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17 18 US 11,365,128B2 Thecarbondioxideformed(stream145)iscoledby rafinatecontainingMn618issentforrecoveryofaman chiler582(stream157)andmixedwithsurpluscarbon ganesesulfateproductliquor62. dioxide(stream140)fromthere-disolutionstep518and Fromthezincextractionstage608,thezincloaded make-upcarbondioxide528(stream158)inaknock-out solvent624isfedintoasecondstagecontactorwhereitis vesel586fromwhichthecondensedwater(stream159)is 5 scrubedwithasuitableaqueoussolution626toremove removedandthecarbondioxide(stream160)iscompressed smalamountsofimpuritiesremaining.Aftersetlinginthe 584andreturned(stream139)tothelithiumre-disolution zincscrubingstage610,thescrubrafinatewilberecycled step518.Thesluryofpurifiedlithiumcarbonate(stream toanapropriatestream628.Theloadedsolvent630isthen 146)ispumped(stream147)tothesecondcentrifuge576in pumpedtothezincstripingstage612andfedintoathird whichitisseparatedandwashedwithproceswater(stream10stagecontactorinwhichtheZnisstripedfromtheorganic 148).Thewashcentrate(stream152)isreturnedtothe phasebyasulfuricacidsolution.Theaqueousconcentrated re-disolutionstep518.Theprimarycentrate(stream150)is stripZnSO4productliquor632thengoesforfurtherpro pumped(stream151)backtotheCa/Mgprecipitationsec cesingdependingonthedesiredproductform.Thestriped solvent616isrecycledbacktothezincextractionstage608. TheSXcircuit600includesamanganeseextractionstage 634,amanganesescrubingstage636,andamanganese stripingstage638.SimilartothezincSX circuit,the Thecondensatefromthecarbondioxideknock-outvesel 586(stream159)andcondensatefromthecarbondioxide Cytex272)arefedinacounter-curentmannerintoafirst compresor584(stream161)arecombinedandsent(stream20stagecontactorinwhichthetwophasesaremixedandMn 195)totheproceswaterreservoir538.Thepermeatefrom istransferedfromtheaqueousphaseintotheorganicphase. thereverseosmosis506(stream100)andthecondensates Themanganeseloadedsolvent640isfedintoasecondstage fromtheevaporationsequence508(streams104,108,14) contactorwhereitisscrubedwithasuitableaqueous alsogototheproceswaterreservoir538.Make-upwater solution642toremovesmalamountsofimpuritiesremain (stream164)isadedtotheproceswaterreservoir5382,if25ing.Aftersetlinginthemanganesescrubingstage636,the necesary,tobalancethefolowingrequirementsforproces scrubrafinatewilberecycledtoanapropriatestream64. water: Theloadedsolvent646isthenpumpedtothemanganese washtotheZn/Mnprecipitatefilter332(stream40); stripingstage638andfedintoathirdstagecontactorin eluatetotheCCADcircuit400(stream149); whichtheMn isstripedfromtheorganicphasebya centrifuge54/576washwater(streams128/132);and 30sulfuricacidsolution.Theaqueousconcentratedstrip reagentmake-upwater(streams178/181/183/187/190). MnSO4productliquor62thengoesforfurtherprocesing SelectiveRecoveryofZincandManganese: dependingonthedesiredproductform.Thestripedsolvent FIG.6showsanilustrativeexampleofmineralrecovery 648isrecycledback themanganeseextractionstage634. aspartofthesystemandproces200disclosedherein.After Itistobeunderstodthattheterms“including”,“com theimpurityremovalcircuit30,therecoveryofmetals35prising”,“consisting”andgramaticalvariantsthereofdo fromthesecondfiltercake316isposiblethroughasolvent notprecludetheaditionofoneormorecomponents, extraction(SX)circuit60.TheSXcircuitleachesmanga- features,steps,orintegersorgroupsthereofandthatthe neseandzincfromthefiltercakewithanaplicationofan termsaretobeconstruedasspecifyingcomponents,fea acidandthenselectivelystripsthemanganeseandzinc tures,stepsorintegers. usingasolventunderdiferentpHconditions.Theresulting40 Ifthespecificationorclaimsreferto“anaditional” intermediateproductsarezincsulfateliquorandmanganese element,thatdoesnotprecludetherebeingmorethanoneof sulfateliquor,bothofwhichcanbesoldasagricultural theaditionalelement. products,procesedfurtherbyelectrowiningintometalic Itistobeunderstodthatwheretheclaimsorspecifica form,orasfedstocktoalternativeproductssuchaselec- tionreferto“a”or“an”element,suchreferenceisnotbe trolyticmanganesedioxideamongothers. 45construedthatthereisonlyoneofthatelement. TheSXcircuit60beginswithleaching604thesecond Itistobeunderstodthatwherethespecificationstates filtercake316inastired,repulpreactor602withsulfuric thatacomponent,feature,structure,orcharacteristic“may”, acid(H2SO4)orhydrochloricacid(HCI)toreducethepH "might”,“can”or“could”beincluded,thatparticularcom downtoabout2.5(606).AreducingagentsuchasNaHSor ponent,feature,structure,orcharacteristicisnotrequiredto SO,isaddedtothereactor602toensurealofthemanga- 50beincluded. neseisinthe+2-valencestateforleaching.Thisimproves Whereaplicable,althoughstatediagrams,flowdiagrams thekineticsandyieldoftheacidleach.Thedischargefrom orbothmaybeusedtodescribeembodiments,theinvention theleachreactor602wilhaveitspHraisedtoaproxi- isnotlimitedtothosediagramsortothecoresponding mately5-6withlimetoprecipitateanyresidualiron.The descriptions.Forexample,flownednotmovethrougheach slurywilthenbepumpedtoapolishingfilter(notshown)5ilustratedboxorstate,orinexactlythesameorderas followedbyapHadjustmenttoapproximately2toaproxi- ilustratedanddescribed. mately3.ThisbecomestheZn/Mn aqueousfedsolution Systemsandprocesesoftheinstantdisclosuremaybe tion(stream155)andtothelithiumre-disolutionstep15 (stream136).Thewashedsolids(stream154)leavethe circuitasthelithiumcarbonateproduct. 614totheSX circuit600. implementedbyperformingorcompletingmanualy,auto a TheSXcircuit60includesazincextractionstage608, maticaly,oracombinationthereof,selectedstepsortasks. a azincscrubingstage610,andazincstripingstage612.60 Theterm“proces”mayrefertomaners,means,tech TheZn/Mnaqueousfedsolution614andanorganic niquesandproceduresforacomplishingagiventask solvent616(e.g.,Cytex272)arefedinacounter-curent including,butnotlimitedto,thosemaners,means,tech mannerintoafirststagecontactorinwhichthetwophases niquesandprocedureseitherknownto,orreadilydeveloped aremixedandZnistransferedfromtheaqueousphaseinto fromknownmanners,means,techniquesandproceduresby theorganicphase.Aftersetling,theaqueousrafinateis65practitionersofthearttowhichtheinventionbelongs. separated618andpHadjustedtobetweenaproximately Forpurposesoftheinstantdisclosure,theterm“atleast” 4.5andaproximately5.5.AfterpHadjustment620,the folowedbyanumberisusedhereintodenotethestartofa rafinatecontainingMn618andanorganicsolvent648(e.g.,PDF 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)