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massratioofmagnesiumtolithiumwas9.1intheorganic extractedphase. 35 The extracted phases from four stages were merged and g.addingsodium carbonateintothewaterphasewith Mg2+removed from stepftoprecipitatelithium car bonate, and then filtering and drying the precipitated US10,246,341B2 sodiumcarbonatesolutionwasadedtoremovemajorityof andthelikemadewithinspiritsandprinciplesofthepresent Mg2+,thensodiumhydroxidewasagainadedintothe inventionshalbeincludedintheprotectionscopeofthe solutionafterseparation,tocompletelyprecipitatemagne presentinvention. sium.Solutionofsodium carbonatewasaddedintothe Whatisclaimedis: filteredsolutiontoformprecipitation,andseparationand5 1.Amethodforproducinglithiumcarbonatefromlow desicationwerecariedouttoobtainalithiumcarbonate lithiumbrinebyseparatingmagnesiumandenriching product. lithium,comprising: Embodiment7 a.heating,evaporatingandcondensingasalt-lakebrineto 10 separatehalidesalts; TheconcentrationofLi+,Mg2+andSO2+wererespec b.extractingtheseparatedhalidesaltswithtrialkylphos tively0.87g/L,104.37g/L,1.13g/L,withamagnesiumto phateoramixtureoftrialkylphosphateandmonohy lithiumratioequivalentto120.0inanoldbrineinasalt dricalcoholasanorganicphase; lakelocatedinQaidam BasinofQinghaiprovince.20mLof theoldbrineinembodiment1wastakenintoa10mL 15 beakerandthemassratioofmagnesiumtolithiuminthe mixturewas equalto52.58.Thebrinewasheated for phaseandremaininghalidesaltsafteratwo-phase condensationaboveatemperatureadjustablefurnace.Water separation; was evaporated,which accounted for30% oftotalmass of thebrine,andthesolutionwerechangedintohydratedhalide 20 saltsaftercoling.Thesaltsweretransferedintoamechani calmixingvessel,and 18.33mL oftributylphosphateas wellas18.34mL of2-ethylhexanolwereaddedtoachieve amasstovolumeratioequivalentto1:2(g/mL).Solid-liquid afterliquidlayersareformedandthenevaporatingand extractionwascariedoutfor30minsunderromtempera-25 concentratingtheseparatedwatertoobtainaconcen ture.Thensolidliquidmixturesweretransferedinasand tratedwaterphase; corefunnelandvacuum filtrationwascariedout,andthe extractedorganic-phasefiltrateandremaininghalidesalts wereobtained.Theremaininghalidesaltsweredissolvedin waterandfixitsvolumeto1000mLinavolumetricflask.30 SamplesweretakentoanalyzetheconcentrationofLitand f.adingsodiumcarbonateorsodiumhydroxideintothe concentratedwaterphasefrom stepetoprecipitate Mg2+thereof.Theresultsshowedthataextractionrateof waterphasehasapHofmorethan10tocompletely Li*was5.5%;aextractionrateofMg2+was4.2%anda precipitateMg2+;and organicextractionphaseandwaterwererespectivelyaded lithiumcarbonatetoproduceafinalproduct. inaseparatingfunelwithaphaseratiooforganicphaseto 2.Themethodofclaim1,whereinstepbcomprises:first waterV/ equivalentto2:1andreverseextractionwas extractingthehalidesalts,andthenheatingandmeltingthe cariedout.Themixtureswerevibratedfor30minsrepeat-40remaininghalidesalts,whereinthewatercontentofthe edlyinatemperature-constantcolingwaterbathSHA-2A remaininghalidesaltsiscontroledsuchthatthehalidesalts at20°C.andataspedof20r/min.Thesolutionswere containingcrystalwaterareseparatedout;adingtrialkyl thenplacedstilfor30minsandareverseextractedwater phosphateoramixtureoftrialkylphosphateandmonohy ater phasewas finaly obtained afterphase separation,with a dricalcoholtothehalidesaltscontainingcrystalwaterata decreasedmagnesium tolithium ratio.Sampleswereana-45 volume-massratioof1.0:0.5~5.0toperform asecondstage lyzedandresultsshowedthatreverseextractionrateofLi* extraction. was up to 93.6%;reverse extraction rate ofMg++was 3.Themethodofclaim 1,whereinstepbismulti-stage 88.2%;andamassratiomagnesiumtolithiumdeclinedto crosflowextractionormulti-stagecounterflowextraction. 8.5inthereserveextractedwaterphase.Intheconcentrated 4.Themethodofclaim 1,whereintrialkylphosphatein reverseextractedsolutionwithalowmagnesium tolithium 50 stepbisselectedfrom thegroupconsistingof:tributyl ratio,sodium carbonate solution was added to remove phosphate,tripentylphosphate,trihexylphosphate,tri-n majorityofMg2+,thensodiumhydroxidewasagainadded heptylphosphate,trioctylphosphateandisomeridesthereof; intothesolutionafterseparation,tocompletelyprecipitate themonohydricalcoholisselectedfromoneormoreof magnesium.Solutionofsodiumcarbonatewasaddedinto saturatedmonohydricalcoholshaving6-20carbonatoms; thefilteredsolutiontoformprecipitation,andseparationand5andavolumeratiooftrialkylphosphatetomonohydric desiccationwerecarriedouttoobtainalithium carbonate alcoholis1.0:0.2-4.0. product. 5.Themethodofclaim 1,wherein,whenamassratioof Theabovecontentsareonlypreferedembodimentsofthe magnesiumtolithiumislargerthan1.0inthereverse presentinvention,andembodimentsofpresentinventionis extractedwaterphasefromstepe,stepsatoearerepeated notlimitedtothis.Thepresentinventionhavediferent60onthereverseextractedwaterphasefrom stepetofurther kindsofmodificationsandchangesforthoseskiledinthe reduceamagnesiumtolithiumratio. art.Anymodification,equivalentreplacement,improvement * * * * * whereinaratioofweight(kg)oftheseparatedhalidesalts toavolume(L)oftheorganicphaseis1.0:0.5-5.0; c.filteringamixturefrom stepbtoproduceanorganic d.reverseextractingtheorganicphasefrom stepcwith waterasareverseextractionagentatavolumeratioof watertoorganicphaseof1.0:0.5-10.0in 1-5stagesof magnesium carbonate ormagnesium hydroxide,and thenfilteringtheprecipitatedmagnesium carbonateor magnesium hydroxidetoremoveMg2+,whereinthe reverseextraction; 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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)