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US 2020/0399137A1 Dec.24,2020 13 tionsthereof.Incertainembodimentsthesolutionmaybe [0125]Theliquidextractionprocescanbeperformed coledpriortoseparationofthesolidfromthesolution. overawidevarietyoftemperatures,preferablybetwen [0121] Inanotherembodiment,analternateprocesforthe optionalpurificationoflithiumchloride-richstream24can beprovidedtoremovecalcium,manganese,magnesium,or [0126]Theratiooftheorganicextractionsolution(which otherdivalentionssuchaszincthatmaybepresentin includestheextractioncompoundandcariersolvent)tothe and80°C.;alternativelybetweenabout70°C.and90°C. lithiumchloride-richstream24.Theprocescanincludethe lithium-richstreamcanbebetweenabout1:4and4:1, liquid-liquidofthelithiumchloride-richstreamwithan organicstreamthatincludesanextractioncompoundthatis selectivefordivalentions.Exemplaryextractioncompounds includematerialsproducedbyCytec,suchasCyanex®272 [0127]Incertainembodiments,theprocesfortheextrac (CytecIndustries,Inc.,havingbis(2,4,4-trimethylpentyl) tionofoneormoredivalention,suchascalcium,magne sium,manganese,and/orzinccanincludemorethanone andphosphoricacids,suchasdi(2-ethylhexyl)phosphoric columnfortheextractionthereof.Forexample,incertain acid,andothercompoundsknownforhavinganafinityto embodiments,twocolumnscanbeemployedinseriesto phosphinicacidasthemainactiveingredient),phosphinic binddivalentions. [012] Exemplarycariersolventsfortheextractionof divalentionscanincludethosethataredescribedforthe IsoparM (anisoparafinichydrocarbon),LINPAR1416(a mixtureoftetradecane,pentadecaneandhexadecane),LPA Solventsandn-Parafins(fromSasol),compoundsdisclosed aboveasliquidcariersfortheconcentrationofthelithium containingstream,andlikecompounds. [0123] Theprocesfortheextractionofcertaindivalent ions,suchasmanganese,magnesium,zinc,andcalcium, procedsasfolows.A lithiumchloride-richsolutionis provided,forexamplefromthelithiumextractioncolumn, andtreatedwithanorganicsolventextractionproduct. Optionaly,thepH ofthelithiumchloride-richstream adjustedpriortocontactinglithiumchloride-richstream withtheorganicsolventextractionproduct.Aftercontacting thelithiumchloride-richstreamwiththeorganicsolvent extractionproduct,thetwophasesarealowedtoseparate, providinganaqueousphaseandanorganicphase.The aqueousphase,consistingofadivalent-leanlithiumchlo ride-richstream,isremovedforfurtherprocesingand/or optionalpurification.Theorganicphase,consistingofthe organiccariersolvent,theextractioncompoundandcap tureddivalentionscanbetreatedwithaconcentratedstrong acid,forexampleHClorH2SO4,suchasa20-36% HCI solution,toreleasethecaptureddivalentions.Optionaly, thedivalentmetalstreamwhichincludesreleaseddivalent ionspresentas,forexample,metalchlorides,canbefurther purified.Incertainembodiments,ionexchange,orother usinga3literjacketedreactorwithaheatingsystem means,canbeusedtoremoveboronfromthedivalentmetal (manufacturedbySyrisReactorSystems,UK).Thereac stream.Boththedivalentmetalstreamandthedivalent-lean tionwascariedoutatatemperatureofabout95°C.using lithiumchloride-richstreamcanbeconcentratedasdesired, aoneliterofa9.5Msolutionofsodiumhydroxide(27.5% bymeansdescribedherein.Forexample,thedivalent-lean solids).Carbondioxidewassupliedforabout1houratthe lithiumchloride-richstreamcanbeconcentratedbyevapo rateof3L/min.(totalingaproximately8moles,aproxi mately1.7molarequivalents)toensurethecompletecon [0124]TheliquidextractionprocesishighlypHdepen versionofsodiumhydroxide.Attheendofthecarbonation dent,andthepHismaintainedsuchthatdivalentionsare ofthesodiumhydroxidesolution,aclearsolutionofsodium rationorsolventextraction. removed from solution while lithium ions remain.For example,inembodimentsusingCyanex®272,itisdesirable reactionwasstopedandheatingofthesodiumcarbonate solution was continued for few minutes.To the clear solu about5,alternativelylesthanabout4.8,alternativelyles tion,lithiumcarbonatesedswereadedbeforereactingit tokepthepHatlesthanabout5.25,alternativelylesthan withalithiumchloridesolution(404glithiumchloridein ofabout4.5,atleastabout70%ofcalciumisremovedfrom 1000mL).Experimentalyieldwas95%.Yieldsvariedfor solution,atleastabout80ofmagnesiumisremovedfrom othersimilarreactionsdependinguponexperimentalcon solution,andatleastabout9%ofmanganeseisremoved, ditionsandwereashighasabout10%insomecases.The whilelesthan2%oflithiumisremoved.Thus,atthelower purityoftheisolatedlithiumcarbonatewasaproximately pH,theCyanex®272showsverygodselectivityforthe 96.6%beforewashing. extractionofcalcium,magnesiumandmanganeseover [013]Beforethefirstwashingoftheproductstream,the lithium. lithiumcarbonatehadthefolowingimpurities:Na (71 thanabout4.6,andalternativelylesthanabout4.5.AtapH about50°C.and100°C.,alternativelybetweenabout60°C. alternatively between about 1:4 and 1:1,alternatively betweenabout1:2and2:1;alternativelybetweenabout1:1 and4:1. increasetheamountofdivalentionsthatareremoved. [0128] Afterremovaloftheoneormoredivalentions,the ionscanberecoveredandseparated,byknownmeans,and supliedtoanalternateproces. [0129] Incertainembodiments,theprocesmayinclude meansfortheneutralizationofanylithiumcarbonatethatis includedinthesodiumchloridesolution,suchasbyneu tralizingthesolutionbyadinganefectiveamountof hydrochloricacidorlikeacid.Inembodimentswhereinthe lithiumcarbonatecanbeefectivelyremoved,thesolution canberecycledtotheelectrochemicalcel,however,any lithiumcarbonateincludedthereinmaycauseproblemswith theperformanceoftheelectrochemicalcel. [0130] Itisunderstodthatcertainprocesesandproce duresdescribedhereincanbeperformedinwholeorinpart. Forexample,itisunderstodthattheprocesforthe concentrationofthelithiumchloridecontainingstreamby solventextractioncanbepracticedwithalornoneofthe otherprocesstepsthataredescribedherein. [0131] Asusedherein,thetermssilicaandsilicatesmay beusedinterchangeablyasitisunderstodthatbothterms areusedtodescribesiliconbasedprecipitatesthatare generatedfromgeothermalbrinesolutions. EXAMPLES Example1.CarbonationofSodiumHydroxide [0132] Carbonationofsodiumhydroxidewascariedout carbonatewasobtained,atwhichpointthecarbonationPDF Image | Patent LITHIUM CHLORIDE CONTAINING BRINE
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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)