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US 10,246,341B2 amixtureoftrialkylphosphateandmonohydricalcoholina separationissimple.TheextractionrateofLitandMg+are proportionof1.0:(0.5–5.0)inamassvolumeratioofsolid bothhigherthan90%.Adirectandrecycleduseoftrialkyl toliquid,andperformingasecondstageextraction,anda phosphateoramixtureoftrialkylphosphateandmonohy stageofthesolid-liquidextractionis1-5. dricalcohol,completelyovercomesthedificultiesinsimul Thesolid-liquidextractionisinmulti-stagecrosflowor 5 taneouscyclingandinsimultaneousreusingofanextraction agent,aco-extractionagentandadilutingagentinliquid Anextractionagenttrialkylphosphateusedinthesolid liquidextraction. liquid extraction comprises one or more of compounds 4.The extractionagenttrialkylphosphate oramixture of consistingof:tributylphosphate,tripentylphosphate,tri- trialkylphosphateandmonohydricalcoholisuniversaland hexylphosphate,tri-n-heptylphosphate,trioctylphosphate 10easytoobtain;whereinthelengthofanalkylgroupimposes andisomeridesthereof;themonohydricalcoholcomprises asignificantinfluenceonthesolubilityofanextraction oneormore ofcompoundsconsistingofsaturatedmono agentinwateraswellasonthesolubilityofwaterinorganic hydricalcoholswithcarbonnumbersbetwenC6-C20;and phase.Regulatingamoleculestructureisabletodecreasea avolumeratiooftrialkylphosphateandmonohydricalcohol solubilitylosoftheextractionagentandfurtherincreasean multi-stagecounterflow. 15abilitythereofinmagnesium/lithiumseparation.Theextrac Whenamassratioofmagnesiumtolithiumislargerthan tionpropertiesoftrialkylphosphateoramixtureoftrialkyl 1.0inawaterphasesolutionofthereverseextraction,the phosphateandmonohydricalcoholisunafectedbyapH waterphasesolutionofthereverseextractionistakenasa valueinbrineandextractioncanbecariedoutinneutralor rawmaterialofthebrineinnext-stagesolid-liquidextrac weakacidicconditions.Thesolid-liquidextractionintensi tion,andanew separationproces forlithium andmagne-20 fiessolubilityofhalidesaltsintheorganicphaseaswellas siumtofurtherreducethemagnesiumtolithiumratiois sphericalstructureformationofmicroemulsion,andis takenbypreparationofhalidesalts,solid-liquidextraction, beneficialtoenrichinglithiumandseparatingLitfrom solid-liquidseparation,reverseextractionandliquid-liquid Mg-+.Thesaidtypeofextractionagentsprovidesalow is1.0:(0.2~4.0). toxicityandcanbedegradednaturaly,imposingaweakly Theextractionagenttrialkylphosphateorthemixtureof25negativeefectonenvironmentalprotectionofsaltlakes. separationfromthestepatothestepe. thetrialkylphosphateandthemonohydricalcoholisreused afterreverseextractionandliquid-liquidseparation. Therawmaterialbrineisprovidedfromdiferentkindsof FIG.1showsaprocesflowdiagramofproducinglithium fieldbrine,wellbrineoracondensingsolutionofseawater 30 carbonatefrom low-lithium brinebyseparatingmagnesium aftersaltpreparation. andenrichinglithiuminpresentinvention. Compared with the prior art, the present invention lithium containedsalt-lakebrine,undergroundbrine,oil DETAILED DESCRIPTION providedastheextractionagenttoextractlithiumfrom withembodimentsasfollows. changesbrineintohalidesalts,andchangesliquid-liquid extractionintosolid-liquidextraction.Trialkylphosphateor amixtureoftrialkylphosphateandmonohydricalcoholis35 Afurtherdescriptionofthepresentinventionisprovided halidesaltsandsolubilizationaswelasselectivityofmicro emulsiontometalionsareutilizedtoperform theseparation ofmagnesium andlithium,achievingunexpectedresults.A ThecontentofLi*,Mg2+andSO42+arerespectively2.24 new aproachisprovidedforthepresentexplorationof40g/L,118.00g/L,39.87g/Landamagnesium tolithiumratio lithiumresourcefromsalt-lakebrinewithahighmagnesium isequivalentto52.58inoldbrineinasaltlakelocatedin tolithiumratio.Thepresentinventionhasthefolowing QaidamBasinofQinghaiprovince.350mLoftheoldbrine advantages. 1.Thechemistry-industryinvolvedunitissimpleto wastakenintoa1000mlbeakerandwasheatedfor 15condensationaboveatemperatureadjustablefurnace.Water operateusingsolid-liquidextractionofhalidesaltsofsalt45Co lake,sincenocalcinationonhalidesaltsisdemandedbefore extraction,andprocessesareeasytorealize.Thismethodis especiallysuitablefordecreasingamagnesium tolithium ratio from salt-lakebrineinwhich amagnesium tolithium wasevaporated,whichaccountedfor25%oftotalmassof thebrine,andthesolutionwerechangedintohydratedhalide saltsaftercoling.Thesaltsweretransferedintoamechani calmixingvesel,and34.5mL oftrihexylphosphatewas soaddedtoachieveamassvolumeratioequivalentto1:1 massratioislowerthan120andobtaininglithiumenriched50(g/mL).Solid-liquidextractionwascariedoutfor30mins solution,whichmetstherequirementforproducinglithium underroomtemperature.Thensolidliquidmixtureswere saltstoproducelithium carbonate. 2.Comparedtotheliquid-liquidextraction,thesolid transferredinasandcorefunnelandvacuum filtrationwas liquidextractionutilizedinthepresentmethodprovidesa cariedout,andtheextractedorganic-phasefiltrateand 5remaininghalidesaltswereobtained.Theremaininghalide greatdistributiondrivingforceonsolute,andisunaffected 55 byatwo-phaseequilibriumoftheextractionagentforbrine. saltswereheatedandmeltedtocompletion.Thenthemelted Noco-extractionagentisdemanded,andanextraction halidesaltswerecooledandcompletelyseparatedout. abilityissignificantlyenhancedbyadirectextractionfrom Hydratedhalidesaltswereobtainedforthesecondtime. halidesaltsusingtrialkylphosphateoramixtureoftrialkyl Multiplestageextraction:2ndstage,3rdstageand4thstage to extractionsweresucesivelycariedoutinacros-flow phosphateandmonohydricalcohol.ALitextractionrate60 higherthan 90% aswelasadecreasedmagnesium to lithium ratiobyseveraltimesisachievedbymulti-stage repeatedprocesesconsistingof:extractionofhalidesalts, disolvingafterseparationandseparatinghalidesaltsout processweresampledandanalyzedrespectivelybyaJapa 3.Ahighemergencerateofmetalionsisachievedby65nese Shimadzu atomic absorption spectrophotometer usingwaterforareverseextractionoforganicphaseasthe AA-7000andanEDTAtitrimetricvolumetry.Theresultsare densitydiferencebetweentwophasesisgreatandaphase shownintable.1. BRIEFDESCRIPTION OFDRAWINGS Embodiment 1 manneracordingtotheoperationrequirementsofthefirst time. TheconcentrationsofLitandMg2+duringtheextractionPDF Image | PRODUCING LITHIUM CARBONATE FROM LOW LITHIUM 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)