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Membranes 2020, 10, 347 3 of 15 device was used to demonstrate the capabilities of shock deionization using a negatively charged silica glass frit as a porous microstructure that was sitting on a cation-exchange membrane, as shown in Figure 1 [16,17]. Further works were published between 2015 and 2020 by prof. Bazant’s group demonstrating the functionalities of improved and scale friendly designs of a new shock electrodialysis unit that once again utilized a porous frit with negative surface charge sandwiched between a pair of cation-exchange membranes to induce the concentration polarization. The device was capable of reducing the ion concentration by four orders of magnitude [4,18–20]. Figure 1. Shock electrodialysis device development. (a) shows the scheme of the “button” unit displayed on (b,c) [17]. (d) shows the operating principle of the “second generation” unit that is displayed in (e) and has overall dimensions “2 × 2 × 1.5” [20]. Deionization shocks spread through the channels of the porous medium as a sharp concentration gradient. From these extended zones, freshwater and brine are separately collected. The outlet points are separated by a splitter, a thin partition that prevents the outlet streams from mixing once discharged from the device [20]. Adapted from [17] for (a–c) and [20] for (d,e). Copyright 2013 and 2015. American Chemical Society. In a sense, the SED unit design is rather similar to that of a classical electrodialysis module. However, as the principle is based on the extension of ion depleted (and enriched) zones in the porous medium, the concentrate and diluate are collected from the same single “desalination chamber”. To promote the desired effects associated with OLC, the thickness of the porous material (and therefore the chamber) is limited. That limits the amount of water produced and brings difficulties with product collection at such a tiny scale. The early experiments of our group at the Technical University of Liberec (TUL) focused on the first scale-up of the unit (what we call “Generation III unit”) inspired by the Bazant Research Group’s work (referenced to as “Generation II unit”) (Figure 2). The unit was made twice as large in all dimensions with an active membrane surface eight times larger (a surface in contact with the porous medium) compared to the unit (“Gen. II unit”) presented in [20]. That allowed for approximately ten times higher flow rates through the porous medium (Figure 2). We also experimented with various types of porous materials. Interestingly, very simple and not well-defined materials, such as simple fired brick, delivered performance similar to the glass frit [21]. However, the desalination performance of the unit was not on par with the results published by Bazant’s group, and we still experienced difficulties with product collection [22,23]. Table 1 compares the results achieved on our “Gen. II” and “Gen. III” units to the results published by [20] using “dimensionless current” Equation (1) proposed in his work (and the work of [17], that collapses thePDF Image | Desalination Performance Assessment Anion-Exchange Membranes
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