Porous Reactive Electrochemical Membrane
 
 
Search for Articles:
Title / Keyword
Author / Affiliation / Email
Journal
Article Type
 
 
Advanced Search
 
Section
Special Issue
Volume
Issue
Number
Page
 
Journals
Membranes
Volume 10
Issue 6
10.3390/membranes10060125
membranes-logo
Submit to this Journal Review for this Journal Propose a Special Issue
► Article Menu

Article Menu

share Share announcement Help format_quote Cite question_answer Discuss in SciProfiles thumb_up
...
Endorse textsms
...
Comment
first_page
settings
Order Article Reprints
Font Type:
Arial Georgia Verdana
Font Size:
Aa Aa Aa
Line Spacing:
Column Width:
Background:
Article

The Development of Electroconvection at the Surface of a Heterogeneous Cation-Exchange Membrane Modified with Perfluorosulfonic Acid Polymer Film Containing Titanium Oxide

by
Violetta Gil
*,
Mikhail Porozhnyy
,
Olesya Rybalkina
,
Dmitrii Butylskii
and
Natalia Pismenskaya
Department of Physical Chemistry, Kuban State University, 149 Stavropolskaya st., 350040 Krasnodar, Russia
*
Author to whom correspondence should be addressed.
Membranes 2020, 10(6), 125; https://doi.org/10.3390/membranes10060125
Submission received: 12 May 2020 / Revised: 14 June 2020 / Accepted: 15 June 2020 / Published: 17 June 2020
(This article belongs to the Special Issue In-Depth on the Fouling and Antifouling of Ion-Exchange Membranes)
Browse Figures
Versions Notes

Abstract

:
One way to enhance mass transfer and reduce fouling in wastewater electrodialysis is stimulation of electroconvective mixing of the solution adjoining membranes by modifying their surfaces. Several samples were prepared by casting the perfluorosulfonic acid (PFSA) polymer film doped with TiO2 nanoparticles onto the surface of the heterogeneous cation-exchange membrane MK-40. It is found that changes in surface characteristics conditioned by such modification lead to an increase in the limiting current density due to the stimulation of electroconvection, which develops according to the mechanism of electroosmosis of the first kind. The greatest increase in the current compared to the pristine membrane can be obtained by modification with the film being 20 μm thick and containing 3 wt% of TiO2. The sample containing 6 wt% of TiO2 provides higher mass transfer in overlimiting current modes due to the development of nonequilibrium electroconvection. A 1.5-fold increase in the thickness of the modifying film reduces the positive effect of introducing TiO2 nanoparticles due to (1) partial shielding of the nanoparticles on the surface of the modified membrane; (2) a decrease in the tangential component of the electric force, which affects the development of electroconvection.

1. Introduction

The broader use of electro-membrane technologies for separation, concentration, and isolation of valuable substances from wastewater and liquid media of the food industry is constrained by fouling which is an accumulation of mineral and organic pollutants on the surface and in the volume of ion-exchange membranes [1,2,3,4]. Fouling leads to an undesired decrease in useful mass transfer and increase in energy consumption [5]. It reduces the lifespan of membranes and requires spending on their regular cleaning [6]. The result is a significant increase in the cost of the final product. One way to prevent fouling is to stimulate electroconvective mixing of the solution [7,8,9] by targeted selection of ion-exchange membranes, modifying their surface [9] and/or using pulsed current modes [7,8,9].
Nowadays, due to the works of Dukhin, Mishchuk [10,11], Rubinstein, Zaltzman [12,13], Nikonenko, Urtenov [14,15], and a number of other researchers [16,17,18] there are certain concepts of the mechanisms of electroconvection (EC) and those factors that can induce electroconvective vortices. The details of these ideas are described in the review [19]. There are two main mechanisms for the development of EC. Bulk EC-I is due to the effect of an electric field on the residual space charge in a quasi-electroneutral electrolyte solution with an uneven concentration distribution. EC-II is caused by the electroosmotic slip of the space charge region (SCR). This SCR is formed in a depleted solution at the boundary with the membrane. A high degree of hydrophobicity of the membrane surface facilitates the fluid slip and stimulates EC-II [20,21,22].
Both EC-I and EC-II can be of two kinds currently known. (Quasi) equilibrium EC develops at low currents/voltages (i ≤ ilim; ilim is the limiting current). In this case, the electrical double layer (EDL) at the membrane/depleted solution boundary is (quasi) equilibrium. The structure of the diffuse part of the EDL retains the Boltzmann distribution of ions which is shifted by an imposed external field [23]. In the case of EC-I, this kind of electroconvection is denoted by the term “electroosmosis of the first kind” [10,11]. Equilibrium EC can develop only at the electrically inhomogeneous and/or curved surface, which stimulates an appearance of the tangential component of an electric force. Its development is facilitated by a high surface charge [24]. In this case, small stable electroconvection vortices arise in the solution adjacent to a membrane. These vortices deliver a more concentrated solution to the depleted diffusion layer. This results in the “negative” conductance of the membrane system, when its resistance near the limiting current becomes lower than at i << ilim, and also in the growth of the experimentally determined limiting current compared to that calculated by the convective-diffusion model [24,25].
In overlimiting current modes (i ≥ ilim), a nonequilibrium EC [13], also called “electroosmosis of the second kind”, develops [11]. An indispensable condition for the development of a nonequilibrium EC is the presence of an extended SCR (which is outside the quasi-equilibrium EDL) and fluctuations in the concentration, electric fields, or the fluid velocity field, which, as a rule, occur in intensive current modes. The reason for the hydrodynamic instability after reaching a certain threshold value of the potential drop is the appearance of a positive feedback between the fluctuation of the local tangential force and the liquid electroosmotic slip velocity [12,26]. As a result, electroconvection vortices become larger than those in the case of equilibrium EC [27]. Their instability with time is the reason for the noticeable oscillations of the current (potential drops) observed in intensive current modes on the current-voltage characteristics (CVCs) and chronopotentiograms (ChPs) [9,28]. Partial removal of the diffusion limitations of salt delivery to the receiving side of the membrane is expressed in a reduction in length and an increase in the slope of the CVC plateau [9,28,29].
Thus, the development of EC is facilitated by electrical [9,28,29,30] and geometric [31,32] heterogeneity of the surface, a high degree of its hydrophobicity [24,25], and also a high electric charge [24]. The specified surface characteristics are achieved by profiling the surface of the membranes [31,32], varying the dispersion of the ion-exchange resin particles in heterogeneous membranes [33,34], and by modifying the membrane surface with various polyelectrolytes [29,30,35], in particular, conductive perfluorosulfonic acid (PFSA) polymer films [9,20,24,28]. Doping such a film with carbon nanotubes enhances electroconvection due to an increase in hydrophobicity and an increase in surface roughness [20]. It is very promising to increase the surface charge by doping the PFSA film with nanoparticles of metal oxides (such as TiO2, ZrO2, SiO2). Currently, these dopants are mainly introduced into the pores of membranes and are widely used to increase their conductivity at low relative humidity in the fuel cells [36,37,38,39] and improving membrane permselectivity [40,41]. Recent studies revealed that the deposition of TiO2-doped films on the surface increases the fouling resistance of the ultrafiltration, osmosis, and ion-exchange membranes [42,43,44]. For example, the authors of [44] modified the surface of the anion-exchange membrane by poly (sodium 4-styrene sulfonate) (PSS) with titanium dioxide nanoparticles. They found an increase in the surface charge and its hydrophilicity, as well as the self-cleaning ability of this surface due to photocatalytic decomposition caused by ultraviolet irradiation. Apparently, the effect of such surface modification on the development of electroconvection has not yet been investigated.
The aim of this work is to study the development of electroconvection as a function of the titanium oxide mass fraction in a perfluorosulfonic acid polymer film that modifies the surface of a heterogeneous cation-exchange membrane.
We hope that in the future, such a modification method can be used to create a new generation of ion-exchange membranes that are resistant to sedimentation and fouling during electrodialysis processing of liquid media of the food industry and natural waters.

2. Materials and Methods

2.1. Membranes

Commercial heterogeneous cation-exchange MK-40 membrane (Shchekinoazot, Pervomayskiy, Tula Region, Russia) is used as the substrate for preparing the modified membrane samples. The MK-40 membrane is produced by hot pressing of a mixture of polyethylene (inert binder) and powdered KU-2 ion-exchange resin (styrene-divinylbenzene sulfonated copolymer) and contain fixed sulfonic acid functional groups. Most of the surface (more than 80%) of the MK-40 membrane is non-conductive [45]. Grains of KU-2 ion-exchange resin, which form crests on the polyethylene surface, provide selective conductivity of the membrane.
The modified membranes were prepared by forming a thin homogeneous film on the MK-40 membrane surface by casting an LF-4SK solution (Plastpolymer, Saint Petersburg, Russia), containing a certain amount of titanium oxide particles. The LF-4SK is a solution of tetrafluoroethylene copolymer with sulfonated perfluorovinylether in isopropyl alcohol. Solvent evaporation gives a film identical to the MF-4SK membrane, a Russian analogue of the Nafion membrane. To prepare the modifier, the required amount of titanium butoxide (EKOS-1, Moscow, Russia) was added to the LF-4SK solution, then the modifier was placed in an ultrasonic bath PSB-2835-05 (Ultrasonic Equipment Center PSB-Gals, Moscow, Russia) to disperse the formed particles.
Modification of the membranes was carried out according to a method similar to that described in [46]. Before applying the modifier, the surface of the MK-40 substrate-membrane was roughened using a fine-grained abrasive sandpaper (P600). Application of the modifier solution on the membrane surface was carried out via drop casting. Preparing the MK-4021 sample, an LF-4SK solution containing no titanium oxide particles was used. The MK-4021 membrane was used as a reference sample to detect the effect of titanium oxide particles. The characteristics of the commercial and modified membranes are given in Table 1.

2.2. Methods

2.2.1. Voltammetry, Chronopotentiometry, and Impedance Spectroscopy

The electrochemical characteristics, the current-voltage curves, chronopotentiograms, and impedance spectra of the studied membranes were obtained using the experimental setup shown in Figure 1, its detailed description is presented in Supplementary Materials. The setup includes a laboratory four-compartment flow electrodialysis cell, described in detail in [45]. The compartments of the cell were formed by the studied cation-exchange membrane (C*) and auxiliary anion-exchange MA-41 (A) and cation-exchange MK-40 (C) membranes. Current was supplied to the cell and the potential drop was measured using an electrochemical complex Autolab PGSTAT-100 (EcoChemi, Utrecht, The Netherlands). The experimental procedure for obtaining ChP and CVC is detailed in [45].
To measure the electrochemical impedance spectra, the closed silver chloride measuring electrodes (immersed in the saturated KCl solution) used in the ChP and CVC measurements were replaced by open silver chloride electrodes (immersed in 0.02 M NaCl solution). It takes about 2 h to get one spectrum. Before recording the complex impedance, the membrane was preliminarily held for 40 min at a given direct current density. Then alternating current was applied. The time required to achieve a quasistationary state at a given frequency was determined automatically by the Autolab PGSTAT-100 complex. Impedance spectrum recording starts at a low frequency equal to 0.003 Hz and ends at a frequency equal to 5 × 105 Hz. From the values of the real (ReZ) and imaginary (ImZ) components of the impedance of the membrane system obtained at a given frequency and at a given direct current density, the corresponding values (ReZ and ImZ) obtained at zero direct current (i = 0 A) were subtracted. This data processing allows one to exclude from consideration (1) the contribution of the measuring electrode system impedance to the studied membrane system impedance, (2) the ohmic resistance of the membrane and the response of the membrane system to the alternating current bias (the amplitude of alternating current is 0.25 mA). In preliminary experiments, it was shown that in the studied direct current range, polarization phenomena do not significantly affect the impedance of the measuring electrodes. The advantage of such processing of the impedance spectra is the reduction of errors, which occur as the result of electrochemical cell reassembling to determine the impedance of the measuring electrode system.
As a rule, the high-frequency arc [48,49] (in the range from 103 to 1.3 × 105 Hz) dominates the impedance spectrum obtained at zero direct current and presented in Nyquist plot. It characterizes the membrane and interphase boundaries [50,51]. The intercept by this arc on the ReZ axis corresponds to the ohmic resistance of the membranes RΩ [48,49,52,53], and the frequency at the maximum of the ImZ, fmax, allows one to estimate the effective electric capacitance C of the membrane/solution interface by the formula [50]:
C = 1 2 π f max ( − Im Z max )
where ‒ImZmax is the maximum value of the imaginary impedance component at the high-frequency arc. This capacitance includes the capacitances of the EDLs on the membrane/solution boundaries, as well as the capacity caused by the asymmetry of the depleted and enriched diffusion boundary layers DBLs, which occurs when a direct electric current flows.
If the applied direct current is greater than zero, taking into account the experimental data processing mentioned above, the intercept by the high-frequency arc on the ReZ axis gives the ohmic resistance of the diffusion layers. The appearance of the Gerischer arc in the medium-frequency range of the spectrum (10–103 Hz) indicates the presence of an intense chemical reaction at the membrane/solution interface, namely, the generation of H+ and OH– ions, catalyzed by fixed groups of membranes [54]. The low-frequency (0.003–10 Hz) arc of the spectrum (finite-length Warburg impedance) characterizes the diffusion and electroconvective transfer of ions in DBL adjacent to a membrane. The DBL thickness can be found from difference in values of real component of the low-frequency arc for the lowest and the highest frequencies [55]. The ratio of the lengths of the intercepts by each of these arcs on the ReZ axis gives information on the contribution of each of the phenomena (the formation of concentration profiles near the membrane surface; the appearance and transport of new charge carriers at the membrane/solution interface; a decrease in the diffusion layer thickness due to electroconvection) to electrochemical characteristics of the studied membrane systems [35].
The experiments are conducted at a constant temperature of 25 ± 1 °C.

2.2.2. Diffusion Permeability and Conductivity Measurements

The concentration dependence of membrane conductivity is measured by the differential method using a clip-type cell [56,57] and a MOTECH MT4080 immittance meter at an AC frequency of 1 kHz. The measurements were carried out in NaCl solutions with different concentrations (0.1, 0.25, 0.5, 0.75, 1 M).
The experimental investigation of the concentration dependence of diffusion permeability was conducted at the same NaCl concentrations. The measurements were carried out using two-compartment cell and conductivity meter Expert 002 (Econix-Expert, Ltd., Moscow, Russia) [58].
The thickness of studied membranes was measured using a digital micrometer Schut Filetta (Schut Geometrical Metrology, Groningen, The Netherlands).

2.2.3. Contact Angles Measurements

The contact angles (θ) of the membranes under study were measured using the sessile drop technique [20] described in detail in Supplementary Materials. The studied membrane was in a swollen state, it was removed from the 0.02 M NaCl solution immediately before the measurements. The contact angles reported in this paper were registered 20 s after the applying a drop of distilled water on the membrane surface.

2.2.4. Surface Roughness Measurements

The surface roughness of the studied membranes was determined by using an optical microscope SOPTOP CX40M (Ningbo Sunny Instruments Co., Ltd., Yuyao, China). The surface of a membrane is shaped of so-called “hills” and “valleys”, corresponding to the highest and lowest areas of the membrane relief. The difference between these two extreme forms of the membrane surface shape, parameter b (μm), characterizes the roughness and is measured by moving the objective and focusing on them, the focal length of the system being the same.

3. Results and Discussion

3.1. Substrate and Modified Membranes Characterization

The results of the contact angle measurements are presented in Table 1. Table 2 shows the values of the effective electric double layer capacity at the membrane/depleted solution interface, as well as the ohmic resistance of the membranes found from the analysis of the high-frequency arc of the electrochemical impedance spectrum.
As expected, perfluorosulfonic acid polymer casting onto the surface of the heterogeneous substrate MK-40 membrane leads to an increase in hydrophobicity of the surface that results in the higher value of contact angle (sample MK-4021). This is attributed the less roughened surface of the modified membranes. Indeed, according to Wenzel [59], the effect of the surface roughness is to magnify its wetting properties: if the surface is hydrophilic, it will be more hydrophilic, the rougher the surface. Applying the PFSA layer results in flattening the surface of the modified membrane compared to the substrate membrane, which leads to lower hydrophilicity of the modified membrane surface and, consequently, the higher contact angle.
Adding the titanium dioxide nanoparticles into the modifying film (samples MK-4021+3%, MK-4021+6%, MK-4033+3%, and MK-4033+6%) results in increasing hydrophilicity of the membrane surface with increasing TiO2 mass fraction due to hydrophilic properties of the particles [60] and as the result of the increase in its roughness [61].
Figure 2 shows that applying the PFSA layer results in flattening the surface of the modified membrane compared to the substrate membrane. Adding the titanium dioxide nanoparticles into the modifying film results in decreasing the flattening effect. The greater the fraction of TiO2, the lesser the effect of the modifying film. However, all the modified membranes have the less roughened surface compared to the substrate membrane.
The application of a modifying film practically does not change the ohmic resistance of the studied membranes, but noticeably affects the effective electric capacitance of their interphase boundary (Table 2). This capacity increases slightly after depositing the PFSA polymer film (sample MK-4021) and increases noticeably after inserting TiO2 particles into this film (samples MK-4021+3% and MK-4021+6%). Note that this increase is observed if the thickness of the modifying film remains almost constant. In the case where the thickness of the PFSA polymer film increases by 1.5 times (samples MK-4033+3% and MK-4033+6%), the addition of TiO2 nanoparticles to it practically does not lead to changes in the effective capacitance of the interphase boundary. It is known from studies in the field of electrode kinetics that the capacitance of the interphase boundary increases with increasing electric charge of the dense part of the electric double layer [50,62]. Apparently, coating the entire surface of the MK-4021 sample with an ion-conducting film leads to an increase in its electric charge in comparison with the substrate membrane (MK-40 sample), about 80% of which is occupied by inert polyethylene [9,28,46]. The introduction of 3 wt% particles into this film (sample MK-4021+3%) increases the charge of the membrane/solution interface. A further increase in the percentage of nanoparticles in the modifying film leads to an increase in the roughness of the modifying film/depleted solution interface, as well as a reorientation of the side chains of PFSA polymer with sulfone fixed groups towards charged nanoparticles. The result of this reorientation is “repulsion” to the surface of the main chains of the modifying material that do not have an electric charge. Similar phenomena are discussed in the works [63,64]. Apparently, in the case of using thicker films (samples MK-4033+3% and MK-4033+6%), the reorientation of the side chains becomes crucial. Therefore, the introduction of nanoparticles does not lead to noticeable changes in the effective capacitance of the interphase boundary. To make sure our assumptions are correct, in the future we plan to conduct a direct measurement of the charge of the samples under study.
An important parameter characterizing the membrane permselectivity is the counterion transport number, t i * . In the case of the studied cation-exchange membranes and sodium chloride solution, the value of t + * shows the portion of the electric current transferred by the Na+ ion in conditions of the absence of diffusion. To evaluate the t + * value, it is possible to use the following relationship, [65]:
t - * = 1 2 − 1 4 − P * F 2 c 2 R T κ * ,     t + * = 1 − t - *
where t - * is the transport number of coion; P* and κ* are the diffusion permeability and the electrical conductivity of the membrane, respectively; c is the concentration of the electrolyte solution; F, R, and T have their usual meanings. Using the experimentally determined values of electrical conductivity and diffusion permeability the counterion transport numbers in the studied membranes are calculated and presented in Figure 3 as function of NaCl solution concentration. It follows from this dependence that the modification of the samples practically does not change the counterion transport numbers in comparison with the substrate membrane. Values of t i * remain high throughout the studied range of NaCl solution concentrations. The concentration dependencies of the conterion (Na+) transport number are approximated and extrapolated to the region of lower concentration (0.02 M), which corresponds to the measurements of the electrochemical characteristics (CVC, ChP, and impedance spectra). As a result, the values of the conterion transport number in the studied membranes at this concentration are virtually the same and equal to 1.

3.2. Electroconvection and Water Splitting at the Surface of the Substrate Membrane and Modified Membranes

3.2.1. Current-Voltage Curves

Figure 4 shows the ratio of the current density to its theoretical limiting value, i / i lim th as well as the difference in the pH between the outlet (pHout) and inlet (pHin) solution passing through the desalination compartment (DC) of the electrodialysis cell, ΔpH (ΔpH = pHout − pHin), as functions of reduced potential drop, ∆φ’. This is a potential drop between the Luggin’s capillaries, from which the ohmic component is subtracted. The exact definition of ∆φ’ is given in the Supplementary Materials. The value i lim th was calculated using the Leveque equation [66], which was derived in the framework of the convective-diffusion model under the assumption that the membrane has a smooth, homogeneous ion-conducting surface. In the conditions of our experiments, this calculation gives i lim th = 2.01 mA cm−2 (see Supplementary Materials).
Three sections can be distinguished on the CVC [12,67]: an initial section (I), a slope plateau (II), and a section of a sharp growth of current density (III). It is believed [13,25,35], that the increase in the experimental current over the theoretical value i lim th is determined by the EC, which develops according to the mechanism of electroosmosis of the first kind. The slope of the plateau characterizes the increase in the depleted diffusion layer conductivity as compared to that achieved at i lim th due to the development of equilibrium EC [12,19]. The plateau length (determined by the potential drop, at which section II of the CVC turns into section III) corresponds to the threshold value of the potential drop at which a nonequilibrium EC occurs [12,19]. These characteristic parameters found by graphical treatment of the CVC (Figure 4) are summarized in Table 3.
Before discussing the obtained results, we recall that the modification of the membranes did not lead to any noticeable change in their selectivity (Figure 3), which could affect the values of the limiting currents.
From these data it follows that in the case of the MK-40 substrate membrane the value i lim exp / i lim th is less than unity. This result is expected, because only 20% of the surface of this membrane conducts electric current. The increase in current above the value i lim exp / i lim th = 0.20 (which would correspond to the fraction of the conductive surface) is due to the tangential transport of salt from non-conductive regions to conductive ones, as well as due to electroconvection. The latter is stimulated by the “funnel effect” described by Rubinstein et al. [68], that is, curvature of streamlines and their crowding at inclusions of ion-exchange resin particles in polyethylene on the MK-40 surface [20] (Figure 5a). The value of the potential drop (plateau length), at which the development of a nonequilibrium EC begins, is close to the theoretically predicted one in the articles by Rubinstein and Zaltsman [12].
As in previous works [20,28], the deposition of the PFSA polymer film is accompanied by an increase in the i lim exp / i lim th ratio, a decrease in the plateau length, and an increase in the conductivity of the depleted diffusion layer. This is facilitated by a decrease in surface hydrophilicity (Table 1), as well as by an increase in ion-conducting gates through which streamlines enter the ion-exchange membrane. Inserting 3 wt% TiO2 into the PFSA polymer film (sample MK-4021+3%) stimulates the development of all types of EC. Indeed, the i lim exp / i lim th ratio, which is an indicator of the contribution of electroosmosis of the first kind to the increase in near-surface salt concentration, increases (Table 3). The plateau length, that is, the threshold potential drop at which a nonequilibrium EC occurs, is reduced in comparison with the MK-40 and MK-4021 samples. Apparently, this is facilitated by an increase in the electric charge while maintaining a rather high degree of hydrophobicity of the MK-4021+3% sample surface (see Section 3.1).
Note that even a slight increase in surface hydrophilicity while maintaining almost the same value of the effective capacitance of the interphase boundary of the modifying film/depleted solution (see Section 3.1) led to a decrease in the i lim exp / i lim th value in the case of MK-4021+6% sample as compared to MK-4021+3%. Nevertheless, in the case of MK-4021+6% sample, the plateau length turned out to be minimal, and the plateau inclination turned out to be maximum among all the studied membranes. It can be assumed that the ratio of surface characteristics achieved in this sample turned out to be the most optimal for facilitating the development of nonequilibrium EC. Which of these characteristics became decisive for the stimulation of this type of EC is to be determined in subsequent experiments.
MK-4033+3% and MK-4033+6% samples, which were modified with a thicker PFSA polymer film, demonstrated a more modest ability to stimulate EC in comparison with not only MK-4021+3% and MK-4021+6% samples, but also with a sample that does not contain TiO2 particles. The reasons for such a behavior of the MK-4033+3% and MK-4033+6% samples were already discussed in Section 3.1. In addition, it can be assumed that at a thickness of the modifying film of about 20 μm (MK-4021, MK-4021+3%, MK-4021+6% samples), the streamlines remain sufficiently curved to stimulate the increase in the tangential component of the electric force at the modifying film/depleted diffusion layer (Figure 5b). A 1.5-fold increase in the thickness of this film (MK-4033+3% and MK-4033+6% samples) apparently weakens the curvature of streamlines in the near-membrane layer of the solution, thereby reducing the tangential component of the electric force (Figure 5c).

3.2.2. Chronopotentiometric Curves

Chronopotentiometry data provide additional details on the effect of modification on the degree of the membrane surface heterogeneity and on the mechanisms of EC development in the studied membrane systems.
Figure 6 shows the chronopotentiometric curves, ChPs, of the studied membranes obtained at i / i lim th = 2. When plotting ChP, the reduced potential drop, ∆φ’, [69] is used (see the Supplementary Materials). Table 4 summarizes the transition times, τexp, for various i / i lim th . They were determined by the inflection points on the initial sections of the ChPs (indicated by points in Figure 6). According to the classical Sand theory [70] and later studies [71], the inflection point on the ChP corresponds to the state of the system where the electrolyte concentration at the membrane surface decreases to minimum values, and the new mechanism of electric charge transfer begins to play a dominant role. These can be large electroconvection vortices that develop according to the mechanism of nonequilibrium electroconvection and deliver a more concentrated electrolyte solution to the membrane surface, and/or the water splitting, which is a source of new charge carriers (H+/OH–) ions [72]. A number of recent studies have shown that equilibrium electroconvection, which develops according to the mechanism of electroosmosis of the first kind, contributes to an increase in the transition times [25,35]. Small EC vortices formed by this mechanism cannot completely obviate the diffusion limitations of electrolyte delivery, which increase with increasing time from the moment the current is turned on. However, the delivery of a slightly more concentrated solution from the depleted diffusion layer shifts the moment of reaching the minimum surface concentration to greater times.
From the obtained data (Figure 6, Table 4) it follows that any modification of the MK-40 substrate membrane contributes to an increase in the transition times. The greatest differences in the behavior of the modified samples are observed in the current range 1.25 < i / i lim th < 2.5. Moreover, the best ability to stimulate equilibrium EC, which is expressed in the prolongation of transition times, demonstrate MK-4021+3% and MK-4033+3% samples. These results are consistent with voltammetry data (Section 3.2.1). Apparently, at too high currents, the values of the transition times are reached so quickly that the equilibrium EC does not have time to fully develop.
As already mentioned in Section 1, in the case of a nonequilibrium EC, large vortices form clusters. Under conditions of forced convection of the solution, these clusters move along the surface of the membranes under the measuring capillaries, which is expressed in the oscillations of the recorded potential drop. We registered such oscillations for all studied membranes (Figure 6). The largest amplitude of oscillations, which indicates the development of larger EC cluster structures, is demonstrated by MK-4021 and MK-4021+6% samples. This result also confirms the conclusions made by us after analyzing the CVCs.
It should be noted that the chronopotentiometry data allow one to assess the degree of membrane surface electrical heterogeneity: the higher this heterogeneity, the faster the potential drop increases in the first few seconds after turning on the current [71]. From the obtained data (Figure 6), it follows that the surface of the MK-4021 and MK-4021+6% samples is less electrically heterogeneous in comparison with other studied membranes. This experimental fact allows one to conclude that the high ability of the MK-4021+6% sample to stimulate EC is mainly caused by an increase in the electric charge of the modifying film/solution interface rather than by an increase in the surface roughness after introducing 6 %wt TiO2 into the PFSA polymer film.

3.2.3. Impedance Spectra under Direct Current Condition and the pH Difference at the Outlet and Inlet of the Desalination Channel of the Electrodialysis Cell

Figure 7 and Figure 8 show the electrochemical impedance spectra obtained for the studied membranes at 1.5 and 1.8 i / i lim th . All these spectra consist of two arcs. The first high-frequency arc is characterized by frequencies at the point of maximum along the ordinate axis from 8.5 to 17.5 kHz. Similar characteristic frequencies for this arc (5–11 kHz) are demonstrated by the homogeneous cation-exchange membrane CMX (Astom, Tokyo, Japan), studied under similar conditions [73].
The length of the high-frequency arc chord corresponds to the resistance of the membrane system, RI (in our case, mainly a depleted diffusion layer), which depends on the degree of polarization caused by direct current [48,49]. From the obtained data, it follows that the maximum value of such resistance at a given direct current is achieved in the case of a substrate membrane MK-40. Any modification of its surface leads to a decrease in RI. The values decrease in the same series in which the ability of membranes to stimulate EC increases: MK-40 > MK-4033+6% ≥ MK-4033+3% > MK-4021+3% > MK-4021+6% ≈ MK-4021. The appearance of the Warburg impedance arc is caused by the time delay of changes in the electrolyte concentration in the quasi-electroneutral layer of the solution adjacent to the membrane in response to the alternating current bias [49,74,75]. According to the classical assumptions [49,75], the reason for this delay (and the delay caused by it in changes in the potential drop) is the finite rate of the electrolyte diffusion. According to modern concepts, this rate can change in the presence of electroconvective vortices at the membrane surface. Their appearance is accompanied by distortion in the regular shape of the arc. The more intensive electroconvective mixing, the stronger the spread of points in this region of the spectrum. The characteristic value of the frequency at the maximum point of the Warburg arc is 10 mHz [35,73]. Our results confirm that the second arc corresponds to Warburg impedance. Moreover, the effect of electroconvection on this arc (expressed in an increasing spread of points), increases with increasing density of the overlimiting current. This effect is characteristic for all the studied samples. Apparently, the electroconvective mixing provides a sufficiently high salt concentration at the membrane/solution interface. As a result, even at sufficiently high current densities (Figure 7 and Figure 8), the Gerischer arc, which appears in the case of a homogeneous CMX membrane with the same sulfonic fixed groups at i / i lim th = 1.6, cannot be identified on the impedance spectra. As mentioned earlier, the Gerischer impedance [54] corresponds to the resistance caused by a chemical reaction (in our case, water splitting) at the membrane surface/depleted diffusion layer interface. In the case of the CMX membrane, the characteristic frequencies corresponding to the maximum points of this arc have values of about 4 Hz. In the considered systems, these values are situated in the region of the spectrum where the second arc is bordering the high-frequency arc. Note that this region is characterized by the absence of spread of points and does not represent a straight line passing at a 45° angle to the ReZ axis (such characteristics should have the initial part of the finite-length Warburg impedance [50]). Apparently, the deviation of this part of the spectrum from the classical form is caused by the influence of water splitting. An indirect evidence of this reaction, at least at high current densities, is the fact that the ReZ takes a negative value, recorded in the case of MK-40 ( i / i lim th = 1.8) in the frequency range 35–500 kHz. A similar shape of spectra was observed in the case of water splitting for many membrane systems [35,73]. However, the rate of this reaction in studied systems is so small that the Gerischer arch does not appear.
Nevertheless, this water splitting at the cation-exchange membrane/solution interface, affects the pH difference at the outlet and inlet of the desalination channel, which is formed by the studied cation-exchange membranes and the MA-41 anion exchange membrane. This follows from Figure 4 that shows the difference in the pH between the outlet and the inlet solution passing through the desalination compartment of the electrodialysis cell, ΔpH, as functions of reduced potential drop, ∆φ’. The MA-41 membrane contains a certain amount of secondary and tertiary amines, whose catalytic activity with respect to the water dissociation reaction is quite high [76,77]. The protons generated on the surface of this membrane acidify the desalinated solution. As a result, ΔpH of the solution is less than zero. In the case where the water splitting also occurs on the surface of the cation-exchange membrane, hydroxyl ions enter the solution. As a result, ΔpH of the solution should tend to zero or even positive values. The closer the ΔpH of the solution to zero, the more intensive the water splitting on the surface of the cation-exchange membrane. Indeed, in intensive current modes, the water splitting rate on the MK-4033+6% surface is close to that observed on the MK-40 substrate membrane. The lowest water splitting rate occurs in the case of MK-4021 and MK-4021+6% samples. As already mentioned, the cause of the decrease in water splitting is electroconvection, which shifts intensive water splitting to the range of higher potential drops.

4. Conclusions

The surface of the MK-40 heterogeneous cation-exchange membrane was modified with a Nafion-type PFSA polymer film containing TiO2 nanoparticles.
It was shown that such modification does not affect the selectivity of the obtained samples. All of them, like the MK-40 substrate membrane, are characterized by counterion transport numbers (Na+) close to 1. Introduction of TiO2 nanoparticles (from 3 to 6 wt%) into the modifying film leads to an increase in surface charge while maintaining a sufficiently low degree of its hydrophilicity.
These changes in surface characteristics result in an increase of the experimental limiting current density on 9–39% due to the stimulation of electroconvection, developing by the mechanism of electroosmosis of the first kind. The greatest increase in current as compared to the substrate membrane can be obtained at a particle concentration of 3 wt%. A sample containing 6 wt% provides greater mass transfer in overlimiting current modes due to the development of nonequilibrium electroconvection. Electroconvective mixing of the solution leads to an increase in the near-surface salt concentration as compared to the substrate membrane. As a result, water splitting on the surface of modified samples exerts an extremely insignificant effect on their mass transfer characteristics in intensive current modes.
The above results are achieved with a thickness of the modifying film equal to 20 μm. A 1.5-fold increase in the thickness of this film reduces the positive effect of the introduction of TiO2 nanoparticles due to (1) partial shielding of the nanoparticles on the surface of the modified membrane; (2) a decrease in the tangential component of the electric force, which affects the development of electroconvection.
The tested relatively simple method of surface modification of commercial membranes can be used to increase mass transfer and increase their resistivity to sedimentation and fouling in the processes of electrodialysis processing of natural water and liquid media of the food industry.

Supplementary Materials

Supplementary materials can be found at https://www.mdpi.com/2077-0375/10/6/125/s1. Figure S1: Principal scheme of the experimental setup: electrodialysis cell (1) consisting of one desalination compartment (DC), one concentration compartment (CC) and two electrode compartments; tanks with solutions (2, 3); Luggin’s capillaries (4), connected with silver chloride electrodes (5); electrochemical complex Autolab PGSTAT-100 (6); flow pass cell with pH combination electrode (7), connected to pH-meter Expert 001 (8). Figure S2: The experimental setup for contact angles measurements: dispenser of the test liquid (1); closed optically transparent box (2); camera with sufficient magnification (3); drop of the test liquid (4); test sample (5); filter paper (6); layer of the test liquid (7); sample stand (8).

Author Contributions

Conceptualization, N.P. and V.G.; Methodology, N.P., V.G. and M.P.; Formal Analysis, N.P., V.G. and M.P.; Investigation, M.P., O.R. and D.B.; Writing—Original Draft Preparation, V.G. and M.P.; Writing—Review and Editing, V.G. and N.P.; Experimentation, M.P., O.R. and D.B.; Supervision, N.P.; Project Administration, V.G.; Funding Acquisition, V.G. All authors approved the final article. All authors have read and agreed to the published version of the manuscript.

Funding

This study was realized with the financial support of the Russian Science Foundation, Grant no. 19-79-00347.

Acknowledgments

We are grateful to V. Konshin for his valuable advice about the methods of membrane modification.

Conflicts of Interest

The authors declare no conflict of interest.

References

  1. Barros, K.S.; Scarazzato, T.; Pérez-Herranz, V.; Espinosa, D.C.R. Treatment of Cyanide-Free Wastewater from Brass Electrodeposition with EDTA by Electrodialysis: Evaluation of Underlimiting and Overlimiting Operations. Membranes (Basel) 2020, 10, 69. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  2. Shi, L.; Hu, Z.; Simplicio, W.S.; Qiu, S.; Xiao, L.; Harhen, B.; Zhan, X. Antibiotics in nutrient recovery from pig manure via electrodialysis reversal: Sorption and migration associated with membrane fouling. J. Memb. Sci. 2020. [Google Scholar] [CrossRef]
  3. Mikhaylin, S.; Bazinet, L. Fouling on ion-exchange membranes: Classification, characterization and strategies of prevention and control. Adv. Colloid Interface Sci. 2016, 229, 34–56. [Google Scholar] [CrossRef] [PubMed]
  4. Ghalloussi, R.; Chaabane, L.; Larchet, C.; Dammak, L.; Grande, D. Structural and physicochemical investigation of ageing of ion-exchange membranes in electrodialysis for food industry. Sep. Purif. Technol. 2014, 123, 229–234. [Google Scholar] [CrossRef]
  5. Shi, L.; Xie, S.; Hu, Z.; Wu, G.; Morrison, L.; Croot, P.; Hu, H.; Zhan, X. Nutrient recovery from pig manure digestate using electrodialysis reversal: Membrane fouling and feasibility of long-term operation. J. Memb. Sci. 2019. [Google Scholar] [CrossRef]
  6. Garcia-Vasquez, W.; Dammak, L.; Larchet, C.; Nikonenko, V.; Grande, D. Effects of acid–base cleaning procedure on structure and properties of anion-exchange membranes used in electrodialysis. J. Memb. Sci. 2016, 507, 12–23. [Google Scholar] [CrossRef]
  7. Mikhaylin, S.; Nikonenko, V.; Pourcelly, G.; Bazinet, L. Intensification of demineralization process and decrease in scaling by application of pulsed electric field with short pulse/pause conditions. J. Memb. Sci. 2014, 468, 389–399. [Google Scholar] [CrossRef]
  8. Dufton, G.; Mikhaylin, S.; Gaaloul, S.; Bazinet, L. Positive Impact of Pulsed Electric Field on Lactic Acid Removal, Demineralization and Membrane Scaling during Acid Whey Electrodialysis. Int. J. Mol. Sci. 2019, 20, 797. [Google Scholar] [CrossRef] [Green Version]
  9. Andreeva, M.A.; Gil, V.V.; Pismenskaya, N.D.; Dammak, L.; Kononenko, N.A.; Larchet, C.; Grande, D.; Nikonenko, V.V. Mitigation of membrane scaling in electrodialysis by electroconvection enhancement, pH adjustment and pulsed electric field application. J. Memb. Sci. 2018, 549, 129–140. [Google Scholar] [CrossRef]
  10. Dukhin, S.S.; Mishchuk, N.A.; Takhistov, P.V. Electroosmosis of the second kind and unrestricted current increase in the mixed monolayer of an ion-exchanger. Colloid J. USSR 1989, 51, 540–542. [Google Scholar]
  11. Mishchuk, N.A. Concentration polarization of interface and non-linear electrokinetic phenomena. Adv. Colloid Interface Sci. 2010, 160, 16–39. [Google Scholar] [CrossRef] [PubMed]
  12. Rubinstein, I.; Zaltzman, B. Electro-osmotically induced convection at a permselective membrane. Phys. Rev. E 2000, 62, 2238–2251. [Google Scholar] [CrossRef] [PubMed]
  13. Rubinstein, I.; Zaltzman, B. Equilibrium electroconvective instability. Phys. Rev. Lett. 2015. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  14. Uzdenova, A.M.; Kovalenko, A.V.; Urtenov, M.K.; Nikonenko, V.V. Effect of electroconvection during pulsed electric field electrodialysis. Numerical experiments. Electrochem. Commun. 2015, 51, 1–5. [Google Scholar] [CrossRef]
  15. Urtenov, M.K.; Uzdenova, A.M.; Kovalenko, A.V.; Nikonenko, V.V.; Pismenskaya, N.D.; Vasil’eva, V.I.; Sistat, P.; Pourcelly, G. Basic mathematical model of overlimiting transfer enhanced by electroconvection in flow-through electrodialysis membrane cells. J. Memb. Sci. 2013, 447, 190–202. [Google Scholar] [CrossRef]
  16. Pham, V.S.; Li, Z.; Lim, K.M.; White, J.K.; Han, J. Direct numerical simulation of electroconvective instability and hysteretic current-voltage response of a permselective membrane. Phys. Rev. E 2012, 86, 046310. [Google Scholar] [CrossRef]
  17. Demekhin, E.A.; Nikitin, N.V.; Shelistov, V.S. Direct numerical simulation of electrokinetic instability and transition to chaotic motion. Phys. Fluids 2013. [Google Scholar] [CrossRef] [Green Version]
  18. De Valença, J.C.; Wagterveld, R.M.; Lammertink, R.G.H.; Tsai, P.A. Dynamics of microvortices induced by ion concentration polarization. Phys. Rev. E—Stat. Nonlinear Soft Matter Phys. 2015. [Google Scholar] [CrossRef] [Green Version]
  19. Nikonenko, V.V.; Mareev, S.A.; Pis’menskaya, N.D.; Uzdenova, A.M.; Kovalenko, A.V.; Urtenov, M.K.; Pourcelly, G. Effect of electroconvection and its use in intensifying the mass transfer in electrodialysis (Review). Russ. J. Electrochem. 2017, 53, 1122–1144. [Google Scholar] [CrossRef]
  20. Belashova, E.D.; Melnik, N.A.; Pismenskaya, N.D.; Shevtsova, K.A.; Nebavsky, A.V.; Lebedev, K.A.; Nikonenko, V.V. Overlimiting mass transfer through cation-exchange membranes modified by Nafion film and carbon nanotubes. Electrochim. Acta 2012. [Google Scholar] [CrossRef]
  21. Shelistov, V.S.; Demekhin, E.A.; Ganchenko, G.S. Electrokinetic instability near charge-selective hydrophobic surfaces. Phys. Rev. E 2014, 90, 013001. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  22. Vinogradova, O.I.; Dubov, A.L. Superhydrophobic Textures for Microfluidics. Mendeleev Commun. 2012, 22, 229–236. [Google Scholar] [CrossRef]
  23. Levich, V.G.; Tobias, C.W. Physicochemical Hydrodynamics. J. Electrochem. Soc. 1963, 110, 251C. [Google Scholar] [CrossRef]
  24. Nebavskaya, K.A.; Sarapulova, V.V.; Sabbatovskiy, K.G.; Sobolev, V.D.; Pismenskaya, N.D.; Sistat, P.; Cretin, M.; Nikonenko, V.V. Impact of ion exchange membrane surface charge and hydrophobicity on electroconvection at underlimiting and overlimiting currents. J. Memb. Sci. 2017, 523, 36–44. [Google Scholar] [CrossRef]
  25. Korzhova, E.; Pismenskaya, N.; Lopatin, D.; Baranov, O.; Dammak, L.; Nikonenko, V. Effect of surface hydrophobization on chronopotentiometric behavior of an AMX anion-exchange membrane at overlimiting currents. J. Memb. Sci. 2016, 500, 161–170. [Google Scholar] [CrossRef]
  26. Karatay, E.; Andersen, M.B.; Wessling, M.; Mani, A. Coupling between Buoyancy Forces and Electroconvective Instability near Ion-Selective Surfaces. Phys. Rev. Lett. 2016. [Google Scholar] [CrossRef] [Green Version]
  27. Rubinstein, S.M.; Manukyan, G.; Staicu, A.; Rubinstein, I.; Zaltzman, B.; Lammertink, R.G.H.; Mugele, F.; Wessling, M. Direct observation of a nonequilibrium electro-osmotic instability. Phys. Rev. Lett. 2008, 101. [Google Scholar] [CrossRef] [Green Version]
  28. Gil, V.V.; Andreeva, M.A.; Jansezian, L.; Han, J.; Pismenskaya, N.D.; Nikonenko, V.V.; Larchet, C.; Dammak, L. Impact of heterogeneous cation-exchange membrane surface modification on chronopotentiometric and current–voltage characteristics in NaCl, CaCl 2 and MgCl 2 solutions. Electrochim. Acta 2018, 281, 472–485. [Google Scholar] [CrossRef]
  29. Roghmans, F.; Evdochenko, E.; Stockmeier, F.; Schneider, S.; Smailji, A.; Tiwari, R.; Mikosch, A.; Karatay, E.; Kühne, A.; Walther, A.; et al. 2D Patterned Ion-Exchange Membranes Induce Electroconvection. Adv. Mater. Interfaces 2019, 6, 1801309. [Google Scholar] [CrossRef] [Green Version]
  30. Davidson, S.M.; Wessling, M.; Mani, A. On the Dynamical Regimes of Pattern-Accelerated Electroconvection. Sci. Rep. 2016, 6, 22505. [Google Scholar] [CrossRef]
  31. Benneker, A.M.; Gumuscu, B.; Derckx, E.G.H.; Lammertink, R.G.H.; Eijkel, J.C.T.; Wood, J.A. Enhanced ion transport using geometrically structured charge selective interfaces. Lab Chip 2018, 18, 1652–1660. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  32. Pawlowski, S.; Crespo, J.G.; Velizarov, S. Profiled ion exchange membranes: A comprehensible review. Int. J. Mol. Sci. 2019, 20, 165. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  33. Vasil’eva, V.I.; Akberova, E.M.; Zabolotsky, V.I.; Novak, L.; Kostylev, D.V. Effect of Dispersity of a Sulfonated Cation-Exchanger on the Current—Voltage Characteristics of Heterogeneous Membranes Ralex CM Pes. Pet. Chem. 2018. [Google Scholar] [CrossRef]
  34. Akberova, E.M.; Vasil’eva, V.I.; Zabolotsky, V.I.; Novak, L. Effect of the sulfocation-exchanger dispersity on the surface morphology, microrelief of heterogeneous membranes and development of electroconvection in intense current modes. J. Memb. Sci. 2018. [Google Scholar] [CrossRef]
  35. Pismenskaya, N.D.; Pokhidnia, E.V.; Pourcelly, G.; Nikonenko, V.V. Can the electrochemical performance of heterogeneous ion-exchange membranes be better than that of homogeneous membranes? J. Memb. Sci. 2018, 566, 54–68. [Google Scholar] [CrossRef]
  36. Laberty-Robert, C.; Vallé, K.; Pereira, F.; Sanchez, C. Design and properties of functional hybrid organic–inorganic membranes for fuel cells. Chem. Soc. Rev. 2011, 40, 961. [Google Scholar] [CrossRef]
  37. Jalani, N.H.; Dunn, K.; Datta, R. Synthesis and characterization of Nafion®-MO2 (M = Zr, Si, Ti) nanocomposite membranes for higher temperature PEM fuel cells. Electrochim. Acta 2005, 51, 553–560. [Google Scholar] [CrossRef]
  38. Adjemian, K.T.; Lee, S.J.; Srinivasan, S.; Benziger, J.; Bocarsly, A.B. Silicon Oxide Nafion Composite Membranes for Proton-Exchange Membrane Fuel Cell Operation at 80–140°C. J. Electrochem. Soc. 2002. [Google Scholar] [CrossRef]
  39. Miyake, N.; Wainright, J.S.; Savinell, R.F. Evaluation of a Sol-Gel Derived Nafion/Silica Hybrid Membrane for Proton Electrolyte Membrane Fuel Cell Applications: I. Proton Conductivity and Water Content. J. Electrochem. Soc. 2001. [Google Scholar] [CrossRef]
  40. Safronova, E.Y.; Prikhno, I.A.; Yurkov, G.Y.; Yaroslavtsev, A.B. Nanocomposite membrane materials based on nafion and cesium acid salt of phosphotungstic heteropolyacid. Chem. Eng. Trans. 2015, 43, 679–684. [Google Scholar] [CrossRef]
  41. Nemati, M.; Hosseini, S.M.; Bagheripour, E.; Madaeni, S.S. Electrodialysis heterogeneous anion exchange membranes filled with TiO2 nanoparticles: Membranes’ fabrication and characterization. J. Membr. Sci. Res. 2015, 1, 135–140. [Google Scholar] [CrossRef]
  42. Li, X.; Li, J.; Van Der Bruggen, B.; Sun, X.; Shen, J.; Han, W.; Wang, L. Fouling behavior of polyethersulfone ultrafiltration membranes functionalized with sol-gel formed ZnO nanoparticles. RSC Adv. 2015. [Google Scholar] [CrossRef]
  43. Tiraferri, A.; Kang, Y.; Giannelis, E.P.; Elimelech, M. Highly Hydrophilic Thin-Film Composite Forward Osmosis Membranes Functionalized with Surface-Tailored Nanoparticles. ACS Appl. Mater. Interfaces 2012, 4, 5044–5053. [Google Scholar] [CrossRef] [PubMed]
  44. Wang, X.; Chen, G.Q.; Zhang, W.; Deng, H. Surface-modified anion exchange membranes with self-cleaning ability and enhanced antifouling properties. J. Taiwan Inst. Chem. Eng. 2019. [Google Scholar] [CrossRef]
  45. Volodina, E.; Pismenskaya, N.; Nikonenko, V.; Larchet, C.; Pourcelly, G. Ion transfer across ion-exchange membranes with homogeneous and heterogeneous surfaces. J. Colloid Interface Sci. 2005, 285, 247–258. [Google Scholar] [CrossRef]
  46. Pismenskaya, N.; Melnik, N.; Nevakshenova, E.; Nebavskaya, K.; Nikonenko, V. Enhancing Ion Transfer in Overlimiting Electrodialysis of Dilute Solutions by Modifying the Surface of Heterogeneous Ion-Exchange Membranes. Int. J. Chem. Eng. 2012, 2012, 1–11. [Google Scholar] [CrossRef]
  47. Berezina, N.P.; Kononenko, N.A.; Dyomina, O.A.; Gnusin, N.P. Characterization of ion-exchange membrane materials: Properties vs structure. Adv. Colloid Interface Sci. 2008, 139, 3–28. [Google Scholar] [CrossRef]
  48. Moya, A.A. Electrochemical Impedance of Ion-Exchange Membranes with Interfacial Charge Transfer Resistances. J. Phys. Chem. C 2016. [Google Scholar] [CrossRef]
  49. Moya, A.A.; Moleón, J.A. Study of the electrical properties of bi-layer ion-exchange membrane systems. J. Electroanal. Chem. 2010. [Google Scholar] [CrossRef]
  50. Barsoukov, E.; Macdonald, J.R. Chapter 4 Applications of Impedance Spectroscopy. In Impedance Spectroscopy: Theory, Experiment, and Applications; Barsoukov, E., Macdonald, J.R., Eds.; John Wiley & Sons, Inc.: Hoboken, NJ, USA, 2005; ISBN 9780471716242. [Google Scholar]
  51. Nikonenko, V.V.; Kozmai, A.E. Electrical equivalent circuit of an ion-exchange membrane system. Electrochim. Acta 2011. [Google Scholar] [CrossRef]
  52. Vorotyntsev, M.A.; Badiali, J.P.; Inzelt, G. Electrochemical impedance spectroscopy of thin films with two mobile charge carriers: Effects of the interfacial charging. J. Electroanal. Chem. 1999. [Google Scholar] [CrossRef]
  53. Vorotyntsev, M.A. Impedance of thin films with two mobile charge carriers. Interfacial exchange of both species with adjacent media. Effect of the double layer charges. Electrochim. Acta 2002, 47, 2071–2079. [Google Scholar] [CrossRef]
  54. Kniaginicheva, E.; Pismenskaya, N.; Melnikov, S.; Belashova, E.; Sistat, P.; Cretin, M.; Nikonenko, V. Water splitting at an anion-exchange membrane as studied by impedance spectroscopy. J. Memb. Sci. 2015, 496, 78–83. [Google Scholar] [CrossRef]
  55. Kozmai, A.E.; Nikonenko, V.V.; Pismenskaya, N.D.; Mareev, S.A.; Belova, E.I.; Sistat, P. Use of electrochemical impedance spectroscopy for determining the diffusion layer thickness at the surface of ion-exchange membranes. Pet. Chem. 2012, 52, 614–624. [Google Scholar] [CrossRef]
  56. Lteif, R.; Dammak, L.; Larchet, C.; Auclair, B. Membrane electric conductivity: A study of the effect of the concentration and nature of the electrolyte and of the structure of the membrane. Eur. Polym. J. 1999, 35, 1187–1195. [Google Scholar] [CrossRef]
  57. Karpenko, L.V.; Demina, O.A.; Dvorkina, G.A.; Parshikov, S.B.; Larchet, C.; Auclair, B.; Berezina, N.P. Comparative study of methods used for the determination of electroconductivity of ion-exchange membranes. Russ. J. Electrochem. 2001, 37, 328–335. [Google Scholar] [CrossRef]
  58. Pismenskaya, N.D.; Nevakshenova, E.E.; Nikonenko, V.V. Using a Single Set of Structural and Kinetic Parameters of the Microheterogeneous Model to Describe the Sorption and Kinetic Properties of Ion-Exchange Membranes. Pet. Chem. 2018, 58, 465–473. [Google Scholar] [CrossRef]
  59. Wenzel, R.N. Resistance of solid surfaces to wetting by water. Ind. Eng. Chem. 1936, 28, 988–994. [Google Scholar] [CrossRef]
  60. Rahimpour, A.; Jahanshahi, M.; Rajaeian, B.; Rahimnejad, M. TiO2 entrapped nano-composite PVDF/SPES membranes: Preparation, characterization, antifouling and antibacterial properties. Desalination 2011. [Google Scholar] [CrossRef]
  61. Erbil, H.Y. The debate on the dependence of apparent contact angles on drop contact area or three-phase contact line: A review. Surf. Sci. Rep. 2014, 69, 325–365. [Google Scholar] [CrossRef]
  62. Grafov, B.M.; Ukshe, E.A. Electrochemical AC Circuits; Nauka: Moscow, Russia, 1973. [Google Scholar]
  63. Goswami, S.; Klaus, S.; Benziger, J. Wetting and absorption of water drops on nafion films. Langmuir 2008. [Google Scholar] [CrossRef] [PubMed]
  64. Bass, M.; Berman, A.; Singh, A.; Konovalov, O.; Freger, V. Surface structure of nafion in vapor and liquid. J. Phys. Chem. B 2010. [Google Scholar] [CrossRef]
  65. Larchet, C.; Dammak, L.; Auclair, B.; Parchikov, S.; Nikonenko, V. A simplified procedure for ion-exchange membrane characterisation. New J. Chem. 2004. [Google Scholar] [CrossRef]
  66. Newman, J.S. Electrochemical Systems, Prentice-Hall International Series in the Physical and Chemical Engineering Sciences; Prentice-Hall: Englewood Clis, NJ, USA, 1972; ISBN 978-0-13-248922-5. [Google Scholar]
  67. Choi, J.H.; Lee, H.J.; Moon, S.H. Effects of electrolytes on the transport phenomena in a cation-exchange membrane. J. Colloid Interface Sci. 2001. [Google Scholar] [CrossRef] [PubMed]
  68. Rubinstein, I.; Zaltzman, B.; Pundik, T. Ion-exchange funneling in thin-film coating modification of heterogeneous electrodialysis membranes. Phys. Rev. E 2002, 65, 041507. [Google Scholar] [CrossRef] [PubMed]
  69. Rösler, H.-W.; Maletzki, F.; Staude, E. Ion transfer across electrodialysis membranes in the overlimiting current range: Chronopotentiometric studies. J. Memb. Sci. 1992, 72, 171–179. [Google Scholar] [CrossRef]
  70. Sand, H.J.S., III. On the concentration at the electrodes in a solution, with special reference to the liberation of hydrogen by electrolysis of a mixture of copper sulphate and sulphuric acid. Lond. Edinb. Dublin Philos. Mag. J. Sci. 1901, 1, 45–79. [Google Scholar] [CrossRef] [Green Version]
  71. Mareev, S.A.; Nichka, V.S.; Butylskii, D.Y.; Urtenov, M.K.; Pismenskaya, N.D.; Apel, P.Y.; Nikonenko, V.V. Chronopotentiometric Response of an Electrically Heterogeneous Permselective Surface: 3D Modeling of Transition Time and Experiment. J. Phys. Chem. C 2016, 120, 13113–13119. [Google Scholar] [CrossRef]
  72. Sistat, P.; Pourcelly, G. Chronopotentiometric response of an ion-exchange membrane in the underlimiting current-range. Transport phenomena within the diffusion layers. J. Memb. Sci. 1997, 123, 121–131. [Google Scholar] [CrossRef]
  73. Rybalkina, O.A.; Tsygurina, K.A.; Melnikova, E.D.; Pourcelly, G.; Nikonenko, V.V.; Pismenskaya, N.D. Catalytic effect of ammonia-containing species on water splitting during electrodialysis with ion-exchange membranes. Electrochim. Acta 2019. [Google Scholar] [CrossRef]
  74. Sistat, P.; Kozmai, A.; Pismenskaya, N.; Larchet, C.; Pourcelly, G.; Nikonenko, V. Low-frequency impedance of an ion-exchange membrane system. Electrochim. Acta 2008, 53, 6380–6390. [Google Scholar] [CrossRef]
  75. Barbero, G. Warburg’s impedance revisited. Phys. Chem. Chem. Phys. 2016. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  76. Simons, R. Strong electric field effects on proton transfer between membrane-bound amines and water. Nature 1979, 280, 824–826. [Google Scholar] [CrossRef]
  77. Zabolotskii, V.I.; Shel’deshov, N.V.; Gnusin, N.P. Dissociation of Water Molecules in Systems with Ion-exchange Membranes. Russ. Chem. Rev. 1988, 57, 801–808. [Google Scholar] [CrossRef]
Membranes 10 00125 g001 550
Figure 1. Principal scheme of the experimental setup: electrodialysis cell (1) consisting of one desalination compartment (DC), one concentration compartment (CC) and two electrode compartments; tanks with solutions (2, 3); Luggin’s capillaries (4), connected with silver chloride electrodes (5); electrochemical complex Autolab PGSTAT-100 (6); flow pass cell with pH combination electrode (7), connected to pH-meter Expert 001 (8).
Figure 1. Principal scheme of the experimental setup: electrodialysis cell (1) consisting of one desalination compartment (DC), one concentration compartment (CC) and two electrode compartments; tanks with solutions (2, 3); Luggin’s capillaries (4), connected with silver chloride electrodes (5); electrochemical complex Autolab PGSTAT-100 (6); flow pass cell with pH combination electrode (7), connected to pH-meter Expert 001 (8).
Membranes 10 00125 g001
Membranes 10 00125 g002 550
Figure 2. Optical images of the studied membranes: MK-40 (a), MK-4021 (b), MK-4021+3% (c), MK-4021+6% (d), MK-4033+3% (e), MK-4033+6% (f). Parameter b characterizes the roughness of the surface and shows the difference between the highest and lowest areas of the membrane relief.
Figure 2. Optical images of the studied membranes: MK-40 (a), MK-4021 (b), MK-4021+3% (c), MK-4021+6% (d), MK-4033+3% (e), MK-4033+6% (f). Parameter b characterizes the roughness of the surface and shows the difference between the highest and lowest areas of the membrane relief.
Membranes 10 00125 g002
Membranes 10 00125 g003 550
Figure 3. Concentration dependences of the conterion (Na+) transport number in the studied membranes.
Figure 3. Concentration dependences of the conterion (Na+) transport number in the studied membranes.
Membranes 10 00125 g003
Membranes 10 00125 g004 550
Figure 4. Current-voltage characteristics (solid lines) and the difference in pH between the outlet and inlet solution passing through the desalination compartment of the electrodialysis cell (dashed lines) of the pristine and modified membranes.
Figure 4. Current-voltage characteristics (solid lines) and the difference in pH between the outlet and inlet solution passing through the desalination compartment of the electrodialysis cell (dashed lines) of the pristine and modified membranes.
Membranes 10 00125 g004
Membranes 10 00125 g005 550
Figure 5. Schematic representation of streamlines near the surface of the MK-40 (a) membrane and that, modified by PFSA polymer film of various thicknesses: about 20 μm (b) and about 30 μm (c).
Figure 5. Schematic representation of streamlines near the surface of the MK-40 (a) membrane and that, modified by PFSA polymer film of various thicknesses: about 20 μm (b) and about 30 μm (c).
Membranes 10 00125 g005
Membranes 10 00125 g006 550
Figure 6. Chronopotentiometric curves of the studied membranes measured at i / i lim th = 2. The circles show the inflection points related to τexp.
Figure 6. Chronopotentiometric curves of the studied membranes measured at i / i lim th = 2. The circles show the inflection points related to τexp.
Membranes 10 00125 g006
Membranes 10 00125 g007 550
Figure 7. Electrochemical impedance spectra of the MK-40 as well as MK-4021, MK-4021+3%, MK-4021+6% (a) and MK-4033+3%, MK-4033+6% (b) samples at i / i lim th = 1.5.
Figure 7. Electrochemical impedance spectra of the MK-40 as well as MK-4021, MK-4021+3%, MK-4021+6% (a) and MK-4033+3%, MK-4033+6% (b) samples at i / i lim th = 1.5.
Membranes 10 00125 g007
Membranes 10 00125 g008 550
Figure 8. Electrochemical impedance spectra of the MK-40 as well as MK-4021, MK-4021+3%, MK-4021+6% (a) and MK-4033+3%, MK-4033+6% (b) samples at i / i lim th = 1.8.
Figure 8. Electrochemical impedance spectra of the MK-40 as well as MK-4021, MK-4021+3%, MK-4021+6% (a) and MK-4033+3%, MK-4033+6% (b) samples at i / i lim th = 1.8.
Membranes 10 00125 g008
Table
Table 1. Studied membranes and some characteristics.
Table 1. Studied membranes and some characteristics.
SampleModifying Film Thickness1, μmMass Fraction TiO2 in the Film, wt%Contact Angles, θ, Degrees (Swollen Membrane)
MK-40––55 ± 2
MK-402121 ± 2–64 ± 3
MK-4021+3%21 ± 2361 ± 3
MK-4021+6%21 ± 2657 ± 2
MK-4033+3%33 ± 2360 ± 3
MK-4033+6%33 ± 2656 ± 2
1 in swollen state
All membrane samples underwent standard salt pretreatment [47] before the measurements.
Table
Table 2. Characteristic points of the high-frequency region of the studied membranes impedance spectra and the effective capacities of the electric double layer and the ohmic resistances of the membranes found from these points.
Table 2. Characteristic points of the high-frequency region of the studied membranes impedance spectra and the effective capacities of the electric double layer and the ohmic resistances of the membranes found from these points.
Samplefmax, Hz−ImZmax, OhmRΩ, OhmC, μF
MK-4013,31822.255 ± 20.5 ± 0.2
MK-402110,80921.754 ± 20.7 ± 0.2
MK-4021+3%850619.050 ± 21.0 ± 0.2
MK-4021+6%850620.449 ± 20.9 ± 0.2
MK-4033+3%10,80920.251 ± 20.7 ± 0.2
MK-4033+6%10,80921.852 ± 20.7 ± 0.2
Table
Table 3. Some parameters of current-voltage curves, current-voltage characteristics (CVCs).
Table 3. Some parameters of current-voltage curves, current-voltage characteristics (CVCs).
Sample i lim exp ,   mA   cm – 2 i lim exp / i lim th Plateau
Length, V		Plateau Slope, mS cm–2
MK-401.570.781.430.61
MK-40211.810.900.601.58
MK-4021+3%2.191.090.851.08
MK-4021+6%1.970.980.501.33
MK-4033+3%2.011.001.030.78
MK-4033+6%1.710.851.250.62
Table
Table 4. Values of the experimental transition time, τexp, at various i / i lim th for the studied membranes.
Table 4. Values of the experimental transition time, τexp, at various i / i lim th for the studied membranes.
i / i lim th MK-40MK-4021MK-4021+3%MK-4021+6%MK-4033+3%MK-4033+6%
1.2515.2 ± 0.218.6 ± 0.218.4 ± 0.217.5 ± 0.217.7 ± 0.217.6 ± 0.2
1.59.2 ± 0.210.5 ± 0.212.1 ± 0.29.9 ± 0.211.8 ± 0.211.7 ± 0.2
2.05.2 ± 0.25.7 ± 0.26.2 ± 0.25.9 ± 0.26.1 ± 0.26.1 ± 0.2
2.52.9 ± 0.23.6 ± 0.23.8 ± 0.23.7 ± 0.23.8 ± 0.23.8 ± 0.2

Share and Cite

MDPI and ACS Style

Gil, V.; Porozhnyy, M.; Rybalkina, O.; Butylskii, D.; Pismenskaya, N. The Development of Electroconvection at the Surface of a Heterogeneous Cation-Exchange Membrane Modified with Perfluorosulfonic Acid Polymer Film Containing Titanium Oxide. Membranes 2020, 10, 125. https://doi.org/10.3390/membranes10060125

AMA Style

Gil V, Porozhnyy M, Rybalkina O, Butylskii D, Pismenskaya N. The Development of Electroconvection at the Surface of a Heterogeneous Cation-Exchange Membrane Modified with Perfluorosulfonic Acid Polymer Film Containing Titanium Oxide. Membranes. 2020; 10(6):125. https://doi.org/10.3390/membranes10060125

Chicago/Turabian Style

Gil, Violetta, Mikhail Porozhnyy, Olesya Rybalkina, Dmitrii Butylskii, and Natalia Pismenskaya. 2020. "The Development of Electroconvection at the Surface of a Heterogeneous Cation-Exchange Membrane Modified with Perfluorosulfonic Acid Polymer Film Containing Titanium Oxide" Membranes 10, no. 6: 125. https://doi.org/10.3390/membranes10060125

Note that from the first issue of 2016, this journal uses article numbers instead of page numbers. See further details here.

Article Metrics

Back to TopTop