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29 30 US 10,695,694B2 methodsuchashydrothermal,solidstate,microwave,or betwenthecoatedionexchangeparticles,theuncoatedion combinationsthereof.Theuncoatedionexchangeparticles exchangeparticles,and/orcombinationsthereof,andthe oftheporousbeadistreatedwithanacidsolutionprepared liquidresource. withhydrochloricacid,sulfuricacid,nitricacid,orcombi When thecoatedionexchangeparticles,porousstruc nationsthereofwhereintheconcentrationoftheacidsolu-5 tures,and/orporousbeadsareusedinanionexchange tionisgreaterthanabout0.1M,greaterthanabout0.5M, greaterthanabout2M,greaterthanabout5M,orcombi nationsthereof.Duringacidtreatment,theuncoatedion exchangeparticlesoftheporousbeadabsorbhydrogenions whilereleasinglithiumions.Theionexchangematerialis10resourcewhilereleasinghydrogen.Aftertheparticleshave convertedtoaprotonatedstate.Aftertreatmentinacid,the protonateduncoatedionexchangeparticlesaretreatedwith aliquidresourcewhereintheliquidresourceisanatural brine,adisolvedsaltflat,aconcentratedbrine,aprocesed15absorbinghydrogenions. brine,asyntheticbrine,anoilfieldbrine,liquidfromanion Thecolumnisoptionalyoperatedinco-flowmodewith exchangeproces,liquidfromasolventextractionproces, theliquidresourceandacidsolutionalternatelyflowing leachate from minerals,leachate from clays,leachate from recycledproducts,leachatefromrecycledmaterials,or optionalyoperatedincounter-flowmodewithaliquid combinationsthereof.Theuncoatedionexchangeparticles20resourceandacidsolutionalternatelyflowingthroughthe absorblithiumionswhilereleasinghydrogenions.After columninopositedirections.Betweenflowsoftheliquid acidtreatment,thelithiumsaltsolutioniscolectedand resourceandtheacidsolution,thecolumnisoptionaly procesedintolithiumcarbonate,lithiumhydroxide,or treatedorwashedwithwaterorothersolutionsforpurposes lithiumphosphate. suchasadjustingpHinthecolumnorremovingpotential In some embodiments,there isa combination of coated 25 contaminants. Before or after the liquid resource flows ionexchangeparticlesanduncoatedionexchangeparticles throughthecolumn,thepHoftheliquidisoptionaly intheporousbead.Thecombinationofcoatedionexchange adjustedwithNaOHorotherchemicalstofacilitatetheion particlesanduncoatedionexchangeparticlesintheporous exchangereactionaswelashandlingordisposalofthe beadistreatedwithanacidsolutionpreparedwithhydro spentliquidresource.Beforeoraftertheliquidresource chloricacid,sulfuricacid,nitricacid,orcombinations30flowsthroughthecolumn,theliquidresourceisoptionaly thereofwhereintheconcentrationoftheacidsolutionis subjectedtootherprocesesincludingotherionexchange greaterthanabout0.1M,greaterthanabout0.5M,greater proceses,solventextraction,evaporation,chemicaltreat thanabout2M,greaterthanabout5M,orcombinations ment,orprecipitationtoremovelithiumions,toremove thereof.Duringacidtreatment,thecombinationofcoated otherchemicalspecies,ortootherwisetreatthebrine.When ionexchangeparticlesanduncoatedionexchangeparticles35theionexchangeparticlesaretreatedwithacid,alithiumion intheporousbeadabsorbhydrogenionswhilereleasing solutionisproduced.Thislithiumionsolutionisfurther lithiumions.Theionexchangematerialisconvertedtoa procesedtoproducelithiumchemicals.Insomeembodi protonatedstate.Aftertreatmentinacid,thecombinationof ments,theselithiumchemicalsaresupliedforanindustrial protonatedcoatedionexchangeparticlesandprotonated aplication. uncoatedionexchangeparticlesintheporousbeadare40 Insomeembodiments,lithiumionsareextractedfroma treatedwithaliquidresourcewhereintheliquidresourceis liquidresource.Theliquidresourceisanaturalbrine,a anaturalbrine,adisolvedsaltflat,aconcentratedbrine,a disolvedsaltflat,aconcentratedbrine,aprocesedbrine,a procesedbrine,asyntheticbrine,anoilfieldbrine,liquid syntheticbrine,anoilfieldbrine,liquidfromanion fromanionexchangeproces,liquidfromasolventextrac exchangeproces,liquidfromasolventextractionproces, tionproces,leachatefromminerals,leachatefrom clays,45leachatefromminerals,leachatefromclays,leachatefrom leachatefromrecycledproducts,leachatefromrecycled recycledproducts,leachatefromrecycledmaterials,or materials,orcombinationsthereof.Thecombinationof combinationsthereof. protonatedcoatedionexchangeparticlesandprotonated LithiumIonSaltSolutions uncoated ion exchange particles in the porous bead absorb In an aspect described herein are lithium salt solutions lithiumionswhilereleasinghydrogenions.Afteracidtreat-50withanimpurityconcentrationofabout1pbtoabout10 ment,thelithiumsaltsolutioniscolectedandprocesedinto ppmwhereintheimpurityconcentrationdenotesthepres lithiumcarbonate,lithiumhydroxide,orlithiumphosphate. enceofcoatedionexchangeparticlesduringtheproduction MethodsUsingCoatedIonExchangeParticles,Porous ofthelithiumsaltsolution.Insomeembodiments,the Structure,and/orPorousBeadsinaColumn impurityispresentinaconcentrationofmorethan1pb, Inanaspectdescribedhereinaremethodsofextracting5morethan5pb,morethan10pb,morethan10pb, lithiumfromaliquidresource,whereinthemethodsusing morethan1ppm,morethan2pm,morethan3ppm,more coatedionexchangeparticles,porousstructures,and/or than4pm,morethan5pm,morethan6pm,morethan porousbeadsisconductedinacolumn.Thecoatedion 7ppm,morethan8ppm,morethan9ppm,lesthan10ppm, exchangeparticlesareashereinbeforedescribed.The lesthan9pm,lesthan8ppm,lesthan7pm,lesthan porousstructuresareashereinbeforedescribed.Theporous60 6pm,lesthan5pm,lesthan4ppm,lesthan3ppm, beads are as hereinbefore described. Thecoatedionexchangeparticles,porousstructures, 10ppb,lesthan5pb,fromabout1pbtoabout10pm, and/orporousbeadsareloadedintoanionexchangecol fromabout5ppbtoabout10ppm,fromabout10ppbto umn.Oneexampleofanionexchangecolumnisshownin about10pm,fromabout50pbtoabout10pm,from 1 FIG.3.Theionexchangecolumndirectsliquidstopercolate65about10pbtoabout10pm,fromabout1pmtoabout aroundthecoatedionexchangeparticles,porousstructures, 10ppm,fromabout2ppmtoabout10ppm,fromabout4 and/orporousbeads,therebyfacilitatingionexchange pmtoabout10pm,fromabout6pmtoaboutpm,or column,theliquidresourcecontaininglithium ionsis pumpedthroughtheionexchangecolumnsothatthecoated ionexchangeparticles,theuncoatedionexchangeparticles, and/orcombinationsthereofabsorblithium from theliquid absorbedlithium,anacidsolutionispumpedthroughthe column so that the coated ion exchange particles, the uncoated ion exchange particles, and/or combinations thereofreleaselithium ionsintotheacidsolutionwhile throughthecolumninthesamedirectionorthecolumnis lesthan2ppm,lesthan1ppm,lesthan10ppb,lesthanPDF Image | Patent Lithium Extraction with coated ion exchange particles
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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 | RSS | AMP |