US20220235436A1 - Process for separating undesirable metals - Google Patents
Process for separating undesirable metals Download PDFInfo
- Publication number
- US20220235436A1 US20220235436A1 US17/719,142 US202217719142A US2022235436A1 US 20220235436 A1 US20220235436 A1 US 20220235436A1 US 202217719142 A US202217719142 A US 202217719142A US 2022235436 A1 US2022235436 A1 US 2022235436A1
- Authority
- US
- United States
- Prior art keywords
- liquid
- undesirable
- metals
- liquid resource
- acid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 229910052751 metal Inorganic materials 0.000 title claims abstract description 475
- 239000002184 metal Substances 0.000 title claims abstract description 475
- 150000002739 metals Chemical class 0.000 title claims abstract description 306
- 238000000034 method Methods 0.000 title claims abstract description 153
- 230000008569 process Effects 0.000 title claims abstract description 135
- 239000007788 liquid Substances 0.000 claims abstract description 564
- 229910052744 lithium Inorganic materials 0.000 claims abstract description 129
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims abstract description 114
- 238000000926 separation method Methods 0.000 claims abstract description 47
- 239000002244 precipitate Substances 0.000 claims description 234
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 192
- 239000000243 solution Substances 0.000 claims description 164
- 239000002253 acid Substances 0.000 claims description 130
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 122
- 238000005342 ion exchange Methods 0.000 claims description 109
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 108
- 150000003624 transition metals Chemical class 0.000 claims description 65
- 229910052723 transition metal Inorganic materials 0.000 claims description 64
- 230000001376 precipitating effect Effects 0.000 claims description 58
- 239000011780 sodium chloride Substances 0.000 claims description 54
- 239000012266 salt solution Substances 0.000 claims description 49
- 239000000203 mixture Substances 0.000 claims description 41
- 238000004062 sedimentation Methods 0.000 claims description 38
- 238000001914 filtration Methods 0.000 claims description 35
- 239000002245 particle Substances 0.000 claims description 34
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 33
- 230000001590 oxidative effect Effects 0.000 claims description 27
- 230000005484 gravity Effects 0.000 claims description 23
- 239000007800 oxidant agent Substances 0.000 claims description 23
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 18
- 239000000920 calcium hydroxide Substances 0.000 claims description 18
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 18
- 238000011084 recovery Methods 0.000 abstract description 43
- 239000002585 base Substances 0.000 description 108
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 102
- 239000012267 brine Substances 0.000 description 91
- 239000012528 membrane Substances 0.000 description 91
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 61
- 239000000463 material Substances 0.000 description 57
- 229920000642 polymer Polymers 0.000 description 56
- 238000005868 electrolysis reaction Methods 0.000 description 53
- 229910052742 iron Inorganic materials 0.000 description 38
- 239000011572 manganese Substances 0.000 description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 33
- -1 aqueous Substances 0.000 description 32
- 229910052748 manganese Inorganic materials 0.000 description 30
- 239000011133 lead Substances 0.000 description 29
- 239000002351 wastewater Substances 0.000 description 24
- 239000002002 slurry Substances 0.000 description 23
- WMFOQBRAJBCJND-UHFFFAOYSA-M Lithium hydroxide Chemical compound [Li+].[OH-] WMFOQBRAJBCJND-UHFFFAOYSA-M 0.000 description 22
- 239000011575 calcium Substances 0.000 description 21
- 229910052725 zinc Inorganic materials 0.000 description 21
- 239000011701 zinc Substances 0.000 description 21
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 20
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 20
- 229910052749 magnesium Inorganic materials 0.000 description 20
- 239000011777 magnesium Substances 0.000 description 20
- 239000011734 sodium Substances 0.000 description 19
- 229910052719 titanium Inorganic materials 0.000 description 19
- 239000010936 titanium Substances 0.000 description 19
- 229910052791 calcium Inorganic materials 0.000 description 18
- 229910052785 arsenic Inorganic materials 0.000 description 17
- 229910052745 lead Inorganic materials 0.000 description 17
- 229910003002 lithium salt Inorganic materials 0.000 description 17
- 159000000002 lithium salts Chemical class 0.000 description 17
- 229910052758 niobium Inorganic materials 0.000 description 17
- 239000010955 niobium Substances 0.000 description 17
- 229910052700 potassium Inorganic materials 0.000 description 17
- 239000007787 solid Substances 0.000 description 17
- 229910052715 tantalum Inorganic materials 0.000 description 17
- 229910052726 zirconium Inorganic materials 0.000 description 17
- 229910052782 aluminium Inorganic materials 0.000 description 16
- 239000011324 bead Substances 0.000 description 16
- 229910052802 copper Inorganic materials 0.000 description 16
- 239000010949 copper Substances 0.000 description 16
- 229910052737 gold Inorganic materials 0.000 description 16
- 239000010931 gold Substances 0.000 description 16
- 238000002156 mixing Methods 0.000 description 16
- 238000001556 precipitation Methods 0.000 description 16
- 229910052701 rubidium Inorganic materials 0.000 description 16
- 229910052708 sodium Inorganic materials 0.000 description 16
- 229910052712 strontium Inorganic materials 0.000 description 16
- 229910052718 tin Inorganic materials 0.000 description 16
- 239000011135 tin Substances 0.000 description 16
- 229910052787 antimony Inorganic materials 0.000 description 15
- 229910052790 beryllium Inorganic materials 0.000 description 15
- 229910052793 cadmium Inorganic materials 0.000 description 15
- 229910052792 caesium Inorganic materials 0.000 description 15
- 229910052804 chromium Inorganic materials 0.000 description 15
- 239000011248 coating agent Substances 0.000 description 15
- 238000000576 coating method Methods 0.000 description 15
- 229910052730 francium Inorganic materials 0.000 description 15
- 229910052733 gallium Inorganic materials 0.000 description 15
- 229910052732 germanium Inorganic materials 0.000 description 15
- 229910052735 hafnium Inorganic materials 0.000 description 15
- 229910052738 indium Inorganic materials 0.000 description 15
- 229910052741 iridium Inorganic materials 0.000 description 15
- 229910052750 molybdenum Inorganic materials 0.000 description 15
- 229910052762 osmium Inorganic materials 0.000 description 15
- 229910052703 rhodium Inorganic materials 0.000 description 15
- 229910052707 ruthenium Inorganic materials 0.000 description 15
- 229910052706 scandium Inorganic materials 0.000 description 15
- 229910052710 silicon Inorganic materials 0.000 description 15
- 229910052709 silver Inorganic materials 0.000 description 15
- 239000010944 silver (metal) Substances 0.000 description 15
- 229910052713 technetium Inorganic materials 0.000 description 15
- 229910052721 tungsten Inorganic materials 0.000 description 15
- 229910052720 vanadium Inorganic materials 0.000 description 15
- 229910052727 yttrium Inorganic materials 0.000 description 15
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 14
- 229920001577 copolymer Polymers 0.000 description 14
- 238000000909 electrodialysis Methods 0.000 description 13
- 229910052500 inorganic mineral Inorganic materials 0.000 description 13
- 239000011707 mineral Substances 0.000 description 13
- 235000010755 mineral Nutrition 0.000 description 13
- 125000000524 functional group Chemical group 0.000 description 12
- 239000013535 sea water Substances 0.000 description 12
- 239000004811 fluoropolymer Substances 0.000 description 11
- 235000011116 calcium hydroxide Nutrition 0.000 description 10
- 239000002131 composite material Substances 0.000 description 10
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 10
- 238000005086 pumping Methods 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 9
- 239000002033 PVDF binder Substances 0.000 description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 9
- 150000001768 cations Chemical class 0.000 description 9
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 9
- 229910001416 lithium ion Inorganic materials 0.000 description 9
- 238000000638 solvent extraction Methods 0.000 description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 8
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 8
- 229920000557 Nafion® Polymers 0.000 description 8
- 150000001805 chlorine compounds Chemical class 0.000 description 8
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 description 8
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 8
- 239000004810 polytetrafluoroethylene Substances 0.000 description 8
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 8
- 239000004800 polyvinyl chloride Substances 0.000 description 8
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 description 8
- 239000002562 thickening agent Substances 0.000 description 8
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 8
- 239000004793 Polystyrene Substances 0.000 description 7
- 150000001450 anions Chemical group 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 229920002313 fluoropolymer Polymers 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 239000004698 Polyethylene Substances 0.000 description 6
- 239000004743 Polypropylene Substances 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 238000005341 cation exchange Methods 0.000 description 6
- 239000004927 clay Substances 0.000 description 6
- 238000010612 desalination reaction Methods 0.000 description 6
- 238000001728 nano-filtration Methods 0.000 description 6
- ZKATWMILCYLAPD-UHFFFAOYSA-N niobium pentoxide Chemical compound O=[Nb](=O)O[Nb](=O)=O ZKATWMILCYLAPD-UHFFFAOYSA-N 0.000 description 6
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 6
- 229920000573 polyethylene Polymers 0.000 description 6
- 229920001155 polypropylene Polymers 0.000 description 6
- 229920000915 polyvinyl chloride Polymers 0.000 description 6
- 125000001453 quaternary ammonium group Chemical group 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 5
- 239000003513 alkali Substances 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 5
- 229910052681 coesite Inorganic materials 0.000 description 5
- 229910052906 cristobalite Inorganic materials 0.000 description 5
- QXYJCZRRLLQGCR-UHFFFAOYSA-N dioxomolybdenum Chemical compound O=[Mo]=O QXYJCZRRLLQGCR-UHFFFAOYSA-N 0.000 description 5
- 230000005684 electric field Effects 0.000 description 5
- 238000000605 extraction Methods 0.000 description 5
- INHCSSUBVCNVSK-UHFFFAOYSA-L lithium sulfate Chemical compound [Li+].[Li+].[O-]S([O-])(=O)=O INHCSSUBVCNVSK-UHFFFAOYSA-L 0.000 description 5
- 229920002492 poly(sulfone) Polymers 0.000 description 5
- 229920002223 polystyrene Polymers 0.000 description 5
- 239000011148 porous material Substances 0.000 description 5
- 239000000377 silicon dioxide Substances 0.000 description 5
- 229910052682 stishovite Inorganic materials 0.000 description 5
- 239000000725 suspension Substances 0.000 description 5
- 229910052905 tridymite Inorganic materials 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- KLZUFWVZNOTSEM-UHFFFAOYSA-K Aluminium flouride Chemical compound F[Al](F)F KLZUFWVZNOTSEM-UHFFFAOYSA-K 0.000 description 4
- 229920001780 ECTFE Polymers 0.000 description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 4
- 239000004693 Polybenzimidazole Substances 0.000 description 4
- 229920000265 Polyparaphenylene Polymers 0.000 description 4
- 239000004372 Polyvinyl alcohol Substances 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical group [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 4
- 230000004075 alteration Effects 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 4
- 150000002170 ethers Chemical class 0.000 description 4
- 239000012065 filter cake Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 229920002755 poly(epichlorohydrin) Polymers 0.000 description 4
- 229920001643 poly(ether ketone) Polymers 0.000 description 4
- 229920002627 poly(phosphazenes) Polymers 0.000 description 4
- 229920000412 polyarylene Polymers 0.000 description 4
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- 229920002451 polyvinyl alcohol Polymers 0.000 description 4
- 239000012465 retentate Substances 0.000 description 4
- WOCIAKWEIIZHES-UHFFFAOYSA-N ruthenium(iv) oxide Chemical compound O=[Ru]=O WOCIAKWEIIZHES-UHFFFAOYSA-N 0.000 description 4
- SBYHFKPVCBCYGV-UHFFFAOYSA-O 1-azoniabicyclo[2.2.2]octane Chemical compound C1CC2CC[NH+]1CC2 SBYHFKPVCBCYGV-UHFFFAOYSA-O 0.000 description 3
- RAXXELZNTBOGNW-UHFFFAOYSA-N 1H-imidazole Chemical group C1=CNC=N1 RAXXELZNTBOGNW-UHFFFAOYSA-N 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- 229910019142 PO4 Inorganic materials 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical group C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 3
- 239000003011 anion exchange membrane Substances 0.000 description 3
- 125000002843 carboxylic acid group Chemical group 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000004132 cross linking Methods 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000007306 functionalization reaction Methods 0.000 description 3
- ISNICOKBNZOJQG-UHFFFAOYSA-O guanidinium ion Chemical group C[NH+]=C(N(C)C)N(C)C ISNICOKBNZOJQG-UHFFFAOYSA-O 0.000 description 3
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 description 3
- 229910052808 lithium carbonate Inorganic materials 0.000 description 3
- 235000021317 phosphate Nutrition 0.000 description 3
- 125000002467 phosphate group Chemical group [H]OP(=O)(O[H])O[*] 0.000 description 3
- 125000005496 phosphonium group Chemical group 0.000 description 3
- 229910052697 platinum Inorganic materials 0.000 description 3
- 229920002239 polyacrylonitrile Polymers 0.000 description 3
- 229920002620 polyvinyl fluoride Polymers 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 125000001174 sulfone group Chemical group 0.000 description 3
- PBCFLUZVCVVTBY-UHFFFAOYSA-N tantalum pentoxide Inorganic materials O=[Ta](=O)O[Ta](=O)=O PBCFLUZVCVVTBY-UHFFFAOYSA-N 0.000 description 3
- RBTVSNLYYIMMKS-UHFFFAOYSA-N tert-butyl 3-aminoazetidine-1-carboxylate;hydrochloride Chemical compound Cl.CC(C)(C)OC(=O)N1CC(N)C1 RBTVSNLYYIMMKS-UHFFFAOYSA-N 0.000 description 3
- CHJAYYWUZLWNSQ-UHFFFAOYSA-N 1-chloro-1,2,2-trifluoroethene;ethene Chemical group C=C.FC(F)=C(F)Cl CHJAYYWUZLWNSQ-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 2
- 239000004812 Fluorinated ethylene propylene Substances 0.000 description 2
- 229910002983 Li2MnO3 Inorganic materials 0.000 description 2
- 229910007848 Li2TiO3 Inorganic materials 0.000 description 2
- 229910007822 Li2ZrO3 Inorganic materials 0.000 description 2
- 229910003327 LiNbO3 Inorganic materials 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000004696 Poly ether ether ketone Substances 0.000 description 2
- 239000005062 Polybutadiene Substances 0.000 description 2
- 239000004734 Polyphenylene sulfide Substances 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- 229910052581 Si3N4 Inorganic materials 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000004676 acrylonitrile butadiene styrene Substances 0.000 description 2
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- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 2
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 description 2
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- 229910021389 graphene Inorganic materials 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910001410 inorganic ion Inorganic materials 0.000 description 2
- HTXDPTMKBJXEOW-UHFFFAOYSA-N iridium(IV) oxide Inorganic materials O=[Ir]=O HTXDPTMKBJXEOW-UHFFFAOYSA-N 0.000 description 2
- 229910003455 mixed metal oxide Inorganic materials 0.000 description 2
- 229910003465 moissanite Inorganic materials 0.000 description 2
- GUCVJGMIXFAOAE-UHFFFAOYSA-N niobium atom Chemical compound [Nb] GUCVJGMIXFAOAE-UHFFFAOYSA-N 0.000 description 2
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- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
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- 229920001084 poly(chloroprene) Polymers 0.000 description 2
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- 239000011591 potassium Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
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- 239000006104 solid solution Substances 0.000 description 2
- 241000894007 species Species 0.000 description 2
- GUVRBAGPIYLISA-UHFFFAOYSA-N tantalum atom Chemical compound [Ta] GUVRBAGPIYLISA-UHFFFAOYSA-N 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- 229920002554 vinyl polymer Polymers 0.000 description 2
- 229910052845 zircon Inorganic materials 0.000 description 2
- 229910000851 Alloy steel Inorganic materials 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229910001477 LaPO4 Inorganic materials 0.000 description 1
- 241000446313 Lamella Species 0.000 description 1
- 229910010158 Li2MO3 Inorganic materials 0.000 description 1
- 229910010177 Li2MoO3 Inorganic materials 0.000 description 1
- FUJCRWPEOMXPAD-UHFFFAOYSA-N Li2O Inorganic materials [Li+].[Li+].[O-2] FUJCRWPEOMXPAD-UHFFFAOYSA-N 0.000 description 1
- 229910001556 Li2Si2O5 Inorganic materials 0.000 description 1
- 229910001555 Li2Si3O7 Inorganic materials 0.000 description 1
- 229910007562 Li2SiO3 Inorganic materials 0.000 description 1
- 229910011312 Li3VO4 Inorganic materials 0.000 description 1
- 229910011981 Li4Mn5O12 Inorganic materials 0.000 description 1
- 229910002986 Li4Ti5O12 Inorganic materials 0.000 description 1
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- 229910052759 nickel Inorganic materials 0.000 description 1
- 150000004767 nitrides Chemical class 0.000 description 1
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- 229910052760 oxygen Inorganic materials 0.000 description 1
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- 230000035515 penetration Effects 0.000 description 1
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- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-UHFFFAOYSA-N 0.000 description 1
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 1
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- 235000011152 sodium sulphate Nutrition 0.000 description 1
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Images
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
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- C25B1/01—Products
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- C25B1/46—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in diaphragm cells
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Definitions
- Liquid resources such as geothermal brines contain a combination of desirable and undesirable metals, and recovery of the desirable metals can be facilitated by separation and handling of the undesirable metals.
- Desirable metals can be recovered from liquid resources using direct extraction technologies. This recovery of desirable metals can be facilitated by separating undesirable metals from the liquid resource. Handling of the separated undesirable metals can present a major challenge.
- This invention relates to separation, handling, and disposal of undesirable metals to facilitate recovery of desirable metals including lithium. Undesirable metals may be precipitated at high pH and separated from the liquid resource to facilitate recovery of the desirable metals, and then the precipitated undesirable metals may be redissolved and recombined with the liquid resource for disposal.
- a process for recovering a desirable metal from a liquid resource comprising: a) precipitating an undesirable metal from the liquid resource to form an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering said desirable metal from the feed liquid to form a raffinate; and d) redissolving said undesirable metal precipitate into said raffinate to form a raffinate mixture.
- said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metal comprises lithium.
- said undesirable metal comprises a transition metal.
- said precipitating comprises adding a base to the liquid resource.
- said precipitating comprises adding a base and/or an oxidant to the liquid resource.
- said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource.
- said precipitating comprises adding air and/or hydrogen peroxide to the liquid resource.
- said redissolving comprises combining an acid with said undesirable metal precipitate.
- said combining an acid with said undesirable metal precipitate occurs 1) prior to combining said undesirable metal precipitate with said raffinate, or 2) after combining said undesirable metal precipitate with said raffinate.
- the acid comprises hydrochloric acid and/or sulfuric acid.
- said acid and/or said base are produced with an electrochemical cell.
- the electrochemical cell comprises electrodes and membranes.
- said acid and/or said base are produced from a salt solution.
- said acid and/or said base are produced by splitting said salt solution.
- said salt solution comprises a sodium chloride solution.
- said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
- the process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution.
- said precipitating comprises adding chemicals to the liquid resource.
- said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, the process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, the process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground.
- a process for separating an undesirable metal from a liquid resource comprising: a) adding a base to said liquid resource to precipitate said undesirable metal thereby forming an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering a desirable metal from the feed liquid; and d) combining an acid to said undesirable metal precipitate to form a solution of redissolved undesirable metals for disposal.
- said recovering comprises contacting said feed liquid with ion exchange particles that absorbs said desirable metal while releasing protons.
- said desirable metal comprises lithium.
- said undesirable metal comprises a transition metal.
- the process further comprises adding an oxidant with said base to said liquid resource.
- said base comprises NaOH and/or Ca(OH) 2 to the liquid resource.
- said oxidant comprises air and/or hydrogen peroxide to the liquid resource.
- the acid comprises hydrochloric acid and/or sulfuric acid.
- said acid and/or said base are produced with an electrochemical cell.
- the electrochemical cell comprises electrodes and membranes.
- said acid and/or said base are produced from a salt solution.
- said acid and/or said base are produced by splitting said salt solution.
- the salt solution comprises a sodium chloride solution.
- said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
- the process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution.
- said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof.
- said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof.
- said separating of the undesirable metal precipitate comprises using a centrifuge.
- said disposal comprises injecting the solution of redissolved undesirable metals underground.
- the liquid resource is obtained from a reservoir.
- the liquid resource is pumped out of the reservoir.
- said disposal comprises injecting the solution of redissolved undesirable metals into said reservoir.
- the reservoir is located underground.
- a process for recovering lithium from a liquid resource comprising: a) precipitating a transition metal from said liquid resource to form a transition metal precipitate; b) separating said transition metal precipitate from the liquid resource to form a feed liquid; c) recovering said lithium from said feed liquid to form a raffinate, wherein said recovering of lithium comprises contacting said feed liquid with ion exchange particles that absorb said lithium while releasing protons; and d) redissolving said transition metal precipitate into said raffinate to form a raffinate mixture.
- said precipitating comprises adding a base to the liquid resource.
- said precipitating comprises adding a base and an oxidant to the liquid resource.
- said precipitating comprises adding NaOH and/or Ca(OH) 2 to the liquid resource. In some embodiments, said precipitating comprises adding air or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with the transition metal precipitate. In some embodiments, said combining an acid with said transition metal precipitate occurs 1) prior to combining said transition metal precipitate with said raffinate, or 2) after combining said transition metal precipitate with said raffinate. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes.
- said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, said salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, the process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said precipitating comprises adding chemicals to the liquid resource.
- said separating of said transitional metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In some embodiments, said separating of said transitional metal comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of said transitional metal comprises using a centrifuge. In some embodiments, the process further comprising injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, the process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground.
- said desirable metal comprises lithium.
- said undesirable metals comprise iron and/or manganese.
- the desirable metal comprises Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, or any combination thereof.
- the undesirable metal comprises Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, or any combination thereof.
- the desirable metal is different from the undesirable metal.
- FIG. 1 illustrates a system for precipitating undesirable metals from a liquid resource, separating precipitated undesirable metals from the liquid resource using sedimentation, recovering desirable metals from the liquid resource, and redissolving the undesirable metals in the liquid resource.
- FIG. 2 illustrates a system for precipitating undesirable metals from a liquid resource, separating precipitated undesirable metals from the liquid resource using a hydrocyclone, recovering desirable metals from the liquid resource, and redissolving the undesirable metals in the liquid resource.
- FIG. 3 illustrates a system for precipitating undesirable metals from a liquid resource, separating precipitated undesirable metals from the liquid resource using a centrifuge, recovering desirable metals from the liquid resource, and redissolving the undesirable metals in the liquid resource.
- lithium lithium ion
- Li + lithium ion
- hydrogen hydrogen ion
- proton hydrogen ion
- H ⁇ hydrogen ion
- liquid resource and “brine” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary.
- the term “about” refers to an amount that is near the stated amount by 10%, 5%, or 1%, including increments therein.
- Desirable metals can be recovered from liquid resources using direct extraction technologies. This recovery of desirable metals can be facilitated by separating undesirable metals from the liquid resource. Handling of the separated undesirable metals can present a major challenge.
- This invention relates to separation, handling, and disposal of undesirable metals to facilitate recovery of desirable metals including lithium. Undesirable metals may be precipitated at high pH and separated from the liquid resource to facilitate recovery of the desirable metals, and then the precipitated undesirable metals may be redissolved and recombined with the liquid resource for disposal.
- the liquid resource refers to a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof
- the liquid resource is at a temperature of ⁇ 10 to 400° C. In one embodiment, the liquid resource is at a temperature of ⁇ 10 to 20° C., 20 to 50° C., 50 to 100° C., 100 to 200° C., or 200 to 400° C. In one embodiment, the liquid resource is heated or cooled to precipitate or dissolve species in the liquid resource, or to facilitate removal of metals from the liquid resource.
- the liquid resource contains lithium at a concentration between 0 to 2000 mg/L. In one embodiment, the liquid resource contains lithium at a concentration of less than 1 mg/L, 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or greater than 2,000 mg/L. In one embodiment, the liquid resource contains calcium at a concentration between 100 to 150,000 mg/L. In one embodiment, the liquid resource contains calcium at a concentration of 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 150,000 mg/L, or greater than 150,000 mg/L. In one embodiment, the liquid resource contains potassium at a concentration between 100 to 150,000 mg/L. In one embodiment, the liquid resource contains potassium at a concentration of 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 150,000 mg/L, or greater than 150,000 mg/L.
- the liquid resource contains iron at a concentration between 0 to 50,000 mg/L. In one embodiment, the liquid resource contains iron at a concentration of less than 1 mg/L, 1 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, or greater than 50,000 mg/L. In one embodiment, the liquid resource contains manganese at a concentration between 0 to 50,000 mg/L. In one embodiment, the liquid resource contains manganese at a concentration of less than 1 mg/L, 1 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, or greater than 50,000 mg/L. In one embodiment, the liquid resource contains lead at a concentration between 0 to 2,000 mg/L. In one embodiment, the liquid resource contains lead at a concentration of less than 1 mg/L, 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or greater than 2,000 mg/L.
- the liquid resource is treated to remove certain metals to produce a feed liquid.
- the feed liquid contains iron at a concentration between 0 to 1,000 mg/L. In one embodiment, the feed liquid contains iron at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains manganese at a concentration between 0 to 1,000 mg/L.
- the feed liquid contains manganese at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains lead at a concentration between 0 to 1,000 mg/L. In one embodiment, the feed liquid contains lead at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains zinc at a concentration between 0 to 1,000 mg/L.
- the feed liquid contains zinc at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains lithium at a concentration between 0 to 2,000 mg/L. In one embodiment, the feed liquid contains lithium at a concentration of 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or greater than 2,000 mg/L.
- the feed liquid is processed to recover metals such as lithium and yield a spent brine or raffinate.
- the raffinate contains residual quantities of the recovered metals at a concentration between 0 to 1,000 mg/L. In one embodiment, the raffinate contains residual quantities of the recovered metals at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
- the pH of the liquid resource, feed liquid, and/or raffinate is corrected to less than 0, 0 to 1, 1 to 2, 2 to 4, 4 to 6, 6 to 8, 4 to 8, 8 to 9, 9 to 10, 9 to 11, or 10 to 12. In one embodiment, the pH of the liquid resource, feed liquid, and/or raffinate is corrected to less than about 4, 4 to 6, 6 to 8, 4 to 8, 8 to 9, 9 to 10, 9 to 11, or 10 to 12. In one embodiment, the pH of the liquid resource, feed liquid, and/or raffinate is corrected to precipitate or dissolve metals.
- At least one metal is precipitated from the liquid resource to form at least one precipitate.
- the precipitates include transition metal hydroxides, oxy-hydroxides, sulfide, flocculants, aggregate, agglomerates, or combinations thereof.
- the precipitates include Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, other metals, or any combination thereof.
- the precipitates are concentrated into a slurry, a filter cake, a wet filter cake, a dry filter cake, a dense slurry, and/or a dilute slurry.
- the precipitates contain iron at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain iron at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain manganese at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain manganese at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain lead at a concentration between 0 to 800,000 mg/kg.
- the precipitates contain lead at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain arsenic at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain arsenic at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain magnesium at a concentration between 0 to 800,000 mg/kg.
- the precipitates contain magnesium at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
- the precipitates contain Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals at a concentration between 0 to 800,000 mg/kg.
- the precipitates contain Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
- the precipitates are toxic and/or radioactive.
- precipitates are redissolved by combining the precipitates with at least one acid. In one embodiment, precipitates are redissolved by combining the precipitates with at least one acid in a mixing apparatus. In one embodiment, precipitates are redissolved by combining the precipitates with at least one acid using a high-shear mixer.
- Lithium is an essential element for batteries and other technologies. Lithium is found in a variety of liquid resources, including natural and synthetic brines and leachate solutions from minerals, clays, and recycled products. Lithium is optionally extracted from such liquid resources using an ion exchange process based on inorganic ion exchange materials. These inorganic ion exchange materials absorb lithium from a liquid resource while releasing hydrogen, and then elute lithium in at least one acid while absorbing hydrogen. This ion exchange process is optionally repeated to extract lithium from a liquid resource and yield a concentrated lithium solution. The concentrated lithium solution is optionally further processed into chemicals for the battery industry or other industries.
- Ion exchange materials are optionally formed into beads and the beads are optionally loaded into ion exchange columns, stirred tank reactors, other reactors, or reactor system for lithium extraction.
- Alternating flows of a liquid resource e.g., brine
- acid e.g., acid
- a liquid resource e.g., brine
- acid e.g., acid
- other solutions e.g., acid, and other solutions
- the ion exchange material absorbs lithium while releasing hydrogen, where both the lithium and hydrogen are cations.
- the release of hydrogen during lithium uptake will acidify the liquid resource and limit lithium uptake unless the pH of the liquid resource is optionally maintained in a suitable range to facilitate thermodynamically favorable lithium uptake and concomitant hydrogen release.
- pH of the liquid resource is maintained near a set-point through addition of base to neutralize protons released from the ion exchange material into the liquid resource.
- bases such as NaOH, Ca(OH) 2 , CaO, KOH, or NH 3 are optionally added to the liquid resource as solids, aqueous solutions, or in other forms.
- bases such as NaOH, Ca(OH) 2 , CaO, KOH, or NH 3
- addition of base to the liquid resource can cause precipitation of solids, such as Mg(OH) 2 or Ca(OH) 2 , which can cause problems for the ion exchange reaction.
- precipitation can remove base from solution, leaving less base available in solution to neutralize protons and maintain pH in a suitable range for lithium uptake in the ion exchange column.
- precipitates that form due to base addition can clog the ion exchange column, including clogging the surfaces and pores of ion exchange beads and the voids between ion exchange beads. This clogging can prevent lithium from entering the beads and being absorbed by the ion exchange material. The clogging can also cause large pressure heads in the column.
- precipitates in the column dissolve during acid elution and thereby contaminate the lithium concentrate produced by the ion exchange system.
- an ideal pH range for the liquid resource is optionally 5 to 7, a preferred pH range is optionally 4 to 8, and an acceptable pH range is optionally 1 to 9.
- an pH range for the liquid resource is optionally about 1 to about 14, about 2 to about 13, about 3 to about 12, about 4 to about 12, about 4.5 to about 11, about 5 to about 10, about 5 to about 9, about 2 to about 5, about 2 to about 4, about 2 to about 3, about 3 to about 8, about 3 to about 7, about 3 to about 6, about 3 to about 5, about 3 to about 4, about 4 to about 10, about 4 to about 9, about 4 to about 8, about 4 to about 7, about 4 to about 6, about 4 to about 5, about 5 to about 6, about 5 to about 7, about 5 to about 8, about 6 to about 7, about 6 to about 8, or about 7 to about 8.
- Direct extraction technologies can be used to recover one or more desirable metals from liquid resources.
- direct extraction technologies include ion exchange technologies, absorption technologies, solvent extraction technologies, membrane technologies, direct precipitation technologies, and combinations thereof.
- desirable metals include Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- liquid resources contain one or more undesirable metals.
- undesirable metals include Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W,M n, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- one or more metals are undesirable for a certain process but are desirable for a different process.
- ion exchange materials are used to recover lithium from a liquid resource.
- metals such as iron, manganese, and/or other metals interfere with the lithium recovery process and are therefore undesirable to have in the liquid resource during lithium recovery.
- undesirable metals such as iron and manganese are precipitated from the liquid resource and the resulting precipitates are separated from the liquid resource to create a feed liquid that has a reduced concentration of these undesirable metals, so as to facilitate recovery of lithium and/or other desirable metals from the feed liquid.
- the precipitated iron, manganese, and/or other undesirable metals present a challenge related to low value and high disposal cost.
- the precipitated iron, manganese, and/or other undesirable metals may be redissolved for disposal.
- the precipitated iron, manganese, and/or other undesirable metals may be precipitated from the liquid resource by the addition of at least one base, such as Ca(OH) 2 and/or NaOH.
- the precipitated iron, manganese, and/or other undesirable metals may be redissolved for disposal using at least one acid, such as HCl and/or H 2 SO 4 .
- metals are recovered from a liquid resource using multiple precipitation steps to remove desirable and/or undesirable metals from the liquid resource, and said undesirable and/or desirable metals may be removed and recombined with the resulting processed liquid resource (e.g., feed liquid or raffinate as described herein).
- metals are recovered from a liquid resource using multiple precipitation steps to remove desirable and undesirable metals from the liquid resource, and said undesirable metals may be removed and recombined with the resulting processed liquid resource (e.g., liquid resource depleted of desirable metals, or feed liquid, or raffinate as described herein).
- desirable metals are precipitated from a liquid resource while undesirable metals remain in the liquid resource.
- desirable metals are co-precipitated from a liquid resource with undesirable metals to form a raffinate, and then the desirable and/or undesirable metals may be redissolved in said raffinate.
- multiple undesirable metals are precipitated from a liquid resource in subsequent steps using a combination of at least one base, at least one oxidant, a specified temperature, chemicals, membranes, and/or solid-liquid separation devices.
- undesirable metals are 1) precipitated from a liquid resource, 2) removed from the liquid resource, 3) re-dissolved (e.g., in a solution), and 4) mixed with another liquid for disposal.
- undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, followed by removal of the resulting solids (via said precipitation of the undesirable metals) from the liquid resource, followed by redissolution of the resulting solids by addition of acid, followed by mixing of the redissolved undesirable metals with another liquid, and followed by disposal of said another liquid mixed with the re-dissolved undesirable metals.
- undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, followed by removal of the resulting solids from the liquid resource, followed by redissolution of the resulting solids (via precipitation of the undesirable metals) by addition of acid, followed by mixing of the redissolved undesirable metals with waste water, and followed by disposal of the waste water.
- redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids.
- redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal.
- solids of undesirable metals may be dissolved in raffinate, waste water, liquid resource, water, or other liquids for disposal.
- undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal.
- metals such as iron, manganese, lead, zinc, and/or other metals are precipitated from the liquid resource (e.g., brine) by adding at least one base and optionally at least one oxidant to the liquid resource, wherein the precipitated metals are separated from the liquid resource to form a feed liquid, lithium is recovered from the feed liquid to form a raffinate, and then the precipitated metals are dissolved into the raffinate for reinjection.
- the precipitated metals are separated from the liquid resource using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
- the raffinate is reinjected underground for disposal, wherein the raffinate is reinjected into the original reservoir from where the liquid resource was obtained, and/or into a different reservoir than from where the liquid resource was obtained.
- undesirable metals are removed from the liquid resource using ion exchange materials.
- the undesirable metals are eluted from ion exchange materials using acid, salt solution, or combinations thereof.
- the undesirable metals are separated from the eluate using nano-filtration membranes, precipitation, or combinations thereof.
- undesirable metals or other metals are eluted from ion exchange materials using a solution of sodium chloride, wherein the metals (undesirable metals or other metals) are removed from the eluate using nano-filtration membranes, such that the eluate with metals removed can be reused to elute metals from the ion exchange materials.
- nano-filtration membranes produce a retentate containing dissolved metals that can be separated and reinjected into a reservoir.
- nano-filtration membranes produce a retentate containing dissolved metals that can be mixed with a processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof.
- a processed liquid resource e.g., raffinate as described herein
- the precipitated and/or separated undesirable metals are dissolved into the raffinate using at least one acid. In one embodiment, the precipitated and/or separated undesirable metals are dissolved into the raffinate using hydrochloric acid and/or sulfuric acid. In one embodiment, the undesirable metals are precipitated from the liquid resource using at least one base. In one embodiment, the undesirable metals are precipitated from the liquid resource using sodium hydroxide, calcium oxide, and/or calcium hydroxide.
- the acid is produced using an electrochemical cell, an electrochemical membrane cell, an electrolytic cell, or combinations thereof. In one embodiment, the acid is produced by combusting sulfur. In one embodiment, the base is produced using an electrochemical cell, an electrochemical membrane cell, an electrolytic cell, or combinations thereof. In one embodiment, the base is produced by roasting lime. In one embodiment, the acid and base are both produced using an electrochemical cell, an electrochemical membrane cell, an electrolytic cell, or combinations thereof.
- undesirable metals such as iron, manganese, lead, zinc, or other metals are precipitated from the liquid resource by adding at least one base and optionally at least one oxidant to the liquid resource, wherein the precipitated metals are separated from the liquid resource to form a feed liquid, desirable metals are recovered from the feed liquid to form a raffinate, and then the undesirable metals are dissolved into the raffinate for disposal (e.g., reinjection into a reservoir underground, such as the reservoir from where the liquid resource was obtained from).
- metals undesirable metals or other metals
- at least one chemical precipitate such as hydroxide, phosphates, sulfides, and/or other chemicals.
- At least one oxidant is used to facilitate precipitation of the undesirable metals, wherein the at least one oxidant includes hydrogen peroxide, air, oxygen, and/or other oxidants.
- at least one flocculant is used to agglomerate precipitates to facilitate solid-liquid separation.
- precipitated undesirable metals are agglomerated using flocculants, coagulants, or combinations thereof to facilitate separation of the precipitated undesirable metals from the liquid resource.
- the precipitated metals are separated from the liquid resource using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
- the raffinate is reinjected underground for disposal, wherein the raffinate is reinjected into the original reservoir of the liquid resource, and/or into a different reservoir of the liquid resource.
- the liquid resource is processed to remove metals to facilitate recovery of other metals.
- the liquid resource is processed to remove metals (e.g., undesirable metals) to facilitate recovery of other metals such as lithium, manganese, zinc, lead, iron, gold, platinum, rubidium, or other metals.
- the liquid resource is processed to remove undesirable metals, forming a feed liquid, to facilitate recovery of desirable metals from said feed liquid, and after recovery of the desirable metals, thereby forming a raffinate, the undesirable metals are redissolved in said raffinate to form a raffinate mixture.
- the undesirable metals are redissolved in the raffinate, forming a raffinate mixture, which is injected underground for disposal. In some embodiments, the undesirable metals are redissolved in the raffinate and injected underground for disposal into the reservoir from which they originated. In some embodiments, the undesirable metals are redissolved in the raffinate and injected underground for disposal into a reservoir different from the reservoir in which they originated.
- undesirable metals or transition metals are precipitated from a liquid resource, and then redissolved in a processed liquid resource (e.g.,raffinateas described herein), liquid resource, water, waste water, another liquid, or combinations thereof by combining the precipitates with acid to form a concentrated solution and then mixing the concentrated solution with the processed liquid resource (e.g., raffinate), liquid resource, water, waste water, another liquid, or combinations thereof.
- a processed liquid resource e.g.,raffinateas described herein
- liquid resource e.g., water, waste water, another liquid, or combinations thereof.
- undesirable metals or transition metals are precipitated from a liquid resource and then redissolved in a processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof by combining the precipitates with the processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof, to form a mixture, and then adding acid to said mixture.
- a processed liquid resource e.g., raffinate as described herein
- liquid resource water, waste water, another liquid, or combinations thereof
- different sets of undesirable metals are precipitated from and separated from the liquid resource at different pH ranges.
- Fe and Mn are precipitated and separated from the liquid resource at different pH points.
- Fe and Mn are precipitated and separated from the liquid resource at one pH range, and Pb and Zn are precipitated and separated from the liquid resource at another pH range.
- Fe and Mn are precipitated and separated from the liquid resource at one pH range, and Pb is precipitated and separated from the liquid resource at another pH range.
- lithium is recovered from a liquid resource, such as a brine, using an ion exchange material.
- a liquid resource such as a brine
- one or more ion exchange columns are loaded with a fixed or fluidized bed of ion exchange material.
- the ion exchange column is a cylindrical construct with entry and exit ports.
- the ion exchange column is optionally a non-cylindrical construct with entry and exit ports.
- the ion exchange column is a tank.
- the ion exchange column optionally has entry and exit ports for brine pumping, and additional doors or hatches for loading and unloading ion exchange material to and from the column.
- the ion exchange column is optionally equipped with one or more security devices to decrease the risk of loss, spilling, or theft of the ion exchange material.
- the material can reversibly absorb lithium from brine and release lithium in acid.
- the ion exchange material is comprised of particles that are optionally protected with coating material such as SiO 2 , ZrO 2 , or TiO 2 to limit dissolution or degradation of the ion exchange material.
- the ion exchange material may be in the form of a powder.
- the material may be in the form of beads.
- the beads contain a structural component such as an acid-resistant polymer that binds the ion exchange materials.
- the beads contain pores that facilitate penetration of brine, acid, aqueous, and other solutions into the beads to deliver lithium and hydrogen to and from the bead or to wash the bead.
- the bead pores are structured to form a connected network of pores with a distribution of pore sizes and are structured by incorporating filler materials during bead formation and later removing that filler material in a liquid or gas.
- the system is a recirculating batch system, which comprises an ion exchange column that is connected to one or more tanks for mixing base into the brine, settling out any precipitates following base addition, and storing the brine prior to reinjection into the ion exchange column or the other tanks.
- the brine is loaded into one or more tanks, pumped through the ion exchange column, pumped through a series of tanks, and then returned to the ion exchange column in a loop.
- the brine optionally traverses this loop repeatedly.
- the brine is recirculated through the ion exchange column to enable optimal lithium uptake by the material.
- base is added to the brine in such a way that pH is maintained at an adequate level for lithium uptake and in such a way that the amount of base-related precipitates in the ion exchange column is minimized.
- the ion exchange material comprises coated ion exchange particles, uncoated ion exchange particles or combinations thereof.
- a coating material comprises a polymer.
- the coating material comprises a chloro-polymer, a fluoro-polymer, a chloro-fluoro-polymer, a hydrophilic polymer, a hydrophobic polymer, co-polymers thereof, mixtures thereof, or combinations thereof.
- the coating material comprises a carbide, a nitride, an oxide, a phosphate, a fluoride, a polymer, carbon, a carbonaceous material, or combinations thereof.
- the coating material comprises Nb 2 O 5 , Ta 2 O 5 , MoO 2 , TiO 2 , ZrO 2 , MoO 2 , SnO 2 , SiO 2 , Li 2 O, Li 2 TiO 3 , Li 2 ZrO 3 , Li 2 MoO 3 , LiNbO 3 , LiTaO 3 , Li 2 SiO 3 , Li 2 Si 2 O 5 , Li 2 MnO 3 , ZrSiO 4 , AlPO 4 , LaPO 4 , ZrP 2 O 7 , MoP 2 O 7 , Mo 2 P 3 O 12 , BaSO 4 , AlF 3 , SiC, TiC, ZrC, Si 3 N 4 , ZrN, BN, carbon, graphitic carbon, a
- the coating material comprises polyvinylidene difluoride, polyvinyl chloride, a fluoro-polymer, a chloro-polymer, or a fluoro-chloro-polymer.
- the coating material comprises TiO 2 , ZrO 2 , SiO 2 MoO 2 , Li 2 TiO 3 , Li 2 ZrO 3 , Li 2 MnO 3 , ZrSiO 4 , or LiNbO 3 , AlF 3 , SiC, Si 3 N 4 , graphitic carbon, amorphous carbon, diamond-like carbon, or combinations thereof.
- the coating material comprises TiO 2 , SiO 2 , or ZrO 2 .
- the coating material comprises TiO 2 .
- the coating material comprises SiO 2 .
- the coating material comprises ZrO 2 .
- a coating material comprises a co-polymer, a block co-polymer, a linear polymer, a branched polymer, a cross-linked polymer, a heat-treated polymer, a solution processed polymer, co-polymers thereof, mixtures thereof, or combinations thereof
- a coating material comprises polyethylene, low density polyethylene, high density polyethylene, polypropylene, polyester, polytetrafluoroethylene (PTFE), types of polyamide, polyether ether ketone (PEEK), polysulfone, polyvinylidene fluoride (PVDF), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), polybutadiene, acrylonitrile butadiene styrene (ABS), polyvinyl chloride (PVC), ethylene tetrafluoroethylene polymer (ETFE), poly(chlorotrifluoroethylene) (PCTFE), ethylene chlorotrifluoro ethylene (Halar), polyvinylfluoride (PVF), fluorinated ethylene-propylene (FEP), perfluorinated elastomer, chlorotrifluoroethylenevinylidene fluoride (FKM), perfluoropolylene
- a coating material comprises polyvinylidene fluoride (PVDF), polyvinyl chloride (PVC), ethylene chlorotrifluoro ethylene (Halar®), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), acrylonitrile butadiene styrene (ABS), expanded polystyrene (EPS), polyphenylene sulfide, sulfonated polymer, carboxylated polymer, other polymers, co-polymers thereof, mixtures thereof, or combinations thereof
- PVDF polyvinylidene fluoride
- PVC polyvinyl chloride
- Halar® ethylene chlorotrifluoro ethylene
- PVPCS poly (4-vinyl pyridine-co-styrene)
- PS polystyrene
- ABS acrylonitrile butadiene styrene
- EPS expanded polystyrene
- the ion exchange material is a porous ion exchange material. In one embodiment, the ion exchange material is in the form of porous beads. In one embodiment, the ion exchange material is in a powder form. In one embodiment, the acid solution is a solution of H 2 SO 4 or HCl.
- lithium or other metals are recovered from the liquid resource (e.g., brine) using a porous structure for ion exchange comprising: a) a structural support; and b) a plurality of particles selected from coated ion exchange particles, uncoated ion exchange particles, and a combination thereof.
- the structural support comprises a polymer, an oxide, a phosphate, or combinations thereof. In some embodiments, the structural support comprises a polymer.
- the polymer is polyvinylidene fluoride, polyvinyl fluoride, polyvinyl chloride, polyvinylidene chloride, a chloro-polymer, a fluoro-polymer, a fluoro-chloro-polymer, polyethylene, polypropylene, polyphenylene sulfide, polytetrafluoroethylene, sulfonated polytetrafluoroethylene, polystyrene, polydivinylbenzene, polybutadiene, a sulfonated polymer, a carboxylated polymer, polyacrylonitrile, Nafion®, copolymers thereof, or combinations thereof.
- lithium or other metals are recovered from the brine using a batch, semi-batch, semi-continuous, or continuous process.
- ion exchange beads are moved through the system in an opposite direction of the brine.
- the precipitated metals are separated from the liquid resource using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
- precipitated metals are removed from the liquid resource using a filter.
- the filter comprises a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof.
- the filter uses a scroll and/or a vibrating device.
- the filter is horizontal, vertical, and/or may use a siphon.
- a filter cake is prevented, limited, or removed by using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter.
- the precipitated metals and a liquid are moved tangentially to the filter to limit cake growth.
- gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation are used before, during, and/or after filtering to prevent cake formation.
- a filter comprises a screen, a metal screen, a sieve, a sieve bend, a bent sieve, a high frequency electromagnetic screen, a resonance screen, or combinations thereof.
- one or more particle traps are a solid-liquid separation apparatus.
- one or more solid-liquid separation apparatuses may be used in series or parallel.
- a dilute slurry of precipitated metals is removed from a tank, transferred to an external solid-liquid separation apparatus, and separated into a concentrated slurry and a solution with low or no suspended solids.
- the concentrated slurry of precipitated metals is returned to the tank or transferred to a different tank.
- the precipitated metals are transferred from a liquid resource tank to another liquid resource tank, from an acid tank to another acid tank, from a washing tank to another washing tank, from a liquid resource tank to a washing tank, from a washing tank to an acid tank, from an acid tank to a washing tank, or from an acid tank to a liquid resource tank.
- solid-liquid separation apparatuses for separating precipitates from a liquid resource use gravitational sedimentation.
- solid-liquid separation apparatuses include a settling tank, a thickener, a clarifier, a gravity thickener.
- solid-liquid separation apparatuses are operated in batch mode, semi-batch mode, semi-continuous mode, or continuous mode.
- solid-liquid separation apparatuses include a circular basin thickener with the slurry of precipitated metals entering through a central inlet, such that the slurry is dispersed into the thickener with one or more raking components that rotate and concentrate the ion exchange particles into a zone where the particles can leave through the bottom of the thickener.
- solid-liquid separation apparatuses include a deep cone, a deep cone tank, a deep cone compression tank, or a tank wherein the slurry is compacted by weight.
- solid-liquid separation apparatuses include a tray thickener with a series of thickeners oriented vertically with a center axle and raking components.
- solid-liquid separation apparatuses include a lamella type thickener with inclined plates and/or tubes that may be smooth, flat, rough, or corrugated.
- solid-liquid separation apparatuses include a gravity clarifier that may be a rectangular basin with feed at one end and overflow at the opposite end optionally with paddles and/or a chain mechanism to move particles.
- the solid-liquid separation apparatuses may be a particle trap.
- the solid-liquid separation apparatuses use centrifugal sedimentation.
- solid-liquid separation apparatuses include a tubular centrifuge, a multi-chamber centrifuge, a conical basket centrifuge, a scroll-type centrifuge, a sedimenting centrifuge, and/or a disc centrifuge.
- precipitated metals are discharged continuously or intermittently from the centrifuge.
- the solid-liquid separation apparatus is a hydrocyclone.
- solid-liquid separation apparatus is an array of hydrocyclones or centrifuges in series and/or in parallel.
- sumps are used to reslurry the precipitated metals.
- the hydrocyclones may have multiple feed points.
- a hydrocyclone is used upside down.
- liquid is injected near the apex of the cone of a hydrocyclone to improve sharpness of cut.
- a weir rotates in the center of the particle trap with a feed of slurry of precipitated metals entering near the middle of the apparatus, wherein the precipitated metals get trapped at the bottom and center of the apparatus due to a “teacup effect”.
- At least one base is used to precipitate undesirable metals from the liquid resource, wherein the precipitated metals are separated from the liquid resource, and then the precipitated metals are redissolved into a processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof using at least one acid.
- a processed liquid resource e.g., raffinate as described herein
- the acid and base are generated using an electrochemical cell.
- the acid and base are generated using electrodes.
- the acid and base are generated using a membrane.
- said membrane comprises an ion-conducting membrane.
- said ion-conducting membrane is a cation-conducting membrane, an anion-conducting membrane or combinations thereof.
- said ion-conducting membrane comprises sulfonated tetrafluoroethylene-based fluoropolymer-copolymer, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, or combinations thereof.
- said anion-conducting membrane comprises a functionalized polymer structure.
- said functionalized polymer structure comprises polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
- said cation-conducting membrane allows for transfer of lithium ions but prevents transfer of anion groups.
- said ion-conducting membrane has a thickness from about 1 ⁇ m to about 1000 ⁇ m. In one embodiment, said ion-conducting membrane has a thickness from about 1 mm to about 10 mm.
- said electrodes are comprised of titanium, niobium, zirconium, tantalum, magnesium, titanium dioxide, oxides thereof, or combinations thereof. In one embodiment, said electrodes further comprise a coating of platinum, TiO 2 , ZrO 2 , Nb 2 O 5 , Ta 2 O 5 , SnO 2 , IrO 2 , RuO 2 , mixed metal oxides, graphene, derivatives thereof, or combinations thereof
- a chlor-alkali setup is used to generate HCl and NaOH from an aqueous NaCl solution.
- the HCl is used to elute lithium from an ion exchange system for selective lithium uptake to produce a lithium eluate solution.
- the NaOH from the chlor-alkali setup is used to control the pH of the brine in the ion exchange system for selective lithium uptake.
- the NaOH is used to precipitate impurities from a lithium eluate solution.
- the system includes one or more electrochemical or electrolysis systems.
- electrochemical and “electrolysis” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary.
- an electrolysis system is comprised of one or more electrochemical cells.
- an electrochemical system is used to produce HCl and NaOH.
- an electrochemical system converts a salt solution into acid in base.
- an electrochemical system converts a salt solution containing NaCl, KCl, and/or other chlorides into a base and an acid.
- a salt solution precipitated or recovered from the liquid resource e.g., brine
- the liquid resource e.g., brine
- an electrolysis system converts a lithium salt solution to form a lithium hydroxide solution, an acidified solution, and optionally a dilute lithium salt solution.
- the lithium salt solution is or is derived from a lithium eluate solution, produced by an ion exchange system that has optionally been concentrated and/or purified.
- acidified solution from an electrolysis system is returned to an ion exchange system to elute more lithium eluate solution.
- the integrated system includes one or more electrolysis systems.
- an electrolysis system is comprised of one or more electrodialysis cells.
- an electrolysis system converts a lithium salt solution to form a lithium hydroxide solution, an acidified solution, and optionally a dilute lithium salt solution.
- the lithium salt solution is or is derived from a lithium eluate solution, produced by an ion exchange system that has optionally been concentrated and/or purified.
- acidified solution from an electrolysis system is returned to an ion exchange system to elute more lithium eluate solution.
- a lithium salt solution contains unreacted acid from the ion exchange system.
- unreacted acid in the lithium salt solution from an ion exchange system passes through an electrolysis system and is further acidified to form an acidified solution.
- a lithium salt solution derived from an ion exchange system is purified to remove impurities without neutralizing the unreacted acid in the lithium salt solution and is then fed into an electrolysis system.
- an acidified solution produced by an electrolysis system contains lithium ions from the lithium salt solution fed into the electrolysis system. In one embodiment, an acidified solution containing lithium ions leaves the electrolysis system and is fed back to an ion exchange system to elute lithium and produce more lithium salt solution.
- the electrolysis cells are electrochemical cells.
- the membranes may be cation-conducting and/or anion-conducting membranes.
- the electrochemical cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
- the electrolysis cells are electrodialysis cells.
- the membranes may be cation-conducting and/or anion-conducting membranes.
- the electrodialysis cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
- the electrolysis cells are membrane electrolysis cells.
- the membranes may be cation-conducting and/or anion-conducting membranes.
- the membrane electrolysis cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
- the membrane electrolysis cell is a three-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions separating a compartment with an electrochemically reducing electrode from a central compartment and with an anion-conducting membrane that allows for transfer of anions ions separating a compartment with an electrochemically oxidizing electrode from the central compartment.
- the cation-conducting membrane prevents transfer of anions such as chloride, sulfate, or hydroxide.
- the anion-conducting membrane prevents transfer of cations such as lithium, sodium, or protons.
- the membranes may be comprised of Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof.
- the cation exchange membranes are comprised of a functionalized polymer structure which may be Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof.
- the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
- the membranes may be comprised of Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof.
- the cation exchange membranes are comprised of a functionalized polymer structure which may be Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof.
- the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof
- the membranes may be comprised of Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof.
- the cation exchange membranes are comprised of a functionalized polymer structure which may be Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof.
- the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
- an anion exchange membrane is comprised of a functionalized polymer structure.
- the polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
- the functional groups are part of the polymer backbone.
- the functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions.
- the functional group may be benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilised quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
- an anion exchange membrane is comprised of a functionalized polymer structure.
- the polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
- the functional groups are part of the polymer backbone.
- the functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions.
- the functional group may be benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilised quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
- an anion exchange membrane is comprised of a functionalized polymer structure.
- the polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof.
- the functional groups are part of the polymer backbone. In one embodiment of the membrane, functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions. In one embodiment of the membrane, the functional group may be benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilised quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
- the membrane may have a thickness of less than 10 ⁇ m, less than 50 ⁇ m, less than 200 ⁇ m, less than 400 ⁇ m, or less than 1,000 ⁇ m. In one embodiment of the membrane electrolysis cell, the membranes may have a thickness of greater than 1,000 ⁇ m.
- the membrane may have a thickness of about 1 ⁇ m to about 1000 ⁇ m, about 1 ⁇ m to about 800 ⁇ m, about 1 ⁇ m to about 600 ⁇ m, about 1 ⁇ m to about 400 ⁇ m, about 1 ⁇ m to about 200 ⁇ m, about 1 ⁇ m to about 100 ⁇ m, about 1 ⁇ m to about 90 ⁇ m, about 1 ⁇ m to about 80 ⁇ m, about 1 ⁇ m to about 70 ⁇ m, about 1 ⁇ m to about 60 ⁇ m, about 1 ⁇ m to about 50 ⁇ m, about 1 ⁇ m to about 40 ⁇ m, about 1 ⁇ m to about 30 ⁇ m, about 1 ⁇ m to about 20 ⁇ m, about 1 ⁇ m to about 15 ⁇ m, or about 1 ⁇ m to about 10 ⁇ m.
- the membrane may have a thickness of less than 10 ⁇ m, less than 50 ⁇ m, less than 200 ⁇ m, less than 400 ⁇ m, or less than 1,000 ⁇ m. In one embodiment of the electrochemical cell, the membranes may have a thickness of greater than 1,000 ⁇ m.
- the membrane may have a thickness of about 1 ⁇ m to about 1000 ⁇ m, about 1 ⁇ m to about 800 ⁇ m, about 1 ⁇ m to about 600 ⁇ m, about 1 ⁇ m to about 400 ⁇ m, about 1 ⁇ m to about 200 ⁇ m, about 1 ⁇ m to about 100 ⁇ m, about 1 ⁇ m to about 90 ⁇ m, about 1 ⁇ m to about 80 ⁇ m, about 1 ⁇ m to about 70 ⁇ m, about 1 ⁇ m to about 60 ⁇ m, about 1 ⁇ m to about 50 ⁇ m, about 1 ⁇ m to about 40 ⁇ m, about 1 ⁇ m to about 30 ⁇ m, about 1 ⁇ m to about 20 ⁇ m, about 1 ⁇ m to about 15 ⁇ m, or about 1 ⁇ m to about 10 ⁇ m.
- the membrane may have a thickness of less than 10 ⁇ m, less than 50 ⁇ m, less than 200 ⁇ m, less than 400 ⁇ m, or less than 1,000 ⁇ m. In one embodiment of the electrodialysis cell, the membranes may have a thickness of greater than 1,000 ⁇ m.
- the membrane may have a thickness of about 1 ⁇ m to about 1000 ⁇ m, about 1 ⁇ m to about 800 ⁇ m, about 1 ⁇ m to about 600 ⁇ m, about 1 ⁇ m to about 400 ⁇ m, about 1 ⁇ m to about 200 ⁇ m, about 1 ⁇ m to about 100 ⁇ m, about 1 ⁇ m to about 90 ⁇ m, about 1 ⁇ m to about 80 ⁇ m, about 1 ⁇ m to about 70 ⁇ m, about 1 ⁇ m to about 60 ⁇ m, about 1 ⁇ m to about 50 ⁇ m, about 1 ⁇ m to about 40 ⁇ m, about 1 ⁇ m to about 30 ⁇ m, about 1 ⁇ m to about 20 ⁇ m, about 1 ⁇ m to about 15 ⁇ m, or about 1 ⁇ m to about 10 ⁇ m.
- an electrolysis system contains electrolysis cells that may be two-compartment electrolysis cells or three-compartment electrolysis cells.
- the cell contains a first compartment that contains an electrochemically oxidizing electrode.
- a lithium salt solution enters the first compartment and is converted into an acidified solution.
- the cell contains a second compartment containing an electrochemically reducing electrode. This second compartment takes as an input a water or dilute LiOH solution, and produces as an output a more concentrated LiOH solution.
- the compartments are separated by a cation-conducting membrane that limits transport of anions.
- the cell contains a first compartment containing an electrochemically oxidizing electrode.
- the first compartment takes as an input water or a dilute salt solution, and produces as an output an acidified solution.
- the cell contains a second compartment containing an electrochemically reducing electrode. This second compartment takes as an input a water or dilute hydroxide solution, and produces as an output a more concentrated hydroxide solution.
- the cell contains a third compartment containing no electrode, which is located between the first and second compartment, and takes as an input a concentrated lithium salt solution, and produces as an output a dilute lithium salt solution.
- the first and the third compartments are separated by an anion-conducting membrane that limits transport of cations.
- the second and the third compartments are separated by a cation-conducting membrane that limits transport of anions.
- the electrodes may be comprised of titanium, niobium, zirconium, tantalum, magnesium, titanium dioxide, oxides thereof, or combinations thereof.
- the electrodes may be coated with platinum, TiO 2 , ZrO 2 , Nb 2 O 5 , Ta 2 O 5 , SnO 2 , IrO 2 , RuO 2 , PtO x , mixed metal oxides, graphene, derivatives thereof, or combinations thereof.
- the electrodes may be comprised of steel, stainless steel, nickel, nickel alloys, steel alloys, or graphite.
- the lithium salt solution is a LiCl solution optionally containing HCl.
- the electrochemically oxidizing electrode oxide s chloride ions to produce chlorine gas.
- the lithium salt solution is a Li 2 SO 4 solution optionally containing H 2 SO 4 .
- the electrochemically oxidizing electrode oxidizes water, hydroxide, or other species to produce oxygen gas.
- the electrochemically reducing electrode reduces hydrogen ions to produce hydrogen gas.
- the chamber containing the electrochemically reducing electrode produces a hydroxide solution or increases the hydroxide concentration of a solution.
- chlorine and hydrogen gas are burned to produce HCl in an HCl burner.
- the HCl burner is a column maintained at approximately 100-300 or 300-2,000 degrees Celsius.
- HCl produced in the HCl burner is cooled through a heat exchange and absorbed into water in an absorption tower to produce aqueous HCl solution.
- the HCl solution produced from the HCl burner is used to elute lithium from an ion exchange system.
- the pH of the acidified solution leaving the electrolysis cell may be 0 to 1, ⁇ 2 to 0, 1 to 2, less than 2, less than 1, or less than 0.
- the membrane electrolysis cell is an electrodialysis cell with multiple compartments. In some embodiments, the electrodialysis cell may have more than about two, more than about five, more than about 10, or more than about twenty compartments.
- NaCl is recovered from the liquid resource by removing water therefrom, and then cooling said liquid resource.
- water is removed from the liquid resource by reducing pressure, distillation, or combinations thereof.
- water is removed from the liquid resource using any separation process described herein and/or distillation.
- NaCl is recovered from the liquid resource by removing water therefrom, cooling said liquid resource, or combinations thereof.
- the base added to precipitate metals from the liquid resource may be calcium hydroxide or sodium hydroxide.
- the calcium hydroxide or sodium hydroxide is produced as described herein.
- the base may be added to the liquid resource as an aqueous solution with a base concentration that may be less than 1N, 1-2 N, 2-4 N, 4-10 N, 10-20 N, or 20-40 N.
- the base may be added to the liquid resource as a solid.
- the acid may be added to the precipitated metals to dissolve the precipitated metals before mixing the redissolved metals with a processed liquid resource (e.g., raffinate), liquid resource, water, waste water, another liquid, or combinations thereof.
- a processed liquid resource e.g., raffinate
- the acid may be added to the liquid resource to acidify the liquid resource, and the precipitated metals may be combined with the acidified liquid resource to redissolve the precipitated metals.
- the acid is produced as described herein.
- metals recovered from a liquid resource may be further processed downstream to produce high purity liquids and solids.
- metals recovered from the liquid resource may be purified with ion exchange, solvent extraction, membranes, filtration, or other purification technologies.
- metals may be converted from a dissolved form to a solid form.
- metals may be converted using precipitation, electrolysis, electrowinning, chelation, or crystallization.
- lithium may be converted from lithium chloride or lithium sulfate to lithium carbonate or lithium hydroxide.
- lithium may be purified by precipitating multivalent metals using sodium carbonate, by removing multivalent metals using ion exchange, by removing boron using ion exchange, by removing impurities using membranes, by removing impurities using solvent extraction, or combinations thereof.
- lithium may be converted from lithium chloride or lithium sulfate solution to a lithium carbonate solid by addition of sodium carbonate, sodium carbonate solution, carbon dioxide, sodium hydroxide, or combinations thereof.
- lithium may be converted form lithium sulfate to lithium hydroxide by addition of sodium hydroxide, crystallization of sodium sulfate, and then crystallization of lithium hydroxide.
- lithium may be converted from lithium carbonate to lithium hydroxide by addition of calcium hydroxide.
- FIG. 1 depicts an exemplary flowchart for separating transition metals from a liquid resource for a lithium recovery process described herein.
- a liquid resource e.g., raw brine ( 102 )
- the raw brine contains 50,000 mg/L Na, 50,000 mg/L Ca, 200 mg/L Li, 1,000 mg/L Fe, 800 mg/L Mn, 50 mg/L Pb, and other dissolved metals.
- An electrochemical cell (not shown) is used to convert NaCl into aqueous solutions of HCl and NaOH.
- the aqueous NaOH ( 104 ) is added to the brine to precipitate ( 106 ) Fe, Mn, and Pb, such that the raw brine becomes a slurry ( 108 ) comprising precipitates.
- the precipitates are separated from the raw brine using a flocculant and a gravity sedimentation tank ( 110 ) to form a feed liquid (feed brine ( 112 )) and a concentrated slurry ( 120 ) containing the precipitates.
- the feed brine ( 112 ) contains ⁇ 5 mg/L Fe, ⁇ 10 mg/L Mn, and ⁇ 10 mg/L Pb.
- the feed brine is processed ( 114 ) to recover lithium by contacting the feed brine with an ion exchange material, which selectivity absorbs the lithium.
- the lithium depleted brine is now a raffinate (e.g., spent brine 116 ).
- the HCl solution ( 118 ) is added to the concentrated slurry ( 120 ) containing the precipitates to redissolve ( 122 ) the precipitates.
- the redissolved metals (redissolved precipitates) are mixed with the raffinate 116 to form a raffinate mixture that is reinjected ( 124 ) into the geothermal reservoir.
- FIG. 2 depicts an exemplary flowchart for separating transition metals from a liquid resource using a hydrocyclone for a lithium recovery process described herein.
- a liquid resource e.g., raw brine ( 202 )
- the raw brine contains 80,000 mg/L Na, 30,000 mg/L Ca, 300 mg/L Li, 1,500 mg/L Fe, 1,200 mg/L Mn, and other dissolved metals.
- NaCl is recovered from the raw brine by removing water and cooling the brine (not shown).
- An electrochemical cell (not shown) is used to convert the NaCl into aqueous solutions of HCl and NaOH.
- the aqueous NaOH ( 204 ) is added to the raw brine to precipitate ( 206 ) Fe and Mn, such that the raw brine becomes a slurry ( 208 ) comprising precipitates.
- the precipitates are separated from the raw brine using a hydrocyclone ( 210 ) to form a feed liquid (feed brine ( 212 )) and a concentrated slurry ( 220 ) containing the precipitates.
- the feed brine ( 212 ) contains 2 mg/L Fe and 5 mg/L Mn.
- the feed brine is processed ( 214 ) to recover lithium by contacting the feed brine with an ion exchange material, which selectivity absorbs the lithium in an ion exchange column.
- the lithium depleted brine is now a raffinate (e.g., spent brine 216 ).
- a raffinate e.g., spent brine 216
- the concentrated slurry ( 220 ) containing the precipitates are added to the raffinate ( 216 ) and HCl ( 218 ) is added to the resulting mixture to redissolve ( 222 ) the precipitates into the raffinate, forming a raffinate mixture.
- the raffinate mixture is then reinjected ( 224 ) into the geothermal reservoir.
- FIG. 3 depicts an exemplary flowchart for separating transition metals from a liquid resource using a centrifuge for a lithium recovery process described herein.
- a liquid resource e.g., raw brine ( 302 )
- the raw brine contains 60,000 mg/L Na, 40,000 mg/L Ca, 200 mg/L Li, 1,800 mg/L Fe, 1,000 mg/L Mn, and other dissolved metals.
- An electrochemical cell (not shown) is used to convert the NaCl into aqueous solutions of HCl and NaOH.
- the aqueous NaOH ( 304 ) is added to the raw brine to precipitate ( 306 ) Fe and Mn such that the raw brine becomes a slurry ( 308 ) comprising precipitates.
- the precipitates are separated from the raw brine using a centrifuge to form a feed liquid (feed brine ( 312 )) and a concentrated slurry ( 320 ) containing the precipitates.
- the feed brine ( 312 ) contains 200 mg/L Li, 2 mg/L Fe, and 6 mg/L Mn.
- the feed brine is processed ( 314 ) to recover lithium by contacting the feed brine with an ion exchange material, which selectivity absorbs the lithium in an ion exchange column.
- the feed brine is depleted of lithium to form a raffinate (e.g., spent brine ( 316 )).
- HCl ( 318 ) is added to the concentrated slurry ( 320 ) to redissolve ( 322 ) the precipitates forming a transition metal concentrate, which is then mixed with the spent brine ( 316 ) to form a raffinate mixture.
- the raffinate mixture containing the redissolved transition metals is then reinjected ( 324 ) into the geothermal reservoir.
- a process for recovering a desirable metal from a liquid resource comprising: a) precipitating an undesirable metal from the liquid resource to form an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering said desirable metal from the feed liquid to form a raffinate; and d) redissolving said undesirable metal precipitate into said raffinate to form a raffinate mixture.
- said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metal comprises lithium.
- said undesirable metal comprises a transition metal.
- said desirable metals comprise lithium and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said undesirable metals comprise transition metals and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metals comprise lithium, said undesirable metals comprise transition metals, and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said precipitating comprises adding a base to the liquid resource. In some embodiments, said precipitating comprises adding a base and/or an oxidant to the liquid resource.
- said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air and/or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with said undesirable metal precipitate. In some embodiments, said combining an acid with said undesirable metal precipitate occurs 1) prior to combining said undesirable metal precipitate with said raffinate, or 2) after combining said undesirable metal precipitate with said raffinate. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said redissolving comprises adding hydrochloric acid or sulfuric acid to dissolve said undesirable metal precipitate.
- said precipitating comprises adding a base to the liquid resource, and said redissolving comprises combining an acid with the undesirable metal precipitate, wherein said acid and said base are produced with an electrochemical cell.
- said acid and/or said base are produced with an electrochemical cell.
- the electrochemical cell comprises electrodes and membranes.
- said acid and/or said base are produced from a salt solution.
- said acid and/or said base are produced by splitting said salt solution.
- said salt solution comprises a sodium chloride solution.
- said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
- said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution.
- said precipitating comprises adding chemicals to the liquid resource.
- said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof.
- said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, said process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground. In some embodiments, said process further comprises agglomerating the undesirable metal precipitate.
- said agglomerating comprises adding a flocculant to the liquid resource.
- said separating the undesirable metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof.
- said separating the undesirable metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, said separating the undesirable metal precipitate further comprises moving the undesirable metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the undesirable metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series.
- said precipitating of an undesirable metal forms a slurry comprising the undesirable metal precipitate and feed liquid.
- the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
- the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate.
- a plurality of desirable metals are separated from the feed liquid.
- the desirable metal is different from the undesirable metal.
- a process for separating an undesirable metal from a liquid resource comprising: a) adding a base to said liquid resource to precipitate said undesirable metal thereby forming an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering a desirable metal from the feed liquid; and d) combining an acid to said undesirable metal precipitate to form a solution of redissolved undesirable metals for disposal.
- said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metal comprises lithium.
- said undesirable metal comprises a transition metal.
- said process further comprises an oxidant with said base to said liquid resource.
- said base comprises NaOH and/or Ca(OH)2 to the liquid resource.
- said oxidant comprises air and/or hydrogen peroxide to the liquid resource.
- the acid comprises hydrochloric acid and/or sulfuric acid.
- said acid and/or said base are produced with an electrochemical cell.
- the electrochemical cell comprises electrodes and membranes.
- said acid and/or said base are produced from a salt solution.
- said acid and/or said base are produced by splitting said salt solution.
- the salt solution comprises a sodium chloride solution.
- said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
- said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution.
- said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof.
- said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof.
- said separating of the undesirable metal precipitate comprises using a centrifuge.
- said disposal comprises injecting the solution of redissolved undesirable metals underground.
- the liquid resource is obtained from a reservoir.
- the liquid resource is pumped out of the reservoir.
- said disposal comprises injecting the solution of redissolved undesirable metals into said reservoir.
- the reservoir is located underground.
- said process further comprises agglomerating the undesirable metal precipitate.
- said agglomerating comprises adding a flocculant to the liquid resource.
- said separating the undesirable metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof.
- said separating the undesirable metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter.
- said separating the undesirable metal precipitate further comprises moving the undesirable metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the undesirable metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series. In some embodiments, said precipitating of an undesirable metal forms a slurry comprising the undesirable metal precipitate and feed liquid.
- the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
- the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate.
- a plurality of desirable metals are separated from the feed liquid.
- the desirable metal is different from the undesirable metal.
- a process for recovering lithium from a liquid resource a) precipitating a transition metal from said liquid resource to form a transition metal precipitate; b) separating said transition metal precipitate from the liquid resource to form a feed liquid; c) recovering said lithium from said feed liquid to form a raffinate, wherein said recovering of lithium comprises contacting said feed liquid with ion exchange particles that absorb said lithium while releasing protons; and d) redissolving said transition metal precipitate into said raffinate to form a raffinate mixture.
- said precipitating comprises adding a base to the liquid resource.
- said precipitating comprises adding a base and an oxidant to the liquid resource.
- said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with the transition metal precipitate. In some embodiments, said combining an acid with said transition metal precipitate occurs 1) prior to combining said transition metal precipitate with said raffinate, or 2) after combining said transition metal precipitate with said raffinate. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said redissolving comprises adding hydrochloric acid or sulfuric acid to dissolve said transition metal precipitate.
- said precipitating comprises adding a base to the liquid resource, and said redissolving comprises combining an acid with the transition metal precipitate, wherein said acid and said base are produced with an electrochemical cell.
- said acid and/or said base are produced with an electrochemical cell.
- the electrochemical cell comprises electrodes and membranes.
- said acid and/or said base are produced from a salt solution.
- said acid and/or said base are produced by splitting said salt solution.
- said salt solution comprises a sodium chloride solution.
- said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
- said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution.
- said precipitating comprises adding chemicals to the liquid resource.
- said separating of said transitional metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
- said separating of said transitional metal comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of said transitional metal comprises using a centrifuge. In some embodiments, said process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground. In some embodiments, said process further comprises agglomerating the transition metal precipitate.
- said agglomerating comprises adding a flocculant to the liquid resource.
- said separating the transition metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof.
- said separating the transition metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, said separating the transition metal precipitate further comprises moving the transition metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the transition metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series.
- said precipitating of a transition metal forms a slurry comprising the transition metal precipitate and feed liquid.
- the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
- the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate.
- a plurality of desirable metals are separated from the feed liquid.
- the desirable metal is different from the undesirable metal.
- a process for recovering a desirable metal from a liquid resource comprising: a) precipitating an undesirable metal from the liquid resource to form an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering said desirable metal from the feed liquid to form a raffinate; and d) redissolving said undesirable metal precipitate into said raffinate, a liquid resource, water, waste water, another liquid, or combinations thereof to form a raffinate mixture.
- said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metal comprises lithium.
- said undesirable metal comprises a transition metal.
- said desirable metals comprise lithium and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said undesirable metals comprise transition metals and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metals comprise lithium, said undesirable metals comprise transition metals, and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons.
- said precipitating comprises adding a base to the liquid resource. In some embodiments, said precipitating comprises adding a base and/or an oxidant to the liquid resource.
- said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air and/or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with said undesirable metal precipitate. In some embodiments, said combining an acid with said undesirable metal precipitate occurs 1) prior to combining said undesirable metal precipitate with said raffinate, liquid resource, water, waste water, another liquid, or combinations thereof, or 2) after combining said undesirable metal precipitate with said raffinate, liquid resource, water, waste water, another liquid, or combinations thereof. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid.
- said redissolving comprises adding hydrochloric acid or sulfuric acid to dissolve said undesirable metal precipitate.
- said precipitating comprises adding a base to the liquid resource, and said redissolving comprises combining an acid with the undesirable metal precipitate, wherein said acid and said base are produced with an electrochemical cell.
- said acid and/or said base are produced with an electrochemical cell.
- the electrochemical cell comprises electrodes and membranes.
- said acid and/or said base are produced from a salt solution.
- said acid and/or said base are produced by splitting said salt solution.
- said salt solution comprises a sodium chloride solution.
- said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
- said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution.
- said precipitating comprises adding chemicals to the liquid resource.
- said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof.
- said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, said process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground. In some embodiments, said process further comprises agglomerating the undesirable metal precipitate.
- said agglomerating comprises adding a flocculant to the liquid resource.
- said separating the undesirable metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof.
- said separating the undesirable metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, said separating the undesirable metal precipitate further comprises moving the undesirable metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the undesirable metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series.
- said precipitating of an undesirable metal forms a slurry comprising the undesirable metal precipitate and feed liquid.
- the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
- the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate, liquid resource, water, waste water, another liquid, or combinations thereof.
- a plurality of desirable metals are separated from the feed liquid.
- the desirable metal is different from the undesirable metal.
- undesirable metals are removed from a liquid resource through precipitation, removal from the liquid resource, redissolution, and mixing with another liquid for disposal.
- undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, removal from the resulting solids from the liquid resource, redissolution of the resulting solids by addition of acid, mixing of the redissolved undesirable metals with another liquid, and disposal of the other liquid.
- undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, removal from the resulting solids from the liquid resource, redissolution of the resulting solids by addition of acid, mixing of the redissolved undesirable metals with waste water, and disposal of the waste water.
- redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids.
- redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal.
- solids of undesirable metals may be dissolved in raffinate, waste water, liquid resource, water, or other liquids for disposal.
- undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal.
- a process for recovering lithium from a liquid resource a) precipitating a transition metal from said liquid resource to form a transition metal precipitate; b) separating said transition metal precipitate from the liquid resource to form a feed liquid; c) recovering said lithium from said feed liquid to form a raffinate, wherein said recovering of lithium comprises contacting said feed liquid with ion exchange particles that absorb said lithium while releasing protons; and d) redissolving said transition metal precipitate into said raffinate a liquid resource, water, waste water, another liquid, or combinations thereof to form a raffinate mixture.
- a process for recovering a desirable metal from a liquid resource comprising: a) eluting an undesirable metal from the liquid resource through ion exchange; b) separating the undesirable metal from the eluate; and c) injecting the undesirable metal into a reservoir.
- said separating the undesirable metal comprises using nano-filtration membranes, precipitation, or combinations thereof.
- said process further comprises producing a retentate comprising the dissolved undesirable metal using nano-filtration membranes.
- said process further comprises separating the dissolved undesirable metal from the retentate.
- the liquid resources is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof.
- the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- a process for recovering desirable metals from a liquid resource that also contains undesirable metals comprising: a) precipitating the undesirable metals from the liquid resource to form one or more precipitates; b) separating said precipitates from the liquid resource; c) recovering said desirable metals from the liquid resource; and d) redissolving said undesirable metals into said liquid resource.
- said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metals comprise lithium.
- said undesirable metals comprise transition metals.
- said desirable metals comprise lithium and said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons.
- said undesirable metals comprise transition metals and said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons.
- said desirable metals comprise lithium, said undesirable metals comprise transition metals, and said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons.
- said precipitating is done by adding base to the liquid resource. In some embodiments, said precipitating is done by adding base and oxidant to the liquid resource.
- said precipitating is done by adding NaOH or Ca(OH) 2 to the liquid resource. In some embodiments, said precipitating is done by adding air or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving is done by adding acid to dissolve said precipitates. In some embodiments, said redissolving is done by adding hydrochloric acid or sulfuric acid to dissolve said precipitates. In some embodiments, said precipitating is done with a base and said redissolving is done with an acid, wherein said acid and said base are produced with an electrochemical cell. In some embodiments, said electrochemical cell comprises electrodes and membranes.
- said separating of precipitates is done using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In some embodiments, said separating is done using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating is done using a centrifuge. In some embodiments, said undesirable metals are redissolved and disposed of by being injected underground.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- a process for recovering lithium from a liquid resource that also contains transition metals comprising: a) precipitating said transition metals from said liquid resource to form one or more precipitates; b) separating said precipitates from the liquid resource; c) recovering said lithium from said liquid resource by contacting said liquid resource with ion exchange particles that absorb lithium while releasing protons; and d) redissolving said transition metals into said liquid resource.
- said precipitating is done by adding base to the liquid resource.
- said precipitating is done by adding base and oxidant to the liquid resource.
- said precipitating is done by adding NaOH or Ca(OH)2 to the liquid resource.
- said precipitating is done by adding air or hydrogen peroxide to the liquid resource.
- said redissolving is done by adding acid to dissolve said precipitates.
- said redissolving is done by adding hydrochloric acid or sulfuric acid to dissolve said precipitates.
- said precipitating is done with a base and redissolving is done with an acid, wherein said acid and said base are produced with an electrochemical cell.
- the electrochemical cell comprises electrodes and membranes.
- said separating of precipitates is done using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof.
- said separating is done using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating is done using a centrifuge. In some embodiments, said undesirable metals are redissolved and disposed of by being injected underground.
- a process for separating transition metals from a liquid resource to facilitate recovery of lithium comprising: a) adding base to said liquid resource to precipitate said transition metals as precipitates; b) separating said precipitates from the liquid resource; c) recovering said lithium from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource using gravity sedimentation; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource using centrifugal sedimentation; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource using filtration; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) splitting a salt solution into acid and base using an electrochemical cell; b)adding said base solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; and e) adding said acid solution to said precipitates to redissolve for disposal.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) splitting a salt solution into acid and base using an electrochemical cell; b) adding said base solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; and e) adding said acid solution to said precipitates to redissolve for disposal.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; b) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; and e) adding said hydrochloric acid solution to said precipitates to redissolve said precipitates for disposal.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; b) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; e) adding said hydrochloric acid solution to said precipitates to redissolve said precipitates; and 0 mixing the redissolved precipitates with the liquid resource.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; b) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; e) mixing said precipitates with the liquid resource to form a mixture; and 0 adding said hydrochloric acid to said mixture to redissolve the precipitates.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; 0 adding said hydrochloric acid solution to said precipitates to redissolve said precipitates; g) mixing the redissolved precipitates with the liquid resource; and h) reinjecting the liquid resource into a reservoir.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; f) mixing said precipitates with the liquid resource to form a mixture; g) adding said hydrochloric acid to said mixture to redissolve the precipitates; and h) reinjecting said liquid resource into a reservoir.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using centrifugation; e) recovering said desirable metals from the liquid resource; f) mixing said precipitates with the liquid resource to form a mixture; g) adding said hydrochloric acid to said mixture to redissolve the precipitates; and h) reinjecting said liquid resource into a reservoir.
- a process for separating transition metals from a liquid resource to facilitate recovery of lithium comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said transition metals as precipitates; d) separating said precipitates from said liquid resource using centrifugation; e) recovering said lithium from said liquid resource by contacting said liquid resource with ion exchange particles that absorb said lithium while releasing protons; f) redissolving said precipitates into said liquid resource by adding said hydrochloric acid solution; and g) reinjecting said liquid resource into a reservoir.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) extracting sodium chloride from said liquid resource to form a sodium chloride solution; b) processing said sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; 0 adding said hydrochloric acid solution to said precipitates to redissolve said precipitates; and g) mixing the redissolved precipitates with the liquid resource.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) extracting sodium chloride from said liquid resource to form a sodium chloride solution; b) processing said sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; 0 mixing said precipitates with the liquid resource to form a mixture; and g) adding said hydrochloric acid to said mixture to redissolve the precipitates.
- a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals comprising: a) adding chemicals to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- said desirable metals include lithium. In some embodiments, in any process disclosed herein, said undesirable metals include iron and manganese.
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Abstract
Disclosed herein are processes and systems relating to separation, handling, and disposal of undesirable metals to facilitate recovery of desirable metals, including lithium. Undesirable metals may be precipitated at high pH and separated from a liquid resource to facilitate recovery of the desirable metals. The precipitated undesirable metals may then be redissolved and recombined with the liquid resource for disposal.
Description
- This application is a continuation of U.S. application Ser. No. 17/169,251, filed Feb. 5, 2021, which is a continuation of International Application No. PCT/US2021/12534, filed Jan. 7, 2021, which claims the benefit of U.S. Provisional Application No. 62/959,078, filed Jan. 9, 2020, which is incorporated by reference herein in its entirety.
- Liquid resources such as geothermal brines contain a combination of desirable and undesirable metals, and recovery of the desirable metals can be facilitated by separation and handling of the undesirable metals.
- Desirable metals can be recovered from liquid resources using direct extraction technologies. This recovery of desirable metals can be facilitated by separating undesirable metals from the liquid resource. Handling of the separated undesirable metals can present a major challenge. This invention relates to separation, handling, and disposal of undesirable metals to facilitate recovery of desirable metals including lithium. Undesirable metals may be precipitated at high pH and separated from the liquid resource to facilitate recovery of the desirable metals, and then the precipitated undesirable metals may be redissolved and recombined with the liquid resource for disposal.
- In one aspect, disclosed herein is a process for recovering a desirable metal from a liquid resource, the process comprising: a) precipitating an undesirable metal from the liquid resource to form an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering said desirable metal from the feed liquid to form a raffinate; and d) redissolving said undesirable metal precipitate into said raffinate to form a raffinate mixture. In some embodiments, said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metal comprises lithium. In some embodiments, said undesirable metal comprises a transition metal. In some embodiments, said precipitating comprises adding a base to the liquid resource. In some embodiments, said precipitating comprises adding a base and/or an oxidant to the liquid resource. In some embodiments, said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air and/or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with said undesirable metal precipitate. In some embodiments, said combining an acid with said undesirable metal precipitate occurs 1) prior to combining said undesirable metal precipitate with said raffinate, or 2) after combining said undesirable metal precipitate with said raffinate. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, said salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, the process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said precipitating comprises adding chemicals to the liquid resource. In some embodiments, said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, the process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, the process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground.
- In another aspect, disclosed herein is a process for separating an undesirable metal from a liquid resource, the process comprising: a) adding a base to said liquid resource to precipitate said undesirable metal thereby forming an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering a desirable metal from the feed liquid; and d) combining an acid to said undesirable metal precipitate to form a solution of redissolved undesirable metals for disposal. In some embodiments, said recovering comprises contacting said feed liquid with ion exchange particles that absorbs said desirable metal while releasing protons. In some embodiments, said desirable metal comprises lithium. In some embodiments, said undesirable metal comprises a transition metal. In some embodiments, the process further comprises adding an oxidant with said base to said liquid resource. In some embodiments, said base comprises NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said oxidant comprises air and/or hydrogen peroxide to the liquid resource. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, the salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, the process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, said disposal comprises injecting the solution of redissolved undesirable metals underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said disposal comprises injecting the solution of redissolved undesirable metals into said reservoir. In some embodiments, the reservoir is located underground.
- In another aspect, disclosed herein is a process for recovering lithium from a liquid resource, said process comprising: a) precipitating a transition metal from said liquid resource to form a transition metal precipitate; b) separating said transition metal precipitate from the liquid resource to form a feed liquid; c) recovering said lithium from said feed liquid to form a raffinate, wherein said recovering of lithium comprises contacting said feed liquid with ion exchange particles that absorb said lithium while releasing protons; and d) redissolving said transition metal precipitate into said raffinate to form a raffinate mixture. In some embodiments, said precipitating comprises adding a base to the liquid resource. In some embodiments, said precipitating comprises adding a base and an oxidant to the liquid resource. In some embodiments, said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with the transition metal precipitate. In some embodiments, said combining an acid with said transition metal precipitate occurs 1) prior to combining said transition metal precipitate with said raffinate, or 2) after combining said transition metal precipitate with said raffinate. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, said salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, the process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said precipitating comprises adding chemicals to the liquid resource. In some embodiments, said separating of said transitional metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In some embodiments, said separating of said transitional metal comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of said transitional metal comprises using a centrifuge. In some embodiments, the process further comprising injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, the process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground.
- For any process disclosed herein, said desirable metal comprises lithium. For any process disclosed herein, said undesirable metals comprise iron and/or manganese. For any process disclosed herein, the desirable metal comprises Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, or any combination thereof. For any process disclosed herein, the undesirable metal comprises Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, or any combination thereof. For any process disclosed herein, the desirable metal is different from the undesirable metal. cl Incorporation by Reference
- All publications, patents, and patent applications mentioned in this specification are herein incorporated by reference to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference.
- The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings of which:
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FIG. 1 illustrates a system for precipitating undesirable metals from a liquid resource, separating precipitated undesirable metals from the liquid resource using sedimentation, recovering desirable metals from the liquid resource, and redissolving the undesirable metals in the liquid resource. -
FIG. 2 illustrates a system for precipitating undesirable metals from a liquid resource, separating precipitated undesirable metals from the liquid resource using a hydrocyclone, recovering desirable metals from the liquid resource, and redissolving the undesirable metals in the liquid resource. -
FIG. 3 illustrates a system for precipitating undesirable metals from a liquid resource, separating precipitated undesirable metals from the liquid resource using a centrifuge, recovering desirable metals from the liquid resource, and redissolving the undesirable metals in the liquid resource. - The terms “lithium”, “lithium ion”, and “Li+” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary. The terms “hydrogen”, “hydrogen ion”, “proton”, and “Hα” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary. The terms “liquid resource” and “brine” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary.
- As used herein, the term “about” refers to an amount that is near the stated amount by 10%, 5%, or 1%, including increments therein.
- Desirable metals can be recovered from liquid resources using direct extraction technologies. This recovery of desirable metals can be facilitated by separating undesirable metals from the liquid resource. Handling of the separated undesirable metals can present a major challenge. This invention relates to separation, handling, and disposal of undesirable metals to facilitate recovery of desirable metals including lithium. Undesirable metals may be precipitated at high pH and separated from the liquid resource to facilitate recovery of the desirable metals, and then the precipitated undesirable metals may be redissolved and recombined with the liquid resource for disposal.
- The liquid resource, as disclosed herein, refers to a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof
- In one embodiment, the liquid resource is at a temperature of −10 to 400° C. In one embodiment, the liquid resource is at a temperature of −10 to 20° C., 20 to 50° C., 50 to 100° C., 100 to 200° C., or 200 to 400° C. In one embodiment, the liquid resource is heated or cooled to precipitate or dissolve species in the liquid resource, or to facilitate removal of metals from the liquid resource.
- In one embodiment, the liquid resource contains lithium at a concentration between 0 to 2000 mg/L. In one embodiment, the liquid resource contains lithium at a concentration of less than 1 mg/L, 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or greater than 2,000 mg/L. In one embodiment, the liquid resource contains calcium at a concentration between 100 to 150,000 mg/L. In one embodiment, the liquid resource contains calcium at a concentration of 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 150,000 mg/L, or greater than 150,000 mg/L. In one embodiment, the liquid resource contains potassium at a concentration between 100 to 150,000 mg/L. In one embodiment, the liquid resource contains potassium at a concentration of 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, 50,000 to 150,000 mg/L, or greater than 150,000 mg/L.
- In one embodiment, the liquid resource contains iron at a concentration between 0 to 50,000 mg/L. In one embodiment, the liquid resource contains iron at a concentration of less than 1 mg/L, 1 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, or greater than 50,000 mg/L. In one embodiment, the liquid resource contains manganese at a concentration between 0 to 50,000 mg/L. In one embodiment, the liquid resource contains manganese at a concentration of less than 1 mg/L, 1 to 100 mg/L, 100 to 1,000 mg/L, 1,000 to 10,000 mg/L, 10,000 to 50,000 mg/L, or greater than 50,000 mg/L. In one embodiment, the liquid resource contains lead at a concentration between 0 to 2,000 mg/L. In one embodiment, the liquid resource contains lead at a concentration of less than 1 mg/L, 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or greater than 2,000 mg/L.
- In one embodiment, the liquid resource is treated to remove certain metals to produce a feed liquid. In one embodiment, the feed liquid contains iron at a concentration between 0 to 1,000 mg/L. In one embodiment, the feed liquid contains iron at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains manganese at a concentration between 0 to 1,000 mg/L. In one embodiment, the feed liquid contains manganese at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains lead at a concentration between 0 to 1,000 mg/L. In one embodiment, the feed liquid contains lead at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains zinc at a concentration between 0 to 1,000 mg/L. In one embodiment, the feed liquid contains zinc at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L. In one embodiment, the feed liquid contains lithium at a concentration between 0 to 2,000 mg/L. In one embodiment, the feed liquid contains lithium at a concentration of 1 to 50 mg/L, 50 to 200 mg/L, 200 to 500 mg/L, 500 to 2,000 mg/L, or greater than 2,000 mg/L.
- In one embodiment, the feed liquid is processed to recover metals such as lithium and yield a spent brine or raffinate. In one embodiment, the raffinate contains residual quantities of the recovered metals at a concentration between 0 to 1,000 mg/L. In one embodiment, the raffinate contains residual quantities of the recovered metals at a concentration of less than 0.01, 0.01 to 0.1 mg/L, mg/L, 0.1 to 1.0 mg/L, 1.0 to 10 mg/L, 10 to 100 mg/L, or 100 to 1,000 mg/L.
- In one embodiment, the pH of the liquid resource, feed liquid, and/or raffinate is corrected to less than 0, 0 to 1, 1 to 2, 2 to 4, 4 to 6, 6 to 8, 4 to 8, 8 to 9, 9 to 10, 9 to 11, or 10 to 12. In one embodiment, the pH of the liquid resource, feed liquid, and/or raffinate is corrected to less than about 4, 4 to 6, 6 to 8, 4 to 8, 8 to 9, 9 to 10, 9 to 11, or 10 to 12. In one embodiment, the pH of the liquid resource, feed liquid, and/or raffinate is corrected to precipitate or dissolve metals.
- In one embodiment, at least one metal is precipitated from the liquid resource to form at least one precipitate. In one embodiment, the precipitates include transition metal hydroxides, oxy-hydroxides, sulfide, flocculants, aggregate, agglomerates, or combinations thereof. In one embodiment, the precipitates include Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, other metals, or any combination thereof. In one embodiment, the precipitates are concentrated into a slurry, a filter cake, a wet filter cake, a dry filter cake, a dense slurry, and/or a dilute slurry.
- In one embodiment, the precipitates contain iron at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain iron at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain manganese at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain manganese at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain lead at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain lead at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain arsenic at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain arsenic at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain magnesium at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain magnesium at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg. In one embodiment, the precipitates contain Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals at a concentration between 0 to 800,000 mg/kg. In one embodiment, the precipitates contain Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals at a concentration of less than 0.01 mg/kg, 0.01 to 1 mg/kg, 1 to 100 mg/kg, 100 to 10,000 mg/kg, or 10,000 to 800,000 mg/kg.
- In one embodiment, the precipitates are toxic and/or radioactive.
- In one embodiment, precipitates are redissolved by combining the precipitates with at least one acid. In one embodiment, precipitates are redissolved by combining the precipitates with at least one acid in a mixing apparatus. In one embodiment, precipitates are redissolved by combining the precipitates with at least one acid using a high-shear mixer.
- Lithium is an essential element for batteries and other technologies. Lithium is found in a variety of liquid resources, including natural and synthetic brines and leachate solutions from minerals, clays, and recycled products. Lithium is optionally extracted from such liquid resources using an ion exchange process based on inorganic ion exchange materials. These inorganic ion exchange materials absorb lithium from a liquid resource while releasing hydrogen, and then elute lithium in at least one acid while absorbing hydrogen. This ion exchange process is optionally repeated to extract lithium from a liquid resource and yield a concentrated lithium solution. The concentrated lithium solution is optionally further processed into chemicals for the battery industry or other industries.
- Ion exchange materials are optionally formed into beads and the beads are optionally loaded into ion exchange columns, stirred tank reactors, other reactors, or reactor system for lithium extraction. Alternating flows of a liquid resource (e.g., brine), acid, and other solutions are optionally flowed through an ion exchange column, reactors, or reactor system to extract lithium from the liquid resource and produce a lithium concentrate, which is eluted from the column using the acid. As the liquid resource flows through the ion exchange column, reactors, or reactor system, the ion exchange material absorbs lithium while releasing hydrogen, where both the lithium and hydrogen are cations. The release of hydrogen during lithium uptake will acidify the liquid resource and limit lithium uptake unless the pH of the liquid resource is optionally maintained in a suitable range to facilitate thermodynamically favorable lithium uptake and concomitant hydrogen release. In one embodiment, pH of the liquid resource is maintained near a set-point through addition of base to neutralize protons released from the ion exchange material into the liquid resource.
- To control the pH of the liquid resource and maintain the pH in a range that is suitable for lithium uptake in an ion exchange column, bases such as NaOH, Ca(OH)2, CaO, KOH, or NH3 are optionally added to the liquid resource as solids, aqueous solutions, or in other forms. For a liquid resource that contain divalent ions such as Mg, Ca, Sr, or Ba, addition of base to the liquid resource can cause precipitation of solids, such as Mg(OH)2 or Ca(OH)2, which can cause problems for the ion exchange reaction. These precipitates cause problems in at least three ways. First, precipitation can remove base from solution, leaving less base available in solution to neutralize protons and maintain pH in a suitable range for lithium uptake in the ion exchange column. Second, precipitates that form due to base addition can clog the ion exchange column, including clogging the surfaces and pores of ion exchange beads and the voids between ion exchange beads. This clogging can prevent lithium from entering the beads and being absorbed by the ion exchange material. The clogging can also cause large pressure heads in the column. Third, precipitates in the column dissolve during acid elution and thereby contaminate the lithium concentrate produced by the ion exchange system. For ion exchange beads to absorb lithium from the liquid resource, an ideal pH range for the liquid resource is optionally 5 to 7, a preferred pH range is optionally 4 to 8, and an acceptable pH range is optionally 1 to 9. In one embodiment, an pH range for the liquid resource is optionally about 1 to about 14, about 2 to about 13, about 3 to about 12, about 4 to about 12, about 4.5 to about 11, about 5 to about 10, about 5 to about 9, about 2 to about 5, about 2 to about 4, about 2 to about 3, about 3 to about 8, about 3 to about 7, about 3 to about 6, about 3 to about 5, about 3 to about 4, about 4 to about 10, about 4 to about 9, about 4 to about 8, about 4 to about 7, about 4 to about 6, about 4 to about 5, about 5 to about 6, about 5 to about 7, about 5 to about 8, about 6 to about 7, about 6 to about 8, or about 7 to about 8.
- Direct extraction technologies can be used to recover one or more desirable metals from liquid resources. In one embodiment, direct extraction technologies include ion exchange technologies, absorption technologies, solvent extraction technologies, membrane technologies, direct precipitation technologies, and combinations thereof. In one embodiment, desirable metals include Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In one embodiment, liquid resources contain one or more undesirable metals. In one embodiment, undesirable metals include Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W,M n, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In one embodiment, one or more metals are undesirable for a certain process but are desirable for a different process.
- In one embodiment, ion exchange materials are used to recover lithium from a liquid resource. In one embodiment, metals such as iron, manganese, and/or other metals interfere with the lithium recovery process and are therefore undesirable to have in the liquid resource during lithium recovery. In one embodiment, undesirable metals such as iron and manganese are precipitated from the liquid resource and the resulting precipitates are separated from the liquid resource to create a feed liquid that has a reduced concentration of these undesirable metals, so as to facilitate recovery of lithium and/or other desirable metals from the feed liquid. In one embodiment, the precipitated iron, manganese, and/or other undesirable metals present a challenge related to low value and high disposal cost. In one embodiment, the precipitated iron, manganese, and/or other undesirable metals may be redissolved for disposal. In one embodiment, the precipitated iron, manganese, and/or other undesirable metals may be precipitated from the liquid resource by the addition of at least one base, such as Ca(OH)2 and/or NaOH. In one embodiment, the precipitated iron, manganese, and/or other undesirable metals may be redissolved for disposal using at least one acid, such as HCl and/or H2SO4.
- In one embodiment, metals are recovered from a liquid resource using multiple precipitation steps to remove desirable and/or undesirable metals from the liquid resource, and said undesirable and/or desirable metals may be removed and recombined with the resulting processed liquid resource (e.g., feed liquid or raffinate as described herein). In one embodiment, metals are recovered from a liquid resource using multiple precipitation steps to remove desirable and undesirable metals from the liquid resource, and said undesirable metals may be removed and recombined with the resulting processed liquid resource (e.g., liquid resource depleted of desirable metals, or feed liquid, or raffinate as described herein). In one embodiment, desirable metals are precipitated from a liquid resource while undesirable metals remain in the liquid resource. In one embodiment, desirable metals are co-precipitated from a liquid resource with undesirable metals to form a raffinate, and then the desirable and/or undesirable metals may be redissolved in said raffinate. In one embodiment, multiple undesirable metals are precipitated from a liquid resource in subsequent steps using a combination of at least one base, at least one oxidant, a specified temperature, chemicals, membranes, and/or solid-liquid separation devices.
- In one embodiment, undesirable metals are 1) precipitated from a liquid resource, 2) removed from the liquid resource, 3) re-dissolved (e.g., in a solution), and 4) mixed with another liquid for disposal. In one embodiment, undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, followed by removal of the resulting solids (via said precipitation of the undesirable metals) from the liquid resource, followed by redissolution of the resulting solids by addition of acid, followed by mixing of the redissolved undesirable metals with another liquid, and followed by disposal of said another liquid mixed with the re-dissolved undesirable metals. In one embodiment, undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, followed by removal of the resulting solids from the liquid resource, followed by redissolution of the resulting solids (via precipitation of the undesirable metals) by addition of acid, followed by mixing of the redissolved undesirable metals with waste water, and followed by disposal of the waste water. In one embodiment, redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids. In one embodiment, redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal. In one embodiment, solids of undesirable metals may be dissolved in raffinate, waste water, liquid resource, water, or other liquids for disposal. In one embodiment, undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal.
- In one embodiment, metals such as iron, manganese, lead, zinc, and/or other metals are precipitated from the liquid resource (e.g., brine) by adding at least one base and optionally at least one oxidant to the liquid resource, wherein the precipitated metals are separated from the liquid resource to form a feed liquid, lithium is recovered from the feed liquid to form a raffinate, and then the precipitated metals are dissolved into the raffinate for reinjection. In one embodiment, the precipitated metals are separated from the liquid resource using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In one embodiment, the raffinate is reinjected underground for disposal, wherein the raffinate is reinjected into the original reservoir from where the liquid resource was obtained, and/or into a different reservoir than from where the liquid resource was obtained.
- In one embodiment, undesirable metals are removed from the liquid resource using ion exchange materials. In one embodiment, the undesirable metals are eluted from ion exchange materials using acid, salt solution, or combinations thereof. In one embodiment, the undesirable metals are separated from the eluate using nano-filtration membranes, precipitation, or combinations thereof. In one embodiment, undesirable metals or other metals are eluted from ion exchange materials using a solution of sodium chloride, wherein the metals (undesirable metals or other metals) are removed from the eluate using nano-filtration membranes, such that the eluate with metals removed can be reused to elute metals from the ion exchange materials. In one embodiment, nano-filtration membranes produce a retentate containing dissolved metals that can be separated and reinjected into a reservoir. In one embodiment, nano-filtration membranes produce a retentate containing dissolved metals that can be mixed with a processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof.
- In one embodiment, the precipitated and/or separated undesirable metals are dissolved into the raffinate using at least one acid. In one embodiment, the precipitated and/or separated undesirable metals are dissolved into the raffinate using hydrochloric acid and/or sulfuric acid. In one embodiment, the undesirable metals are precipitated from the liquid resource using at least one base. In one embodiment, the undesirable metals are precipitated from the liquid resource using sodium hydroxide, calcium oxide, and/or calcium hydroxide. In one embodiment, the acid is produced using an electrochemical cell, an electrochemical membrane cell, an electrolytic cell, or combinations thereof. In one embodiment, the acid is produced by combusting sulfur. In one embodiment, the base is produced using an electrochemical cell, an electrochemical membrane cell, an electrolytic cell, or combinations thereof. In one embodiment, the base is produced by roasting lime. In one embodiment, the acid and base are both produced using an electrochemical cell, an electrochemical membrane cell, an electrolytic cell, or combinations thereof.
- In one embodiment, undesirable metals such as iron, manganese, lead, zinc, or other metals are precipitated from the liquid resource by adding at least one base and optionally at least one oxidant to the liquid resource, wherein the precipitated metals are separated from the liquid resource to form a feed liquid, desirable metals are recovered from the feed liquid to form a raffinate, and then the undesirable metals are dissolved into the raffinate for disposal (e.g., reinjection into a reservoir underground, such as the reservoir from where the liquid resource was obtained from). In one embodiment, metals (undesirable metals or other metals) are precipitated using at least one chemical precipitate such as hydroxide, phosphates, sulfides, and/or other chemicals. In one embodiment, at least one oxidant is used to facilitate precipitation of the undesirable metals, wherein the at least one oxidant includes hydrogen peroxide, air, oxygen, and/or other oxidants. In one embodiment, at least one flocculant is used to agglomerate precipitates to facilitate solid-liquid separation. In one embodiment, precipitated undesirable metals are agglomerated using flocculants, coagulants, or combinations thereof to facilitate separation of the precipitated undesirable metals from the liquid resource. In one embodiment, the precipitated metals are separated from the liquid resource using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In one embodiment, the raffinate is reinjected underground for disposal, wherein the raffinate is reinjected into the original reservoir of the liquid resource, and/or into a different reservoir of the liquid resource.
- In some embodiments, the liquid resource is processed to remove metals to facilitate recovery of other metals. In some embodiments, the liquid resource is processed to remove metals (e.g., undesirable metals) to facilitate recovery of other metals such as lithium, manganese, zinc, lead, iron, gold, platinum, rubidium, or other metals. In some embodiments, the liquid resource is processed to remove undesirable metals, forming a feed liquid, to facilitate recovery of desirable metals from said feed liquid, and after recovery of the desirable metals, thereby forming a raffinate, the undesirable metals are redissolved in said raffinate to form a raffinate mixture. In some embodiments, the undesirable metals are redissolved in the raffinate, forming a raffinate mixture, which is injected underground for disposal. In some embodiments, the undesirable metals are redissolved in the raffinate and injected underground for disposal into the reservoir from which they originated. In some embodiments, the undesirable metals are redissolved in the raffinate and injected underground for disposal into a reservoir different from the reservoir in which they originated.
- In some embodiments, undesirable metals or transition metals are precipitated from a liquid resource, and then redissolved in a processed liquid resource (e.g.,raffinateas described herein), liquid resource, water, waste water, another liquid, or combinations thereof by combining the precipitates with acid to form a concentrated solution and then mixing the concentrated solution with the processed liquid resource (e.g., raffinate), liquid resource, water, waste water, another liquid, or combinations thereof. In some embodiments, undesirable metals or transition metals are precipitated from a liquid resource and then redissolved in a processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof by combining the precipitates with the processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof, to form a mixture, and then adding acid to said mixture.
- In some embodiments, different sets of undesirable metals are precipitated from and separated from the liquid resource at different pH ranges. In some embodiments, Fe and Mn are precipitated and separated from the liquid resource at different pH points. In some embodiments, Fe and Mn are precipitated and separated from the liquid resource at one pH range, and Pb and Zn are precipitated and separated from the liquid resource at another pH range. In some embodiments, Fe and Mn are precipitated and separated from the liquid resource at one pH range, and Pb is precipitated and separated from the liquid resource at another pH range.
- In one embodiment, lithium is recovered from a liquid resource, such as a brine, using an ion exchange material. In one embodiment of the ion exchange system, one or more ion exchange columns are loaded with a fixed or fluidized bed of ion exchange material. In one embodiment of the system, the ion exchange column is a cylindrical construct with entry and exit ports. In a further embodiment, the ion exchange column is optionally a non-cylindrical construct with entry and exit ports. In a further embodiment, the ion exchange column is a tank. In a further embodiment, the ion exchange column optionally has entry and exit ports for brine pumping, and additional doors or hatches for loading and unloading ion exchange material to and from the column. In a further embodiment, the ion exchange column is optionally equipped with one or more security devices to decrease the risk of loss, spilling, or theft of the ion exchange material. The material can reversibly absorb lithium from brine and release lithium in acid. In one embodiment, the ion exchange material is comprised of particles that are optionally protected with coating material such as SiO2, ZrO2, or TiO2 to limit dissolution or degradation of the ion exchange material. In one embodiment, the ion exchange material may be in the form of a powder. In one embodiment, the material may be in the form of beads. In one embodiment, the beads contain a structural component such as an acid-resistant polymer that binds the ion exchange materials. In one embodiment, the beads contain pores that facilitate penetration of brine, acid, aqueous, and other solutions into the beads to deliver lithium and hydrogen to and from the bead or to wash the bead. In one embodiment, the bead pores are structured to form a connected network of pores with a distribution of pore sizes and are structured by incorporating filler materials during bead formation and later removing that filler material in a liquid or gas.
- In one embodiment of the ion exchange system, the system is a recirculating batch system, which comprises an ion exchange column that is connected to one or more tanks for mixing base into the brine, settling out any precipitates following base addition, and storing the brine prior to reinjection into the ion exchange column or the other tanks. In one embodiment of the recirculating batch system, the brine is loaded into one or more tanks, pumped through the ion exchange column, pumped through a series of tanks, and then returned to the ion exchange column in a loop. In one embodiment, the brine optionally traverses this loop repeatedly. In one embodiment, the brine is recirculated through the ion exchange column to enable optimal lithium uptake by the material. In one embodiment, base is added to the brine in such a way that pH is maintained at an adequate level for lithium uptake and in such a way that the amount of base-related precipitates in the ion exchange column is minimized.
- In one embodiment, the ion exchange material is selected from the group consisting of LiFePO4, LiMnPO4, Li2MO3 (M=Ti, Mn, Sn), Li4Ti5O12, Li4Mn5O12, LiMn2O4, Li1.6Mn1.6O4, LiMO2 (M=Al, Cu, Ti), Li4TiO4, Li7Ti11O24, Li3VO4, Li2Si3O7, Li2CuP2O7, Al(OH)3, LiCl.xAl(OH)3.yH2, SnO2.xSb2O5.yH2O, TiO2.xSb2P5.yH2O, solid solutions thereof, or combinations thereof; wherein xis from 0.1-10 and y is from 0.1-10. In one embodiment, the ion exchange material comprises coated ion exchange particles, uncoated ion exchange particles or combinations thereof. In a further one aspect, a coating material comprises a polymer. In an embodiment, the coating material comprises a chloro-polymer, a fluoro-polymer, a chloro-fluoro-polymer, a hydrophilic polymer, a hydrophobic polymer, co-polymers thereof, mixtures thereof, or combinations thereof.
- In some embodiments, the coating material comprises a carbide, a nitride, an oxide, a phosphate, a fluoride, a polymer, carbon, a carbonaceous material, or combinations thereof. In some embodiments, the coating material comprises Nb2O5, Ta2O5, MoO2, TiO2, ZrO2, MoO2, SnO2, SiO2, Li2O, Li2TiO3, Li2ZrO3, Li2MoO3, LiNbO3, LiTaO3, Li2SiO3, Li2Si2O5, Li2MnO3, ZrSiO4, AlPO4, LaPO4, ZrP2O7, MoP2O7, Mo2P3O12, BaSO4, AlF3, SiC, TiC, ZrC, Si3N4, ZrN, BN, carbon, graphitic carbon, amorphous carbon, hard carbon, diamond-like carbon, solid solutions thereof, or combinations thereof. In some embodiments, the coating material comprises polyvinylidene difluoride, polyvinyl chloride, a fluoro-polymer, a chloro-polymer, or a fluoro-chloro-polymer. In some embodiments, the coating material comprises TiO2, ZrO2, SiO2MoO2, Li2TiO3, Li2ZrO3, Li2MnO3, ZrSiO4, or LiNbO3, AlF3, SiC, Si3N4, graphitic carbon, amorphous carbon, diamond-like carbon, or combinations thereof. In some embodiments, the coating material comprises TiO2, SiO2, or ZrO2. In some embodiments, the coating material comprises TiO2. In some embodiments, the coating material comprises SiO2. In some embodiments, the coating material comprises ZrO2.
- In a further aspect, a coating material comprises a co-polymer, a block co-polymer, a linear polymer, a branched polymer, a cross-linked polymer, a heat-treated polymer, a solution processed polymer, co-polymers thereof, mixtures thereof, or combinations thereof
- In a further aspect, a coating material comprises polyethylene, low density polyethylene, high density polyethylene, polypropylene, polyester, polytetrafluoroethylene (PTFE), types of polyamide, polyether ether ketone (PEEK), polysulfone, polyvinylidene fluoride (PVDF), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), polybutadiene, acrylonitrile butadiene styrene (ABS), polyvinyl chloride (PVC), ethylene tetrafluoroethylene polymer (ETFE), poly(chlorotrifluoroethylene) (PCTFE), ethylene chlorotrifluoro ethylene (Halar), polyvinylfluoride (PVF), fluorinated ethylene-propylene (FEP), perfluorinated elastomer, chlorotrifluoroethylenevinylidene fluoride (FKM), perfluoropolyether (PFPE), perfluorosulfonic acid (Nafion®), polyethylene oxide, polyethylene glycol, sodium polyacrylate, polyethylene-block-poly(ethylene glycol), polyacrylonitrile (PAN), polychloroprene (neoprene), polyvinyl butyral (PVB), expanded polystyrene (EPS), polydivinylbenzene, co-polymers thereof, mixtures thereof, or combinations thereof.
- In a further aspect, a coating material comprises polyvinylidene fluoride (PVDF), polyvinyl chloride (PVC), ethylene chlorotrifluoro ethylene (Halar®), poly (4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), acrylonitrile butadiene styrene (ABS), expanded polystyrene (EPS), polyphenylene sulfide, sulfonated polymer, carboxylated polymer, other polymers, co-polymers thereof, mixtures thereof, or combinations thereof
- In one embodiment, the ion exchange material is a porous ion exchange material. In one embodiment, the ion exchange material is in the form of porous beads. In one embodiment, the ion exchange material is in a powder form. In one embodiment, the acid solution is a solution of H2SO4 or HCl.
- In some embodiments, lithium or other metals are recovered from the liquid resource (e.g., brine) using a porous structure for ion exchange comprising: a) a structural support; and b) a plurality of particles selected from coated ion exchange particles, uncoated ion exchange particles, and a combination thereof. In some embodiments, the structural support comprises a polymer, an oxide, a phosphate, or combinations thereof. In some embodiments, the structural support comprises a polymer. In some embodiments, the polymer is polyvinylidene fluoride, polyvinyl fluoride, polyvinyl chloride, polyvinylidene chloride, a chloro-polymer, a fluoro-polymer, a fluoro-chloro-polymer, polyethylene, polypropylene, polyphenylene sulfide, polytetrafluoroethylene, sulfonated polytetrafluoroethylene, polystyrene, polydivinylbenzene, polybutadiene, a sulfonated polymer, a carboxylated polymer, polyacrylonitrile, Nafion®, copolymers thereof, or combinations thereof.
- In some embodiments, lithium or other metals are recovered from the brine using a batch, semi-batch, semi-continuous, or continuous process. In some embodiments, ion exchange beads are moved through the system in an opposite direction of the brine.
- Solid-Liquid Separation of Precipitates from Liquid Resource
- In one embodiment, the precipitated metals are separated from the liquid resource using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In some embodiments, precipitated metals are removed from the liquid resource using a filter. In some embodiments, the filter comprises a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof. In some embodiments, the filter uses a scroll and/or a vibrating device. In some embodiments, the filter is horizontal, vertical, and/or may use a siphon.
- In some embodiments, a filter cake is prevented, limited, or removed by using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, the precipitated metals and a liquid are moved tangentially to the filter to limit cake growth. In some embodiments, gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation are used before, during, and/or after filtering to prevent cake formation.
- In some embodiments, a filter comprises a screen, a metal screen, a sieve, a sieve bend, a bent sieve, a high frequency electromagnetic screen, a resonance screen, or combinations thereof. In some embodiments, one or more particle traps are a solid-liquid separation apparatus.
- In some embodiments, one or more solid-liquid separation apparatuses may be used in series or parallel. In some embodiments, a dilute slurry of precipitated metals is removed from a tank, transferred to an external solid-liquid separation apparatus, and separated into a concentrated slurry and a solution with low or no suspended solids. In some embodiments, the concentrated slurry of precipitated metals is returned to the tank or transferred to a different tank. In some embodiments, the precipitated metals are transferred from a liquid resource tank to another liquid resource tank, from an acid tank to another acid tank, from a washing tank to another washing tank, from a liquid resource tank to a washing tank, from a washing tank to an acid tank, from an acid tank to a washing tank, or from an acid tank to a liquid resource tank.
- In some embodiments, solid-liquid separation apparatuses for separating precipitates from a liquid resource use gravitational sedimentation. In some embodiments, solid-liquid separation apparatuses include a settling tank, a thickener, a clarifier, a gravity thickener. In some embodiments, solid-liquid separation apparatuses are operated in batch mode, semi-batch mode, semi-continuous mode, or continuous mode. In some embodiments, solid-liquid separation apparatuses include a circular basin thickener with the slurry of precipitated metals entering through a central inlet, such that the slurry is dispersed into the thickener with one or more raking components that rotate and concentrate the ion exchange particles into a zone where the particles can leave through the bottom of the thickener.
- In some embodiments, solid-liquid separation apparatuses include a deep cone, a deep cone tank, a deep cone compression tank, or a tank wherein the slurry is compacted by weight. In some embodiments, solid-liquid separation apparatuses include a tray thickener with a series of thickeners oriented vertically with a center axle and raking components. In some embodiments, solid-liquid separation apparatuses include a lamella type thickener with inclined plates and/or tubes that may be smooth, flat, rough, or corrugated. In some embodiments, solid-liquid separation apparatuses include a gravity clarifier that may be a rectangular basin with feed at one end and overflow at the opposite end optionally with paddles and/or a chain mechanism to move particles. In some embodiments, the solid-liquid separation apparatuses may be a particle trap.
- In some embodiments, the solid-liquid separation apparatuses use centrifugal sedimentation. In some embodiments, solid-liquid separation apparatuses include a tubular centrifuge, a multi-chamber centrifuge, a conical basket centrifuge, a scroll-type centrifuge, a sedimenting centrifuge, and/or a disc centrifuge. In some embodiments, precipitated metals are discharged continuously or intermittently from the centrifuge. In some embodiments, the solid-liquid separation apparatus is a hydrocyclone. In some embodiments, solid-liquid separation apparatus is an array of hydrocyclones or centrifuges in series and/or in parallel. In some embodiments, sumps are used to reslurry the precipitated metals. In some embodiments, the hydrocyclones may have multiple feed points. In some embodiments, a hydrocyclone is used upside down. In some embodiments, liquid is injected near the apex of the cone of a hydrocyclone to improve sharpness of cut. In some embodiments, a weir rotates in the center of the particle trap with a feed of slurry of precipitated metals entering near the middle of the apparatus, wherein the precipitated metals get trapped at the bottom and center of the apparatus due to a “teacup effect”.
- In one embodiment, at least one base is used to precipitate undesirable metals from the liquid resource, wherein the precipitated metals are separated from the liquid resource, and then the precipitated metals are redissolved into a processed liquid resource (e.g., raffinate as described herein), liquid resource, water, waste water, another liquid, or combinations thereof using at least one acid. In one embodiment, the acid and base are generated using an electrochemical cell. In one embodiment, the acid and base are generated using electrodes. In one embodiment, the acid and base are generated using a membrane. In some embodiments, said membrane comprises an ion-conducting membrane.
- In one embodiment, said ion-conducting membrane is a cation-conducting membrane, an anion-conducting membrane or combinations thereof. In one embodiment, said ion-conducting membrane comprises sulfonated tetrafluoroethylene-based fluoropolymer-copolymer, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, or combinations thereof. In one embodiment, said anion-conducting membrane comprises a functionalized polymer structure.
- In one embodiment, said functionalized polymer structure comprises polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof. In one embodiment, said cation-conducting membrane allows for transfer of lithium ions but prevents transfer of anion groups. In one embodiment, said ion-conducting membrane has a thickness from about 1 μm to about 1000 μm. In one embodiment, said ion-conducting membrane has a thickness from about 1 mm to about 10 mm.
- In one embodiment, said electrodes are comprised of titanium, niobium, zirconium, tantalum, magnesium, titanium dioxide, oxides thereof, or combinations thereof. In one embodiment, said electrodes further comprise a coating of platinum, TiO2, ZrO2, Nb2O5, Ta2O5, SnO2, IrO2, RuO2, mixed metal oxides, graphene, derivatives thereof, or combinations thereof
- In one embodiment of an integrated system, a chlor-alkali setup is used to generate HCl and NaOH from an aqueous NaCl solution. In one embodiment, the HCl is used to elute lithium from an ion exchange system for selective lithium uptake to produce a lithium eluate solution. In one embodiment, the NaOH from the chlor-alkali setup is used to control the pH of the brine in the ion exchange system for selective lithium uptake. In one embodiment, the NaOH is used to precipitate impurities from a lithium eluate solution.
- In one embodiment, the system includes one or more electrochemical or electrolysis systems. The terms “electrochemical” and “electrolysis” are used interchangeably in the present specification and these terms are synonymous unless specifically noted to the contrary. In one embodiment, an electrolysis system is comprised of one or more electrochemical cells. In one embodiment, an electrochemical system is used to produce HCl and NaOH. In one embodiment, an electrochemical system converts a salt solution into acid in base. In one embodiment, an electrochemical system converts a salt solution containing NaCl, KCl, and/or other chlorides into a base and an acid. In one embodiment, a salt solution precipitated or recovered from the liquid resource (e.g., brine) is fed into an electrochemical system to produce acid and base. In one embodiment, an electrolysis system converts a lithium salt solution to form a lithium hydroxide solution, an acidified solution, and optionally a dilute lithium salt solution. In one embodiment, the lithium salt solution is or is derived from a lithium eluate solution, produced by an ion exchange system that has optionally been concentrated and/or purified. In one embodiment, acidified solution from an electrolysis system is returned to an ion exchange system to elute more lithium eluate solution.
- In one embodiment of the integrated system, the integrated system includes one or more electrolysis systems. In one embodiment, an electrolysis system is comprised of one or more electrodialysis cells. In one embodiment, an electrolysis system converts a lithium salt solution to form a lithium hydroxide solution, an acidified solution, and optionally a dilute lithium salt solution. In one embodiment, the lithium salt solution is or is derived from a lithium eluate solution, produced by an ion exchange system that has optionally been concentrated and/or purified. In one embodiment, acidified solution from an electrolysis system is returned to an ion exchange system to elute more lithium eluate solution.
- In one embodiment, a lithium salt solution contains unreacted acid from the ion exchange system. In one embodiment, unreacted acid in the lithium salt solution from an ion exchange system passes through an electrolysis system and is further acidified to form an acidified solution. In one embodiment, a lithium salt solution derived from an ion exchange system is purified to remove impurities without neutralizing the unreacted acid in the lithium salt solution and is then fed into an electrolysis system.
- In one embodiment, an acidified solution produced by an electrolysis system contains lithium ions from the lithium salt solution fed into the electrolysis system. In one embodiment, an acidified solution containing lithium ions leaves the electrolysis system and is fed back to an ion exchange system to elute lithium and produce more lithium salt solution.
- In one embodiment of an electrolysis system, the electrolysis cells are electrochemical cells. In one embodiment of an electrochemical cell, the membranes may be cation-conducting and/or anion-conducting membranes. In one embodiment, the electrochemical cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
- In one embodiment of an electrolysis system, the electrolysis cells are electrodialysis cells. In one embodiment of an electrodialysis cell, the membranes may be cation-conducting and/or anion-conducting membranes. In one embodiment, the electrodialysis cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
- In one embodiment of an electrolysis system, the electrolysis cells are membrane electrolysis cells. In one embodiment of a membrane electrolysis cell, the membranes may be cation-conducting and/or anion-conducting membranes. In one embodiment, the membrane electrolysis cell is a two-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions between the chambers but prevents transfer of anion groups such as chloride, sulfate, and hydroxide groups.
- In one embodiment, the membrane electrolysis cell is a three-compartment cell with a cation-conducting membrane that allows for transfer of lithium ions separating a compartment with an electrochemically reducing electrode from a central compartment and with an anion-conducting membrane that allows for transfer of anions ions separating a compartment with an electrochemically oxidizing electrode from the central compartment. In one embodiment, the cation-conducting membrane prevents transfer of anions such as chloride, sulfate, or hydroxide. In one embodiment, the anion-conducting membrane prevents transfer of cations such as lithium, sodium, or protons.
- In one embodiment of the membrane electrolysis cell, the membranes may be comprised of Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof. In one embodiment of the membrane electrolysis cell, the cation exchange membranes are comprised of a functionalized polymer structure which may be Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof. In one embodiment of the membrane electrolysis cell, the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
- In one embodiment of the electrochemical cell, the membranes may be comprised of Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof. In one embodiment of the electrochemical cell, the cation exchange membranes are comprised of a functionalized polymer structure which may be Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof. In one embodiment of the electrochemical cell, the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof
- In one embodiment of the electrodialysis cell, the membranes may be comprised of Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, MK-40, co-polymers, other membrane materials, composites, or combinations thereof. In one embodiment of the electrodialysis cell, the cation exchange membranes are comprised of a functionalized polymer structure which may be Nafion®, sulfonated tetrafluoroethylene, sulfonated fluoropolymer, co-polymers, different polymers, composites of polymers, or combinations thereof. In one embodiment of the electrodialysis cell, the polymer structures of the cation exchange membrane are functionalized with sulfone groups, carboxylic acid groups, phosphate groups, other negatively charged functional groups, or combinations thereof.
- In one embodiment of the membrane electrolysis cell, an anion exchange membrane is comprised of a functionalized polymer structure. The polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof. In one embodiment of the membrane, the functional groups are part of the polymer backbone. In one embodiment of the membrane, functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions. In one embodiment of the membrane, the functional group may be benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilised quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
- In one embodiment of the electrochemical cell, an anion exchange membrane is comprised of a functionalized polymer structure. The polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof. In one embodiment of the membrane, the functional groups are part of the polymer backbone. In one embodiment of the membrane, functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions. In one embodiment of the membrane, the functional group may be benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilised quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
- In one embodiment of the electrodialysis cell, an anion exchange membrane is comprised of a functionalized polymer structure. The polymer structure may be comprised of polyarylene ethers, polysulfones, polyether ketones, polyphenylenes, perfluorinated polymers, polybenzimidazole, polyepichlorohydrins, unsaturated polypropylene, polyethylene, polystyrene, polyvinylbenzyl chlorides, polyphosphazenes, polyvinyl alcohol, polytetrafluoroethylene, polyvinyl chloride, polyvinylidene fluoride, alterations of these polymers or other kinds of polymers, or composites thereof. In one embodiment of the membrane, the functional groups are part of the polymer backbone. In one embodiment of the membrane, functional groups are added using plasma techniques, radiation-grafting, or by other functionalization reactions. In one embodiment of the membrane, the functional group may be benzyltrialkylammonium, alkyl-side-chain quaternary ammonium groups, crosslinking diammonium groups, quinuclidinium-based quaternary ammonium groups, imidazolium groups, pyridinium groups, pentamethylguanidinium groups, alkali stabilised quaternary phosphonium groups, metal containing cation groups, other cation containing groups, or combinations thereof.
- In one embodiment of the membrane electrolysis cell, the membrane may have a thickness of less than 10 μm, less than 50 μm, less than 200 μm, less than 400 μm, or less than 1,000 μm. In one embodiment of the membrane electrolysis cell, the membranes may have a thickness of greater than 1,000 μm. In one embodiment of the membrane electrolysis cell, the membrane may have a thickness of about 1 μm to about 1000 μm, about 1 μm to about 800 μm, about 1 μm to about 600 μm, about 1 μm to about 400 μm, about 1 μm to about 200 μm, about 1 μm to about 100 μm, about 1 μm to about 90 μm, about 1 μm to about 80 μm, about 1 μm to about 70 μm, about 1 μm to about 60 μm, about 1 μm to about 50 μm, about 1 μm to about 40 μm, about 1 μm to about 30 μm, about 1 μm to about 20 μm, about 1 μm to about 15 μm, or about 1 μm to about 10 μm.
- In one embodiment of the electrochemical cell, the membrane may have a thickness of less than 10 μm, less than 50 μm, less than 200 μm, less than 400 μm, or less than 1,000 μm. In one embodiment of the electrochemical cell, the membranes may have a thickness of greater than 1,000 μm. In one embodiment of the electrochemical cell, the membrane may have a thickness of about 1 μm to about 1000 μm, about 1 μm to about 800 μm, about 1 μm to about 600 μm, about 1 μm to about 400 μm, about 1 μm to about 200 μm, about 1 μm to about 100 μm, about 1 μm to about 90 μm, about 1 μm to about 80 μm, about 1 μm to about 70 μm, about 1 μm to about 60 μm, about 1 μm to about 50 μm, about 1 μm to about 40 μm, about 1 μm to about 30 μm, about 1 μm to about 20 μm, about 1 μm to about 15 μm, or about 1 μm to about 10 μm.
- In one embodiment of the electrodialysis cell, the membrane may have a thickness of less than 10 μm, less than 50 μm, less than 200 μm, less than 400 μm, or less than 1,000 μm. In one embodiment of the electrodialysis cell, the membranes may have a thickness of greater than 1,000 μm. In one embodiment of the electrodialysis cell, the membrane may have a thickness of about 1 μm to about 1000 μm, about 1 μm to about 800 μm, about 1 μm to about 600 μm, about 1 μm to about 400 μm, about 1 μm to about 200 μm, about 1 μm to about 100 μm, about 1 μm to about 90 μm, about 1 μm to about 80 μm, about 1 μm to about 70 μm, about 1 μm to about 60 μm, about 1 μm to about 50 μm, about 1 μm to about 40 μm, about 1 μm to about 30 μm, about 1 μm to about 20 μm, about 1 μm to about 15 μm, or about 1 μm to about 10 μm.
- In one embodiment, an electrolysis system contains electrolysis cells that may be two-compartment electrolysis cells or three-compartment electrolysis cells.
- In one embodiment of a two-compartment electrolysis cell, the cell contains a first compartment that contains an electrochemically oxidizing electrode. A lithium salt solution enters the first compartment and is converted into an acidified solution. In one embodiment of a two-compartment electrolysis cell, the cell contains a second compartment containing an electrochemically reducing electrode. This second compartment takes as an input a water or dilute LiOH solution, and produces as an output a more concentrated LiOH solution. In one embodiment, the compartments are separated by a cation-conducting membrane that limits transport of anions.
- In one embodiment of a three-compartment electrolysis cell, the cell contains a first compartment containing an electrochemically oxidizing electrode. The first compartment takes as an input water or a dilute salt solution, and produces as an output an acidified solution. In one embodiment of a three-compartment electrolysis cell, the cell contains a second compartment containing an electrochemically reducing electrode. This second compartment takes as an input a water or dilute hydroxide solution, and produces as an output a more concentrated hydroxide solution. In one embodiment of a three-compartment electrolysis cell, the cell contains a third compartment containing no electrode, which is located between the first and second compartment, and takes as an input a concentrated lithium salt solution, and produces as an output a dilute lithium salt solution. In one embodiment, the first and the third compartments are separated by an anion-conducting membrane that limits transport of cations. In one embodiment, the second and the third compartments are separated by a cation-conducting membrane that limits transport of anions.
- In one embodiment of the electrolysis cell, the electrodes may be comprised of titanium, niobium, zirconium, tantalum, magnesium, titanium dioxide, oxides thereof, or combinations thereof. In one embodiment of the electrolysis cell, the electrodes may be coated with platinum, TiO2, ZrO2, Nb2O5, Ta2O5, SnO2, IrO2, RuO2, PtOx, mixed metal oxides, graphene, derivatives thereof, or combinations thereof. In one embodiment of the electrolysis cell, the electrodes may be comprised of steel, stainless steel, nickel, nickel alloys, steel alloys, or graphite.
- In one embodiment of the electrolysis system, the lithium salt solution is a LiCl solution optionally containing HCl. In one embodiment of the electrolysis system, the electrochemically oxidizing electrode oxides chloride ions to produce chlorine gas.
- In one embodiment of the electrolysis system, the lithium salt solution is a Li2SO4 solution optionally containing H2SO4. In one embodiment of the electrolysis system, the electrochemically oxidizing electrode oxidizes water, hydroxide, or other species to produce oxygen gas.
- In one embodiment of the electrolysis system, the electrochemically reducing electrode reduces hydrogen ions to produce hydrogen gas. In one embodiment of the electrolysis system, the chamber containing the electrochemically reducing electrode produces a hydroxide solution or increases the hydroxide concentration of a solution.
- In one embodiment of the electrolysis system, chlorine and hydrogen gas are burned to produce HCl in an HCl burner. In one embodiment, the HCl burner is a column maintained at approximately 100-300 or 300-2,000 degrees Celsius. In one embodiment, HCl produced in the HCl burner is cooled through a heat exchange and absorbed into water in an absorption tower to produce aqueous HCl solution. In one embodiment, the HCl solution produced from the HCl burner is used to elute lithium from an ion exchange system.
- In one embodiment, the pH of the acidified solution leaving the electrolysis cell may be 0 to 1, −2 to 0, 1 to 2, less than 2, less than 1, or less than 0. In some embodiments, the membrane electrolysis cell is an electrodialysis cell with multiple compartments. In some embodiments, the electrodialysis cell may have more than about two, more than about five, more than about 10, or more than about twenty compartments.
- In one embodiment, NaCl is recovered from the liquid resource by removing water therefrom, and then cooling said liquid resource. In one embodiment, water is removed from the liquid resource by reducing pressure, distillation, or combinations thereof. In one embodiment, water is removed from the liquid resource using any separation process described herein and/or distillation. In one embodiment, NaCl is recovered from the liquid resource by removing water therefrom, cooling said liquid resource, or combinations thereof.
- In one embodiment, the base added to precipitate metals from the liquid resource may be calcium hydroxide or sodium hydroxide. In one embodiment, the calcium hydroxide or sodium hydroxide is produced as described herein. In one embodiment, the base may be added to the liquid resource as an aqueous solution with a base concentration that may be less than 1N, 1-2 N, 2-4 N, 4-10 N, 10-20 N, or 20-40 N. In one embodiment, the base may be added to the liquid resource as a solid.
- In one embodiment, the acid may be added to the precipitated metals to dissolve the precipitated metals before mixing the redissolved metals with a processed liquid resource (e.g., raffinate), liquid resource, water, waste water, another liquid, or combinations thereof. In one embodiment, the acid may be added to the liquid resource to acidify the liquid resource, and the precipitated metals may be combined with the acidified liquid resource to redissolve the precipitated metals. In one embodiment, the acid is produced as described herein.
- In one embodiment, metals recovered from a liquid resource may be further processed downstream to produce high purity liquids and solids. In one embodiment, metals recovered from the liquid resource may be purified with ion exchange, solvent extraction, membranes, filtration, or other purification technologies. In one embodiment, metals may be converted from a dissolved form to a solid form. In one embodiment, metals may be converted using precipitation, electrolysis, electrowinning, chelation, or crystallization.
- In one embodiment, lithium may be converted from lithium chloride or lithium sulfate to lithium carbonate or lithium hydroxide. In one embodiment, lithium may be purified by precipitating multivalent metals using sodium carbonate, by removing multivalent metals using ion exchange, by removing boron using ion exchange, by removing impurities using membranes, by removing impurities using solvent extraction, or combinations thereof. In one embodiment, lithium may be converted from lithium chloride or lithium sulfate solution to a lithium carbonate solid by addition of sodium carbonate, sodium carbonate solution, carbon dioxide, sodium hydroxide, or combinations thereof. In one embodiment, lithium may be converted form lithium sulfate to lithium hydroxide by addition of sodium hydroxide, crystallization of sodium sulfate, and then crystallization of lithium hydroxide. In one embodiment, lithium may be converted from lithium carbonate to lithium hydroxide by addition of calcium hydroxide.
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FIG. 1 depicts an exemplary flowchart for separating transition metals from a liquid resource for a lithium recovery process described herein. A liquid resource (e.g., raw brine (102)) is pumped from a geothermal reservoir. The raw brine contains 50,000 mg/L Na, 50,000 mg/L Ca, 200 mg/L Li, 1,000 mg/L Fe, 800 mg/L Mn, 50 mg/L Pb, and other dissolved metals. An electrochemical cell (not shown) is used to convert NaCl into aqueous solutions of HCl and NaOH. The aqueous NaOH (104) is added to the brine to precipitate (106) Fe, Mn, and Pb, such that the raw brine becomes a slurry (108) comprising precipitates. The precipitates are separated from the raw brine using a flocculant and a gravity sedimentation tank (110) to form a feed liquid (feed brine (112)) and a concentrated slurry (120) containing the precipitates. The feed brine (112) contains <5 mg/L Fe, <10 mg/L Mn, and <10 mg/L Pb. The feed brine is processed (114) to recover lithium by contacting the feed brine with an ion exchange material, which selectivity absorbs the lithium. The lithium depleted brine is now a raffinate (e.g., spent brine 116). After lithium recovery, the HCl solution (118) is added to the concentrated slurry (120) containing the precipitates to redissolve (122) the precipitates. Then the redissolved metals (redissolved precipitates) are mixed with theraffinate 116 to form a raffinate mixture that is reinjected (124) into the geothermal reservoir. -
FIG. 2 depicts an exemplary flowchart for separating transition metals from a liquid resource using a hydrocyclone for a lithium recovery process described herein. A liquid resource (e.g., raw brine (202)) is pumped from a geothermal reservoir. The raw brine contains 80,000 mg/L Na, 30,000 mg/L Ca, 300 mg/L Li, 1,500 mg/L Fe, 1,200 mg/L Mn, and other dissolved metals. NaCl is recovered from the raw brine by removing water and cooling the brine (not shown). An electrochemical cell (not shown) is used to convert the NaCl into aqueous solutions of HCl and NaOH. The aqueous NaOH (204) is added to the raw brine to precipitate (206) Fe and Mn, such that the raw brine becomes a slurry (208) comprising precipitates. The precipitates are separated from the raw brine using a hydrocyclone (210) to form a feed liquid (feed brine (212)) and a concentrated slurry (220) containing the precipitates. The feed brine (212) contains 2 mg/L Fe and 5 mg/L Mn. The feed brine is processed (214) to recover lithium by contacting the feed brine with an ion exchange material, which selectivity absorbs the lithium in an ion exchange column. The lithium depleted brine is now a raffinate (e.g., spent brine 216). After lithium recovery, the concentrated slurry (220) containing the precipitates are added to the raffinate (216) and HCl (218) is added to the resulting mixture to redissolve (222) the precipitates into the raffinate, forming a raffinate mixture. The raffinate mixture is then reinjected (224) into the geothermal reservoir. -
FIG. 3 depicts an exemplary flowchart for separating transition metals from a liquid resource using a centrifuge for a lithium recovery process described herein. A liquid resource (e.g., raw brine (302)) is pumped from a geothermal reservoir. The raw brine contains 60,000 mg/L Na, 40,000 mg/L Ca, 200 mg/L Li, 1,800 mg/L Fe, 1,000 mg/L Mn, and other dissolved metals. An electrochemical cell (not shown) is used to convert the NaCl into aqueous solutions of HCl and NaOH. The aqueous NaOH (304) is added to the raw brine to precipitate (306) Fe and Mn such that the raw brine becomes a slurry (308) comprising precipitates. The precipitates are separated from the raw brine using a centrifuge to form a feed liquid (feed brine (312)) and a concentrated slurry (320) containing the precipitates. The feed brine (312) contains 200 mg/L Li, 2 mg/L Fe, and 6 mg/L Mn. The feed brine is processed (314) to recover lithium by contacting the feed brine with an ion exchange material, which selectivity absorbs the lithium in an ion exchange column. The feed brine is depleted of lithium to form a raffinate (e.g., spent brine (316)). HCl (318) is added to the concentrated slurry (320) to redissolve (322) the precipitates forming a transition metal concentrate, which is then mixed with the spent brine (316) to form a raffinate mixture. The raffinate mixture containing the redissolved transition metals is then reinjected (324) into the geothermal reservoir. - Exemplary Aspects for Separating Undesirable Metals from a Liquid Resource
- In one aspect, disclosed herein is a process for recovering a desirable metal from a liquid resource, the process comprising: a) precipitating an undesirable metal from the liquid resource to form an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering said desirable metal from the feed liquid to form a raffinate; and d) redissolving said undesirable metal precipitate into said raffinate to form a raffinate mixture. In some embodiments, said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metal comprises lithium. In some embodiments, said undesirable metal comprises a transition metal. In some embodiments, said desirable metals comprise lithium and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said undesirable metals comprise transition metals and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metals comprise lithium, said undesirable metals comprise transition metals, and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said precipitating comprises adding a base to the liquid resource. In some embodiments, said precipitating comprises adding a base and/or an oxidant to the liquid resource. In some embodiments, said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air and/or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with said undesirable metal precipitate. In some embodiments, said combining an acid with said undesirable metal precipitate occurs 1) prior to combining said undesirable metal precipitate with said raffinate, or 2) after combining said undesirable metal precipitate with said raffinate. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said redissolving comprises adding hydrochloric acid or sulfuric acid to dissolve said undesirable metal precipitate. In some embodiments, said precipitating comprises adding a base to the liquid resource, and said redissolving comprises combining an acid with the undesirable metal precipitate, wherein said acid and said base are produced with an electrochemical cell. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, said salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said precipitating comprises adding chemicals to the liquid resource. In some embodiments, said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, said process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground. In some embodiments, said process further comprises agglomerating the undesirable metal precipitate. In some embodiments, said agglomerating comprises adding a flocculant to the liquid resource. In some embodiments, said separating the undesirable metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof. In some embodiments, said separating the undesirable metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, said separating the undesirable metal precipitate further comprises moving the undesirable metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the undesirable metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series. In some embodiments, said precipitating of an undesirable metal forms a slurry comprising the undesirable metal precipitate and feed liquid. In some embodiments, the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof. In some embodiments, the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In some embodiments, the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In some embodiments, a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate. In some embodiments, a plurality of desirable metals are separated from the feed liquid. In some embodiments, the desirable metal is different from the undesirable metal.
- In another aspect, disclosed herein is a process for separating an undesirable metal from a liquid resource the process comprising: a) adding a base to said liquid resource to precipitate said undesirable metal thereby forming an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering a desirable metal from the feed liquid; and d) combining an acid to said undesirable metal precipitate to form a solution of redissolved undesirable metals for disposal. In some embodiments, said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metal comprises lithium. In some embodiments, said undesirable metal comprises a transition metal. In some embodiments, said process further comprises an oxidant with said base to said liquid resource. In some embodiments, said base comprises NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said oxidant comprises air and/or hydrogen peroxide to the liquid resource. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, the salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, said disposal comprises injecting the solution of redissolved undesirable metals underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said disposal comprises injecting the solution of redissolved undesirable metals into said reservoir. In some embodiments, the reservoir is located underground. In some embodiments, said process further comprises agglomerating the undesirable metal precipitate. In some embodiments, said agglomerating comprises adding a flocculant to the liquid resource. In some embodiments, said separating the undesirable metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof. In some embodiments, said separating the undesirable metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, said separating the undesirable metal precipitate further comprises moving the undesirable metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the undesirable metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series. In some embodiments, said precipitating of an undesirable metal forms a slurry comprising the undesirable metal precipitate and feed liquid. In some embodiments, the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof. In some embodiments, the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In some embodiments, the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In some embodiments, a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate. In some embodiments, a plurality of desirable metals are separated from the feed liquid. In some embodiments, the desirable metal is different from the undesirable metal.
- In another aspect, disclosed herein is a process for recovering lithium from a liquid resource: a) precipitating a transition metal from said liquid resource to form a transition metal precipitate; b) separating said transition metal precipitate from the liquid resource to form a feed liquid; c) recovering said lithium from said feed liquid to form a raffinate, wherein said recovering of lithium comprises contacting said feed liquid with ion exchange particles that absorb said lithium while releasing protons; and d) redissolving said transition metal precipitate into said raffinate to form a raffinate mixture. In some embodiments, said precipitating comprises adding a base to the liquid resource. In some embodiments, said precipitating comprises adding a base and an oxidant to the liquid resource. In some embodiments, said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with the transition metal precipitate. In some embodiments, said combining an acid with said transition metal precipitate occurs 1) prior to combining said transition metal precipitate with said raffinate, or 2) after combining said transition metal precipitate with said raffinate. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said redissolving comprises adding hydrochloric acid or sulfuric acid to dissolve said transition metal precipitate. In some embodiments, said precipitating comprises adding a base to the liquid resource, and said redissolving comprises combining an acid with the transition metal precipitate, wherein said acid and said base are produced with an electrochemical cell. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, said salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said precipitating comprises adding chemicals to the liquid resource. In some embodiments, said separating of said transitional metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In some embodiments, said separating of said transitional metal comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of said transitional metal comprises using a centrifuge. In some embodiments, said process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground. In some embodiments, said process further comprises agglomerating the transition metal precipitate. In some embodiments, said agglomerating comprises adding a flocculant to the liquid resource. In some embodiments, said separating the transition metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof. In some embodiments, said separating the transition metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, said separating the transition metal precipitate further comprises moving the transition metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the transition metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series. In some embodiments, said precipitating of a transition metal forms a slurry comprising the transition metal precipitate and feed liquid. In some embodiments, the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof. In some embodiments, the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In some embodiments, a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate. In some embodiments, a plurality of desirable metals are separated from the feed liquid. In some embodiments, the desirable metal is different from the undesirable metal.
- In one aspect, disclosed herein is a process for recovering a desirable metal from a liquid resource, the process comprising: a) precipitating an undesirable metal from the liquid resource to form an undesirable metal precipitate; b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid; c) recovering said desirable metal from the feed liquid to form a raffinate; and d) redissolving said undesirable metal precipitate into said raffinate, a liquid resource, water, waste water, another liquid, or combinations thereof to form a raffinate mixture. In some embodiments, said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metal comprises lithium. In some embodiments, said undesirable metal comprises a transition metal. In some embodiments, said desirable metals comprise lithium and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said undesirable metals comprise transition metals and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metals comprise lithium, said undesirable metals comprise transition metals, and said recovering is done by contacting said feed liquid with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said precipitating comprises adding a base to the liquid resource. In some embodiments, said precipitating comprises adding a base and/or an oxidant to the liquid resource. In some embodiments, said precipitating comprises adding NaOH and/or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating comprises adding air and/or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving comprises combining an acid with said undesirable metal precipitate. In some embodiments, said combining an acid with said undesirable metal precipitate occurs 1) prior to combining said undesirable metal precipitate with said raffinate, liquid resource, water, waste water, another liquid, or combinations thereof, or 2) after combining said undesirable metal precipitate with said raffinate, liquid resource, water, waste water, another liquid, or combinations thereof. In some embodiments, the acid comprises hydrochloric acid and/or sulfuric acid. In some embodiments, said redissolving comprises adding hydrochloric acid or sulfuric acid to dissolve said undesirable metal precipitate. In some embodiments, said precipitating comprises adding a base to the liquid resource, and said redissolving comprises combining an acid with the undesirable metal precipitate, wherein said acid and said base are produced with an electrochemical cell. In some embodiments, said acid and/or said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said acid and/or said base are produced from a salt solution. In some embodiments, said acid and/or said base are produced by splitting said salt solution. In some embodiments, said salt solution comprises a sodium chloride solution. In some embodiments, said acid and/or said base are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base. In some embodiments, said process further comprises extracting sodium chloride from the liquid resource to form the sodium chloride solution. In some embodiments, said precipitating comprises adding chemicals to the liquid resource. In some embodiments, said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating of the undesirable metal precipitate comprises using a centrifuge. In some embodiments, said process further comprises injecting the raffinate mixture underground. In some embodiments, the liquid resource is obtained from a reservoir. In some embodiments, the liquid resource is pumped out of the reservoir. In some embodiments, said process further comprises injecting the raffinate mixture into said reservoir. In some embodiments, the reservoir is located underground. In some embodiments, said process further comprises agglomerating the undesirable metal precipitate. In some embodiments, said agglomerating comprises adding a flocculant to the liquid resource. In some embodiments, said separating the undesirable metal precipitate comprises using a filter, wherein said filter is a belt filter, plate-and-frame filter press, pressure vessel containing filter elements, rotary drum filter, rotary disc filter, cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforate basket centrifuge, a three-point centrifuge, a peeler type centrifuge, a pusher centrifuge, or combinations thereof. In some embodiments, said separating the undesirable metal precipitate further comprises using gravity, centrifugal force, an electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, crow-flow filtration, and/or pumping suspensions across the surface of the filter. In some embodiments, said separating the undesirable metal precipitate further comprises moving the undesirable metal precipitate and the feed liquid tangentially to the filter. In some embodiments, said separating the undesirable metal precipitate further comprises gravitational, magnetic, centrifugal sedimentation, and/or other means of solid-liquid separation before, during, and/or after filtering. In some embodiments, said process further comprises a plurality of separating processes operated in parallel and/or series. In some embodiments, said precipitating of an undesirable metal forms a slurry comprising the undesirable metal precipitate and feed liquid. In some embodiments, the liquid resource is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof. In some embodiments, the desirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In some embodiments, the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals. In some embodiments, a plurality of undesirable metals are precipitated and separated from the liquid resource, and redissolved into the raffinate, liquid resource, water, waste water, another liquid, or combinations thereof. In some embodiments, a plurality of desirable metals are separated from the feed liquid. In some embodiments, the desirable metal is different from the undesirable metal.
- In an embodiment, for an aspect disclosed herein, undesirable metals are removed from a liquid resource through precipitation, removal from the liquid resource, redissolution, and mixing with another liquid for disposal. In one embodiment, undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, removal from the resulting solids from the liquid resource, redissolution of the resulting solids by addition of acid, mixing of the redissolved undesirable metals with another liquid, and disposal of the other liquid. In one embodiment, undesirable metals are removed from a liquid resource through precipitation by addition of base, oxidant, or combinations thereof, removal from the resulting solids from the liquid resource, redissolution of the resulting solids by addition of acid, mixing of the redissolved undesirable metals with waste water, and disposal of the waste water. In one embodiment, redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids. In one embodiment, redissolved undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal. In one embodiment, solids of undesirable metals may be dissolved in raffinate, waste water, liquid resource, water, or other liquids for disposal. In one embodiment, undesirable metals may be mixed with raffinate, waste water, liquid resource, water, or other liquids for disposal.
- In another aspect, disclosed herein is a process for recovering lithium from a liquid resource: a) precipitating a transition metal from said liquid resource to form a transition metal precipitate; b) separating said transition metal precipitate from the liquid resource to form a feed liquid; c) recovering said lithium from said feed liquid to form a raffinate, wherein said recovering of lithium comprises contacting said feed liquid with ion exchange particles that absorb said lithium while releasing protons; and d) redissolving said transition metal precipitate into said raffinate a liquid resource, water, waste water, another liquid, or combinations thereof to form a raffinate mixture.
- In another aspect, disclosed herein is a process for recovering a desirable metal from a liquid resource, the process comprising: a) eluting an undesirable metal from the liquid resource through ion exchange; b) separating the undesirable metal from the eluate; and c) injecting the undesirable metal into a reservoir. In some embodiments, said separating the undesirable metal comprises using nano-filtration membranes, precipitation, or combinations thereof. In some embodiments, said process further comprises producing a retentate comprising the dissolved undesirable metal using nano-filtration membranes. In some embodiments, said process further comprises separating the dissolved undesirable metal from the retentate. In some embodiments, the liquid resources is a natural brine, a dissolved salt flat, seawater, concentrated seawater, a geothermal brine, a desalination effluent, a concentrated brine, a processed brine, an oilfield brine, a liquid from an ion exchange process, a liquid from a solvent extraction process, a synthetic brine, a leachate from an ore or combination of ores, a leachate from a mineral or combination of minerals, a leachate from a clay or combination of clays, a leachate from recycled products, a leachate from recycled materials, or combinations thereof. In some embodiments, the undesirable metal is Li, Na, K, Rb, Cs, Fr, Be, Mg, Ca, Sr, Ba, Ra, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Tc, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, Si, Ge, Sn, Pb, As, Sb, Bi, Se, Te, Po, and/or other metals.
- In another aspect, disclosed herein is a process for recovering desirable metals from a liquid resource that also contains undesirable metals, said process comprising: a) precipitating the undesirable metals from the liquid resource to form one or more precipitates; b) separating said precipitates from the liquid resource; c) recovering said desirable metals from the liquid resource; and d) redissolving said undesirable metals into said liquid resource. In some embodiments, said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metals comprise lithium. In some embodiments, said undesirable metals comprise transition metals. In some embodiments, said desirable metals comprise lithium and said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said undesirable metals comprise transition metals and said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said desirable metals comprise lithium, said undesirable metals comprise transition metals, and said recovering is done by contacting said liquid resource with ion exchange particles that absorb said desirable metals while releasing protons. In some embodiments, said precipitating is done by adding base to the liquid resource. In some embodiments, said precipitating is done by adding base and oxidant to the liquid resource. In some embodiments, said precipitating is done by adding NaOH or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating is done by adding air or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving is done by adding acid to dissolve said precipitates. In some embodiments, said redissolving is done by adding hydrochloric acid or sulfuric acid to dissolve said precipitates. In some embodiments, said precipitating is done with a base and said redissolving is done with an acid, wherein said acid and said base are produced with an electrochemical cell. In some embodiments, said electrochemical cell comprises electrodes and membranes. In some embodiments, said separating of precipitates is done using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In some embodiments, said separating is done using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating is done using a centrifuge. In some embodiments, said undesirable metals are redissolved and disposed of by being injected underground.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- In another aspect, disclosed herein is a process for recovering lithium from a liquid resource that also contains transition metals, said process comprising: a) precipitating said transition metals from said liquid resource to form one or more precipitates; b) separating said precipitates from the liquid resource; c) recovering said lithium from said liquid resource by contacting said liquid resource with ion exchange particles that absorb lithium while releasing protons; and d) redissolving said transition metals into said liquid resource. In some embodiments, said precipitating is done by adding base to the liquid resource. In some embodiments, said precipitating is done by adding base and oxidant to the liquid resource. In some embodiments, said precipitating is done by adding NaOH or Ca(OH)2 to the liquid resource. In some embodiments, said precipitating is done by adding air or hydrogen peroxide to the liquid resource. In some embodiments, said redissolving is done by adding acid to dissolve said precipitates. In some embodiments, said redissolving is done by adding hydrochloric acid or sulfuric acid to dissolve said precipitates. In some embodiments, said precipitating is done with a base and redissolving is done with an acid, wherein said acid and said base are produced with an electrochemical cell. In some embodiments, the electrochemical cell comprises electrodes and membranes. In some embodiments, said separating of precipitates is done using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or combinations thereof. In some embodiments, said separating is done using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof. In some embodiments, said separating is done using a centrifuge. In some embodiments, said undesirable metals are redissolved and disposed of by being injected underground.
- In another aspect, disclosed herein is a process for separating transition metals from a liquid resource to facilitate recovery of lithium, comprising: a) adding base to said liquid resource to precipitate said transition metals as precipitates; b) separating said precipitates from the liquid resource; c) recovering said lithium from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource using gravity sedimentation; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource using centrifugal sedimentation; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) adding base to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource using filtration; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) splitting a salt solution into acid and base using an electrochemical cell; b)adding said base solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; and e) adding said acid solution to said precipitates to redissolve for disposal.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) splitting a salt solution into acid and base using an electrochemical cell; b) adding said base solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; and e) adding said acid solution to said precipitates to redissolve for disposal.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; b) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; and e) adding said hydrochloric acid solution to said precipitates to redissolve said precipitates for disposal.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; b) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; e) adding said hydrochloric acid solution to said precipitates to redissolve said precipitates; and 0 mixing the redissolved precipitates with the liquid resource.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; b) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; c) separating said precipitates from the liquid resource using filtration; d) recovering said desirable metals from the liquid resource; e) mixing said precipitates with the liquid resource to form a mixture; and 0 adding said hydrochloric acid to said mixture to redissolve the precipitates.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; 0 adding said hydrochloric acid solution to said precipitates to redissolve said precipitates; g) mixing the redissolved precipitates with the liquid resource; and h) reinjecting the liquid resource into a reservoir.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; f) mixing said precipitates with the liquid resource to form a mixture; g) adding said hydrochloric acid to said mixture to redissolve the precipitates; and h) reinjecting said liquid resource into a reservoir.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using centrifugation; e) recovering said desirable metals from the liquid resource; f) mixing said precipitates with the liquid resource to form a mixture; g) adding said hydrochloric acid to said mixture to redissolve the precipitates; and h) reinjecting said liquid resource into a reservoir.
- In another aspect, disclosed herein is a process for separating transition metals from a liquid resource to facilitate recovery of lithium, comprising: a) pumping said liquid resource out of a reservoir; b) processing a sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said transition metals as precipitates; d) separating said precipitates from said liquid resource using centrifugation; e) recovering said lithium from said liquid resource by contacting said liquid resource with ion exchange particles that absorb said lithium while releasing protons; f) redissolving said precipitates into said liquid resource by adding said hydrochloric acid solution; and g) reinjecting said liquid resource into a reservoir.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) extracting sodium chloride from said liquid resource to form a sodium chloride solution; b) processing said sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; 0 adding said hydrochloric acid solution to said precipitates to redissolve said precipitates; and g) mixing the redissolved precipitates with the liquid resource.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) extracting sodium chloride from said liquid resource to form a sodium chloride solution; b) processing said sodium chloride solution into a hydrochloric acid solution and a sodium hydroxide solution using one or more electrochemical cells; c) adding said sodium hydroxide solution to said liquid resource to precipitate said undesirable metals as precipitates; d) separating said precipitates from the liquid resource using filtration; e) recovering said desirable metals from the liquid resource; 0 mixing said precipitates with the liquid resource to form a mixture; and g) adding said hydrochloric acid to said mixture to redissolve the precipitates.
- In another aspect, disclosed herein is a process for separating undesirable metals from a liquid resource to facilitate recovery of desirable metals, said process comprising: a) adding chemicals to said liquid resource to precipitate said undesirable metals as precipitates; b) separating said precipitates from the liquid resource; c) recovering said desirable metals from the liquid resource; and d) adding acid to said precipitates to redissolve for disposal.
- In some embodiments, in any process disclosed herein, said desirable metals include lithium. In some embodiments, in any process disclosed herein, said undesirable metals include iron and manganese.
- While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. It should be understood that various alternatives to the embodiments of the invention described herein is optionally employed in practicing the invention. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby.
Claims (30)
1. A process for recovering a desirable metal from a liquid resource, the process comprising:
a) precipitating an undesirable metal from the liquid resource to form an undesirable metal precipitate;
b) separating said undesirable metal precipitate from the liquid resource to form a feed liquid;
c) recovering said desirable metal from the feed liquid to form a raffinate; and
d) redissolving said undesirable metal precipitate into said raffinate to form a raffinate mixture.
2. The process of claim 1 , wherein said recovering comprises contacting said feed liquid with ion exchange particles that absorb said desirable metal while releasing protons.
3. The process of claim 1 , wherein said desirable metal comprises lithium.
4. The process of claim 1 , wherein said undesirable metal comprises a transition metal.
5. The process of claim 1 , wherein said precipitating comprises adding a base, an oxidant, or both, to the liquid resource.
6. The process claim 1 , wherein said precipitating comprises adding NaOH, Ca(OH)2, or both, to the liquid resource.
7. The process of claim 1 , wherein said redissolving comprises combining an acid with said undesirable metal precipitate.
8. The process of claim 7 , wherein said combining an acid with said undesirable metal precipitate occurs 1) prior to combining said undesirable metal precipitate with said raffinate, or 2) after combining said undesirable metal precipitate with said raffinate.
9. The process of claim 7 , wherein the acid comprises hydrochloric acid, sulfuric acid, or both.
10. The process of claim 1 , wherein said precipitating comprises adding a base to the liquid resource, wherein said redissolving comprises combining an acid with said undesirable metal precipitate, wherein said acid, said base, or both are produced 1) with an electrochemical cell, or 2) from a salt solution.
11. The process of claim 10 , wherein said salt solution comprises a sodium chloride solution, wherein said acid, said base, or both, are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
12. The process of claim 1 , wherein said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof
13. The process of claim 12 , wherein said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof.
14. The process of claim 13 , wherein said separating of the undesirable metal precipitate comprises using a centrifuge.
15. The process of claim 1 , further comprising injecting the raffinate mixture underground.
16. The process of claim 1 , further comprising injecting the raffinate mixture into 1) a reservoir from where the liquid resource is obtained, 2) a different reservoir from the liquid resource is obtained, or 3) both.
17. A process for separating an undesirable metal from a liquid resource, the process comprising:
a) adding a base to said liquid resource to precipitate said undesirable metal, thereby forming an undesirable metal precipitate;
b) separating said undesirable metal precipitate from said liquid resource to form a feed liquid;
c) recovering a desirable metal from the feed liquid; and
d) combining an acid to said undesirable metal precipitate to form a solution of redissolved undesirable metals for disposal.
18. The process of claim 17 , wherein said recovering comprises contacting said feed liquid with ion exchange particles that absorbs said desirable metal while releasing protons.
19. The process of claim 17 , wherein said desirable metal comprises lithium.
20. The process of claim 17 , wherein said undesirable metal comprises a transition metal.
21. The process of claim 17 , further comprising adding an oxidant with said base to said liquid resource.
22. The process of claim 17 , wherein said base comprises NaOH, Ca(OH)2, or both.
23. The process of claim 17 , wherein the acid comprises hydrochloric acid, sulfuric acid, or both.
24. The process of claim 17 , wherein said acid, said base, or both, are produced 1) with an electrochemical cell, or 2) from a salt solution.
25. The process of claim 24 , wherein said salt solution comprises a sodium chloride solution, wherein said acid, said base, or both, are produced by processing said sodium chloride solution into a hydrochloric acid solution and/or a sodium hydroxide solution, wherein the hydrochloric acid solution comprises said acid and the sodium hydroxide solution comprises said base.
26. The process of claim 17 , wherein said separating of the undesirable metal precipitate comprises filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other methods of solid-liquid separation, or any combination thereof
27. The process of claim 26 , wherein said separating of the undesirable metal precipitate comprises using a filter, a settling tank, a clarifier, a hydrocyclone, a centrifuge, or combinations thereof
28. The process of claim 27 , wherein said separating of the undesirable metal precipitate comprises using a centrifuge.
29. The process of claim 17 , wherein said disposal comprises injecting the solution of redissolved undesirable metals underground.
30. The process of claim 17 , wherein said disposal comprises injecting the solution of redissolved undesirable metals into 1) a reservoir from where the liquid resource is obtained, 2) a different reservoir from the liquid resource is obtained, or 3) both.
Priority Applications (1)
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- 2021-01-07 KR KR1020227027413A patent/KR20220119166A/en unknown
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US11806641B2 (en) | 2016-11-14 | 2023-11-07 | Lilac Solutions, Inc. | Lithium extraction with coated ion exchange particles |
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US11986816B2 (en) | 2021-04-23 | 2024-05-21 | Lilac Solutions, Inc. | Ion exchange devices for lithium extraction |
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JP2023514803A (en) | 2023-04-11 |
CA3166921A1 (en) | 2021-07-15 |
EP4087825A1 (en) | 2022-11-16 |
US20210214820A1 (en) | 2021-07-15 |
EP4087825A4 (en) | 2024-01-24 |
KR20220119166A (en) | 2022-08-26 |
US11339457B2 (en) | 2022-05-24 |
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