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Membranes 2020, 10, 347 10 of 15 Figure 7. Comparison of performance of our unit with various installed porous media and AMEs and reference units with silica glass frit and cation-exchange membranes (CEMs) using the model (4) to fit the data. It is important to note that anion-exchange membranes were used in these experiments, whereas we compared the results to a unit with cation-exchange membranes. The combination of positively charged porous material and AEMs should promote deionization shocks to effectively separate the anions from the bulk solution. This explains the somewhat lower desalination performance observed with Na2SO4 compared to NaCl, as the diffusivity coefficient of sulfate anion is approximately twice lower than that of Cl− (≈ 1.07 × 10−9 m2/s for SO42− compared to 2.03 × 10−9 m2/s for Cl− [26]), which leads to lower ion mobility despite the higher negative charge. 3.2. Flow Rates and Water Recovery As far as water recovery is concerned, the obtained data is again in conflict with the observations reported by [4,18–20], as described above. The water recovery stayed rather the same, moving in the range of 45% to 55%, occasionally dropping below 40% or rising above 60% without any apparent reason. That said, the splitter was positioned in the middle along the outlet edge, and therefore water recovery of 50% would be expected without the effects of EOF. The changes in values were probably connected to the unstable flow rates through the porous medium that was present despite the fixed flow rate of the inlet. The flow rate Q used in Equation (1) to estimate the dimensionless current was, therefore, the actual flow rate measured at the outlets. The inconsistency may have added errors to the experiments, while the reason behind this behaviour is not clear. One possible explanation is the change of hydrodynamic resistivity of the porous material caused by some sort of impurities from the feeding solution or, more likely, debris and loose particles released from the porous material itself, which may have blocked channels at the output. To minimize the influences caused by the medium, the porous material needs to be revised. Structural irregularities present in not very well-defined material, which the Siltep 11 mainly is, may have interfered with the flow rates and water recovery as well. Besides these effects, peristaltic pumps are not ideal for driving the solution into the unit because of the pulsating flow produced by these systems. To minimize these effects, either pulsation dampeners or flow buffer capacitors developed later by Bazant’s group could be used to smooth out the pulses and stabilize the flow rates [19]. In future work, we are planning to test product withdrawal using peristaltic or injection pumps, which, based on the initial experiments we have performed, seemed to work rather well, even stabilizing the desalination.PDF Image | Desalination Performance Assessment Anion-Exchange Membranes
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