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15 16 US 11,365,128B2 156)fromasecondprecipitationoflithiumcarbonate524 withwashcentrate(stream131)fromafirstlithiumcarbon andthespentregenerantfromtheboronIXcircuit528 atecentrifuge54.Thecombinedsolutionissplit,part (stream192)arealsotreatedintheCa/Mgprecipitation (stream162)beingusedtodisolvesodiumcarbonateand sectionofthelithiumchlorideconversioncircuit50.The thebalance(stream98)beingpumped(stream99)through alkaliearthions(mainlyCa2+andMg2+)areprecipitated5areverseosmosisstageinwhichthewaterremovalis acordingtothefolowingstoichiometry: Mg2+2NaOH2Na+Mg(OH)2 Ba2++2NaOH2Na+Ba(OH)2 Sr2+2NaOH >2Na+Sr(OH)2 Ca2+Na2CO3->2Na+Ca(CO)3 manipulatedtogive95percentsaturationoflithiumcar bonateintheconcentrate(stream101).Thepermeategoes totheproceswaterreservoir(stream10). Thepartialyconcentratedsolutionfromreverseosmosis 10506isfurtherconcentratedinatriple-efectevaporation508. The solution ex reverse osmosis (stream 101) is partly evaporatedbyheatexchanger56withincomingsteam (stream103).Thesteamcondensate(stream104)goestothe proceswaterreservoir538,andthesteam/liquidmixtureto Anyvaporevolvedisvented(stream61).Theexitslury15theheatexchanger56(stream105)isseparatedina (stream62)ispumped(stream63)toathickenerorclarifier knock-outvesel58.Theliquidphase(stream109)pases 540,floculentisaded(stream64/65)andtheprecipitateis throughapresurereduction560(stream10)andisfurther setledout.Theoverflow(stream68)ispumped(stream69) evaporatedinaheatexchanger562withsteam(stream106) throughapolishingfilter542.Theunderflow(stream6)is fromthefirstknock-outvesel58.Thecondensate(stream pumped(stream67)toamixingtank54whereitjoinsthe20107)ispumped(stream108)totheproceswaterreservoir solids(stream70)fromthepolishingfilter542andthe 538.Thesteam-liquid(stream1)mixtureisseparatedina combinedslury(stream72)ispumped(stream73)backto secondknock-outvesel564.Theliquid(stream15)goes thefeedtank326aheadoftheFe/Sifilter32.Thefiltrate throughanotherpresurereductionstep566(stream116) (stream71)fromthepolishingfilter542ispumped(stream andisevaporatedfurtheranotherheatexchanger568with 74)toafedtank546aheadoftheboronIXcircuit528. 25 steam(stream12)fromthesecondknock-outvesel564. Thefiltrate(stream75)fromtheCa/Mgprecipitation Thecondensate(stream13)ispumped(stream14)tothe sectionofthelithiumchlorideconversioncircuit500is proceswaterreservoir538.Thesteam-liquidmixture pumped(stream76)throughtheboronIXcircuit528in (stream17)isseparatedinathirdknock-outvesel570. whichboronisextractedontoanionexchangeresin.The Thesteam(stream18)iscondensed(stream19)byheat loadedresinisstripedwithdilutehydrochloricacid(stream30exchanger572withcolingwaterandpumped(stream120) 78)thatismadefromconcentratedhydrochloricacid totheproceswaterreservoir538. (stream185),proceswater(stream186)andrecycledeluate Theconcentratedsolution(stream121)ispumped(stream (stream80).Thefirst50%ofthespentacid(stream79), 122)tothelithiumcarbonatecrystalizationsection514. assumedtocontain80%oftheboronelutedfromtheloaded Sodiumcarbonate536(stream175)isdissolvedindilute resin,ismixedwithsimilarspentacidfromthesubsequent35lithiumsolution(stream163)fromthefedtank52ahead divalentIXcircuit530andrecycledtothefedtotheCCAD ofreverseosmosis506andadded(stream123/124)to circuit400(stream94).Thebalanceofthespentacid precipitatelithiumcarbonate.Anyvaporevolvedisvented (stream80)isrecycledtotheeluantmake-uptankand (stream125).Theresultingslury(stream126)ispumped recycled(stream77).Thestripedresinisregeneratedwith (stream127)toacentrifugeinwhichthesolutionis dilutesodiumhydroxide(stream82)thatismadefromfresh40removed,leavingahighsolidscake.Asmalamount(stream sodiumhydroxide(stream188),proceswater(stream189) 129)ofproceswaterisusedtowashthesolids.Thewash andrecycledregenerant(stream84).Thefirst50%ofthe centrate(stream130)isreturnedtothefedtankaheadof spentregenerant(stream83)isrecycledtotheCa/Mg reverseosmosis506.Theprimarycentrate(stream13)is precipitationsectionandthebalance(stream84)returnsto recycledtoafedtank36aheadofthepolishingfilter34 aregenerantmake-uptank548andisrecycled(stream81).45beforetheCCADcircuit40. Theboron-freproductsolution(stream85)ispumped Thewashedsolids(stream135)fromthefirstcentrifuge (stream86)throughdivalentIXcircuit530inwhich9 554aremixedwithwash(stream136)andprimarycentrate percentofanyremainingdivalentions(esentialyonly (stream153)fromasecondcentrifuge576.Theresulting 2+ Ca2+andMg2+)arecapturedbytheresin.Theloadedresin slury(stream137)ispumpedto15barabs.(stream138) isstripedwithdilutehydrochloricacid(stream8)thatis50andcontactedwithpresurizedcarbondioxide526(stream madefromfreshhydrochloricacid(stream182),proces 139)tocompletelydisolvethelithiumcarbonateacording water(stream184)andrecycledspentacid(stream93).The tothefolowingstoichiometry: first50% ofthespentacid(stream91)joinsthefirsthalfof Li2CO3+CO2+H20 ?2Lit+2HCO3 the spent acid from the boron IX circuit 528 and the Theamountofprimarycentrateismanipulatedtogive95 combinedsolution(stream94)issentbacktothefedtank 5 percent saturation of lithium carbonate in the solution 340aheadoftheCCADcircuit40.Thebalanceofthespent (stream141)leavingtheredisolutionstep518.Anyother acid(stream93)goesbacktoaneluantmake-uptank50 species(Ca,Mg)remainasundisolvedcarbonates.The andisrecycled(stream87).Thestripedresinisconverted backtothesodiumformbyregenerationwithdilutesodium temperatureofthisstepisheldat80°F.byheatexchange hydroxide(stream89).Thefirst50%ofthespentregenerant60withchiledwater578(stream194in,stream193out).The resultingsolutionoflithiumbicarbonate(stream141)is joinsthespentregenerant(stream83)fromtheboronion filtered580andthesolidimpuritiesleavethecircuit500 exchangestageandgoesback(stream191)totheCa/Mg (stream142).Thefiltrate(stream143)isheatedbylive precipitationsection.Thebalanceofthespentregenerant steam(stream14)injection,todecomposethedisolved (stream90)returnstotheregenerantmake-uptank548. 65 lithiumbicarbonatetosolidlithiumcarbonateandgaseous (stream92),asumedtohaveregenerated80%oftheresin, Thepurifiedsolution(stream96)ispumped(stream97) toafeedtank552aheadofreverseosmosis506andmixed carbondioxide: 2Li*+2HCO3 ?Li2CO3+C021+H20PDF 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 (Standard Web Page)