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Membranes 2021, 11, 175 14 of 20 Table 7. Comparison of different configurations and performance of MD process reported in the literature and inthis work (two months of operation). Simulation conditions: RR = 50%, S = 2.5 m2, CF = 20, ER(Li+) = 90%. MD Temperature Process Mode Configura- (Hot/Cold tion side) Hollow fiber 65/30 (DCMD) Hollow fiber 85/25 (DCMD) Hollow fiber 85/50 (DCMD) Flat sheet (AGMD- 60/20 MC) Flat sheet (AGMD- 80/20 MC) Build-Up Time, Hours Number of Membrane Washings Number of Replaced Membrane Modules Recovered Li+, kg 0.914 3.954 4.427 1.410 2.138 Evaporated Water, kg 5836 20901 29134 9231 13677 Crystallized NaCl, kg 2076 7456 10399 3290 4879 Specific Output, Ref. g(Li+)/Module 24.7 [52] 233 [49] 2214 [61] 353 This work 428 This work 778 480 37 228 72 17 131342 467 288 4 333 288 5 The energy and cost evaluations were out of the scope of this study; however, it should be pointed out that 1/3 of hot solution at 60 ◦C after the membrane distillation unit was fed to the crystallizer to be cooled down to 15 ◦C. Variation of different system parameters did not noticeably change the mass flow-rate of saline solution that went to the crystallizer (6 kg/min), which means that about 259 tons of saline solution per month had to be cooled down and then heated up. Bearing this in mind, a very critical parameter for this application would be not only the cost and robust performance of the membrane modules but also the effective heat recuperation, which will be complicated by the fact that the saline solution is near saturation or oversaturation with regard to its temperature. As a result, not all developments and achievements proposed and used for effective heat recuperation in the membrane distillation of low or moderate saline solutions would be applicable in the membrane crystallization process. 3.3.2. Effect of Lithium Recovery and Concentration As discussed above, the efficiency of the membrane extraction process is based on the lithium concentration in the feed solution, which should be 0.7 g/L and preferably above 2.0 g/L. Therefore, we have considered three case scenarios, when the initial saline solution was concentrated by the factor of 5, 20, and 50 to achieve Li+ concentration in the liquid loop of 0.6, 2.3, or 6.0 g/kg, respectively. Table 8 presents the data for the initial build-up step and followed by two months of operation when the desired lithium concentration was reached and maintained at the same level. As can be seen, Li+ presence in the 140 kg of the solution with the continuous make-up flow can be increased by a factor of 5 within 92 h by using one membrane module. However, one fold change of concentration factor CF from 5 up to 50 required 13.3 times longer time of operation (92 vs. 1227 h) and three replacements of membrane modules to reach lithium concentration of 6.0 g/kg. Ten times higher concentration of lithium in the circulated solution does not lead to a noticeable change of the process parameters except the dramatic reduction of the amount of solution fed to the membrane extraction unit by a factor of 6.2 (1662 vs. 269 kg). The increase of lithium recovery by 6% was also noticed, but this improvement in lithium extraction would be greater once the membrane extraction process is considered and simulated in detail. The decrease of extraction rate of lithium from 90 down to 50% did not have a noticeable impact on the recovered lithium in this simulation because this change of ER(Li+) parameter was compensated by a nearly double increase of the amount of solution fed to the membrane extraction unit from 650 up to 1151 kg during two months of operation (see Table 9).PDF Image | Process of Lithium Recovery from Geothermal Brine
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