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11 fromthelastofthethre(3)pairsofparalelcolumnsata flow rate of 53 mL /min and the remainder of the flow enteredzoneAtodisplacebrinetothebrinefedportatthe flowrateof80mL/min(asstatedabove). 12 TABLE 2 CCADProductVolume= 9.3%ofFeedBrine Product 6.3% 99.91% 99.83% 99.98% 99.98% whilethelithiumproductstreamhadanaveragelithium Element Ca 43,130 50,893 407 0.09% US 11,365,128B2 TheCCADcircuit40,afterachievingsteadystateopera5 tion,providedexcelentresultsforlithiumrecovery.The fedbrinehadanaveragelithiumconcentrationof216mg/L Li 240 283 3,250 93.70% 19 concentrationof2,50mg/L,andassuch,inthisexample, Mg 86.4 102 1.64 0.17% 10 Na 64,760 76,417 117 0.02% greaterthan93%ofthelithiumfromthefedbrinewas K 19,180 22,632 39 0.02% recovered. Inadition,theinventiveprocesprovidesexcelent Inadition,similartothefirstexampleandasilustrated resultsforthepreparationofalithiumchlorideproduct inFIG.7,theinventiveCCADcircuit40providesexcel havinglowcalciumandmagnesiumconcentrations,which15 lentresultsforthepreparationofalithiumchlorideproduct isparticularlysuitedasafedstockforasolventextraction havinglowcalciumandmagnesiumconcentrations,which andelectrowining(SX/EW)proces,asolventextraction isparticularlysuitedasafedstockforaSX/EWproces,a andmembraneelectrolysis(SX/EL)proces,orotherrecov SX/ELproces,orotherrecoverytechnologyprocesfor erytechnologyprocesforproductionofhighpuritylithium productionofhighpuritylithiumhydroxideandlithium hydroxideandlithiumcarbonateforbateryproduction.The20 carbonateforbateryproduction.Thefedbrinecontained fedbrinecontained27,80mg/Lofcalciumyetthelithium 29,70mg/kgofcalciumyetthelithiumproductstream productstreamcontainedonly30mg/Lofcalcium,repre containedonly403mg/kgofcalcium,representinga sentinga9.98%rejectionofcalciumfromthefedbrineto 9.98%rejectionofcalciumfromthefedbrinetothe thelithiumproductstream. calciumrejectiongivingindicationthattheinventivepro cescouldbewelsuitedtosalar,continental,petro-,or AnotherexemplaryCCADcircuit40wasconfiguredin25lithiumproductstream.Magnesiumrejectionwassimilarto generalacordancewithFIG.5usingthirty(30)individual adsorptioncolumnsarangedinarotatingcarouselpilot skidwithacentralrotaryvalvedesignwitheachcolumn othernon-geothermalfedstockbrines. havinga2.0inchinerdiameterand48inchesinlength, TheCCADcircuit40havingonlyonemulti-portvalve eachpackedwith2.8Lofmacroporousresinimbibedwith30isfarsimplertooperatethanclasicalcontinuousfixedbed lithiumaluminaintercalate.Almetalanalysiswasper- systemshaving50-60valves.Inaditiontothehighlithium formedusingICPanalysis.Theadsorbentbedadvancerate yields,theCCADcircuit40alsousesabsorbent,water,and was se to6.0minutesperforwardstepoftherotating reagentsmoreeficientlythanfixedbedsystems.Inthe carousel.Theturetofcolumnswasmaintainedinan aboveexamples,theCCADcircuit400requiresonlyabout enclosureatabout40°C.Alfedsolutionswereintroduced35halfthevolumeabsorbentasacomparableclasicalfixed tothesystemat7°C.ThebrinedisplacementzoneA bedsystem. comprisedfour(4)columnsinseriesandtheflowratewas TurnbacknowtoFIG.2,afterleavingtheCCADcircuit setat340mL/min.TheadsorptionzoneBcomprisedsix(6) 40,theenhancedlithiumchlorideproductstream342 setsofthre(3)paralelcolumnsarangedinseries.Thefed (stream57inFIG.4A)(stream417orstream420inFIG.5) brinecomprisedtreatedSaltonSeageothermalbrineatpH40ispasedtothelithiumchlorideconversioncircuit50 5.6wherethesilica,iron,manganese,andzinchadbeen wherethelithiumconcentrationisfurtherincreasedtoin removedinapretreatmentprotocolandthebrineflowrate excesofabout3,0ppm.Thelithiumchlorideconversion wassetat3,050mL/min,specificgravity1.18.NexttheER circuit50removesselectedremainingimpuritiesandfur zoneCcomprisedtwo(2)columnsinseriesandthelithium therconcentrateslithiuminthelithiumchlorideproduct depletedbrinerafinateenteredtheERzoneCataflowrate45stream342beforecrystalizationorelectrolysis. of250mL/min.TheelutionzoneDcomprisedthre(3)pairs The lithiumchlorideconversioncircuit500 initialy ofparalelcolumnsarangedinseriesandwasfedby580 removesanyremainingimpurities502,namelycalcium, mL/minoflowconcentrationlithium(10mg/kg)inwater magnesiumandboron,fromthelithiumchlorideproduct aseluate.Theproductlithiumwastakenfromthelastofthe stream342.First,sodiumhydroxide(causticsoda)isaded thre(3)pairsofparalelcolumnsataflowrateof24050inordertoprecipitatecalciumandmagnesiumoxidesfrom mL/minandtheremainderoftheflowenteredthezoneAto thelithiumchlorideproductstream342.Theprecipitated displacebrinetothebrinefedportattheflowrateof340 solidscanproduceaCa/Mgfiltercake504.Boronisthen mL/min. removedbypasingthelithiumchlorideproductstream342 Inthisexample,theCCADcircuit40,afterachieving throughaboronionexchange(IX)circuit528.TheboronIX steadystateoperation,providedexcelentresultsforlithium5circuitisfiledwithanadsorbentthatpreferentialyatracts recovery.Thefedbrinehadanaveragelithiumconcentra- boron,anddivalentions(esentialycalciumandmagne a tionof240mg/kgwhilethelithiumproductstreamhadan sium)arefurtherremovedinadivalentionexchange(IX) averagelithiumconcentrationof3,270mg/kg,andthe circuit530.This“polishing”step502ensuresthatthese averageconcentrationoflithiumintherafinatewas8 calcium,magnesiumandboroncontaminantsdonotendup mg/kg,assuch,inthisexample,lithiumrecoverywas 60inthelithiumcarbonateorlithiumhydroxidecrystals. greaterthan93% ofthelithiumfromthefedbrine.Table2 Then,thelithiumchlorideconversioncircuit500usesa belowshowsthesteadystateperformanceoftheinventive reverseosmosismembranestep506toinitialyconcentrate procesasexemplifiedinthisexample.TheCCADproduct lithiuminthelithiumproductstream342(targetestimate streamwas7.9%ofthevolumeofthetreatedSaltonSea fromapproximately3,000ppmto5,000ppm).Atripleefect Brinefedstream.Quantitiesofmetalsareexpresedin65evaporator508isthenusedtodriveofwatercontentand mg/kgandarecorectedfordiferencesinspecificgravityof furtherconcentratethelithiumproductstream.Thetriple fedbrinevsCCADproduct. efectevaporator508utilizessteam510fromgeothermal Feed Feed CCAD %Reporting%Rejection Brine Brine Product toCCAD fromCCAD (mg/kg) (mg/L) (mg/L) ProductPDF Image | RECOVERY OF LITHIUM FROM NATURAL AND SYNTHETIC BRINES
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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 |