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5,993,759 S6 produceddensepulp6canbeseparatedinaSolid/liquid Theclearbrine30oftheoptionalthickeningstage26is separator(S/L)7,suchaswithadiscfilterorpresfilter.It mixedwiththefiltrate31toformpurifiedbrine32,which iswashedwithcoldwater8foreliminatingimpurities trappedintheliquidretainedinthecrystals.Theobtained boricacid9isofhighpurityandisSubjectedtoadryingStep 10atatemperatureof0to80 C.forobtainingdry commercial boric acid 11. Thefiltrate12fromthesolid/liquidseparationstage7is added to the brine of the overflow 13 of the thickener 5 and followsintheproces.Thewashingwater14oftheboric acidobtainedduringthefiltrationStage7canbediscarded. Thebrineoftheoverflow13,mixedwiththefiltrate12, normallyhasaboroncontentof0.3%to0.5%byweightand canbesubjectedtoanextractionbysolventprocess15for extractingtherestoftheboroninoneormoreextraction Stages. The extraction Solvent can be an organic Solvent. 15 ThisextractionStageiscariedoutpreferablywithapHof 0to5,measuredforadilutionofthebrineinwaterof1:10, usinganorganic/brineratioof1/5to5/1. Thechargedorganicextractant16isSubjectedtooneor moreStagesofStripingorre-extraction17usinganalkaline aqueousSolution18SuchasSodiumhydroxide,potassium hydroxide, or the like, at a concentration of preferably between0.02and2.0mol,withanorganic/aqueousratioof 1/5to5/1. isSenttoaSecondpurificationStage.Thepurifiedbrine32 with0.01%to0.05%byweightofmagnesiumissubjected toaprecipitationStep,forwhichitisfedintoareactor33 togetherwithasolutionofcalciumhydroxide34(milkof lime) of 5 to 50% by weight, maintaining a mole ratio NaCO/Ca(OH) of0.3to2,beingmixedatatemperature of50to95 C.andforatimespanof5to180minutes, maintainingapHof8to10.Undertheseconditions,therest of the magnesium contained in the brine precipitates togetherwiththecalcium.Thereactionswhichoccurarethe folowing: Theprecipitatedpulp35canbedecantedinasuitable equipment,Suchasathickener36andthedensepulp37(or theprecipitatedpulp35inthecasethattheoptionalthick eningStage36isnotaplied)isSubjectedtoaseparation step39atatemperatureof50to95 C.utilizing,for Thedischargedorganicextractant19isreturnedtothe25 example,apressfilter.Themagnesiumhydroxideand initialextractioncircuit15,whiletheaqueous20containing theboroncanbediscardedorusedforrecoveringtheboron, dependingonthecontentleveloftheSame. Thebrine21,virtualydevoidofboronorwithaboron contentoflesthan5partspermilion(i.e.,“boron-fre brine”),isthenfurtherpurifiedforeliminatingtheremainder oftheothermetalscontainedtherein,Suchasmagnesium andcalcium,beforetheprecipitationofthelithiumcarbon calciumcarbonatecake40isdiscarded,whiletheeventual purifiedbrine38 withmagnesiumlevelsbelow0.002%by weight(i.e.,"magnesium-freebrine')andofcalciumlevels lower than 0.005% by weight-from the overflow of the thickener36,andthefiltrate41,obtainedintheseparation step39,aresenttogetherasbrine42toalithiumcarbonate precipitation stage in a reactor 43. If purified brine 38 contains Suspended magnesium hydroxide particles can ate. eventuallybefilteredinafilter64,forexampleinapress InthefirstStageofpurification,thebrine21passestoa35 filter,generatingamagnesiumhydroxidecake65,whichis reactor22,whereitisdilutedwithmotherliquor23ofthe precipitation Stage of lithium carbonate which wil be definedfurtherbelow.Themotherliquor23hasalithium discarded,andfilteredbrine66,whichisaddedtothefiltered brine41fororiginatingafilteredbrine42. In the reaction stage 43 (precipitation of lithium contentof0.1to0.3%byweightandasodiumcontentof640 carbonate),thebrine42withalithiumcontentof0.8%to to9.5%byweight.Thisdilutionofthebrine21withmother 1.2%isreactedwithasolutionof20%to30%byweightof liquor23lowersthecontentoflithiuminthebrinefrom 4-6% to 0.9 to 1.5%, which prevents the precipitation of largeamountsoflithiumduringtheprecipitationofthe magnesiumwithSodiumcarbonate. Thebrine21dilutedwithmotherliquor23isreactedin the reactor 22 with a solution of Sodium carbonate 24 of 20 to 30% by weight for maintaining a pH of 7 to 9 at a temperaturebetween15and95 C.foratimespanof5to 120 minutes. Under these conditions, 60 to 95% of the magnesiumcontainedinthebrineisprecipitatedintheform ofmagnesiumcarbonateaccordingtothefollowingreac tion: Sodiumcarbonate(Sodaash)44formaintainingapHof8to 12.Thereactiontemperatureismaintainedat50to98 C. and the total reaction time is between 5 to 180 minutes. 45 Undertheseconditions,40%to90%,typicaly80%–90%, ofthelithiumcontainedinthebrineprecipitatesaccording tothefollowingreaction: 50 2LiCl+Na2CO=LiCO+2NaCl (9) Theprecipitatedlithiumcarbonatepulp45canbesub jectedtoaSolid/liquidSeparationStagecomprisedbyafirst Solid/liquidSeparationSubstage46andaSecondSolid/liquid SeparationSubstage48.ThisfirstSolid/liquidSeparation 55 Substage46isrealizedpreferablyinahydrocycloneorina At80C.,thesolubilityconstantofmagnesiumcarbonate Seriesofhydrocyclones,wherebyadensepulp47is is3.5x10 withapHof8. obtained.Thedensepulp47isthenSubjectedtoaseparation Theresultingpulp25isoptionalythickenedinaSuitable step51,forexampleinadrumfilter,inabeltfilteror equipmentSuchasathickener26andthethickenedpulp27 centrifuge,followedbyawashwithdemineralizedorsoft (orthepulp25,inthecasethatnothickeningStage26is60 water52at60-98C.Inordertoavoiddisolvinganexcess existent)isSubjectedtoaSolid/liquidSeparationstep28at amountoflithiumcarbonateinthewashwater,thetem atemperaturebetween50and95C.,utilizing,forexample, peraturemustbemaintainedabove60°C.,sincelithium adrumfilter,andthecakeofmagnesiumcarbonateis carbonatehasaninverseSolubilitywithrespecttotempera washedwithmotherliquor23atatemperaturebetween30 ture(i.e.,1.52%at0°C.and0.71%at100°C). and95 C. 65 Theoverflow55ofthefirstsolid/liquidseparationSub Themagnesiumcarbonatecake29ofthefilterobtainedin Stage46,whichcontainsthefinerparticlesoflithium theSeparationStep28isdiscarded. carbonate,isSubjectedtoaSecondSeparationSubStage48,PDF Image | Patent PRODUCTION OF LITHIUM CARBONATE FROM 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)