CN115821040A - Solvent extraction system for efficiently extracting lithium - Google Patents
Solvent extraction system for efficiently extracting lithium Download PDFInfo
- Publication number
- CN115821040A CN115821040A CN202211585047.XA CN202211585047A CN115821040A CN 115821040 A CN115821040 A CN 115821040A CN 202211585047 A CN202211585047 A CN 202211585047A CN 115821040 A CN115821040 A CN 115821040A
- Authority
- CN
- China
- Prior art keywords
- lithium
- organic phase
- extraction
- solution
- extraction system
- 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.)
- Granted
Links
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 124
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 124
- 238000000638 solvent extraction Methods 0.000 title claims abstract description 28
- -1 carbonyl enol Chemical class 0.000 claims abstract description 30
- 239000000654 additive Substances 0.000 claims abstract description 10
- 230000000996 additive effect Effects 0.000 claims abstract description 10
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 8
- 239000011574 phosphorus Substances 0.000 claims abstract description 8
- 230000002209 hydrophobic effect Effects 0.000 claims abstract description 7
- 125000003118 aryl group Chemical group 0.000 claims abstract description 5
- 125000003545 alkoxy group Chemical group 0.000 claims abstract description 3
- 125000003277 amino group Chemical group 0.000 claims abstract description 3
- 238000000605 extraction Methods 0.000 claims description 92
- 239000000243 solution Substances 0.000 claims description 68
- 239000012074 organic phase Substances 0.000 claims description 57
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 45
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 40
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 18
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 18
- 239000008346 aqueous phase Substances 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 14
- 238000005406 washing Methods 0.000 claims description 14
- 239000003513 alkali Substances 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 12
- 239000012267 brine Substances 0.000 claims description 10
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 9
- 239000012071 phase Substances 0.000 claims description 7
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 6
- 229910003002 lithium salt Inorganic materials 0.000 claims description 6
- 159000000002 lithium salts Chemical class 0.000 claims description 6
- 239000012452 mother liquor Substances 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 5
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 4
- 239000003085 diluting agent Substances 0.000 claims description 4
- UEZVMMHDMIWARA-UHFFFAOYSA-M phosphonate Chemical compound [O-]P(=O)=O UEZVMMHDMIWARA-UHFFFAOYSA-M 0.000 claims description 4
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 4
- 238000001556 precipitation Methods 0.000 claims description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 2
- 229910019142 PO4 Inorganic materials 0.000 claims description 2
- 150000001335 aliphatic alkanes Chemical group 0.000 claims description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 2
- 150000002148 esters Chemical class 0.000 claims description 2
- 150000002576 ketones Chemical class 0.000 claims description 2
- AUONHKJOIZSQGR-UHFFFAOYSA-N oxophosphane Chemical compound P=O AUONHKJOIZSQGR-UHFFFAOYSA-N 0.000 claims description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 2
- 239000010452 phosphate Substances 0.000 claims description 2
- ACVYVLVWPXVTIT-UHFFFAOYSA-M phosphinate Chemical compound [O-][PH2]=O ACVYVLVWPXVTIT-UHFFFAOYSA-M 0.000 claims description 2
- 229910000027 potassium carbonate Inorganic materials 0.000 claims description 2
- 239000012266 salt solution Substances 0.000 claims description 2
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 description 26
- 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 22
- 229910052708 sodium Inorganic materials 0.000 description 22
- 239000011734 sodium Substances 0.000 description 22
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 12
- 229910052700 potassium Inorganic materials 0.000 description 10
- 239000011591 potassium Substances 0.000 description 10
- 239000011259 mixed solution Substances 0.000 description 9
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 8
- 239000011777 magnesium Substances 0.000 description 8
- 229910052749 magnesium Inorganic materials 0.000 description 8
- 239000002904 solvent Substances 0.000 description 8
- 239000003350 kerosene Substances 0.000 description 7
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 description 7
- 229910052808 lithium carbonate Inorganic materials 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 102100040653 Tryptophan 2,3-dioxygenase Human genes 0.000 description 5
- 101710136122 Tryptophan 2,3-dioxygenase Proteins 0.000 description 5
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 238000001728 nano-filtration Methods 0.000 description 4
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 125000000217 alkyl group Chemical group 0.000 description 3
- 238000004945 emulsification Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- PTTPXKJBFFKCEK-UHFFFAOYSA-N 2-Methyl-4-heptanone Chemical compound CC(C)CC(=O)CC(C)C PTTPXKJBFFKCEK-UHFFFAOYSA-N 0.000 description 2
- WBLGXIFKKXGJGJ-UHFFFAOYSA-N CC(CCCCCC)(C)OP(O)(=O)C Chemical compound CC(CCCCCC)(C)OP(O)(=O)C WBLGXIFKKXGJGJ-UHFFFAOYSA-N 0.000 description 2
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 2
- NTIZESTWPVYFNL-UHFFFAOYSA-N Methyl isobutyl ketone Chemical compound CC(C)CC(C)=O NTIZESTWPVYFNL-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- 239000012965 benzophenone Substances 0.000 description 2
- 125000001797 benzyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])([H])* 0.000 description 2
- XSIFPSYPOVKYCO-UHFFFAOYSA-N butyl benzoate Chemical compound CCCCOC(=O)C1=CC=CC=C1 XSIFPSYPOVKYCO-UHFFFAOYSA-N 0.000 description 2
- 229910052792 caesium Inorganic materials 0.000 description 2
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- MWKFXSUHUHTGQN-UHFFFAOYSA-N decan-1-ol Chemical compound CCCCCCCCCCO MWKFXSUHUHTGQN-UHFFFAOYSA-N 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 125000005594 diketone group Chemical group 0.000 description 2
- LQZZUXJYWNFBMV-UHFFFAOYSA-N dodecan-1-ol Chemical compound CCCCCCCCCCCCO LQZZUXJYWNFBMV-UHFFFAOYSA-N 0.000 description 2
- 125000003438 dodecyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 125000004051 hexyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- INHCSSUBVCNVSK-UHFFFAOYSA-L lithium sulfate Inorganic materials [Li+].[Li+].[O-]S([O-])(=O)=O INHCSSUBVCNVSK-UHFFFAOYSA-L 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 2
- WCJLCOAEJIHPCW-UHFFFAOYSA-N octyl 2-hydroxybenzoate Chemical compound CCCCCCCCOC(=O)C1=CC=CC=C1O WCJLCOAEJIHPCW-UHFFFAOYSA-N 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
- 229910052701 rubidium Inorganic materials 0.000 description 2
- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-UHFFFAOYSA-N 0.000 description 2
- 230000002195 synergetic effect Effects 0.000 description 2
- 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 2
- 125000006732 (C1-C15) alkyl group Chemical group 0.000 description 1
- BPIUIOXAFBGMNB-UHFFFAOYSA-N 1-hexoxyhexane Chemical compound CCCCCCOCCCCCC BPIUIOXAFBGMNB-UHFFFAOYSA-N 0.000 description 1
- AOPDRZXCEAKHHW-UHFFFAOYSA-N 1-pentoxypentane Chemical compound CCCCCOCCCCC AOPDRZXCEAKHHW-UHFFFAOYSA-N 0.000 description 1
- YEVQZPWSVWZAOB-UHFFFAOYSA-N 2-(bromomethyl)-1-iodo-4-(trifluoromethyl)benzene Chemical compound FC(F)(F)C1=CC=C(I)C(CBr)=C1 YEVQZPWSVWZAOB-UHFFFAOYSA-N 0.000 description 1
- 241001086438 Euclichthys polynemus Species 0.000 description 1
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 1
- UIHCLUNTQKBZGK-UHFFFAOYSA-N Methyl isobutyl ketone Natural products CCC(C)C(C)=O UIHCLUNTQKBZGK-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- ZCZSIDMEHXZRLG-UHFFFAOYSA-N acetic acid heptyl ester Natural products CCCCCCCOC(C)=O ZCZSIDMEHXZRLG-UHFFFAOYSA-N 0.000 description 1
- CNLWCVNCHLKFHK-UHFFFAOYSA-N aluminum;lithium;dioxido(oxo)silane Chemical compound [Li+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O CNLWCVNCHLKFHK-UHFFFAOYSA-N 0.000 description 1
- 150000005840 aryl radicals Chemical class 0.000 description 1
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- JPXGPRBLTIYFQG-UHFFFAOYSA-N heptan-4-yl acetate Chemical compound CCCC(CCC)OC(C)=O JPXGPRBLTIYFQG-UHFFFAOYSA-N 0.000 description 1
- 125000003187 heptyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 229910052629 lepidolite Inorganic materials 0.000 description 1
- 229910001416 lithium ion Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- ZQQUEKSGSWSLKF-UHFFFAOYSA-N n,n-dibutyl-2-hydroxybenzamide Chemical compound CCCCN(CCCC)C(=O)C1=CC=CC=C1O ZQQUEKSGSWSLKF-UHFFFAOYSA-N 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 125000005447 octyloxy group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])O* 0.000 description 1
- 239000010826 pharmaceutical waste Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000011151 potassium sulphates Nutrition 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229960000581 salicylamide Drugs 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 229910052642 spodumene Inorganic materials 0.000 description 1
- STCOOQWBFONSKY-UHFFFAOYSA-N tributyl phosphate Chemical compound CCCCOP(=O)(OCCCC)OCCCC STCOOQWBFONSKY-UHFFFAOYSA-N 0.000 description 1
- SFENPMLASUEABX-UHFFFAOYSA-N trihexyl phosphate Chemical compound CCCCCCOP(=O)(OCCCCCC)OCCCCCC SFENPMLASUEABX-UHFFFAOYSA-N 0.000 description 1
- ZMBHCYHQLYEYDV-UHFFFAOYSA-N trioctylphosphine oxide Chemical compound CCCCCCCCP(=O)(CCCCCCCC)CCCCCCCC ZMBHCYHQLYEYDV-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- 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
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Extraction Or Liquid Replacement (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a solvent extraction system for extracting lithium efficiently, which comprises carbonyl enol with a structure shown as a formula (IA or IB), organic phosphorus with a structure shown as a formula (IIA, IIB, IIC or IID), and an optional polar hydrophobic additive. In the formulae (IA) and (IB), R 1 、R 2 、R 3 Same or different and is H or C 1 ‑C 15 Alkyl or aryl, or alkoxy, or amine groups; or, R 1 And R 3 Or R 2 And R 3 Are connected into a ring. In the formulae (IIA, IIB, IIC, IID), R 1 、R 2 、R 3 Identical or different, each independently is C 1 ‑C 15 Alkyl or aryl of (a).
Description
Technical Field
The invention belongs to the technical field of chemical separation, and particularly relates to a solvent extraction system for efficiently extracting lithium.
Background
Lithium is the metal with the highest energy density, is an important constituent element of a lithium ion battery, and has an important role in the field of new energy. With the increasing popularity of electric vehicles, the demand of lithium salts in the market is rapidly increasing. However, lithium is associated with various alkali metals, thereby resulting in low lithium extraction yield and low lithium salt purity. Especially for low-grade lithium resources, the extraction efficiency of lithium is extremely low at present.
Currently, lithium salts are mainly derived from ores (such as spodumene and lepidolite), salt lake brines and battery recycling. Extraction of lithium from these three sources all involves the separation of lithium from other alkali metals (sodium, potassium), such as: (1) The salt lake brine after magnesium removal is a mixed solution containing lithium, sodium and potassium; (2) The solution after extracting the divalent and trivalent metals from the battery leachate is a mixed solution containing lithium and sodium; (3) Lithium-containing wastewater generated in the battery recovery process is a mixed solution containing lithium and sodium; (4) the lithium precipitation mother liquor is a mixed solution containing lithium and sodium; (5) The oil field brine after removing the calcium and the magnesium is a mixed solution containing lithium, sodium and potassium; (6) The pharmaceutical waste water of part of synthetic drugs is a mixed solution containing lithium and sodium, etc.
The existing lithium, sodium and potassium separation method mainly comprises the following steps: (1) The lithium was concentrated by repeated evaporation to precipitate sodium sulfate and potassium sulfate. The method has the advantages of complex process, high energy consumption and low lithium recovery rate. (2) Lithium is selectively extracted from the mixed solution by solvent extraction, and then purified and concentrated by washing and back extraction. Typical solvent extraction systems are those based on beta diketones and neutral organophosphorus. However, beta-diketones are unstable compounds that interconvert with multiple isomers; meanwhile, beta diketone has low acidity (pKa is approximately equal to 10), and the activity of reaction with lithium is very low, so that the lithium extraction efficiency is low, and the alkali consumption is very large. In addition, beta-diketone is easily decomposed in an alkaline environment, which causes a series of problems such as loss of an extracting agent and emulsification, and the like, so that the extraction process is difficult to stably operate.
In view of the problems of the prior art, the invention provides a solvent extraction system based on carbonyl enol and organophosphorus, which can effectively extract and extract lithium from a lithium-containing solution. The solvent extraction system has high reaction activity, high extraction selectivity, low alkali consumption and energy consumption in the extraction process, stable structure of the extracting agent, repeated recycling and no emulsification and other problems.
Disclosure of Invention
The invention aims to provide a synergistic solvent extraction system based on carbonyl enol and organic phosphorus, which can efficiently extract lithium from a lithium-containing solution, efficiently recover the lithium and separate the lithium from impurities such as sodium, potassium and the like.
A solvent extraction system for efficient extraction of lithium comprises a carbonyl enol having a structure represented by formula (IA or IB), an organophosphorus having a structure represented by formula (IIA, IIB, IIC or IID), and optionally a polar hydrophobic additive.
In the formulae (IA) and (IB), R 1 、R 2 、R 3 May be the same or different and is H or C 1 -C 15 Alkyl or aryl groups such as methyl, butyl, hexyl, octyl, dodecyl, phenyl, benzyl, phenylbutyl, and the like; or alkoxy, such as octyloxy; or an amine group, such as N, N-dibutylamino; or, R 1 And R 3 Or R 2 And R 3 Can be connected into a ring, and other arbitrary groups can be connected on the ring.
The carbonyl enol may be, for example, (Z) -1-hydroxy-1-phenyl-1-dodecen-3-one, (Z) -3-hydroxy-1-phenyl-3-decen-1-one, (Z) -3-hydroxy-1-phenyl-2-decen-1-one, 1- (5-hydroxy-3-methyl-1-phenyl-4-pyrazolyl) -1-benzophenone, 4- (1-hydroxyphenylmethylene) -5-methyl-2-benzyl-2, 4-dihydro-3-pyrazolone, (Z) -3-hydroxy-1-phenyl-3-dodecen-1-one, octyl 2-hydroxybenzoate, N-dibutyl-2-hydroxybenzamide, or the like.
In the formulae (IIA) to (IID), R 1 、R 2 、R 3 May be the same or different and are each independently C 1 -C 15 Alkyl or aryl radicals of (a), e.g. methyl, butyl,Hexyl, octyl, dodecyl, phenyl, benzyl, phenylbutyl, and the like.
The organophosphorus may be selected from one or a mixture of two or more of phosphine oxide (IIA), phosphinate (IIB), phosphonate (IIC) and phosphate (IID).
The molar ratio of the carbonyl enol to the organic phosphorus is 10.
The polar hydrophobic additive refers to a hydrophobic solvent with certain polarity, and can be one or a mixture of two or more of alcohol, ketone, ether and ester, and the alcohol can be selected from octanol, decanol, dodecanol and the like; such as 4-methyl-2-pentanone (MIBK), diisobutyl ketone (DIBK), etc.; such as diamyl ether, dihexyl ether, etc.; such as heptyl acetate, butyl benzoate, and the like. The additive content is 0vol% to 30vol%, based on the total volume of the carbonyl enol, the organic phosphorus and the additive. The polar hydrophobic additive helps to improve the solubility of organic substances and the phase separation effect.
The invention further relates to a method for extracting lithium from lithium-containing solution with high efficiency by using the solvent extraction system of the invention, which comprises the following steps:
(1) Dissolving a solvent extraction system according to the present invention in a diluent to prepare an organic phase, the volume concentration of the extraction system being 3vol% to 95vol%, based on the total volume of the organic phase;
(2) Measuring the concentration of lithium in the lithium-containing solution to be detected, and adding a proper amount of alkali into the lithium-containing solution to improve the activity of an extraction system for extracting lithium so as to obtain a water phase to be extracted;
(3) Introducing the organic phase prepared in the step (1) and the water phase obtained in the step (2) into extraction equipment, and carrying out countercurrent extraction reaction to obtain a lithium-loaded organic phase;
(4) Carrying out countercurrent washing on the lithium-loaded organic phase in the step (3) by using a washing solution to obtain a washed organic phase;
(5) Carrying out counter-current back extraction on the organic phase washed in the step (4) to obtain a back-extracted organic phase and a high-purity lithium salt solution;
(6) And returning the organic phase after back extraction to the organic phase storage tank for recycling, and extracting lithium by countercurrent extraction.
In the step (1), the diluent is alkane (such as kerosene, D70 solvent oil and the like), aromatic hydrocarbon (such as toluene, S150 solvent oil and the like) or a mixed solvent thereof.
In the step (2), the alkali is selected from sodium hydroxide, potassium hydroxide, ammonia water, sodium carbonate, potassium carbonate or any mixture thereof. And controlling the addition amount of the alkali in the solution to ensure that the concentration of the alkali is 0.5-3.0 times of the molar concentration of the lithium based on the molar concentration of the lithium in the lithium-containing solution to be measured.
In the step (3), the extraction equipment can use an extraction clarifier, an extraction tower or a centrifugal extractor, the extraction stage number is 1-20 stages, and the volume ratio of the organic phase to the water phase is 1.
In the step (4), the washing liquid is water, dilute hydrochloric acid or dilute sulfuric acid, and the concentration of the hydrochloric acid or sulfuric acid solution is 0.01-3.0mol/L; the volume ratio of the organic phase to the washing liquid is 1.
In the step (5), hydrochloric acid solution or sulfuric acid solution is used as stripping solution, and the concentration of the stripping solution is 0.1-12.0mol/L; the volume ratio of the organic phase to the stripping solution is 1-50, and the stripping stage number is 1-20.
The solvent extraction system for extracting lithium efficiently has the lithium recovery rate of more than 99 percent and the lithium purity of more than 99.5 percent.
The solvent extraction system for extracting lithium efficiently can be used for extracting lithium from various lithium-containing solutions such as salt lake brine, oil field brine, battery leachate, ore leachate, lithium precipitation mother liquor, lithium-containing wastewater and the like.
Advantageous effects
Compared with the prior art, the solvent extraction system is a synergistic extraction system based on the mixing of carbonyl enol and organic phosphorus, the stability is obviously improved, the emulsification phenomenon is eliminated, and the solvent extraction system can be recycled for a long time; the total organic content (i.e. COD) in the raffinate is low, and the raffinate is simple to treat. The solvent extraction system of the invention has high reaction activity, can fully utilize the alkali in the solution, and greatly reduces the alkali consumption in the lithium extraction process, thereby reducing the production cost of the lithium salt. The solvent extraction system of the invention can be advantageously applied to the extraction of lithium in various lithium-containing solutions, and has particularly remarkable advantages for extracting lithium from low-grade lithium-containing solutions and alkalescent lithium-containing solutions. The method for extracting lithium from lithium-containing solution (such as lithium, sodium and potassium (rubidium and cesium) mixed solution) by utilizing the solvent extraction system can simultaneously realize the purification and concentration of lithium, shorten the process flow and improve the recovery rate of lithium. The solvent extraction system of the invention has important significance for fully utilizing low-grade lithium resources.
Drawings
FIG. 1 is a schematic flow diagram of a solvent extraction system of the present invention for extraction, washing and stripping processes from lithium-containing solutions.
Detailed Description
The following examples are intended to illustrate the present invention more specifically, but the present invention is not limited to these examples at all, and those skilled in the art can make various modifications within the technical idea of the present invention.
Example 1
The lithium-containing solution to be treated is salt lake brine, and the magnesium is removed by a nanofiltration method, so that the obtained solution contains 0.2g/L of lithium, 85g/L of sodium, 8.6g/L of potassium and trace amounts of magnesium, calcium, rubidium and cesium.
6vol% (Z) -1-hydroxy-1-phenyl-1-dodecen-3-one, 6vol% Cyanex 923 (mixture of alkyl phosphine oxides, where the alkyl groups are hexyl and octyl) and 88vol% kerosene were made up into the organic phase. NaOH was added to the lithium-containing solution so that the NaOH concentration was 0.04mol/L to prepare an aqueous phase. And (3) carrying out 4-stage continuous countercurrent extraction on the organic phase and the aqueous phase in an extraction clarifying tank according to the volume ratio of 1. The lithium-loaded organic is washed by 0.3mol/L hydrochloric acid for 2 grades in an extraction clarifying tank according to the volume ratio of 20; and (3) carrying out back extraction on the washed organic substances in an extraction clarifying tank by using 4mol/L hydrochloric acid according to the volume ratio of 20 to 1, and carrying out back extraction for 2 grades to obtain a high-purity lithium chloride solution with the lithium concentration of 18-20g/L, wherein the lithium purity is more than 99.8 percent. The organic phase after the back extraction is returned to the extraction section for recycling. The lithium chloride solution was precipitated at 80 ℃ with sodium carbonate in a stoichiometric ratio of 0.8 times the lithium to give battery grade lithium carbonate with a purity of >99.8%.
Example 2
The lithium-containing solution to be treated is taken from a solution obtained by disassembling, crushing, leaching and removing divalent and trivalent metals from a recovered lithium battery, and contains 2.7g/L of lithium, 50g/L of sodium, and trace amounts of cobalt, nickel, magnesium and the like.
An organic phase was prepared by dissolving 18vol% (Z) -3-hydroxy-1-phenyl-3-decen-1-one, 30vol% TRPO (a mixture of alkyl phosphine oxides, wherein the alkyl groups are heptyl and octyl) and 5vol% octanol in 47vol% kerosene. NaOH was added to the lithium-containing solution so that the NaOH concentration was 0.45mol/L to prepare an aqueous phase. Carrying out 3-stage continuous countercurrent extraction on the organic phase and the aqueous phase in an extraction clarifying tank according to the volume ratio of 1>99 percent. The loaded organic phase is continuously washed with 0.2mol/L sulfuric acid in the volume ratio of 10; and (3) the washed organic matters are sequentially and continuously back extracted by 2mol/L sulfuric acid in an extraction clarifying tank according to the volume ratio of 10 to 1, and the back extraction is carried out for 2 grades, so that high-purity Li with the lithium concentration of 25-27g/L is obtained 2 SO 4 Solution of lithium purity>99.8 percent. The organic phase after the back extraction is returned to the extraction section for recycling. The lithium sulfate solution was precipitated at 80 ℃ with sodium carbonate in an amount 0.8 times the stoichiometric ratio of lithium to obtain battery grade lithium carbonate with a purity of 99.8%.
Example 3
The solution to be treated is lithium-containing wastewater generated in the process of recovering the battery, and the lithium concentration of the solution to be treated is 0.5g/L and the sodium concentration of the solution to be treated is 48g/L.
15vol% (Z) -3-hydroxy-1-phenyl-2-decen-1-one and 2vol% (20vol%) Cyanex 925 (alkyl phosphine oxide containing branched alkyl group) were dissolved in 65vol% kerosene to prepare an organic phase. NaOH was added to the lithium-containing solution so that the concentration of NaOH was 0.10mol/L to prepare an aqueous phase. The organic phase and the aqueous phase are subjected to 3-stage continuous countercurrent extraction in an extraction clarifier according to the volume ratio of 1. The loaded organic phase is continuously washed with 1.0mol/L hydrochloric acid in the volume ratio of 20; and (3) carrying out back extraction on the washed organic matters in an extraction clarifying tank by using hydrochloric acid of 8.0mol/L according to the volume ratio of 20 to 1, and carrying out back extraction for 2 grades to obtain a LiCl solution with the lithium concentration of 45-50 g/L. The organic phase after the back extraction is returned to the extraction section for recycling. The lithium chloride solution was precipitated at 80 ℃ with sodium carbonate in a stoichiometric ratio of 0.7 times the lithium to give battery grade lithium carbonate with a purity of > 99.6%.
Example 4
The solution to be treated is lithium deposition mother liquor obtained after adding sodium carbonate into lithium sulfate solution to deposit lithium carbonate, and the lithium deposition mother liquor contains 3.4g/L of lithium and 46g/L of sodium.
1- (5-hydroxy-3-methyl-1-phenyl-4-pyrazolyl) -1-benzophenone in an amount of 18vol%, TOPO (trioctylphosphine oxide) in an amount of 15vol% and P350 (dimethylheptyl methylphosphonate) in an amount of 15vol% in a solvent of 62vol% S150 to prepare an organic phase. The lithium precipitation mother liquor is directly used as a water phase without adding alkali. The organic phase and the aqueous phase are subjected to 3-stage continuous countercurrent extraction in an extraction clarifier according to the volume ratio of 1. Continuously washing the lithium-loaded organic phase in an extraction clarifying tank by using 0.5mol/L hydrochloric acid to wash the co-extracted sodium in a volume ratio of 10; and (3) carrying out back extraction on the washed organic matters in an extraction clarifying tank by using 5mol/L hydrochloric acid according to the volume ratio of 10. The organic phase after the back extraction is returned to the extraction section for recycling. The lithium chloride solution was precipitated at 80 ℃ with sodium carbonate in a stoichiometric ratio of 0.7 times the lithium to give battery grade lithium carbonate with a purity of > 99.6%.
Example 5
The solution to be treated is a mixed solution containing 0.12g/L of lithium, 35g/L of sodium and 10g/L of potassium, which is obtained by removing calcium and magnesium from oil field brine through nanofiltration.
25vol% of 4- (1-hydroxyphenylmethylene) -5-methyl-2-benzyl-2, 4-dihydro-3-pyrazolone, 20vol% of TRPO and 10vol% of trioctylphosphate were dissolved in 45vol% of S150 solvent to prepare an organic phase. NaOH was added to the lithium-containing solution so that the NaOH concentration was 0.02mol/L to prepare an aqueous phase. The organic phase and the aqueous phase are subjected to 4-stage continuous countercurrent extraction in an extraction clarifying tank according to the volume ratio of 1. The loaded organic phase is continuously washed by 0.8mol/L hydrochloric acid in an extraction clarifying tank according to the volume ratio of 10; and (3) carrying out back extraction on the washed organic matters in an extraction clarifying tank by using 10mol/L hydrochloric acid according to the volume ratio of 10 to 1, and carrying out back extraction for 2 grades to obtain a LiCl solution with the lithium concentration of 55-60 g/L. The organic phase after the back extraction is returned to the extraction section for recycling. Evaporating and crystallizing the lithium chloride solution to obtain a lithium chloride product with the purity of more than 99.6 percent.
Example 6
The solution to be treated is pharmaceutical wastewater containing 8.2g/L of lithium and 65g/L of sodium.
An organic phase was prepared by dissolving 20vol% (Z) -3-hydroxy-1-phenyl-3-dodecen-1-one, 20vol% TRPO and 15vol% trihexyl phosphate in 20vol% kerosene and 25vol% S150 solvent. NaOH was added to the lithium-containing solution to a concentration of 1.3mol/L to prepare an aqueous phase. And (3) carrying out 4-stage continuous countercurrent extraction on the organic phase and the aqueous phase in an extraction clarifying tank according to the volume ratio of 1.5. Continuously washing the lithium-loaded organic phase in an extraction clarifying tank by using 1.0mol/L hydrochloric acid to wash the co-extracted sodium in a volume ratio of 10; and (3) carrying out back extraction on the washed organic matters in an extraction clarifying tank by using 8mol/L hydrochloric acid according to the volume ratio of 10. The organic phase after the back extraction is returned to the extraction section for recycling. Evaporating and crystallizing the lithium chloride solution to obtain lithium chloride crystals with the purity of more than 99.6 percent.
Example 7
The solution to be treated is underground brine, and after calcium and magnesium are removed by nanofiltration, the solution contains 0.26g/L of lithium, 102g/L of sodium and 24g/L of potassium.
1% by 15vol 2-hydroxybenzoic acid octyl ester, 15vol TRPO and 5vol tributyl phosphate were dissolved in 65vol% kerosene solvent to prepare an organic phase. NaOH was added to the lithium-containing solution so that the NaOH concentration was 0.045mol/L, and the aqueous phase was prepared. The organic phase and the aqueous phase are subjected to 3-stage continuous countercurrent extraction in an extraction clarifier according to the volume ratio of 1. Continuously washing the lithium-loaded organic phase in an extraction clarifying tank by using 0.6mol/L hydrochloric acid to wash the co-extracted sodium in a volume ratio of 10; and (3) carrying out back extraction on the washed organic matters in an extraction clarifying tank by 6mol/L hydrochloric acid according to the volume ratio of 10 to 1, and carrying out back extraction for 2 grades to obtain a LiCl solution with the lithium concentration of 35-39 g/L. The organic phase after the back extraction is returned to the extraction section for recycling. The lithium chloride solution was precipitated at 80 ℃ with sodium carbonate in a stoichiometric ratio of 0.7 times the lithium to give battery grade lithium carbonate with a purity of > 99.6%.
Example 8
The lithium-containing solution to be treated is salt lake old brine, and the magnesium is removed by a nanofiltration method to obtain a solution containing 1.2g/L of lithium, 14g/L of sodium and 2.5g/L of potassium.
2vol% of N, N-dibutyl-2-hydroxybenzamide, 2vol% of TRPO and 10vol% of dimethylheptyl methylphosphonate were dissolved in 50vol% of kerosene solvent to prepare an organic phase. NaOH was added to the lithium-containing solution to adjust the NaOH concentration to 0.2mol/L, and a water phase was prepared. The organic phase and the aqueous phase are subjected to 3-stage continuous countercurrent extraction in an extraction clarifier according to the volume ratio of 1. Continuously washing the lithium-loaded organic phase in an extraction clarifying tank by using 0.8mol/L hydrochloric acid to wash the co-extracted sodium in a volume ratio of 10; and (3) carrying out back extraction on the washed organic matters in an extraction clarifying tank by using 7mol/L hydrochloric acid according to the volume ratio of 10. The organic phase after the back extraction is returned to the extraction section for recycling. The lithium chloride solution was precipitated at 80 ℃ with sodium carbonate in an amount 0.7 times the stoichiometric ratio of lithium to obtain battery grade lithium carbonate with a purity of > 99.6%.
Claims (10)
1. A solvent extraction system for extracting lithium efficiently comprises carbonyl enol having a structure shown in formula (IA or IB), organic phosphorus having a structure shown in formula (IIA, IIB, IIC or IID), and an optional polar hydrophobic additive;
in the formulae (IA, IB), R 1 、R 2 、R 3 Same or different and is H or C 1 -C 15 Alkyl or aryl ofA group, or an alkoxy group, or an amine group; or, R 1 And R 3 Or R 2 And R 3 Are connected into a ring;
in the formulae (IIA, IIB, IIC, IID), R 1 、R 2 、R 3 Identical or different, each independently is C 1 -C 15 Alkyl or aryl of (a).
2. The solvent extraction system for high efficiency extraction of lithium according to claim 1, wherein the organophosphorus is selected from one, a mixture of two or more of phosphine oxide (IIA), phosphinate (IIB), phosphonate (IIC) and phosphate (IID).
3. The solvent extraction system for extracting lithium with high efficiency according to claim 1, wherein the polar hydrophobic additive is one or a mixture of two or more of alcohol, ketone, ether and ester.
4. The solvent extraction system for high-efficiency extraction of lithium according to claim 1, wherein the molar ratio of the carbonyl enol to the organic phosphorus is 10; the amount of additive is from 0vol% to 30vol%, based on the total volume of the carbonyl enol, the organic phosphorus and the additive.
5. A method for efficient extraction of lithium using a solvent extraction system according to any one of the preceding claims, comprising the steps of:
(1) Dissolving a solvent extraction system according to any one of the preceding claims in a diluent to produce an organic phase, the volume concentration of the extraction system being from 3vol% to 95vol%, based on the total volume of the organic phase;
(2) Measuring the lithium concentration in the lithium-containing solution to be detected, and adding a proper amount of alkali into the lithium-containing solution to obtain a water phase to be extracted;
(3) Introducing the organic phase prepared in the step (1) and the water phase obtained in the step (2) into extraction equipment, and carrying out countercurrent extraction reaction to obtain a lithium-loaded organic phase;
(4) Carrying out countercurrent washing on the lithium-loaded organic phase in the step (3) by using a washing solution to obtain a washed organic phase;
(5) Carrying out counter-current back extraction on the organic phase washed in the step (4) to obtain a back-extracted organic phase and a high-purity lithium salt solution;
(6) And returning the organic phase after back extraction to the organic phase storage tank for recycling, and extracting lithium by countercurrent extraction.
6. The process of claim 5, wherein in step (1), the diluent is an alkane, an aromatic hydrocarbon, or a mixture thereof; in the step (2), the alkali is sodium hydroxide, potassium hydroxide, ammonia water, sodium carbonate, potassium carbonate or a mixture thereof, and the adding amount of the alkali in the solution is controlled so that the concentration of the alkali is 0.5-3.0 times of the molar concentration of lithium based on the molar concentration of lithium in the lithium-containing solution to be measured.
7. The process according to claim 5, wherein in step (3), the volume ratio of the organic phase to the aqueous phase is 1.
8. The method according to claim 5, wherein in step (4), the washing solution is water, diluted hydrochloric acid or diluted sulfuric acid, and the concentration of hydrochloric acid or sulfuric acid is 0.01-3.0mol/L; the volume ratio of the organic phase to the washing solution is 1.
9. The method according to claim 5, wherein in the step (5), a hydrochloric acid solution or a sulfuric acid solution is used as the stripping solution, and the concentration of hydrochloric acid or sulfuric acid is 0.1-12.0mol/L; the volume ratio of the organic phase to the stripping solution is 1.
10. Use of the solvent extraction system for high efficiency lithium extraction according to any one of the preceding claims 1 to 4 for extracting lithium from salt lake brine, oil field brine, battery leachate, ore leachate, lithium precipitation mother liquor, lithium containing wastewater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211585047.XA CN115821040B (en) | 2022-12-09 | 2022-12-09 | Solvent extraction system for efficiently extracting lithium |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211585047.XA CN115821040B (en) | 2022-12-09 | 2022-12-09 | Solvent extraction system for efficiently extracting lithium |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115821040A true CN115821040A (en) | 2023-03-21 |
| CN115821040B CN115821040B (en) | 2024-10-08 |
Family
ID=85546260
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211585047.XA Active CN115821040B (en) | 2022-12-09 | 2022-12-09 | Solvent extraction system for efficiently extracting lithium |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115821040B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107502741A (en) * | 2017-05-25 | 2017-12-22 | 中国科学院过程工程研究所 | A kind of compound extracting system and its extracting process that lithium is extracted from bittern containing lithium |
| CN107779612A (en) * | 2017-12-08 | 2018-03-09 | 中国科学院青海盐湖研究所 | A kind of technique that lithium is extracted from alkaline bittern |
| CN107937734A (en) * | 2017-12-08 | 2018-04-20 | 中国科学院青海盐湖研究所 | The technique that lithium is extracted from the bittern of alkalescence containing lithium based on mixer-settler |
| CN108004420A (en) * | 2017-12-08 | 2018-05-08 | 中国科学院青海盐湖研究所 | The technique that lithium is extracted from the bittern of alkalescence containing lithium based on centrifugal extractor |
| CN111057848A (en) * | 2018-10-16 | 2020-04-24 | 中国科学院过程工程研究所 | Method for extracting lithium from lithium-containing solution by solvent extraction |
| CN111850302A (en) * | 2020-07-16 | 2020-10-30 | 中国科学院青海盐湖研究所 | Method for extracting metal ions from lithium battery |
| CN113073209A (en) * | 2021-01-12 | 2021-07-06 | 宿迁哈托科技有限公司 | Extraction system for extracting lithium from brine, preparation method of extraction system and method for extracting lithium from brine |
| US20220356545A1 (en) * | 2021-04-23 | 2022-11-10 | Ut-Battelle, Llc | Lithium extractant compounds and their use in selective lithium extraction from aqueous solutions |
-
2022
- 2022-12-09 CN CN202211585047.XA patent/CN115821040B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107502741A (en) * | 2017-05-25 | 2017-12-22 | 中国科学院过程工程研究所 | A kind of compound extracting system and its extracting process that lithium is extracted from bittern containing lithium |
| CN107779612A (en) * | 2017-12-08 | 2018-03-09 | 中国科学院青海盐湖研究所 | A kind of technique that lithium is extracted from alkaline bittern |
| CN107937734A (en) * | 2017-12-08 | 2018-04-20 | 中国科学院青海盐湖研究所 | The technique that lithium is extracted from the bittern of alkalescence containing lithium based on mixer-settler |
| CN108004420A (en) * | 2017-12-08 | 2018-05-08 | 中国科学院青海盐湖研究所 | The technique that lithium is extracted from the bittern of alkalescence containing lithium based on centrifugal extractor |
| CN111057848A (en) * | 2018-10-16 | 2020-04-24 | 中国科学院过程工程研究所 | Method for extracting lithium from lithium-containing solution by solvent extraction |
| CN111850302A (en) * | 2020-07-16 | 2020-10-30 | 中国科学院青海盐湖研究所 | Method for extracting metal ions from lithium battery |
| CN113073209A (en) * | 2021-01-12 | 2021-07-06 | 宿迁哈托科技有限公司 | Extraction system for extracting lithium from brine, preparation method of extraction system and method for extracting lithium from brine |
| US20220356545A1 (en) * | 2021-04-23 | 2022-11-10 | Ut-Battelle, Llc | Lithium extractant compounds and their use in selective lithium extraction from aqueous solutions |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115821040B (en) | 2024-10-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU2020374016B2 (en) | Method for extracting lithium by means of extraction-back extraction separation and purification | |
| CN111057848A (en) | Method for extracting lithium from lithium-containing solution by solvent extraction | |
| US20180320247A1 (en) | Process for producing lithium carbonate from concentrated lithium brine | |
| CN109852797B (en) | Extraction solvent for extracting and separating lithium element and method for extracting and separating lithium element by using extraction solvent | |
| JP5514844B2 (en) | Method for separating valuable metals from waste secondary batteries and method for recovering valuable metals using the same | |
| CN107988495B (en) | Method for recovering rare earth from process of decomposing phosphorite by nitric acid | |
| CN109628758B (en) | Extraction solvent and extraction method for lithium element | |
| CA3205995A1 (en) | Recovering mixed-metal ions from aqueous solutions | |
| CN112522517A (en) | Method for recycling nickel, cobalt, manganese and lithium | |
| CN109574181B (en) | Method for resource treatment of rare earth oxalic acid precipitation wastewater | |
| CN112575193A (en) | Method for separating copper and manganese and application thereof | |
| CN110835687B (en) | Method for extracting rubidium and cesium from steel smoke dust and/or volatile dust | |
| CN112281001B (en) | Method for preparing manganese salt by using manganese-containing waste liquid | |
| CA3191479A1 (en) | Method for recycling nickel, cobalt and manganese from feed liquid containing nickel, cobalt and manganese | |
| CN109536741B (en) | Extraction method of lithium element | |
| CN107299225A (en) | A kind of method that C272 fractional extractions prepare 6N grades of cobalt chlorides | |
| CN107746977B (en) | The method of recovering rare earth from containing rare earth phosphate rock | |
| CN112342407A (en) | Back extraction method of lithium extraction liquid | |
| CN114134322B (en) | Method for separating copper and manganese from copper-manganese-calcium-zinc-containing mixed solution | |
| CN115821040B (en) | Solvent extraction system for efficiently extracting lithium | |
| CN102701262B (en) | Method for recovering scandium from titanium dioxide wastewater on large scale | |
| TW202430656A (en) | Method for producing aqueous solution containing nickel or cobalt | |
| CN106892479B (en) | Method for recovering oxalic acid and hydrochloric acid from rare earth oxalic acid precipitation wastewater | |
| CN107674974B (en) | The purposes and method of the phosphine extractant extraction and recovery copper of neutrality containing amino | |
| CN114645143B (en) | Method for separating nickel, cobalt, copper and manganese from laterite-nickel ore |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20240704 Address after: Room 804, Unit 1, Building 1, Courtyard 1, Longyu Middle Street, Huilongguan Town, Changping District, Beijing 100085 Applicant after: Zhongke Chuncui Technology (Beijing) Co.,Ltd. Country or region after: China Address before: 100190 north two street, Zhongguancun, Haidian District, Beijing, 1 Applicant before: Institute of Process Engineering, Chinese Academy of Sciences Country or region before: China |
|
| GR01 | Patent grant |