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contain divalent cations such as Ca2+, Mg2+, etc. That removes any need to remove those ions ahead of the lithium extraction step. Anions like sulphate and borate are not extracted, therefore sulphate and boron do not need to be removed from the feed brine. Table 6 – Published selectivity values for of LIS materials Sea water Ion mg/kg Li+ 0.18 Na+ 10561 K+ 380 Mg2+ 1272 Ca2 400 mmol/kg Selectivity Li/Other - 149242 5491 85012 16212 Dissolved 0.02593 459.38 9.72 52.33 9.98 Adsorbed 1982.4 235.3 135.3 94.1 94.1 Simplistically, stripping the loaded LIS with HCl would require one mole of HCl per mole of lithium stripped. If the resulting strip solution is used to precipitate lithium carbonate, that would consume one mole of sodium carbonate per mole of lithium carbonate produced. Copying the logic used for the other chemistry and assuming that the levels of divalent cations in the strip solution are low enough that precipitating them as hydroxide or carbonate requires amounts of sodium hydroxide and carbonate too small to register in these overall calculations, this leads to the results shown in Table 7. The reagent cost calculated for making lithium carbonate via this new lithium-ion sieve chemistry is slightly below the number calculated for applying established chemistry to the Clayton Valley Project, and the same as for producing lithium hydroxide in the Clayton Valley Project. Table 7 – Lithium-ion sieve chemistry producing Li2CO3 or LiOH, $/kg LCE Reagent HCl NaOH Na2CO3 Power Cost, $/t 240 560 370 Sub-total Li2CO3 LiOH 0.1 0 0.6 0.6 0.5 0 - 0.5 1.3 1.1 At this level of analysis, the LIS-based chemistry gives the same calculated major reagent (and power, in the case of making lithium hydroxide) costs, regardless of the type of brine, thus this approach would seem to be applicable to high-calcium brines that are not amenable to the established chemistry. Conclusion The established chemistry for producing lithium carbonate from salar brines would appear to be applicable only to salar brines. Extracting lithium from other brines will need new chemistry, two variations of which have been presented. At the calculated reagent cost of about $0.8/kg LCE, the established chemistry appears to have an economic edge over the other two, but only for salar brines. As can be seem from Table 3, the Presented at the Critical Materials Symposium, EXTRACTION 2018, Ottawa, August 26-29PDF Image | Extraction of Lithium from Brine Chemistry
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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)