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Figure 5.32 Adsorption density vs. temperature in the case of sulfite (SF) reduction (B2–B4 brine solution). The theoretical maximum of the adsorption density is 46.0 mg/g. .............115 Figure 5.33 Weight percentage of lithium iron phosphate in solid vs. temperature in the case of sulfite (SF) reduction (B2–B4 brine solution). ....................................................................116 Figure 5.34 Iron (Fe) dissolution and final pH in the case of thiosulfate (TS) reduction (B1– B8 brine solution).......................................................................................................................117 Figure 5.35 Iron (Fe) dissolution and final pH in the case of sulfite (SF) reduction (B1–B8 brine solution).............................................................................................................................119 Figure 5.36 Adsorption density and iron (Fe) dissolution at pH 4 (uncontrolled) and 7 (controlled with sodium hydroxide) in the case of thiosulfate (TS) reduction (B1 brine solution)...................................................................................................................................... 120 Figure 5.37 Schematic flowsheet of the ferric phosphate method. Flow of FP and LFP solid is in orange and flow of brine solution is in blue. FP and LFP are recycled by a continuous loading and stripping cycle. ..................................................................................................... 121 Figure 5.38 XRD patterns of battery-grade (BG-) LFP and BG-FP (delithiated LFP by PS oxidation), and products after two cycles of loading and stripping experiments. The loading experiments used B1 brine solution at pH 7 controlled by sodium hydroxide and lithium was loaded by thiosulfate (TS) at 65 °C. The stripping experiments used persulfate to oxidize the loaded materials. ....................................................................................................................... 122 Figure 5.39 Concentration of metal ions in the initial brine solution (B1 brine solution) and solution after stripping in the first and second cycle of the loading and stripping experiments. The loading experiments used B1 brine solution at pH 7 controlled by sodium hydroxide and lithium was loaded by thiosulfate (TS) at 65 °C. The stripping experiments used persulfate to oxidize the loaded materials and it was carried out with a solid concentration of 10 wt%. - xviii -PDF Image | LITHIUM EXTRACTION FROM BRINE using ion resin
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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)