RECOVERY OF LITHIUM FROM NATURAL AND SYNTHETIC BRINES

PDF Publication Title:

RECOVERY OF LITHIUM FROM NATURAL AND SYNTHETIC BRINES ( recovery-lithium-from-natural-and-synthetic-brines )

Previous Page View | Next Page View | Return to Search List

Text from PDF Page: 014

7 8 US 11,365,128B2 oftheHBFisapH1.0acidwashoftheslurywith circuit30.Accumulatedsolidsinthefirstclarifier304and hydrochloricacidtoremoveanyleadprecipitatesfromthe thesecondclarifier308arerespectivelyroutedtoapneu filtercake.ThesecondstageisapH9.5condensatewater mapresfilterHBFtoprepareanFe/Sifiltercake314anda washtoneutralizeanyresidualacidinthefiltercake.The Mn/Znfiltercake316. thirdstageoftheHBFsteamdriesthefiltercake.Thefilter5 Acidisthenadded318tothebrinefromthesecond cakeistransportedtoalocallandfilfordisposal. clarifier308toreducethepHbackdowntobetweenabout ThesilicaandironconcentrationsinthebrineatthePCO, 4.5andabout6.0,withabrinetemperaturebetweenabout SCOandinjectionwelsofthepowerplantoperationsare 5°C.andabout100°C.,whichissuitablefortheCCAD summarizedasfollowsinTable1: TABLE 1 Sias Fe As K Zn Mn Li Location(mg/kg) (mg/kg) (mg/kg) (mg/kg) (mg/kg) (mg/kg) (mg/kg) PCO 167+251,579 123 17.0+4.020,600+2,200625+421,705+101 264+24 SCO 159=191,560=88 16.9+4.020,60=2,60639=411,693 134 265+23 Injection160=191,578716.9+4.020,400+2,500621+451,696=92 265+22 Wells 20 Thepolishedbrine1038thatexitstheSCOfromthe pointintheprocescompriseprimarilysalts(aschlorides) powerplant1000withreducedamountsofscalingconstitu- withhighconcentrationsofsodium,potasium,andcalcium. entsiswelsuitedformineralextraction,andratherthan Thelithiumconcentrationiscomparativelylowatonly£250 injectingthepolishedbrine1038intotheinjectionwel ppm. 1032,itismadeavailabletothesystemandproces200 25 Thepolishedbrine(stream54inFIG.4A)canthenpased and/ortotheCCADproces400forselectiverecoveryof totheCCADcircuit400,whichconcentratesthelithiumin lithiumand/orothermineralsfromthepolishedbrine1038. thepolishedbrinebyaproximately10timesandsimulta RecoveryofLithiumCarbonate: neouslyseparatesthelithiumfromtheothersalts(calcium AsilustratedinFIG.2,afedbrine,suchasageothermal30 isofparticularconcernfordownstreamoperations).The brineorthebrine1038thatexitstheSCOfromthepower targetresultisanenhancedlithiumchlorideproductstream plant10havingreducedamountsofscalingconstituents 342inFIGS.2and3(stream57inFIG.4A)(stream417or pasestothesystemandproces200formineraland/or stream420inFIG.5)(withsomeresidualimpurities)of lithiumextraction.Thefedbrineispasedintotheimpurity aroundaproximately2,50to3,0ppmlithium.The removalcircuit30havingafirstsetofreactiontanks30235residualbrinecanbereturnedforreinjectionthroughinjec andafirstclarifier304toremoveironandsilicafollowedby tionwels320. asecondsetofreactiontanks306andasecondclarifier308 IftheinventiveCCAD systemisusedwithsalar,conti toremovemanganeseandzincprimarily.Afirstoriron/ nentalorothernon-geothermalbrines,thebrinefedstock silicaprecipitationstage300Aoftheimpurityremoval canbepaseddirectlytotheCCADcircuit40withminimal circuit30includesadinglimestone310Aandinjectingair40pretreatmentsuchasgranularmediafiltration(GMF)and,if 310Bintobrine.Theaircausesthedisolvedirontooxidize necesary,residualorganicremoval.Salarorcontinental andthepHtodrop.AlowpHsolutionreducestherateof brineswithlowironandsilicacontentmayrequireonly reaction;therefore,limestoneisusedtoneutralizethisefect minimalpretreatmentbeforebeingpasedtotheCCAD andmaintainthepHaround5.5.Thefirstclarifier304is circuit40forconcentratinglithiumwhencomparedto positioneddownstreamofthefirstsetofreactiontanks30245brinesfromtheSaltonSeaKnownGeothermalResource tosetleoutthesilicaandironinthebrine.Theprecipitated Area(SSKGRA).Thepretreatmentprocesmayinclude solidsaresetledtothebottomofthefirstclarifiertank304. dilutionwithwatertopreventsolidsprecipitatingfrom Thefirststage300Aoftheimpurityremovalcircuit300 brinesthatareclosetosaturation.Inadition,GMFcanbe reducestheironconcentrationinthebrineoverflowfrom usedtoreducetotalsuspendedsolids(TSS)tobelow10ppm about1,60partpermilion(ppm)downtolesthanabout50beforeintroducingthebrinesolution.Oilfieldbrinesmay 5ppmandreducesthesilicaconcentrationinthebrine requirepretreatmentprocesingtoremoveanyresidual overflowfromabout60ppmdowntolesthanabout5ppm. organicmaterialbeforebeingpasedtotheCCADcircuit Arelativelyclearbrineoverflowpasesfromthefirst 40.Thebulkoftheorganicmaterialcanberemovedbya clarifier304toasecondorzincm/anganeseprecipitation devicesuchasanAPIoil-waterseparator.Anyremaining stage300Bofimpurityremovalcircuit300. 5organicmaterialscanberemovedwithamixedbedGMF Thesecondstage300Boftheimpurityremovalcircuit thatincludesactivatedcarbonaspartofthemixedbed. 30includesadinglimestone312Aand/orlime312Btothe ReferingnowtoFIG.5,theCCADcircuit40includes brineinthesecondsetofreactiontanks306.Thiscausesthe aseriesofsequentialstepsinacyclicproces.TheCCAD brinepHtoelevatetoaround8.Thesecondclarifier308is circuit400hasapluralityofadsorptionbedsorcolumns402 positioneddownstreamofthesecondsetofreactiontanks60eachcontainingalithiumselectiveadsorbent.Theadsorp 306andalowsthemetalsasoxidesand/orhydroxides tionbeds402aresequentialysubjectedtoindividualpro (primarilyzincandmanganese)tosetle.Duringthesecond ceszones(A,B,C,D)aspartoftheCCADcircuit40. stage300Boftheimpurityremovalcircuit30,theman- EachoftheproceszonesA,B,C,andDincludesoneor ganeseconcentrationinthebrineisreducedfromabout moreoftheadsorbentbeds402configuredinparalel,in 170ppmdowntolesthanabout10ppm,whilezinc65series,orincombinationsofparalelandseries,flowing concentrationisreducedabout60ppmdowntolesthan5 eitherinupflowordownflowmodes.Theproceszonesof ppminthesecondstage300Boftheimpurityremoval theCCADcircuit40includeanadsorptiondisplacement SiO2 circuit40.Thedisolvedsolidsinthepolishedbrineatthis

PDF Image | RECOVERY OF LITHIUM FROM NATURAL AND SYNTHETIC BRINES

recovery-lithium-from-natural-and-synthetic-brines-014

PDF Search Title:

RECOVERY OF LITHIUM FROM NATURAL AND SYNTHETIC BRINES

Original File Name Searched:

US11365128.pdf

DIY PDF Search: Google It | Yahoo | Bing

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 | RSS | AMP