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Membranes 2021, 11, 175 the results were similar, only with higher fluxes; this resulted in a decrease in time before the flushing (120 min instead of 270 min), but the flushing duration was in- tentionally the same (30 min) because we need to flush a similar amount of foulants. Performance data at different temperatures were approximated linearly using the first experimental points and taking into account zero flow when the temperatures of the hot and the cold parts of the module are equal (20 °C, Figure 5). These de- pendencies were used for further simulation in Simulink. due to the deposition of precipitated salt crystals and organic substances. Salt deposition occur due to the deposition of precipitated salt crystals and organic substances. Salt can be considered as an almost reversible process because salts can be washed off with deposition can be considered as an almost reversible process because salts can be either water or dilute acid solutions (for carbonates). Deposition of organic compounds washed off with either water or dilute acid solutions (for carbonates). Deposition of is an almost irreversible process that reduces membrane hydrophobicity by up to 70%, organic compounds is an almost irreversible process that reduces membrane hy- 8 of 20 Figure 5. Experimental data of AGMD-MC module performance as a function of feed temperature. Figure 5. Experimental data of AGMD-MC module performance as a function of feed temperature. Fouling in membrane distillation with hydrophobic membranes can mainly occur Fouling in membrane distillation with hydrophobic membranes can mainly according to [51]. The solubility of NaCl increases from ~26.3 to ~27.3 wt. %, i.e., for drophobicity by up to 70%, according to [51]. The solubility of NaCl increases from only 1 wt. %, while heating from 10 to 75 ◦C. This greatly complicates the crystallization ~26.3 to ~27.3 wt. %, i.e., for only 1 wt. %, while heating from 10 to 75 °C. This greatly processes by cooling, and it is probably the main reason for very limited data on NaCl complicates the crystallization processes by cooling, and it is probably the main saturated solutions published in the literature. Table 3 presents the data on the performance reason for very limited data on NaCl saturated solutions published in the literature. drop in the membrane distillation with the crystallization of NaCl solutions. Most of the Table 3 presents the data on the performance drop in the membrane distillation works either do not provide information about the long-term operation of the membrane with the crystallization of NaCl solutions. Most of the works either do not provide module or do not indicate the parameters for the performance drop. Therefore, the flux information about the long-term operation of the membrane module or do not in- drop in one run (ratio of fluxes at the beginning and the end of the run) and recovery ratio dicate the parameters for the performance drop. Therefore, the flux drop in one run (ratio of the fluxes in the first and second run) were estimated in this work if these data (ratio of fluxes at the beginning and the end of the run) and recovery ratio (ratio of were missed in the corresponded articles. As can be seen, the flux drop in one run and the the fluxes in the first and second run) were estimated in this work if these data were recovery ratio are varied in a quite wide range, which is subject to operation conditions, missed in the corresponded articles. As can be seen, the flux drop in one run and membrane nature, and system configuration including the crystallization step. In this the recovery ratio are varied in a quite wide range, which is subject to operation work, we used our experimental data for further simulation of membrane performance. conditions, membrane nature, and system configuration including the crystalliza- tion step. In this work, we used our experimental data for further simulation of Table 3. Comparison of performance drop in the membrane distillation with crystallization for NaCl saturated solution. membrane performance. Process Membrane Temperatures, Duration of Flux Drop in Recovery Source ◦C (Hot/Cold) One Run, h One Run, % Ratio, % Table 3. Comparison of performance drop in the membrane distillation with crystallization for NaCl saturated solution. 82 [49] 94 [52] DCMD DCMD PP 80/50 PVDF 65/30 20 4 30.3 61.8 Process DCMD DCMDDCMD DCMD SMDC DCMD VMD AGMD-MC Membrane Temperatures, PP °C8(5H/5o5t/Cold) Flux Drop in One10R.7un, % Recovery Ratio, Source Duration of One42Run, h 0.260 4 PVDF 40–70/25 3.3 0–47 PVDFPP 60/8105/50 53–105.3 9%4 98.26 [53] [50[5]4] PVDF 65/30 61.8 94 [52] DCMD DCMD DCMD DCMD PTFE 80/70 0.8 100 CF4-MP-PVDF 60/20 PVDF 70–80/20 5–8.5 92–93 PVDF 50–60/20–30 5–8.5 100 - 35 - - - - - - - 99 [55] [56] [57] [58] [59] [60] [61] this work PFDV/PAN PTFE MFFK-1 60/25 50/vacuum 60–80/20 9 40 6 24 2–4.5 24PDF Image | Process of Lithium Recovery from Geothermal Brine
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