Next Article in Journal
Measurement of Multi Ion Transport through Human Bronchial Epithelial Cell Line Provides an Insight into the Mechanism of Defective Water Transport in Cystic Fibrosis
Next Article in Special Issue
Synthesis of Silica Membranes by Chemical Vapor Deposition Using a Dimethyldimethoxysilane Precursor
Previous Article in Journal
Electrospun Weak Anion-Exchange Fibrous Membranes for Protein Purification
Previous Article in Special Issue
Comparison of Supported Ionic Liquid Membranes and Polymeric Ultrafiltration and Nanofiltration Membranes for Separation of Lignin and Monosaccharides
 
 
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 3
10.3390/membranes10030040
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

Effect of Surface Inhomogeneity of Ion-Exchange Membranes on the Mass Transfer Efficiency in Pulsed Electric Field Modes

by
Dmitrii Butylskii
*,
Ilya Moroz
,
Kseniya Tsygurina
and
Semyon Mareev
Membrane Institute, Kuban State University, 149 Stavropolskaya st., 350040 Krasnodar, Russia
*
Author to whom correspondence should be addressed.
Membranes 2020, 10(3), 40; https://0-doi-org.brum.beds.ac.uk/10.3390/membranes10030040
Submission received: 19 February 2020 / Revised: 5 March 2020 / Accepted: 9 March 2020 / Published: 11 March 2020
(This article belongs to the Special Issue Membranes: 10th Anniversary)
Browse Figures
Versions Notes

Abstract

:
Despite the growing interest in pulsed electric field modes in membrane separation processes, there are currently not many works devoted to studying the effect of the surface properties and composition of ion-exchange membranes on their efficiency in these modes. In this paper, we have shown the effect of increasing mass transfer using different kinds of ion-exchange membranes (heterogeneous and homogeneous with smooth, undulated, and rough surfaces) during electrodialysis in the pulsed electric field modes at underlimiting and overlimiting currents. It was found that the maximum increment in the average current is achieved when the average potential corresponds to the right-hand edge of the limiting current plateau of the voltammetric curve, i.e., at the maximum resistance of the system in the DC mode. For the first time, the development of electroconvective vortices was visualized in pulsed electric field modes and it was experimentally shown that even at relatively low frequencies, a non-uniform concentration field is preserved at the time of a pause, which stimulates the rapid development of electroconvection when pulses are switched on again. In the case of relatively high pulse frequencies, the electroconvective vortices formed during a pulse lapse do not completely decay during a pause; they only slightly decrease in size.

Graphical Abstract

1. Introduction

In recent years, in the field of electrodialysis, considerable interest has been focused on the study of intense current regimes. The use of such regimes allows one to save on the most expensive component of the system—the ion-exchange membrane [1,2]. The operation of the electrodialysis apparatus in these modes is accompanied by the development of coupled effects of concentration polarization, such as electro- and gravitational convection, and the water splitting at the membrane/solution interface [3,4,5,6,7].
One of the main mechanisms of overlimiting mass transfer is electroconvection, which not only increases the effective transport of salt ions [8] but also partially suppresses the water splitting at the interface [9], which impedes the process of precipitation in the electrodialyzer chambers [10].
It is known that the greatest influence on the development of electroconvection is exerted by the electric and/or geometric heterogeneities of the membrane surface [11,12,13,14,15], hydrophobicity of the surface and its charge [16,17], and heterogeneity of the concentration distribution at the membrane/solution interface [3]. All these effects are synergistic and contribute to the appearance of the tangential component of the electric force, which sets the volume of the solution at the membrane surface in motion [2,18].
As it was shown in the theoretical works of Davidson at al. [13] and Rubinstein and Zaltzman [4], to intensify electroconvective mixing, the length of the elementary region on the surface of a heterogeneous membrane (the sum of the lengths of the conductive and non-conductive regions) should correspond to the channel width of the electrodialyzer. In the case of a flow electromembrane system, the size of electroconvective vortices will be limited by the thickness of the diffusion layer [19].
The presence of a geometric heterogeneity in the form of waviness or other types of relief on the membrane surface, as well as electrical heterogeneity, leads to a significant increase in the mass transfer rate [12,20,21,22] due to several effects: Increase in the active area of the membrane available for mass transfer; increase in the contribution of forced convection due to improved hydrodynamic conditions, and increase in the tangential component of electric force [20,23].
Another effective way to intensify electroconvection is to use pulsed electric field (PEF) modes [24,25,26,27]. The essence of the electrodialysis desalination of solutions using PEF modes is to alternate cycles of switching on and off the external electric field. It allows the reduction in concentration polarization and, as a result, increase in mass transfer rate [24,27,28], reduction in the rate of water dissociation at the membrane/depleted solution boundary [29], as well as the rate of precipitate formation in the electrodialyzer chambers during the processing of multicomponent solutions [30,31,32]. Nevertheless, energy consumption in the PEF mode should be greater [28].
At the underlimiting current regimes of the PEF, the above-mentioned effects are achieved due to partial relaxation of the concentration profile near the membrane surface, and the solution resistance is significantly reduced. Therefore, a high current value is reached at the beginning of the next cycle [28]. On average, the increment in mass transfer rate per cycle is due to the high contribution of electromigration transport when the voltage is switched on again. A similar effect is observed with metal deposition on the electrode [33]. The upper limit of the mass transfer rate is reached when the thickness of the solution layer, in which changes in the concentration occur during the application of pulses, becomes sufficiently small [28]. Thus, the mass transfer rate in the PEF mode increases with increasing frequency and decreasing duty cycle. According to [28], in electrodialysis, this dependence was first established by Karlin and Kropotov [34,35].
When using the PEF modes at overlimiting currents during a pause (where the current is zero), the concentration field does not disappear [25,36]. Its non-uniformity plays the same role as the membrane surface electrical heterogeneity by favoring the formation of new electroconvective vortices [3]. The results of the calculation [25] showed that the reason for the prolonged lifetime of the vortices after switching off the current/voltage is the non-uniform distribution of the electric body force at the membrane surface.
Currently, the PEF modes are actively used in electrodialysis for processing complex solutions of the food industry [31,37,38,39]. However, the effect of the surface properties of ion-exchange membranes on the process efficiency has not been studied enough. It was shown in [10] that the hydrophobicity and heterogeneity of the ion-exchange membrane surface lead to the development of electroconvection. This results in an increase in the rate of demineralization at PEF modes. On the other hand, heterogeneity of the ion-exchange membrane leads to the blocking of pores by the precipitates, turning into non-conductive regions, thus leading to the fast increase in resistance observed from the beginning of the current pulses [40].
Electrochemical methods (such as voltammetry, chronopotentiometry, and electrochemical impedance spectroscopy) are usually used to study the coupled effects of concentration polarization and, in particular, electroconvection [5,8,11,12]. These methods allow important quantitative characteristics that determine the economic indicators of the process to be obtained [2]. However, for the elucidation of occurring phenomena mechanisms, the received information is indirect.
The development of experimental methods for visualizing electroconvection and other related effects of concentration polarization is a necessary step to deepen the knowledge in this field of science and, in particular, for verifying assumptions and developing mathematical models. In 2008, a joint team of scientists from Ben-Gurion University of the Negev (Israel) and University of Twente (The Netherlands) proposed an effective way to directly visualize electroconvective vortices [41] by adding 1 μm neutrally buoyant polystyrene tracer particles to the electrolyte solution. It should be noted that the phenomenon of electroconvection began to be considered as generally recognized in the literature only after the publication of the visualization results. Later, similar visualization methods were developed in other leading research centers [41,42,43,44,45].
It is worth noting that other methods for the visualization of electroconvection were previously known. The scientific group of Shaposhnik and Vasil’eva used the laser interferometry method to visualize concentration profiles at the surface of ion-exchange membranes. These concentration profiles change their form due to the development of electroconvection [46,47]. The Schlieren-diagonal method also allows one to monitor changes in concentration at the membrane surface [48].
The methods for visualization make it possible to determine, for example, the moment of vortices occurrence at the membrane surface in the electro-membrane system with an increase in the set current [45]; the effect of the alternating current frequency on the size of the vortices [49]; the influence of the shape of the surface geometric heterogeneity of the ion-conductive material on the size of the vortices [50].
In this work, we evaluated the effect of the surface properties of ion-exchange membranes on the efficiency of mass transfer using PEF modes. Additionally, the kinetics of electroconvective vortices formation near the surface of an ion-exchange membrane in these electric field modes is visualized for the first time.

2. Materials and Methods

2.1. Membranes

Homogeneous (Nafion 438 and Neosepta AMX) and heterogeneous (M1, M2, MK-40) membranes, which differ in surface structure and chemical composition, were chosen as the objects of study.
Nafion 438 (DuPont, Wilmington, DE, USA) is a homogeneous perfluorosulfonic cation-exchange membrane. A distinctive feature of this membrane is a flat profile on one side and a rough and undulated surface on the other side (Figure 1a). In addition, the membrane is reinforced with a polytetrafluoroethylene net (Figure 1b).
The homogeneous Neosepta AMX anion-exchange membrane (Astom Corp., Tokyo, Japan) consists of a copolymer of styrene-divinylbenzene (45–65%) with fixed quaternary amino groups and polyvinyl chloride (45–55%). The membrane is reinforced with a polyvinyl chloride mesh, which causes the undulation of its surface. It is visualized in the form of longitudinal strips in the vicinity of the surface (Figure 2a). The wave height varies from 10 μm in the dry state (Figure 2b) to 30 μm in the swollen state (Figure 2c) [51].
The surface images of the membranes presented in Figure 1a and Figure 2a were obtained using a MERLIN scanning electron microscope (SEM) (Carl Zeiss, Jena, Germany). The images of dry (Figure 2b) and swollen membranes (Figure 1b and Figure 2c) were obtained using an optical microscope SOPTOP CX40M (Ningbo Sunny Instruments Co., Ltd., Yuyao, China).
The substrates (track-etched membranes) used in the fabrication of M1 (Figure 3a) and M2 (Figure 3b) membranes were produced from a 30 µm thick polyethylene terephthalate (PET) film (Hostaphan RNK, Mitsubishi Polyester Films) at JINR, Dubna. To make the substrates permselective, they were covered from one side with a dispersion of Nafion® sulfonated perfluorinated material in alcohol; the Nafion® material filled the pores (Figure 3c) and formed a ~3 µm thick layer on one side of the membrane. The second side of the membrane was heterogeneous: Only the pores filled with Nafion were conductive. Membranes differed in distribution density of the conductive regions on the heterogeneous surface and their diameter: For M1 and M2, the density of the conductive regions was 1.47 × 104 and 8.78 × 104 per square centimeter, respectively, and their average diameter was 25.9 and 21.5 μm, respectively; thus, the mean surface fraction of conductive regions on the heterogeneous side of the resulting ion-exchange membrane (IEM) was 7.7% for M1 and 31.8% for M2.
The densities of pore distribution and pore diameter were determined from the micrographs (Figure 3a,b) obtained using a Hitachi TM3000 scanning electron microscope (Hitachi High-Technologies Corp., Tokyo, Japan).
MK-40 (Shchekinoazot, Pervomayskiy, Tula Region, Russia) is produced by hot pressing the ion-exchange material (KU-2-8 cation-exchange resin), dispersed to linear dimensions of 5–50 μm, with high-density polyethylene as the inert binder. Most of the surface (about 85%) of the MK-40 membrane is covered with polyethylene film. The areas where grains of ion-exchanger come out of the surface are evenly distributed over the membrane surface (Figure 3d). The surface image of the MK-40 membrane (Figure 3d) was obtained using a MERLIN scanning electron microscope.

2.2. Experimental Setups and Solutions

Tests of the studied membranes in the PEF and DC modes, as well as measurement of the current–voltage curves (CVC), were carried out using the laboratory flow-through electrodialysis cell described in [52]. The experimental setup was described in detail in our previous work [27]. All measurements were conducted in 0.02 M NaCl solution. The linear flow velocity of the electrolyte solution was 3.6 mm/s.
To visualize the electroconvective vortices, a laboratory flow-through electrodialysis cell was used. Two Neosepta AMX anion-exchange membranes formed the studied channel of which the width of the chamber was 3.0 mm and the length was 5.0 mm. A mixture of 0.02 M NaCl and 10 μM Rhodamine 6G was used as a working solution for visualizing electroconvective flows and salt concentration. Visualization was carried out under conditions of laminar flow of an electrolyte solution with a linear velocity of 0.6 mm/s. Video recording of the formation of electroconvective vortices was carried out using an optical microscope SOPTOP CX40M (Ningbo Sunny Instruments Co., Ltd., Yuyao, China) equipped with a Toupcam camera (ToupTek Photonics Co., Ltd., Hangzhou, China).

2.3. PEF Protocol

The pulsed electric field experiment conditions were chosen as follows: 15 different frequencies (f) in a range from 0.01 to 20 Hz were used. A pulse lapse of constant voltage (Ton) was alternated with the pause lapse of zero current (Toff) (Figure 4).
We used five duty cycles (α) (1/4, 1/3, 1/2, 2/3, 3/4), where α is the ratio of Ton to (Ton + Toff) (Figure 4). The voltages (Uav) needed for the membrane systems to reach several selected current densities are found from current–voltage curves. We compared the systems at i/iimLev ratios 0.75, 1.0, 1.25, and 1.4, where ilimLev is the theoretical value of the limiting current calculated by the Leveque equation.
For example, we determined from a preliminarily obtained voltammetry curve of a hypothetical ion-exchange membrane that at a ratio i/iimLev = 1.0, the potential value is 0.5 V. This potential value in the PEF mode was used as Uav, and in the DC mode, it was set as constant in time (UDC). The potential value at the pulse lapse of a constant voltage (Uon) in the PEF mode is determined by the expression Uon = Uav/α, and, for example, at α = 1/2, it will be equal to 1.0 V. At the time of a pause in the PEF mode, the current value is reset independently of the frequency and duty cycles; therefore, the potential at this time slowly decreases to zero or, if the pulse rate is high enough, reaches some minimum value (Figure 4). The average value for the period (T) of the measured current (iav) is determined from its time dependence presented in Figure 4 by the following expression:
i av ( A ) = 1 T ∫ 0 T i d t ,   where   T   =   T on   +   T off .
When visualizing electroconvective vortices, a pulse lapse of a constant current (Ton) is alternated with the pause lapse of zero current (Toff). We used two frequencies (0.5 and 5.0 Hz) and one duty cycle value equal to 1/2. The average current for the period was set equal to 3.0 ilimLev, where ilimLev was 0.55 mA.

3. Results and Discussion

3.1. The Study of Mass Transfer Rate

Current–voltage curves were obtained to determine the effect of the surface structure and chemical composition of the studied ion-exchange membranes on their electrochemical characteristics (Figure 5). The limiting current for homogeneous membranes Nafion 438 and Neosepta AMX, determined experimentally, exceeds the theoretical value calculated by the Leveque equation (ilimLev equals to 7.9 mA and 12.0 mA for cation- and anion-exchange membranes, respectively) and is shown in Figure 5 by a horizontal dashed line with the corresponding mark. The reason for this effect is the presence of a geometric heterogeneity in the form of a rough and undulated surface facing the desalination chamber of the electrodialysis cell, in the case of the Nafion 438 membrane (Figure 1a), and a wavy surface, in the case of the Neosepta AMX membrane (Figure 2c).
In the case of heterogeneous membranes, the limiting current and the plateau length are mainly a function of the ratio of conductive/non-conductive regions [15]. It is known from the literature that the fraction of the conductive surface of a commercial MK-40 membrane can reach up to 30% and substantially depends on the state of the membrane (dry/swollen) [53]. Particles of the ion-exchange material emerging on the surface are randomly distributed and have different shapes, and their size varies in the range from 4 to 50 μm [52,53,54]. A small fraction of the conductive surface causes a low value of limiting current for a given membrane (Figure 5).
Membranes M1 and M2 are identical but differ in the fraction of conductive regions that are easily visualized (Figure 3a,b). Earlier, we tested these samples and showed the influence of the fraction of the conductive region on various electrochemical characteristics of the membranes [55,56,57]. It was found that a low fraction of conductive regions on the surface of the M1 membrane leads to a low value of the limiting current (Figure 5). Apparently, the fraction of conductive regions in the case of the M2 membrane is large enough for the development of electroconvection, which is the reason for the high limiting current and the short plateau.
In Figure 5, dashed lines indicate the currents at which the studied membrane samples were compared in the PEF mode. It was found that if the average switching potential in the PEF mode corresponds to underlimiting currents, it is possible to obtain only a small increase in the average current over a period (Figure 6a,b), which, under the condition of a low water splitting rate [29], characterizes the increase in mass transfer rate in the PEF mode as compared to the DC mode where the same potential drop is set.
The results obtained are in good agreement with the data presented in [27,28]. With an increase in the pulse rate and a decrease in the duty cycle, the mass transfer rate increases. For all studied membrane samples with an average potential drop corresponding to 0.75 ilimLev, the highest average current value for the period was reached at a duty cycle of 1/4 (Figure 6a). The long pause was necessary for the concentration of counterions at the membrane surface to take the value as close as possible to the concentration in the bulk solution. It explains the efficiency of the regime in which the current is set to zero in most of the period (Toff = 3/4T at α = 1/4). At the beginning of the next cycle, when setting a large potential drop (Uon = 4Uav at α = 1/4), after a pause, the maximum value of the average current over the period among all duty cycles was reached. This is because the resistance became lower during the pause at α = 1/4 than with any other value of the duty cycle from those studied in this work.
It is worth noting that the largest increase in the average current value was obtained for Nafion 438 and M2 membranes, which have good current–voltage curves. This was apparently due to more favorable conditions (surface roughness and undulation, and a high fraction of conductive regions, respectively, as well as high hydrophobicity of the surface in both cases) for the development of electroconvective vortices at the pulse lapse of a constant voltage (Uon) equal to Uav /α = 0.35 × 4 V = 1.4 V in the case of Nafion 438 and M2 membranes compared to other samples, although Uav at 0.75 ilimLev for the other membranes was slightly larger (M1 and MK-40) or had the same value (Neosepta AMX) (Figure 5).
Table 1 shows the values of the maximum average increment in measured current over the period, ω (%), in the PEF mode at the most effective duty cycle, α, (indicated in parentheses in Table 1) compared to the DC mode for the selected i/iimLev ratios. The obtained values of the increment correspond to the maximum points in the frequency dependences of the average current value presented in Figure 6a,b and Figure 7a,b. The formula determines the increment values, ω (%), (Table 1):
ω ( % ) = ( i av / i − 1 ) × 100 %
where iav is the average value of the measured current in the PEF mode over the period, determined by Equation (1), A; i is the current value achieved in the DC mode when the potential drop UDC corresponding to Uav in the PEF mode is set on the membrane under study, A.
With an average potential drop corresponding to 1.0 ilimLev, the highest average current value for the period when using the PEF modes was also achieved with a duty cycle of 1/4 (Figure 6b, Table 1). The only exception is the Neosepta AMX membrane, for which at i = 1.0 ilimLev, the most effective duty cycle was 2/3, but no significant increase in mass transfer rate was observed (only 2.0%) (Table 1).
However, it was found that in the case of using the M1 membrane in the PEF mode with a potential drop corresponding to 1.0 ilimLev, the increase in mass transfer rate compared to the DC mode can be significant (Figure 6b) and equal to about 20% (Table 1).
A further increase in the set potential drop leads to significant energy consumptions both in the DC and in the PEF mode. For example, for the MK-40 membrane, with an increase in the potential drop from a value corresponding to 1.0 ilimLev to a value corresponding to 1.25 ilimLev, it leads to an increase in energy consumption by almost six times (from 1.8 to 10.3 mW cm−2 per half-cell pair) in the case of the DC mode and by two times (from 7.3 to 15.4 mW cm−2 per half-cell pair) in the case of the PEF mode.
However, it was shown that with a potential drop corresponding to 1.25 ilimLev, in the case of the MK-40 membrane, there is a significant increase in the mass transfer rate by almost 30% (Table 1) compared to the DC mode (Figure 7a). It should be noted that the frequencies at which the maximum mass transfer rate for a given membrane is observed become quite small (<0.1 Hz), and the optimal duty cycle for almost all membranes becomes 1/2.
The optimal value of the duty cycle equal to 1/2 at overlimiting currents was also determined in [31,37], including the case of using homogeneous Neosepta membranes in electrodialyzers [58,59]. Probably, the surface inhomogeneity of the MK-40 membrane leads to the shift in the optimal frequency to a relatively low-frequency range. As was shown in [25,36], a higher average current value is achieved due to the development of electroconvection. In the case of heterogeneous membranes, the size of electroconvective vortices depends on the length of the elementary unit of heterogeneity and may be larger than that near the surface of homogeneous membranes under similar conditions [13]. During a pause in the case of a homogeneous membrane, the transport of electrolyte ions is mainly due to diffusion from the bulk solution in the normal direction to the membrane surface. These ions are transported not only in the normal but also in the tangential direction along non-conductive sections in the case of a heterogeneous membrane [19]. As a result, more time is needed for efficient mass transfer in the case of a heterogeneous membrane, which leads to a shift in the optimal frequency to a relatively low-frequency range.
The same effect was also manifested on other heterogeneous membranes under study at a potential drop corresponding to 1.4 ilimLev. For membranes M1 and M2, the optimal frequency value also shifted to the low-frequency range and was approximately equal to 0.5 Hz (Figure 7b).
For homogeneous Nafion 438 and Neosepta AMX membranes, a noticeable increase in the average current value was also observed at a potential drop corresponding to 1.4 ilimLev. However, the course of the frequency dependencies for Nafion 438 and Neosepta AMX with the most optimal duty cycle equal to 1/2 and 3/4, respectively, remained the same as in the underlimiting current regimes. As in our previous work [27], we assumed that in this case, a certain resonance phenomenon occurs. The essence of this phenomenon is in the fact that the concentration field formed during a short pause effectively stimulates the increase in electroconvection after the application of a second voltage pulse.
It was found that the maximum increment in the average current is achieved when the average potentials correspond to the right-hand edge of the limiting current plateau in the voltammetric curves. For example, for the M1 membrane, the maximum increase was observed at a potential drop corresponding to 1.0 ilimLev. However, its current–voltage curve (Figure 5) shows that the experimental value of the limiting current for this membrane is low. In the region of the potential drop, corresponding to 1.0 ilimLev, an inflection was observed, i.e., the transition of the electromembrane system from the limiting state to the overlimiting one.
A similar transition and maximum increase in the average current were observed at 1.4 ilimLev for M2, Nafion 438, and Neosepta AMX membranes and at 1.25 ilimLev for the MK-40 membrane (Figure 5, Table 1).
It should be noted that the maximum increment in the average current for all studied samples was also achieved when the average potential corresponded to 1.4 ilimLev (Table 1). The maximum resistance of the electro-membrane system was achieved at this point on the current–voltage curves (Figure 8). That is, this current was the least attractive for electrodialysis at the DC mode. When using the PEF mode, this resistance decreased markedly because, during pulses with a high switching potential and pauses with zero current, favorable conditions for the development of electroconvection were made at the membrane surface.
Thus, the surface properties of ion-exchange membranes affect the limiting current value and CVC plateau length (Figure 5), which ultimately affects the efficiency and energy consumption of electrodialysis desalination both in the PEF and DC modes. The maximum current increase in the PEF compared to the DC mode at underlimiting and overlimiting currents was achieved at α = 1/4, and at potentials corresponding to overlimiting currents, at α = 1/2 (Table 1). Apparently, this is because electroconvection is absent or develops weakly at the underlimiting and limiting currents. Therefore, the increment in the mass transfer rate in the PEF mode is associated with a significant decrease in the solution resistance during a pause, which should be long.

3.2. Visualization of Electroconvective Vortices

The formation of electroconvective vortices in a PEF mode was visualized near the surface of the Neosepta AMX membrane at frequencies of 0.5 and 5.0 Hz, which, as was established in the previous section, are included in the optimal frequency ranges for the maximum increase in mass transfer rate. The duty cycle value of 1/2 was chosen as the most characteristic optimal value for overlimiting current regimes.
As it can be seen from the videos (Supplementary Materials) and Figure 9, the profile of the membrane under study is visible at the bottom of the image. When setting the DC mode at the current corresponding to 3.0 ilimLev (Figure 9a), in the video recording (Video 1), it can be seen that the formation of electroconvective vortices after the current is turned on (the current turns on for about 5 s) takes about 15 s. Dark areas correspond to a low concentration of the solution, light ones to a high concentration. The shape of the electroconvective vortices is clearly visible. The average size of the vortices increases with time (Video 1).
When using the PEF mode at the same average current value (over the period) (iav) corresponding to 3.0 ilimLev and a pulse frequency of 0.5 Hz, electroconvective vortices formed much faster. This was because the set current was two times higher than the average one at the pulse lapse (α = 1/2) (Video 2). The next time the pulse lapse of a direct current switched on, the vortices reached the maximum possible size (Figure 9c). It can be seen that, at the time of the pause, the vortices had time to decay. However, the inhomogeneous concentration field was preserved and did not have time to completely wash off by the laminar flow of the electrolyte (Figure 9d). This heterogeneity stimulates the development of electroconvection [25] in the same way it occurs in the case of an electrically inhomogeneous surface, which was first shown in the theoretical work of Urtenov et al. [3].
In the case where a relatively high pulse frequency (5.0 Hz) was set, an increase in the size of vortices in time was also observed (Video 3). However, during a pause, the electroconvective vortices formed during the pulse lapse of a direct current did not completely decay, as was established in theoretical works [25,36]. During the pause, the electroconvective vortices had time only to decrease slightly in size. Alternating vortex sizes during the pulse lapse of a direct current and pause lapse of zero current are visually observed in Video 3 in the form of a flickering concentration field.
It was shown in [25] that after turning off the voltage in the membrane system, electroosmotic fluid flows are retained for some time. These flows are due to the uneven distribution of the concentration of counterions along the longitudinal coordinate inside the electric double layer. The consequence of this is the uneven distribution of the volumetric electric force that feeds the vortices.

4. Conclusions

In this paper, the effect of surface inhomogeneity of ion-exchange membranes on the mass transfer efficiency in PEF modes was studied. It was found that the maximum increment in the average current is achieved when the average potentials correspond to the right-hand edge of the limiting current plateau in the voltammetric curves. In addition, it was shown that the maximum current increase in the PEF mode compared to the DC mode at underlimiting and limiting currents is most often achieved at α = 1/4, and at potentials corresponding to overlimiting currents, at α = 1/2.
It has been established that at potentials corresponding to overlimiting currents, a shift in the optimal frequency in the PEF mode to a relatively low-frequency range is observed. It is assumed that this is due to the relaxation rate of the concentration field at the membrane surface during a pause, which is low in the case of heterogeneous membranes compared to homogeneous ones.
It was experimentally shown that at relatively low frequencies in the PEF mode at the time of a pause, the vortices have time to decay. However, the inhomogeneous concentration field is retained and does not have time to completely wash off by the laminar flow of the electrolyte. It stimulates the rapid development of electroconvection when the electric field is switched back on. In the case where a relatively high pulse frequency is set during a pause, the electroconvective vortices formed during the pulse lapse of a direct current do not completely decay; they only slightly decrease in size.

Supplementary Materials

The following are available online at https://0-www-mdpi-com.brum.beds.ac.uk/2077-0375/10/3/40/s1, Video 1: Visualization of the vortex structures at the Neosepta AMX membrane surface in the desalination channel of the electrodialysis cell in the DC mode at i = 3.0 ilimLev; Video 2: Visualization of the vortex structures at the Neosepta AMX membrane surface in the desalination channel of the electrodialysis cell in the PEF mode at iav = 3.0 ilimLev (f = 0.5 Hz, α = 1/2); Video 3: Visualization of the vortex structures at the Neosepta AMX membrane surface in the desalination channel of the electrodialysis cell in the PEF mode at iav = 3.0 ilimLev (f = 5.0 Hz, α = 1/2).

Author Contributions

Conceptualization, D.B. and S.M.; methodology, D.B. and S.M.; validation, D.B. and S.M.; formal analysis, D.B. and K.T.; investigation, D.B., I.M. and K.T.; resources, D.B.; writing—original draft preparation, D.B. and S.M.; writing—review and editing, D.B. and S.M.; visualization, I.M. and K.T.; supervision, D.B.; project administration, D.B.; funding acquisition, D.B. All authors have read and agreed to the published version of the manuscript.

Funding

We are grateful to the Russian Foundation for Basic Research, Russia (grant No. 18-38-00600 mol_a), for the financial support of this study.

Acknowledgments

The authors are grateful to P.Yu. Apel (Joint Institute for Nuclear Research, Dubna, Russia) and V.V. Nikonenko (Kuban State University, Krasnodar, Russia) for help at various stages of the preparation of this article.

Conflicts of Interest

The authors declare no conflict of interest.

References

  1. Długołęcki, P.; Anet, B.; Metz, S.J.; Nijmeijer, K.; Wessling, M. Transport limitations in ion exchange membranes at low salt concentrations. J. Membr. Sci. 2010, 346, 163–171. [Google Scholar] [CrossRef]
  2. Nikonenko, V.V.; Kovalenko, A.V.; Urtenov, M.K.; Pismenskaya, N.D.; Han, J.; Sistat, P.; Pourcelly, G. Desalination at overlimiting currents: State-of-the-art and perspectives. Desalination 2014, 342, 85–106. [Google Scholar] [CrossRef]
  3. 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. Membr. Sci. 2013, 447, 190–202. [Google Scholar] [CrossRef]
  4. Rubinstein, I.; Zaltzman, B. Electro-osmotically induced convection at a permselective membrane. Phys. Rev. E 2000, 62, 2238–2251. [Google Scholar] [CrossRef]
  5. Pismenskaya, N.D.; Nikonenko, V.V.; Belova, E.I.; Lopatkova, G.Y.; Sistat, P.; Pourcelly, G.; Larshe, K. Coupled convection of solution near the surface of ion-exchange membranes in intensive current regimes. Russ. J. Electrochem. 2007, 43, 307–327. [Google Scholar] [CrossRef]
  6. 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. Membr. Sci. 2015, 496, 78–83. [Google Scholar] [CrossRef]
  7. Tanaka, Y. Acceleration of water dissociation generated in an ion exchange membrane. J. Membr. Sci. 2007, 303, 234–243. [Google Scholar] [CrossRef]
  8. 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]
  9. Andreeva, M.A.; Gil, V.V.; Pismenskaya, N.D.; Nikonenko, V.V.; Dammak, L.; Larchet, C.; Grande, D.; Kononenko, N.A. Effect of homogenization and hydrophobization of a cation-exchange membrane surface on its scaling in the presence of calcium and magnesium chlorides during electrodialysis. J. Membr. Sci. 2017, 540, 183–191. [Google Scholar] [CrossRef]
  10. Mikhaylin, S.; Nikonenko, V.; Pismenskaya, N.; Pourcelly, G.; Choi, S.; Kwon, H.J.; Han, J.; Bazinet, L. How physico-chemical and surface properties of cation-exchange membrane affect membrane scaling and electroconvective vortices: Influence on performance of electrodialysis with pulsed electric field. Desalination 2016, 393, 102–114. [Google Scholar] [CrossRef]
  11. 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] [PubMed]
  12. Zabolotskii, V.I.; Loza, S.A.; Sharafan, M.V. Physicochemical properties of profiled heterogeneous ion-exchange membranes. Russ. J. Electrochem. 2005, 41, 1053–1060. [Google Scholar] [CrossRef]
  13. Davidson, S.M.; Wessling, M.; Mani, A. On the Dynamical Regimes of Pattern-Accelerated Electroconvection. Sci. Rep. 2016, 6, 22505. [Google Scholar] [CrossRef] [PubMed]
  14. 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. Membr. Sci. 2016, 500, 161–170. [Google Scholar] [CrossRef]
  15. Nebavskaya, K.A.; Butylskii, D.Y.; Moroz, I.A.; Nebavsky, A.V.; Pismenskaya, N.D.; Nikonenko, V.V. Enhancement of Mass Transfer Through a Homogeneous Anion-Exchange Membrane in Limiting and Overlimiting Current Regimes by Screening Part of Its Surface with Nonconductive Strips. Pet. Chem. 2018, 58, 780–789. [Google Scholar] [CrossRef]
  16. 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, 59, 412–423. [Google Scholar] [CrossRef]
  17. 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. Membr. Sci. 2017, 523, 36–44. [Google Scholar] [CrossRef]
  18. Rubinstein, I. Electroconvection at an electrically inhomogeneous permselective interface. Phys. Fluids A 1991, 3, 2301–2309. [Google Scholar] [CrossRef]
  19. Pismenskaya, N.D.; Mareev, S.A.; Pokhidnya, E.V.; Larchet, C.; Dammak, L.; Nikonenko, V.V. Effect of surface modification of heterogeneous anion-exchange membranes on the intensity of electroconvection at their surfaces. Russ. J. Electrochem. 2019, 55, 1203–1220. [Google Scholar] [CrossRef]
  20. Balster, J.; Yildirim, M.H.; Stamatialis, D.F.; Ibanez, R.; Lammertink, R.G.H.; Jordan, V.; Wessling, M. Morphology and microtopology of cation-exchange polymers and the origin of the overlimiting current. J. Phys. Chem. B 2007, 111, 2152–2165. [Google Scholar] [CrossRef]
  21. Larchet, C.; Zabolotsky, V.I.; Pismenskaya, N.; Nikonenko, V.V.; Tskhay, A.; Tastanov, K.; Pourcelly, G. Comparison of different ED stack conceptions when applied for drinking water production from brackish waters. Desalination 2008, 222, 489–496. [Google Scholar] [CrossRef]
  22. Eigenberger, G.; Strathmann, H.; Grabovskiy, A. Membrane Assembly, Electrodialysis Device and Method for Continuous Electrodialytic Desalination. Patent of Germany No WO 2005/009596, 3 February 2005. [Google Scholar]
  23. Vermaas, D.A.; Saakes, M.; Nijmeijer, K. Enhanced mixing in the diffusive boundary layer for energy generation in reverse electrodialysis. J. Membr. Sci. 2014, 453, 312–319. [Google Scholar] [CrossRef]
  24. Mishchuk, N.A.; Koopal, L.K.; Gonzalez-Caballero, F. Intensification of electrodialysis by applying a non-stationary electric field. Colloids Surf. A: Physicochem. Eng. Asp. 2001, 176, 195–212. [Google Scholar] [CrossRef]
  25. 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]
  26. 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]
  27. Zyryanova, S.V.; Butylskii, D.Y.; Mareev, S.A.; Pis’menskaya, N.D.; Nikonenko, V.V.; Pourcelly, G. Effect of Parameters of Pulsed Electric Field on Average Current Density through Nafion 438 Membrane in Electrodialysis Cell. Russ. J. Electrochem. 2018, 54, 775–781. [Google Scholar] [CrossRef]
  28. Sistat, P.; Huguet, P.; Ruiz, B.; Pourcelly, G.; Mareev, S.A.; Nikonenko, V.V. Effect of pulsed electric field on electrodialysis of a NaCl solution in sub-limiting current regime. Electrochim. Acta 2015, 164, 267–280. [Google Scholar] [CrossRef]
  29. Malek, P.; Ortiz, J.M.; Richards, B.S.; Schäfer, A.I. Electrodialytic removal of NaCl from water: Impacts of using pulsed electric potential on ion transport and water dissociation phenomena. J. Membr. Sci. 2013, 435, 99–109. [Google Scholar] [CrossRef] [Green Version]
  30. 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]
  31. Dufton, G.; Mikhaylin, S.; Gaaloul, S.; Bazinet, L. Systematic Study of the Impact of Pulsed Electric Field Parameters (Pulse/Pause Duration and Frequency) on ED Performances during Acid Whey Treatment. Membranes 2020, 10, 14. [Google Scholar] [CrossRef] [Green Version]
  32. 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. Membr. Sci. 2014, 468, 389–399. [Google Scholar] [CrossRef]
  33. Ibl, N. Some theoretical aspects of pulse electrolysis. Surf. Technol. 1980, 10, 81–104. [Google Scholar] [CrossRef]
  34. Karlin, Y.V.; Kropotov, V.N. Electrodialysis separation of Na+ and Ca2+ in pulsed current mode. Elektrochimiya 1995, 31, 517–521. [Google Scholar]
  35. Karlin, Y.V.; Kropotov, V.N. The effects of unsteadiness in the initial period of electrodialysis. Elektrochimiya 1989, 25, 1654–1658. [Google Scholar]
  36. Mishchuk, N.A.; Verbich, S.V.; Gonzales-Caballero, F. Concentration Polarization and Specific Selectivity of Membranes in Pulse Mode. Colloid J. 2001, 63, 586–594. [Google Scholar] [CrossRef]
  37. 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] [PubMed] [Green Version]
  38. Ruiz, B.; Sistat, P.; Huguet, P.; Pourcelly, G.; Araya-Farias, M.; Bazinet, L. Effect of pulsed electric field on anion-exchange membrane fouling during electrodialysis of a casein solution. Desalination 2006, 200, 208–209. [Google Scholar] [CrossRef]
  39. Suwal, S.; Amiot, J.; Beaulieu, L.; Bazinet, L. Effect of pulsed electric field and polarity reversal on peptide/amino acid migration, selectivity and fouling mitigation. J. Membr. Sci. 2016, 510, 405–416. [Google Scholar] [CrossRef]
  40. Martí-Calatayud, M.C.; Buzzi, D.C.; García-Gabaldón, M.; Bernardes, A.M.; Tenório, J.A.S.; Pérez-Herranz, V. Ion transport through homogeneous and heterogeneous ion-exchange membranes in single salt and multicomponent electrolyte solutions. J. Membr. Sci. 2014, 466, 45–57. [Google Scholar] [CrossRef] [Green Version]
  41. 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]
  42. Chang, H.-C.; Yossifon, G.; Demekhin, E.A. Nanoscale Electrokinetics and Microvortices: How Microhydrodynamics Affects Nanofluidic Ion Flux. Annu. Rev. Fluid Mech. 2012, 44, 401–426. [Google Scholar] [CrossRef] [Green Version]
  43. Kwak, R.; Pham, V.S.; Lim, K.M.; Han, J. Shear Flow of an Electrically Charged Fluid by Ion Concentration Polarization: Scaling Laws for Electroconvective Vortices. Phys. Rev. Lett. 2013, 110, 114501. [Google Scholar] [CrossRef] [PubMed]
  44. Kim, S.J.; Ko, S.H.; Kwak, R.; Posner, J.D.; Kang, K.H.; Han, J. Multi-vortical flow inducing electrokinetic instability in ion concentration polarization layer. Nanoscale 2012, 4, 7406. [Google Scholar] [CrossRef] [PubMed]
  45. Vobecká, L.; Belloň, T.; Slouka, Z. Behavior of Embedded Cation-Exchange Particles in a DC Electric Field. Int. J. Mol. Sci. 2019, 20, 3579. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  46. Vasil’eva, V.I.; Shaposhnik, V.A.; Grigorchuk, O.V.; Petrunya, I.P. The membrane–solution interface under high-performance current regimes of electrodialysis by means of laser interferometry. Desalination 2006, 192, 408–414. [Google Scholar] [CrossRef]
  47. Shaposhnik, V.A.; Vasil’eva, V.I.; Grigorchuk, O.V. The interferometric investigations of electromembrane processes. Adv. Colloid Interface Sci. 2008, 139, 74–82. [Google Scholar] [CrossRef]
  48. Takemoto, N. The Concentration Distribution in the Interfacial Layer at the Desalting Side in Ion Exchange Membrane Electrodialysis. Nippon Kagaku Kaishi 1972, 2053. [Google Scholar] [CrossRef]
  49. Yossifon, G.; Chang, H.-C. Selection of Nonequilibrium Overlimiting Currents: Universal Depletion Layer Formation Dynamics and Vortex Instability. Phys. Rev. Lett. 2008, 101, 254501. [Google Scholar] [CrossRef] [Green Version]
  50. 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 A Chip 2018, 18, 1652–1660. [Google Scholar] [CrossRef] [Green Version]
  51. Mareev, S.A.; Butylskii, D.Y.; Pismenskaya, N.D.; Larchet, C.; Dammak, L.; Nikonenko, V.V. Geometric heterogeneity of homogeneous ion-exchange Neosepta membranes. J. Membr. Sci. 2018, 563, 768–776. [Google Scholar] [CrossRef]
  52. 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] [PubMed]
  53. Vasil’eva, V.I.; Kranina, N.A.; Malykhin, M.D.; Akberova, E.M.; Zhiltsova, A.V. The surface inhomogeneity of ion-exchange membranes by SEM and AFM data. J. Surf. Investig. X-RaySynchrotron Neutron Tech. 2013, 7, 144–153. [Google Scholar] [CrossRef]
  54. Vasil’eva, V.I.; Akberova, E.M.; Zhiltsova, A.V.; Chernykh, E.I.; Sirota, E.A.; Agapov, B.L. SEM diagnostics of the surface of MK-40 and MA-40 heterogeneous ion-exchange membranes in the swollen state after thermal treatment. J. Surf. Investig. X-RaySynchrotron Neutron Tech. 2013, 7, 833–840. [Google Scholar] [CrossRef]
  55. Butylskii, D.Y.; Mareev, S.A.; Pismenskaya, N.D.; Apel, P.Y.; Polezhaeva, O.A.; Nikonenko, V.V. Phenomenon of two transition times in chronopotentiometry of electrically inhomogeneous ion exchange membranes. Electrochim. Acta 2018, 273, 289–299. [Google Scholar] [CrossRef]
  56. 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]
  57. Butylskii, D.Y.; Mareev, S.A.; Nikonenko, V.V.; Pismenskaya, N.D.; Larchet, C.; Dammak, L.; Grande, D.; Apel, P.Y. In situ investigation of electrical inhomogeneity of ion exchange membrane surface using scanning electrochemical microscopy. Pet. Chem. 2016, 56, 1006–1013. [Google Scholar] [CrossRef]
  58. Cifuentes-Araya, N.; Pourcelly, G.; Bazinet, L. Impact of pulsed electric field on electrodialysis process performance and membrane fouling during consecutive demineralization of a model salt solution containing a high magnesium/calcium ratio. J. Colloid Interface Sci. 2011, 361, 79–89. [Google Scholar] [CrossRef]
  59. Pelletier, S.; Serre, É.; Mikhaylin, S.; Bazinet, L. Optimization of cranberry juice deacidification by electrodialysis with bipolar membrane: Impact of pulsed electric field conditions. Sep. Purif. Technol. 2017, 186, 106–116. [Google Scholar] [CrossRef]
Membranes 10 00040 g001 550
Figure 1. SEM image of the surface of a homogeneous Nafion 438 membrane (a) and its micrograph obtained using an optical microscope (b).
Figure 1. SEM image of the surface of a homogeneous Nafion 438 membrane (a) and its micrograph obtained using an optical microscope (b).
Membranes 10 00040 g001
Membranes 10 00040 g002 550
Figure 2. SEM image of the surface of a homogeneous Neosepta AMX membrane (a) and micrograph of its cross-sections in a dry (b) and swollen state (c) (b and c were adapted from [51]).
Figure 2. SEM image of the surface of a homogeneous Neosepta AMX membrane (a) and micrograph of its cross-sections in a dry (b) and swollen state (c) (b and c were adapted from [51]).
Membranes 10 00040 g002
Membranes 10 00040 g003 550
Figure 3. SEM images of the surface of the heterogeneous M1 (a) and M2 (b) membranes, as well as a cross-section through the conductive region of the membrane M1 (c) and the surface of the MK-40 (d) membrane.
Figure 3. SEM images of the surface of the heterogeneous M1 (a) and M2 (b) membranes, as well as a cross-section through the conductive region of the membrane M1 (c) and the surface of the MK-40 (d) membrane.
Membranes 10 00040 g003
Membranes 10 00040 g004 550
Figure 4. Schematic current and voltage versus time dependencies in pulsed electric field mode. The dashed lines show the period-averaged applied potential (Uav) and the period-averaged measured current (iav).
Figure 4. Schematic current and voltage versus time dependencies in pulsed electric field mode. The dashed lines show the period-averaged applied potential (Uav) and the period-averaged measured current (iav).
Membranes 10 00040 g004
Membranes 10 00040 g005 550
Figure 5. Current–voltage curves of the studied membranes in a 0.02 M NaCl solution at a linear flow velocity of 3.6 mm/s. Tangents and their intersection points show the right-hand edge of the limiting current plateau for M1 and MK-40 membranes.
Figure 5. Current–voltage curves of the studied membranes in a 0.02 M NaCl solution at a linear flow velocity of 3.6 mm/s. Tangents and their intersection points show the right-hand edge of the limiting current plateau for M1 and MK-40 membranes.
Membranes 10 00040 g005
Membranes 10 00040 g006 550
Figure 6. The results of testing the Nafion 438, Neosepta AMX, M1, M2, and MK-40 membranes in the pulsed electric field mode: i = 0.75 ilimLev, duty cycle 1/4 (a), and 1.0 ilimLev, duty cycle 1/4 (excluding results for Neosepta AMX membrane for which they are shown at 1.0 ilimLev and α = 2/3) (b). The horizontal dashed line denotes the i/ilimLev ratio corresponding to a given potential drop Uav in the DC mode.
Figure 6. The results of testing the Nafion 438, Neosepta AMX, M1, M2, and MK-40 membranes in the pulsed electric field mode: i = 0.75 ilimLev, duty cycle 1/4 (a), and 1.0 ilimLev, duty cycle 1/4 (excluding results for Neosepta AMX membrane for which they are shown at 1.0 ilimLev and α = 2/3) (b). The horizontal dashed line denotes the i/ilimLev ratio corresponding to a given potential drop Uav in the DC mode.
Membranes 10 00040 g006
Membranes 10 00040 g007 550
Figure 7. The results of testing the Nafion 438, Neosepta AMX, M1, M2, and MK-40 membranes in the pulsed electric field mode: i = 1.25 ilimLev, duty cycle 1/2 (excluding results for M1, M2 membranes for which they are shown at 1.25 ilimLev and α = 1/3) (a), and 1.4 ilimLev, duty cycle 1/2 (excluding results for Neosepta AMX membrane for which they are shown at 1.4 ilimLev and α = 3/4) (b). The horizontal dashed line denotes the i/ilimLev ratio corresponding to a given potential drop Uav in the DC mode.
Figure 7. The results of testing the Nafion 438, Neosepta AMX, M1, M2, and MK-40 membranes in the pulsed electric field mode: i = 1.25 ilimLev, duty cycle 1/2 (excluding results for M1, M2 membranes for which they are shown at 1.25 ilimLev and α = 1/3) (a), and 1.4 ilimLev, duty cycle 1/2 (excluding results for Neosepta AMX membrane for which they are shown at 1.4 ilimLev and α = 3/4) (b). The horizontal dashed line denotes the i/ilimLev ratio corresponding to a given potential drop Uav in the DC mode.
Membranes 10 00040 g007
Membranes 10 00040 g008 550
Figure 8. Resistance (∆ϕ/i) versus i/ilimLev dependencies for the studied membranes determined from current–voltage curves (Figure 5).
Figure 8. Resistance (∆ϕ/i) versus i/ilimLev dependencies for the studied membranes determined from current–voltage curves (Figure 5).
Membranes 10 00040 g008
Membranes 10 00040 g009 550
Figure 9. Visualization of the vortex structures at the Neosepta AMX membrane surface in the desalination channel of the electrodialysis cell in the DC mode at i = 3.0 ilimLev (a) and in the absence of current (b), and in the PEF mode at iav = 3.0 ilimLev (f = 0.5 Hz, α = 1/2) at the pulse lapse of a direct current (c) and pause lapse of zero current (d).
Figure 9. Visualization of the vortex structures at the Neosepta AMX membrane surface in the desalination channel of the electrodialysis cell in the DC mode at i = 3.0 ilimLev (a) and in the absence of current (b), and in the PEF mode at iav = 3.0 ilimLev (f = 0.5 Hz, α = 1/2) at the pulse lapse of a direct current (c) and pause lapse of zero current (d).
Membranes 10 00040 g009
Table
Table 1. The values of the maximum average increment in measured current over the period, ω (%) *, at the most effective duty (the value of α is indicated in round brackets) in the pulsed electric field (PEF) mode compared to the DC mode.
Table 1. The values of the maximum average increment in measured current over the period, ω (%) *, at the most effective duty (the value of α is indicated in round brackets) in the pulsed electric field (PEF) mode compared to the DC mode.
Set Potential Drop (Uav)
at i/ilimLev		Nafion 438Neosepta AMXM1M2MK-40
0.7512.0 (α = 1/4)4.0 (α = 1/4)4.6 (α = 1/4)9.2 (α = 1/4)4.7 (α = 1/4)
1.03.9 (α = 1/4)2.0 (α = 2/3)20.1 (α = 1/4)7.0 (α = 1/4)0.2 (α = 1/4)
1.254.6 (α = 1/2)1.6 (α = 1/2)5.6 (α = 1/3)6.6 (α = 1/3)30.1 (α = 1/2)
1.432.9 (α = 1/2)11.1 (α = 3/4)19.3 (α = 1/2)25.9 (α = 1/2)19.2 (α = 1/2)
* average values from 3 experiments.

Share and Cite

MDPI and ACS Style

Butylskii, D.; Moroz, I.; Tsygurina, K.; Mareev, S. Effect of Surface Inhomogeneity of Ion-Exchange Membranes on the Mass Transfer Efficiency in Pulsed Electric Field Modes. Membranes 2020, 10, 40. https://0-doi-org.brum.beds.ac.uk/10.3390/membranes10030040

AMA Style

Butylskii D, Moroz I, Tsygurina K, Mareev S. Effect of Surface Inhomogeneity of Ion-Exchange Membranes on the Mass Transfer Efficiency in Pulsed Electric Field Modes. Membranes. 2020; 10(3):40. https://0-doi-org.brum.beds.ac.uk/10.3390/membranes10030040

Chicago/Turabian Style

Butylskii, Dmitrii, Ilya Moroz, Kseniya Tsygurina, and Semyon Mareev. 2020. "Effect of Surface Inhomogeneity of Ion-Exchange Membranes on the Mass Transfer Efficiency in Pulsed Electric Field Modes" Membranes 10, no. 3: 40. https://0-doi-org.brum.beds.ac.uk/10.3390/membranes10030040

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