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13 14 US 11,365,128B2 operationsand/orfuelboilertooperate.Afterprocesing thickenerorclarifier304wherefloculent(stream12/13)is throughtheevaporator508,lithiumconcentrationinthe addedandthesolidsaresetledout.Theunderflowfromthe productstreamisincreasedfromabout5,0ppmtoabout clarifier304(stream15)ispumped(stream16)backtothe 30,0ppm. firstsetofreactiontanks302assed(stream17)and(stream Thenextstepsinthelithiumchlorideconversioncircuit 5 19)tothefilterfedtank326.PrecipitatefromtheCa/Mg 500convertthelithiumchlorideinsolutiontoalithium precipitationstage540oftheimpurityremovalcircuit502 carbonatecrystal.Sodiumcarbonateisaded512tothe isaded(stream73)andthecombinedslury(stream20)is lithiumchlorideproductstream342toprecipitatelithium filteredintheFe/Sifilter32.TheresultingFe/Sifiltercake carbonate514.Thelithiumcarbonate514sluryissenttoa iswashedwithdilutionwater(stream22)andthewashed centrifuge516toremoveanyexcesmoistureresultingin10filtercake328(stream23)leavesthecircuit30.Thefiltrate lithiumcarbonatecake.Thelithiumcarbonatecakeisre- (stream24)ispump(stream25)tothedilutionwatertank disolved518,pasedthroughafinalpurificationorimpu- 330. rityremovalstep520,andrecrystalized52withthe Theclarifieroverflow(stream14)fromtheFe/Siprecipi aditionofcarbondioxide524.Thecrystalizedlithium tationstage300AiscombinedwithfiltratefromaZn/Mn a carbonateproductisthensuitableforpackaging527. 15precipitatefilter32(stream45)inafedtank338andthe RecoveryofLithiumHydroxide: combinedsolution(stream26)ispumped(stream27)tothe FIG.3ilustratesanotherexemplaryembodimentofthe Zn/Mn precipitationstage300B.Recycledprecipitate systemandproces20forrecoveryoflithium.After (stream38)isadedassedandlime312B(stream173)is leavingtheCCADcircuit40,ratherthanusingevaporation slakedwithrecycledbarensolution(stream172).Anygas 508exemplifiedinFIG.2,asolventextractionproces702 20releasedisvented(stream174).Thelime/recycledbaren concentrateslithiumintheenhancedlithiumchlorideprod- solutionisadded(stream28)tothesecondsetofreaction uctstream342inFIGS.2and3(stream57inFIG.4A) tanks306toraisethepHtojustover8andprecipitatezinc, (stream417orstream420inFIG.5)usingliquid-liquid manganeseandleadoxides/hydroxides. separation,andaftersolventextraction702andelectrolysis Anygasreleasedisvented(stream29)fromthesecond 708,thelithiumissubsequentlycrystalized710intolithium25setofreactiontanks306.Theexitslury(stream30)is hydroxideproduct712. pumped(stream31)totheclarifier308.Recycledsolids SimilartotheembodimentilustratedinFIG.2,the fromasubsequentpolishingfilter334(stream47)and lithiumchlorideconversioncircuit500firstprecipitates floculent(stream32/3)areaddedandtheprecipitated calciumandmagnesium502throughtheaditionsodium hydroxidesaresetledout.Theclarifierunderflow(stream hydroxide(causticsoda)resultingwithaCa/Mgfiltercake3035)ispumped(stream36)tosedrecycle(stream37)and isproduced504.ThepHofthelithiumchlorideproduct totheZn/Mnprecipitatefilter332(stream39).Theresulting stream342isloweredtoabout2.5instep700andthenthe Zn/Mnfiltercakeiswashedwithproceswater(stream41) acidifiedlithiumchlorideproductstream342isintroduced andthewashedfiltercake336(stream43)leavesthecircuit tothesolventextractionstep702inpulsedcolumns(tal 30.Thefiltrate(stream4)ispumped(stream45)tothe verticalreactionvesels).Theflowisscrubed704andthen35fedtank38aheadoftheZn/Mnprecipitationstage300B. striped706withsulfuricacidproducingalithiumsulfate Theclarifieroverflow(stream34)ismixedwithmother product.Thelithiumsulfateproductgoesthroughanelec- liquor(stream134)fromafirstprecipitationoflithium trolysisunit708producinglithiumhydroxidecrystals710. carbonate514andthecombinedsolution(stream49)is Thelithiumhydroxidecrystalsarethendriedandpackaged pumped(stream50)throughthepolishingfilter334to 712. 40captureresidualsolids.Thecapturedsolidsarebackwashed SelectiveRecoveryofZinc,ManganeseandLithium: out(stream46)andsenttotheZn/Mnprecipitateclarifier TurningnowtoFIG.4ilustratingyetanotherexemplary 308. embodimentoftheprocesforrecoveryoflithium,thefed Thefiltratefromthepolishingfilter34(stream51)is sourceisanincomingbrine(e.g.,ageothermalbrineorthe mixedwithspenteluantfromthedivalentIXcircuit(stream polishedbrine1038)(stream1)anddilutionwater(stream4595)andhydrochloricacid338(stream52/53)isaddedto 2).Theincomingdilutionwater(stream2)ismixedwith reducethepHtoaproximately5.5.Theresultingsolution filtrate(stream25)fromaFe/Siprecipitatefilter32,then iscoledtoaproximately185°F.inthemixingtank340 split,part(stream21)beingusedaswashtotheFe/Si andthecoledsolution(stream54)ispasedthroughthe precipitatefilter322andthebalance(stream3)beingadded CCADcircuit400inwhichthelithiumchlorideisselec totheincomingbrine(stream1).Thecombinedbrine,50tivelycapturedontothelithiumselectiveadsorbent.The dilutionwaterandFe/Sifiltrate(stream4)ispumped resultingbarensolution(stream5)ispumped(stream48) (stream5)totheFe/Siprecipitationstage300Aofthe toaholdingtank343fromwhichitisdistributedasfolows: impurityremovalcircuit30.Limestone310A(stream169) toslurythelimestonetotheFe/Siprecipitationstage issluriedwithrecycledbarenbrine(stream168).The 300A(stream167); limestone/recycledbarenbrinesluryisaded(stream6)to5 toslakethelimetotheZn/Mnprecipitationstage300B thefirstsetofreactiontanks302alongwithrecycled (stream171);and precipitatesed(stream18).Airisinjected(stream7/8)into thebalance(stream165)ispumpedaway(stream16)to thefirsttank302usingablower324.Theironisoxidized, bereinjectedintotheinjectionwels320. andironandsilicaareprecipitatedacordingtothefolow- Theloadedadsorbentiselutedwithproceswater(stream ingstoichiometry: 2CaCO3+2Fe2+3H20+1/202—2Fe(OH)3+2C02+ 2Ca2+ 3CaCO3+3H4SiO4+2Fe(OH)3?CazFeSiz012+ 3C02+9H20 6056)andtheresultingeluate(stream57)ispumped(stream 58)toathirdsetofreactiontanks532foraditionimpurity removal502,initialycalciumandmagnesiumprecipitation. Sodiumhydroxide554(stream179)isdisolvedinproces water(stream181)andadded(stream59)tothetanks532. 65 Sodiumcarbonate536(stream 176)isdisolvedinproces Thespentairisvented(stream9)fromthefirsttanks302, water(stream(177)pumpedfromaproceswaterreservoir andtheexitslury(stream10)ispumped(stream1)toa 538andaded(stream60).Abledofmotherliquor(streamPDF Image | RECOVERY OF LITHIUM FROM NATURAL AND SYNTHETIC 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 | RSS | AMP |