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Membranes 2022, 12, 3x73 66ooff 29 Figure 4. Precipitation schematic diagram. Figure 4. Precipitation schematic diagram. A high Mg/Li ratio has been shown to have a negative effect on Li separation, although Mg + Strong Alkali → Mg Carbonate or Mg Salt (1) double hydroxides (LDH) intercalated with the Mg had unveiled many other shortcomings, this has been improved over the years. Newer precipitation methods such as using layered 2+ Mg2+ + Ca(OH)2 → Mg(OH)2 + Ca2+ (2) for instance, low Li recovery due to primary formation of LiAl2(OH)6Cl·xH2O [51,52]. Despite recent advanceme2+nts, most precipitation-based processes are usually very time- Ca + CaCl2 + coexisting ions → CaSO4•2H2O (3) consuming and produce significant amounts of waste. 2Li+ + Na2CO3 → Li2CO3 + 2Na+ (4) 3.1.2. Solvent Extraction Solvent extraction has been considered as an effective hydro-metallurgical separation Mg2+ + Ca(OH)2 + SO42− + 2H2O → CaSO4•2H2O + Mg(OH)2 (5) A high Mg/Li ratio has been shown to have a negative effect on Li separation, alt- technique and has demonstrated several technological strengths—a simple, continuous hough this has been improved over the years. Newer precipitation methods such as using operation that is easily adaptable [53,54]. This process normally consists of four major layered double hydroxides (LDH) intercalated with the Mg had unveiled many other stages, as shown in Figure 5, with the solvent being recirculated throughout the process shortcomings, for instance, low Li recovery due to primary formation of and lithium removed as an extractant [55]. The solutes are induced into equilibrium with LiAl2(OH)6Cl·xH2O [51,52]. Despite recent advancements, most precipitation-based pro- the organic solvent before scrubbing to remove the undesired solutes. The addition of ++ cHeCssleisnatorethuesuralflfiynvaetreystirmipes-cthonesmumixitnugrea,nredpplarocidnugceLisigwnitfhicaHnt,aamnodutnhtesnoefwamstiex.ture is then regenerated to restart the process [56]. A typical example of this method is using 3.1.2. Solvent Extraction tributylphosphate (TBP)/Kerosene with FeCl3 as a co-extraction agent which requires low pH to avoid hydrolysis of ferric ions [55,57]. In this method, one of the challenges is the Solvent extraction has been considered as an effective hydro-metallurgical separation selection of suitable solvents, as common solvents have a preference for H+ rather than Li+ technique and has demonstrated several technological strengths—a simple, continuous or a low attraction affinity for the solute. In addition, the development of a more efficient operation that is easily adaptable [53,54]. This process normally consists of four major scrubbing stage is highly desirable. It has been found that in a continuous operation with stages, as shown in Figure 5, with the solvent being recirculated throughout the process multiple scrubbing stages aided by centrifugation, Li extraction rate has been improved and lithium removed as an extractant [55]. The solutes are induced into equilibrium with significantly [58,59]. the organic solvent before scrubbing to remove the undesired solutes. The addition of HCl Inrecentstudies,ionicliquids(ILs)wereem+ployed+toimprovethepracticalityof into the raffinate strips the mixture, replacing Li with H , and the new mixture is then the process. They have attractive solvent extraction properties such as negligible volatil- regenerated to restart the process [56]. A typical example of this method is using tribu- ity, nonflammability, high thermal and electrochemical stability, and outstanding ionic tylphosphate (TBP)/Kerosene with FeCl3 as a co-extraction agent which requires low pH conductivity even under anhydrous conditions [60]. Previously, typical ILs such as hexaflu- to avoid hydrolysis of ferric ions [55,57]. In this method, one of the challenges is the selec- orophosphate (PF−) and bis(trifluoromethyl sulfonyl)imide (NTf−) were employed due to tion of suitable so6lvents, as common solvents have a preference f2or H+ rather than Li+ or a their immiscibility in water. However, this results in fluoride hydrolysis to hydrofluoric low attraction affinity for the solute. In addition, the development of a more efficient acid (Equation (6)) [61]. scrubbing stage is highly desirable. It has been found that in a continuous operation with multiple scrub+bing st−ages aided by centrifugation, Li extraction rate has been improved 6H +PF6 +6H2O+HNO3 → H3PO4 +6HF+HNO3 +2H2O (6) significantly [58,59]. In recent studies, ionic liquids (ILs) were employed to improve the practicality of the process. They have attractive solvent extraction properties such as negligible volatility,PDF Image | Lithium Harvesting using Membranes
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Product and Development Focus for Infinity Turbine
ORC Waste Heat Turbine and ORC System Build Plans: All turbine plans are $10,000 each. This allows you to build a system and then consider licensing for production after you have completed and tested a unit.Redox Flow Battery Technology: With the advent of the new USA tax credits for producing and selling batteries ($35/kW) we are focussing on a simple flow battery using shipping containers as the modular electrolyte storage units with tax credits up to $140,000 per system. Our main focus is on the salt battery. This battery can be used for both thermal and electrical storage applications. We call it the Cogeneration Battery or Cogen Battery. One project is converting salt (brine) based water conditioners to simultaneously produce power. In addition, there are many opportunities to extract Lithium from brine (salt lakes, groundwater, and producer water).Salt water or brine are huge sources for lithium. Most of the worlds lithium is acquired from a brine source. It's even in seawater in a low concentration. Brine is also a byproduct of huge powerplants, which can now use that as an electrolyte and a huge flow battery (which allows storage at the source).We welcome any business and equipment inquiries, as well as licensing our turbines for manufacturing.CONTACT TEL: 608-238-6001 Email: greg@infinityturbine.com (Standard Web Page)