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US 8,753,594B1 9 10 LiClpresent,suchasatleast100ppmoflithium,suficientto ensurethatatleastaportionofthecapturesitesontheLAI matrixarefiledwithionstopreventtheLAImatrixfrom colapsing.Theprocesscanberepeatedmanytimes,as desired solution,andbrinesolutionthathashadlithiumionsremoved therefromisrecoveredincollectionvessel114vialine128. Simultaneously,secondcolumn112,whichcanbesatu ratedwithlithiumions,canbeunloaded.Washsolutionfrom vesel102canbesuppliedvialine130tosolenoidvalve105, andthensuppliedtoDPP106vialine134.Washsolutionis thensuppliedvialine136tosecondcolumn112,whereit contacts the LAI matrix and removes lithium ions Saturated thereon.Awashsolutionthatisrichinlithium,ascompared withthewashsolutioncontainedinvessel102,isrecoveredin productcolectionfractionator116,vialine142. TheloadingandunloadingoftheLAImatrixcanbemoni toredbymeasuringthelithiumconcentrationoftheoutletof thecolumn.Meansformonitoringtheconcentrationofthe lithiumcanincludeionselectiveelectrodes,ionchromatog raphy,orspectrometricanalysis,suchasatomicabsorptionor10 inductivelycoupledplasmaspectroscopy,andothermeans knownintheart.Theloadingprocessistypicalyfairlyefi AscanbeseeninFIG.1,theoperationsoffirstandsecond cient,suchthatatleast50%ofthelithiumionsinthebrineor solutionarecapturedbytheLAImatrix,preferablyatleast15 90%ofthelithiumionsinthebrineorsolutionarecaptured bytheLAImatrix.Assuch,arapidincreaseinthelithiumion concentrationattheoutletoftheLAI matrixisindicativeof saturationofthecolumn.Similarly,whenrecoveringthe lithiumionsfromtheLAImatrix,astheprocessisproceeding andionsarebeingremoved,aSuddendecreaseintheconcen trationthereofcanbeindicativeoftheremovalofamajority oftheionscapturedbythematrix. Incertainembodiments,theLAImatrixpreparedaccord ingtothepresentmethodshasanextractioncapacitySuitable25 foruseinbrineshavingalithiumconcentrationsimilartothat oftheHudsonRanchgeothermalbrines,i.e.,alithiumcon centrationofabout260ppm,ofatleastabout1mgoflithium pergramoftheLAImatrix,preferablyatleastabout1.5mg oflithiumpergramoftheLAImatrix,evenmorepreferably30 atleastabout2mgoflithiumpergramoftheLAImatrix.The extractioncapacitieswouldbelargerforbrinescontaining higherconcentrationsoflithium. columns110and112canbereversedandthefirstcolumncan thenbesuppliedwithwashwaterforrecoveryoflithiumions andthesecondcolumncanthenbesuppliedwithabrine solutionfortheremovaloflithiumtherefrom. ReferringnowtoFIG.2,theperformanceofacolumn,as shownbythelithiumconcentrationoftheliquidexitingthe columnduringtheloadingandunloadingthereof,ispro vided.Thecolumnisloadedwithapproximately9.4ccofa granularLAImatrixhavinganaverageparticlediameterof betweenabout0.18and0.3mmconsistingofapproximately 95%byweightlithiumaluminateintercalateand5%by weightpolyvinylidinefluoridetosimulatetheloadingand unloadingofthecolumn.A waterSolutionthatincludes betweenapproximately100and1,000mg/Loflithiumis usedasthestripingSolutionfortheLAImatrixbed. Duringtheloadingstep,approximately4bedVolumes (i.e.,approximately40mL,fourtimesthevolumeofthe column)ofasimulatedbrinehavingalithiumconcentration ofbetweenabout284mg/Landabout332mg/LwereSup pliedtothecolumn.Theoutputstreamfromthecolumn ReferringnowtoFIG.1,anexemplarylaboratoryappara tusforthecaptureandrecoveryoflithiumionsfromasolu35 tionorbrineisprovided.Apparatus100includesfirstvesel 102forholdingawash(strip)solutionandsecondvesel104 forthebrineorlithiumcontainingsolution.Solenoidvalves 103and105areconnectedtocomputer108andcontrolthe inputoffluid,i.e.,brineorwashsolution.Apparatus10040 furtherincludesdigitalperistalticpump106(DPP).Com puter108canbecoupledtovariousinstruments,suchasDPP 106,andsolenoidvalves103and105,andisalsoacompo mumLiClconcentrationofabout21,000. nentofapparatus100.Apparatus100furtherincludesfirst Theloadingandunloadingofthecolumnwasrepeated LAImatrixcolumn110andsecondLAImatrixcolumn112. 45 Washliquidsandexcessbrinearecolectedinbulkcolection vesel114,andlithiumionproducedcanberecoveredin sequentialaliquotsinproductcolectionfractionator116.As isunderstood,apparatus100mayalsoincludevariousheat exchangers,valves,andfilters,forthecontroloftheproces.50 Apparatus100includestwocolumns,110and112respec tively,whicharepreferablypackedwiththeLAImatrix, typicalyasparticulatemater,accordingtothepresentinven tion.Itisunderstoodthattheapparatuscanincludeasingle column,orcanincludemultiplecolumns.Glasswool,filters,55 orthelikecanbeusedatthetopandbottomofthecolumnto ensurethattheLAImatrix,orfinesthereof,arenotwashed outofthecolumn.Inoperation,columns110and112are operatedinparalel,althoughincertainembodimentsthe columnscanbealternatedSuchthatwhileonecolumnis60 beingloaded,thesecondcolumnisbeingunloaded. Forexample,duringtheloadingoffirstcolumn110,brine fromvesel104issuppliedvialine122tosolenoidvalve103. andcanthenbesuppliedvialine124toDPP106.Thebrine isthensuppliedfromDPP106vialine126tofirstcolumn65 110,wherethebrinecontactstheLAImatrix,whichisoper able to remove lithium ions from said brine. Excess brine morethan500times,withunexpectedlyrepeatableresultsfor thecaptureofbetweenabout83%and96%oftheLiCl presentinthebrinesolution.ReferringnowtoFIG.2,the loadingandunloadingofthecolumnisshown.(FIG.2shows cycles130and131ofatotalof550consecutivecyclesof loadingandunloadingthecolumn).Thefigureshowstwoful loading-unloadingcycles,withlithiumconcentrationofthe liquidexitingthecolumninmg/LplotedontheY-axisand bedvolumesofliquidsuppliedtothecolumnontheX-axis. Point10ofFIG.2indicatesthemidpointofanunloading cycleforthecolumn.Frompoint10topoint12ofFIG.2,the brine(loadingSolution)isSuppliedtothecolumnandis replacingthestripsolution(unloadingSolution).Between points12and14ofFIG.2,thebrinecontaininglithiumis exitingthecolumn.Betweenpoints12and14theconcentra tionoflithiumintheliquidexitingthecolumnisrelatively low,typicalymuchlesthantheconcentrationoftheStrip solution.Afterpoint14ofFIG.2,theconcentrationoflithium exitingthecolumnincreases.Atapproximately1BVpriorto point14ofFIG.2,thesolutionbeingfedtothecolumnis switchedfromthelithiumcontainingbrinesolutiontostrip pingsolution(havingalithiumconcentrationofabout1000 mg/L)andatotalof1to1.5BVispassedthroughthecolumn. duringloadingunexpectedlyhadalithiumconcentrationof betweenabout10and50mg/L,correspondingtothecapture ofbetweenabout83%and96%ofthelithiumpresentinthe feedsolution. UnloadingofthecolumnisachievedbySupplyingapproxi mately2bedvolumes(i.e.,approximately20mL)ofalithium stripsolution(i.e.,asolutionhavingaLiClconcentrationof approximately6,000mg/L).TheoutputstreamhadamaxiPDF Image | Patent SORBENT FOR LITHIUM EXTRACTION
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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 |