CN112058090B - System for separating lithium isotopes by multistage air-floatation extraction - Google Patents
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- 238000000605 extraction Methods 0.000 title claims abstract description 139
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 122
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 239000007788 liquid Substances 0.000 claims abstract description 136
- 238000000926 separation method Methods 0.000 claims abstract description 132
- 238000005188 flotation Methods 0.000 claims abstract description 99
- 229910003002 lithium salt Inorganic materials 0.000 claims abstract description 70
- 159000000002 lithium salts Chemical class 0.000 claims abstract description 70
- 239000012266 salt solution Substances 0.000 claims abstract description 54
- 239000000243 solution Substances 0.000 claims abstract description 39
- 238000000034 method Methods 0.000 claims abstract description 24
- 239000002608 ionic liquid Substances 0.000 claims abstract description 19
- 239000003085 diluting agent Substances 0.000 claims abstract description 15
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000007864 aqueous solution Substances 0.000 claims abstract description 10
- ZXMGHDIOOHOAAE-UHFFFAOYSA-N 1,1,1-trifluoro-n-(trifluoromethylsulfonyl)methanesulfonamide Chemical compound FC(F)(F)S(=O)(=O)NS(=O)(=O)C(F)(F)F ZXMGHDIOOHOAAE-UHFFFAOYSA-N 0.000 claims abstract description 6
- 230000005587 bubbling Effects 0.000 claims abstract description 5
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 28
- 229910052757 nitrogen Inorganic materials 0.000 claims description 17
- 150000001768 cations Chemical class 0.000 claims description 13
- RDOXTESZEPMUJZ-UHFFFAOYSA-N anisole Chemical compound COC1=CC=CC=C1 RDOXTESZEPMUJZ-UHFFFAOYSA-N 0.000 claims description 12
- 150000001875 compounds Chemical class 0.000 claims description 10
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 claims description 9
- 150000001450 anions Chemical class 0.000 claims description 7
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims description 6
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 claims description 6
- 125000000217 alkyl group Chemical group 0.000 claims description 6
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical group [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 claims description 6
- UZKWTJUDCOPSNM-UHFFFAOYSA-N methoxybenzene Substances CCCCOC=C UZKWTJUDCOPSNM-UHFFFAOYSA-N 0.000 claims description 6
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 claims description 6
- 238000007664 blowing Methods 0.000 claims description 5
- 125000004432 carbon atom Chemical group C* 0.000 claims description 4
- UBOXGVDOUJQMTN-UHFFFAOYSA-N 1,1,2-trichloroethane Chemical compound ClCC(Cl)Cl UBOXGVDOUJQMTN-UHFFFAOYSA-N 0.000 claims description 3
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 229910013684 LiClO 4 Inorganic materials 0.000 claims description 3
- NTIZESTWPVYFNL-UHFFFAOYSA-N Methyl isobutyl ketone Chemical compound CC(C)CC(C)=O NTIZESTWPVYFNL-UHFFFAOYSA-N 0.000 claims description 3
- UIHCLUNTQKBZGK-UHFFFAOYSA-N Methyl isobutyl ketone Natural products CCC(C)C(C)=O UIHCLUNTQKBZGK-UHFFFAOYSA-N 0.000 claims description 3
- 125000003545 alkoxy group Chemical group 0.000 claims description 3
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 239000003350 kerosene Substances 0.000 claims description 3
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 claims description 3
- PJGSXYOJTGTZAV-UHFFFAOYSA-N pinacolone Chemical compound CC(=O)C(C)(C)C PJGSXYOJTGTZAV-UHFFFAOYSA-N 0.000 claims description 3
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims 2
- 239000012071 phase Substances 0.000 description 80
- 238000009423 ventilation Methods 0.000 description 22
- 238000012360 testing method Methods 0.000 description 17
- 238000006243 chemical reaction Methods 0.000 description 12
- 230000000155 isotopic effect Effects 0.000 description 12
- 238000001816 cooling Methods 0.000 description 11
- 239000011259 mixed solution Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 6
- YZCKVEUIGOORGS-NJFSPNSNSA-N Tritium Chemical compound [3H] YZCKVEUIGOORGS-NJFSPNSNSA-N 0.000 description 5
- 239000012074 organic phase Substances 0.000 description 5
- 229910052722 tritium Inorganic materials 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910001416 lithium ion Inorganic materials 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 3
- 230000004927 fusion Effects 0.000 description 3
- 238000005372 isotope separation Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000005192 partition Methods 0.000 description 3
- 238000000053 physical method Methods 0.000 description 3
- XQQZRZQVBFHBHL-UHFFFAOYSA-N 12-crown-4 Chemical compound C1COCCOCCOCCO1 XQQZRZQVBFHBHL-UHFFFAOYSA-N 0.000 description 2
- 229910000497 Amalgam Inorganic materials 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 230000004992 fission Effects 0.000 description 2
- 239000001307 helium Substances 0.000 description 2
- 229910052734 helium Inorganic materials 0.000 description 2
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
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- 239000000126 substance Substances 0.000 description 2
- KAIPKTYOBMEXRR-UHFFFAOYSA-N 1-butyl-3-methyl-2h-imidazole Chemical compound CCCCN1CN(C)C=C1 KAIPKTYOBMEXRR-UHFFFAOYSA-N 0.000 description 1
- IQQRAVYLUAZUGX-UHFFFAOYSA-N 1-butyl-3-methylimidazolium Chemical compound CCCCN1C=C[N+](C)=C1 IQQRAVYLUAZUGX-UHFFFAOYSA-N 0.000 description 1
- -1 1-ethyl-3-methylimidazole bis (trifluoromethanesulfonyl) imide salt Chemical class 0.000 description 1
- NJMWOUFKYKNWDW-UHFFFAOYSA-N 1-ethyl-3-methylimidazolium Chemical compound CCN1C=C[N+](C)=C1 NJMWOUFKYKNWDW-UHFFFAOYSA-N 0.000 description 1
- RVEJOWGVUQQIIZ-UHFFFAOYSA-N 1-hexyl-3-methylimidazolium Chemical compound CCCCCCN1C=C[N+](C)=C1 RVEJOWGVUQQIIZ-UHFFFAOYSA-N 0.000 description 1
- UKHHINKAMGATES-UHFFFAOYSA-N CCCCCCN1CN(C)C=C1.FC(F)(F)S(=O)(=O)NS(=O)(=O)C(F)(F)F Chemical compound CCCCCCN1CN(C)C=C1.FC(F)(F)S(=O)(=O)NS(=O)(=O)C(F)(F)F UKHHINKAMGATES-UHFFFAOYSA-N 0.000 description 1
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- 229910013553 LiNO Inorganic materials 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- FNEPSTUXZLEUCK-UHFFFAOYSA-N benzo-15-crown-5 Chemical compound O1CCOCCOCCOCCOC2=CC=CC=C21 FNEPSTUXZLEUCK-UHFFFAOYSA-N 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- 150000003983 crown ethers Chemical class 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 229910052805 deuterium Inorganic materials 0.000 description 1
- QSBFECWPKSRWNM-UHFFFAOYSA-N dibenzo-15-crown-5 Chemical compound O1CCOCCOC2=CC=CC=C2OCCOC2=CC=CC=C21 QSBFECWPKSRWNM-UHFFFAOYSA-N 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000009616 inductively coupled plasma Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004255 ion exchange chromatography Methods 0.000 description 1
- 238000000622 liquid--liquid extraction Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000000199 molecular distillation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000027756 respiratory electron transport chain Effects 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D59/00—Separation of different isotopes of the same chemical element
- B01D59/22—Separation by extracting
- B01D59/24—Separation by extracting by solvent extraction
-
- 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
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a system for separating lithium isotopes by multistage air floatation extraction, which comprises a floatation column, an organic extraction phase, a lithium salt solution phase and m parts of exchange liquid; wherein, based on the condition of bubbling gas in the flotation column, the organic extraction phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation to obtain an extraction enrichment solution, and m parts of exchange solution are sequentially subjected to m-stage air flotation exchange separation with the extraction enrichment solution to obtain the enriched solution 6 An mth exchange enriched liquid of Li; the organic extraction phase comprises an extracting agent, an ionic liquid and a diluent which are mixed with each other, the lithium salt solution phase is an aqueous solution of lithium salt, and the exchange liquid is an aqueous solution of bis (trifluoromethanesulfonyl) imide, sulfuric acid or hydrochloric acid; m is an integer of 2 or more. The method for extracting and separating the lithium isotope can effectively improve 6 The separation of Li enriches the abundance.
Description
Technical Field
The invention belongs to the field of lithium isotope separation, and particularly relates to a system for separating lithium isotopes by multistage air floatation extraction.
Background
Lithium (Li) exists in nature as two stable isotopes 6 Li and Li 7 Li, their natural abundance (refer to 6 Li and Li 7 Natural relative percentages of Li) are 7.42% and 92.58%, respectivelyIsotopes play an extremely important role in the field of nuclear energy. Wherein the thermal neutron absorption cross section reaches 940b 6 Li can generate tritium and helium after being bombarded and fissile by neutron (n) 6 Li+n→T+ 4 He), so of a certain abundance 6 Li can be used as a feedstock for nuclear fusion and other uses; while the thermal neutron absorption cross section is only 0.037b 7 Li plays an important role in the regulation and control of the nuclear reaction process and the maintenance of equipment. The nuclear fusion energy supply is to polymerize deuterium (D) and tritium (T) into helium # 4 He), estimated to be 1kg 6 Li fission generates tritium, and the total energy released during fusion can generate at least 10000 kilowatts which is far greater than the same mass 235 Energy released upon U fission. However, the storage of tritium in nature is extremely limited and tritium production must rely on neutron bombardment 6 Li is generated and added.
Currently, there are various single-stage separation methods of lithium isotopes, which can be classified into chemical methods and physical methods, wherein the chemical methods include a lithium amalgam exchange method, an ion exchange chromatography method, an extraction method, and the like; physical methods include electromagnetic methods, electron transfer, molecular distillation, laser separation, and the like. The physical method is not suitable for industrial production due to the characteristics of expensive production equipment, harsh production conditions, high energy consumption, small yield and the like. Among the separation methods of lithium isotopes, only the lithium amalgam method is used as the separation method for realizing industrialization, but a large amount of toxic mercury is needed in the method, so that the ecological environment is damaged, the physical health of workers is also endangered, and therefore, a method for replacing the method is highly desired.
Chinese patent application (application number: 201811366815.6) discloses a separation and enrichment method of lithium isotopes, which utilizes multistage superposition extraction to separate lithium isotopes, and adopts 10-stage superposition extraction separation 6 The abundance of Li increases to 8.39%. In the method, the extraction liquid is required to be used for repeatedly carrying out multi-stage extraction, the problems of complex operation, high raw material cost and the like exist, and the abundance of lithium isotopes after multi-stage superposition extraction separation is still small.
Disclosure of Invention
In view of the deficiencies of the prior art, the present invention providesSystem for separating lithium isotopes by multistage air-floatation extraction for improving 6 The separation of Li enriches the abundance.
In order to achieve the aim of the invention, the invention provides a system for separating lithium isotopes by multistage air floatation extraction, which comprises a floatation column, an organic extraction phase, a lithium salt solution phase and m parts of exchange liquid; wherein, based on the condition of bubbling gas in the flotation column, the organic extraction phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation to obtain an extraction enrichment solution, and m parts of exchange solution are sequentially subjected to m-stage air flotation exchange separation with the extraction enrichment solution to obtain the enriched solution 6 An mth exchange enriched liquid of Li;
the organic extraction phase comprises an extracting agent, an ionic liquid and a diluting agent which are mixed with each other, wherein the lithium salt solution phase is an aqueous solution of lithium salt, and the exchange liquid is an aqueous solution of bis (trifluoromethanesulfonyl) imide, sulfuric acid or hydrochloric acid;
wherein m is an integer of 2 or more.
In a preferred embodiment, the extractant is selected from any one of the compounds represented by the following formulas 1 to 3,
in the compounds shown in the formulas 1 to 3, R is selected from alkyl, alkoxy, amino, nitro or phenyl with 0 to 20 carbon atoms, X is N or O, and N is 0, 1 or 2;
the ionic liquid consists of anions and cations; the cation is selected from any one of cations represented by the following formulas 2-1 to 2-10,
r, R in the cations of the formulae 2-1 to 2-10 1 、R 2 、R 3 And R is 4 Independently selected from alkyl groups having 0 to 20 carbon atoms; the anion is selected from [ PF ] 6 ] - 、[(SO 2 CF 3 ) 2 N] - 、[(SO 2 CF 2 CF 3 ) 2 N] - 、[CF 3 SO 3 ] - 、[CH 3 COO] - And [ BF ] 4 ] - One or two or more of them;
the diluent is selected from one or more of anisole, dichloromethane, chloroform, 1, 2-dichloroethane, nitrobenzene, 1, 2-trichloroethane, acetone, methyl isobutyl ketone, methyl tert-butyl ketone and kerosene.
In a preferred embodiment, in the organic extraction phase, the volume ratio of the ionic liquid to the diluent is (1-10): (1-15), wherein the concentration of the extractant is 0.1 mol/L-0.5 mol/L.
In a preferred embodiment, the lithium salt in the lithium salt solution phase is selected from LiCl, liBr, liI, liOH, liNO 3 、LiClO 4 、LiSCN、CH 3 COOLi、CF 3 COOLi、CHF 2 COOLi、CH 2 FCOOLi and Li [ NTf 2 ]Any one of them; the concentration of lithium salt in the lithium salt solution phase is 0.2mol/L to 5mol/L.
In a preferred embodiment, the concentration of the exchange liquid is 0.4mol/L to 0.6mol/L.
In a preferred scheme, when the organic extraction phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation in the flotation column or m parts of exchange liquid are sequentially subjected to m-stage air flotation exchange separation with an extraction enrichment liquid, gas blown into the flotation column is selected from any one of nitrogen, oxygen, carbon dioxide, hydrogen or rare gas, the gas flow is 1-25 mL/min, and the gas blowing time is 60-90 min.
In a preferred embodiment, when the organic extract phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation based on the flotation column, the organic extract phase and the lithium salt solution phase are mixed in a volume ratio of 1: (1-15) is placed in the flotation column.
In a preferred scheme, when n parts of exchange liquid and the extraction enrichment liquid are sequentially subjected to n-level air flotation exchange separation based on the flotation column, the volume ratio of the extraction enrichment liquid to the exchange liquid is 1: (1-15) is placed in the flotation column.
In a preferred scheme, the floatation column is a temperature-controllable floatation column, and the temperature is controlled to be 260K-295K when extraction separation or exchange separation is carried out in the floatation column.
In a preferred scheme, the value of m is 4-20.
The system for separating lithium isotopes by multistage air-floatation extraction provided by the embodiment of the invention comprises a floatation column, an organic extraction phase, a lithium salt solution phase and m parts of exchange liquid:
firstly, organic extraction is adopted in a flotation column to carry out extraction separation of lithium isotopes relative to a lithium salt solution phase, wherein the organic extraction phase comprises an extractant, an ionic liquid and a diluent which are mixed with each other, and crown ether with very low water solubility is adopted as the extractant, so that the dissolution loss of the extractant in the extraction process is reduced; the crown ether-ionic liquid extraction system is adopted, and the selected ionic liquid can better participate in cation exchange, so that the crown ether-ionic liquid extraction system has good synergistic effect, and the distribution ratio of lithium in an organic phase is increased;
secondly, the air floatation method is introduced into the liquid-liquid extraction process based on a floatation column, so that the exchange balance time is shortened, the first-stage air floatation process step is to extract and separate lithium isotopes relative to a lithium salt solution phase by organic extraction to obtain a preliminary enrichment solution, the second-stage air floatation process step is to introduce exchange liquid to replace the organic extraction liquid in the prior art to extract, exchange and enrich the lithium isotopes, and the exchange liquid is aqueous solution of bis (trifluoromethanesulfonyl) imide, sulfuric acid or hydrochloric acid, so that the material cost is lower compared with that of the organic extraction liquid, the operation process of separation and enrichment is simpler, and the method can be remarkably improved after multi-stage air floatation exchange and separation 6 The abundance of Li.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the following detailed description. This invention may, however, be embodied in many different forms and should not be construed as limited to the specific embodiments set forth herein. Rather, these embodiments are provided to explain the principles of the invention and its practical application so that others skilled in the art will be able to understand the invention for various embodiments and with various modifications as are suited to the particular use contemplated.
In the extraction and separation of lithium isotopes by an organic extractant, the extractant in an organic phase is extracted from a lithium salt solution 6 Li (lithium) 7 Extraction exchange of Li to achieve an organic phase 6 And (3) enriching Li. Partition ratio (D) is the total concentration of lithium from the lithium salt solution into the organic phase c (Li + ) (org) And the residual concentration c (Li) + ) (aq) The larger the partition ratio is, the more lithium ions in the solution enter the organic phase, and the calculation formula of the partition ratio is as follows:
the abundance of a lithium isotope refers to the ratio of the content of one isotope of lithium in the total lithium elements, and the increased abundance of a lithium isotope refers to the percentage of one isotope of lithium that is increased after isotope separation and enrichment, compared to before enrichment, and 6 abundance of Li 6 Li%) and the increased abundance (. DELTA.h #) 6 Li%)) can be expressed as: Δh% 6 Li％)＝h 2 ( 6 Li％)-h 1 ( 6 Li%; wherein, deltah is% 6 Li%) refers to increased lithium isotope abundance, h 1 ( 6 Li%) refers to the abundance of lithium isotopes before separation and enrichment, h 2 ( 6 Li%) refers to the abundance of the lithium isotope after separation and enrichment.
The abundance before and after separation is calculated and obtained after testing the thousandth deviation of the lithium isotope by using an inductively coupled plasma mass spectrometer, and the calculation formula is as follows:in the formula: 7 Li/ 6 Li SVEC = 12.177, standard lithium for test unit 7 Li and Li 6 Abundance ratio of Li; delta 7/6 Li (mill) is the relative deviation of one thousandth and is directly given by the test instrument. Thus, two out of the three quantities in the above equation are known [ ] 7 Li/ 6 Li SVEC And delta 7/6 Li (mill)) so that the experimental sample can be calculated 7 Li/ 6 Li Sample of Is a numerical value of (2).
Since the total content of two isotopes of lithium is 100%, it is set 6 The abundance of Li is x, then 7 The abundance of Li is 1-x, then: 7 Li/ 6 Li sample of = (1-x)/x, thereby obtaining 6 Specific values of Li abundance x.
The multi-stage separation coefficient (α) of the lithium isotope represents the effect of multi-stage separation of the lithium isotope, i.e., the quotient of the abundance ratio of the lithium isotope in the organic extraction phase after multi-stage separation and the abundance ratio of the lithium isotope in the originally used lithium salt solution:
wherein S is 0 Represents the coordination environment of lithium ions in the original lithium salt stock solution, Y n Representing the coordination environment of lithium ions in the organic extraction phase after multistage separation. A multi-stage separation coefficient equal to 1 indicates that separation of lithium isotopes is not achieved; the greater the degree of deviation of the multistage separation coefficient from 1, the greater the degree of lithium isotope separation.
The embodiment of the invention provides a system for separating lithium isotopes by multistage air floatation extraction, which comprises a floatation column, an organic extraction phase, a lithium salt solution phase and m parts of exchange liquid. Wherein, based on the condition of bubbling gas in the flotation column, the organic extraction phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation to obtain an extraction enrichment solution, and m parts of exchange solution are sequentially mixed with the flotation columnThe extraction enrichment liquid is subjected to m-level air floatation exchange separation to obtain the enrichment liquid 6 The m-th exchange enriched liquid of Li, m is an integer of 2 or more.
The organic extraction phase comprises an extracting agent, an ionic liquid and a diluting agent which are mixed with each other, the lithium salt solution phase is an aqueous solution of lithium salt, and the exchange liquid is an aqueous solution of bis (trifluoromethanesulfonyl) imide, sulfuric acid or hydrochloric acid.
In a preferred embodiment, the extractant is selected from any one of the compounds represented by the following formulas 1 to 3,
in the compounds shown in the formulas 1 to 3, R is selected from alkyl, alkoxy, amino, nitro or phenyl with the carbon number of 0 to 20, X is N or O, and N is 0, 1 or 2.
The ionic liquid consists of anions and cations; the cation is selected from any one of cations represented by the following formulas 2-1 to 2-10,
r, R in the cations of the formulae 2-1 to 2-10 1 、R 2 、R 3 And R is 4 Independently selected from alkyl groups having 0 to 20 carbon atoms; the anion is selected from [ PF ] 6 ] - 、[(SO 2 CF 3 ) 2 N] - 、[(SO 2 CF 2 CF 3 ) 2 N] - 、[CF 3 SO 3 ] - 、[CH 3 COO] - And [ BF ] 4 ] - One or two or more of them.
The diluent is selected from one or more of anisole, dichloromethane, chloroform, 1, 2-dichloroethane, nitrobenzene, 1, 2-trichloroethane, acetone, methyl isobutyl ketone, methyl tert-butyl ketone and kerosene.
In a preferred embodiment, in the organic extraction phase, the volume ratio of the ionic liquid to the diluent is (1-10): (1-15), wherein the concentration of the extractant is 0.1 mol/L-0.5 mol/L.
In a preferred embodiment, the lithium salt in the lithium salt solution phase is selected from LiCl, liBr, liI, liOH, liNO 3 、LiClO 4 、LiSCN、CH 3 COOLi、CF 3 COOLi、CHF 2 COOLi、CH 2 FCOOLi and Li [ NTf 2 ]Any one of them; the concentration of lithium salt in the lithium salt solution phase is 0.2mol/L to 5mol/L.
In a preferred embodiment, the concentration of the exchange liquid is 0.4mol/L to 0.6mol/L.
In a preferred scheme, when the organic extraction phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation in the flotation column or m parts of exchange liquid are sequentially subjected to m-stage air flotation exchange separation with an extraction enrichment liquid, gas blown into the flotation column is selected from any one of nitrogen, oxygen, carbon dioxide, hydrogen or rare gas, the gas flow is 1-25 mL/min, and the gas blowing time is 60-90 min.
In a preferred embodiment, when the organic extract phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation based on the flotation column, the organic extract phase and the lithium salt solution phase are mixed in a volume ratio of 1: (1-15) is placed in the flotation column.
In a preferred scheme, when m parts of exchange liquid and the extraction enrichment liquid are sequentially subjected to m-level air flotation exchange separation based on the flotation column, the volume ratio of the extraction enrichment liquid to the exchange liquid is 1: (1-15) is placed in the flotation column.
In a preferred scheme, the floatation column is a temperature-controllable floatation column, and the temperature is controlled to be 260K-295K when extraction separation or exchange separation is carried out in the floatation column.
In a preferred scheme, the value of m is 4.ltoreq.m.ltoreq.20
The system for extracting and separating the lithium isotopes by multistage air floatation based on the above method is applied to the process of extracting and separating the lithium isotopes, and comprises the following steps:
s1, preparing the organic extract phase: mixing the extractant, the ionic liquid and the diluent to prepare the organic extract phase.
S2, preparing the lithium salt solution phase: dissolving lithium salt in water to prepare the lithium salt solution phase.
S3, preparing the exchange liquid: and preparing an aqueous solution of bis (trifluoromethanesulfonyl) imide, sulfuric acid or hydrochloric acid as an exchange liquid to obtain m parts of the exchange liquid.
S4, placing the organic extraction phase and the lithium salt solution phase into a flotation column, blowing gas into the flotation column for extraction, and centrifugally separating and removing unreacted lithium salt solution phase after extraction is completed to obtain an extraction enrichment solution.
S5, placing the extraction enrichment liquid and the first part of exchange liquid into a flotation column, bubbling gas into the flotation column for exchange, and centrifugally separating and removing unreacted exchange liquid after the exchange is completed to obtain the first exchange enrichment liquid.
S6, placing the first exchange enrichment liquid and the second exchange liquid into a flotation column, blowing gas into the flotation column for exchange, and centrifugally separating and removing unreacted exchange liquid after the exchange is completed to obtain a second exchange enrichment liquid.
S7, repeating the step S6 until the m exchange liquid and the m-1 exchange enrichment liquid finish air floatation exchange, thereby obtaining enriched liquid 6 An mth exchange enriched liquid of Li; wherein m is an integer of 2 or more.
Example 1
The system for separating lithium isotopes by multistage air-floatation extraction provided by the embodiment, in particular to a system for separating lithium isotopes by three-stage air-floatation extraction, which comprises a floatation column, an organic extraction phase, a lithium salt solution phase and 2 parts of exchange liquid. The process for extracting and separating the lithium isotopes comprises the following steps:
1. preparing an organic extract phase: ionic liquid 1-butyl-3-methylimidazole tetrafluoroborophosphate [ BMIm ]][BF 4 ]Mixing with anisole as diluent at volume ratio of 3:5, and adding 12-crown-4 as extractant to obtain organic extract phase with concentration of 0.7 mol/L.
In this example, the extractant was selected from 12-crown-4, the compound of formula 3; the cation in the ionic liquid is selected as the compound of the formulas 2-9, and the anion is selected as [ PF ] 4 ] - 。
2. Preparing a lithium salt solution phase: lithium salt LiNO 3 Dissolving in water to prepare a lithium salt solution phase with the concentration of 2 mol/L. Wherein, liNO before separation 3 In solution 6 The abundance of Li was 7.57%.
3. Preparation of 0.5mol/L H 2 SO 4 The solution was used as exchange liquid, and a total of 2 parts of exchange liquid was used.
4. First stage air flotation separation enrichment
And placing the organic extraction phase and the lithium salt solution phase into a flotation column for extraction, and then extracting and separating to obtain an extraction enrichment solution. Specifically comprising: and respectively transferring the organic extraction phase and the lithium salt solution phase by using a liquid transferring gun, putting the organic extraction phase and the lithium salt solution phase into a temperature-controllable flotation column according to the volume ratio of 1:5, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to 283K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to 5mL/min, and ventilating for 90min for extraction. And (3) placing the mixed solution after the extraction reaction in a centrifugal machine for centrifugal separation to obtain an extracted enrichment solution.
The isotopic abundance of lithium in the extraction enrichment was tested, 6 the abundance of Li is 7.78%, 6 the abundance of Li is improved by 0.21%, and the single-stage separation coefficient of the lithium isotope is 1.030.
5. Second stage air flotation separation enrichment
And (3) placing the extraction enrichment liquid and the 1 st part of exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 1 st part of exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:2 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to 283K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to 5mL/min, and ventilating for 90min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 1-1.
The isotopic abundance of lithium in exchange enrichment 1-1 was tested, 6 the abundance of Li is 7.98%, 6 the abundance of Li is increased by 0.41%, and the multi-stage separation coefficient of the lithium isotope is 1.059.
6. Third stage air floatation separation and enrichment
And (3) placing the exchange enrichment liquid 1-1 obtained in the step (V) and the 2 nd part of exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 2 nd exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:2 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to 283K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to 5mL/min, and ventilating for 90min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 1-2.
The isotopic abundance of lithium in exchange enrichment 1-2 was tested, 6 the abundance of Li is 8.17%, 6 the abundance of Li is increased by 0.60%, and the multi-stage separation coefficient of the lithium isotope is 1.086.
Example 2
The system for separating lithium isotopes by multistage air-flotation extraction provided by the embodiment, in particular to a system for separating lithium isotopes by five-stage air-flotation extraction, which comprises a flotation column, an organic extraction phase, a lithium salt solution phase and 4 parts of exchange liquid. The process for extracting and separating the lithium isotopes comprises the following steps:
1. preparing an organic extract phase: ionic liquid 1-ethyl-3-methylimidazole bis (trifluoromethanesulfonyl) imide salt ([ EMIm)][NTf 2 ]) Mixing with anisole as diluent at volume ratio of 3:10, and adding dibenzo-15-crown-5 (i.e. the compound of formula 2) as extractant to obtain organic extract phase with concentration of 0.4 mol/L.
2. Preparation of lithiumSalt solution phase: the lithium salt LiI is dissolved in water to prepare a lithium salt solution phase with the concentration of 1 mol/L. Wherein, in LiI solution before separation 6 The abundance of Li was 7.61%.
3. As exchange liquid, 0.6mol/L HCl solution was prepared, and a total of 4 parts of exchange liquid was prepared.
4. First stage air flotation separation enrichment
And placing the organic extraction phase and the lithium salt solution phase into a flotation column for extraction, and then extracting and separating to obtain an extraction enrichment solution. Specifically comprising: and respectively transferring the organic extraction phase and the lithium salt solution phase by using a liquid transferring gun, putting the organic extraction phase and the lithium salt solution phase into a temperature-controllable flotation column according to the volume ratio of 1:3, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to 293K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to 15mL/min, and ventilating for 70min for extraction. And (3) placing the mixed solution after the extraction reaction in a centrifugal machine for centrifugal separation to obtain an extracted enrichment solution.
The isotopic abundance of lithium in the extraction enrichment was tested, 6 the abundance of Li is 7.80%, 6 the abundance of Li is increased by 0.19%, and the single-stage separation coefficient of the lithium isotope is 1.027.
5. Second stage air flotation separation enrichment
And (3) placing the extraction enrichment liquid and the 1 st part of exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 1 st exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:3 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to be 293K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to be 15mL/min, and ventilating for 70min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 2-1.
The isotopic abundance of lithium in exchange enrichment 2-1 was tested, 6 the abundance of Li is 7.99%, 6 the abundance of Li is improved by 0.38%, and the multi-stage separation coefficient of the lithium isotope is 1.054.
6. Third stage air floatation separation and enrichment
And (3) placing the exchange enrichment liquid 2-1 obtained in the step (V) and the 2 nd part of exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 2 nd exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:3 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to be 293K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to be 15mL/min, and ventilating for 70min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 2-2.
The isotopic abundance of lithium in exchange enrichment 2-2 was tested, 6 the abundance of Li is 8.17%, 6 the abundance of Li is increased by 0.56%, and the multi-stage separation coefficient of the lithium isotope is 1.080.
7. Fourth stage air flotation separation and enrichment
And (3) placing the exchange enrichment liquid 2-2 obtained in the step (V) and the 3 rd part of exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 3 rd exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:3 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to be 293K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to be 15mL/min, and ventilating for 70min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 2-3.
The isotopic abundance of lithium in exchange enrichment 2-3 was tested, 6 the abundance of Li is 8.36%, 6 the abundance of Li is increased by 0.75%, and the multi-stage separation coefficient of the lithium isotope is 1.110.
8. Fifth stage air floatation separation and enrichment
And (3) placing the exchange enrichment liquid 2-3 obtained in the step (V) and the 4 th exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 4 th exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:3 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to be 293K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to be 15mL/min, and ventilating for 70min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 2-4.
The isotopic abundance of lithium in exchange enrichment 2-4 was tested, 6 the abundance of Li is 8.49%, 6 the abundance of Li is increased by 0.88%, and the multi-stage separation coefficient of the lithium isotope is 1.130.
Example 3
The system for separating lithium isotopes by multi-stage air-flotation extraction provided by the embodiment, in particular to a system for separating lithium isotopes by twenty-stage air-flotation extraction, which comprises a flotation column, an organic extraction phase, a lithium salt solution phase and 19 parts of exchange liquid. The process for extracting and separating the lithium isotopes comprises the following steps:
1. preparing an organic extract phase: ionic liquid 1-hexyl-3-methylimidazole bistrifluoromethane sulfonimide salt ([ HMIm)][NTf 2 ]) Mixing with anisole as diluent at volume ratio of 3:7, and adding benzo-15-crown-5 (compound of formula 1) as extractant to obtain organic extract phase with concentration of 0.6mol/L.
2. Preparing a lithium salt solution phase: lithium salt Li [ NTf 2 ]Dissolving in water to prepare a lithium salt solution phase with the concentration of 3 mol/L. Wherein Li [ NTf ] before separation 2 ]In solution 6 The abundance of Li was 7.51%.
3. As exchange liquid, 0.4mol/L HCl solution was prepared, and a total of 19 parts of exchange liquid was prepared.
4. First stage air flotation separation enrichment
And placing the organic extraction phase and the lithium salt solution phase into a flotation column for extraction, and then extracting and separating to obtain an extraction enrichment solution. Specifically comprising: and respectively transferring the organic extraction phase and the lithium salt solution phase by using a liquid transferring gun, putting the organic extraction phase and the lithium salt solution phase into a temperature-controllable flotation column according to the volume ratio of 1:1, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to 272K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to 10mL/min, and ventilating for 60min for extraction. And (3) placing the mixed solution after the extraction reaction in a centrifugal machine for centrifugal separation to obtain an extracted enrichment solution.
Isotopic abundance of lithium in the extraction enrichmentThe test was performed with the aid of a test, 6 the abundance of Li is 7.62%, 6 the abundance of Li is improved by 0.11%, and the single-stage separation coefficient of the lithium isotope is 1.016.
5. Second stage air flotation separation enrichment
And (3) placing the extraction enrichment liquid and the 1 st part of exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 1 st part of exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:1 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to 272K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to 10mL/min, and ventilating for 60min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 3-1.
The isotopic abundance of lithium in exchange enrichment 3-1 was tested, 6 the abundance of Li was 7.71%, 6 the abundance of Li is increased by 0.20%, and the single-stage separation coefficient of the lithium isotope is 1.029.
6. Third stage air floatation separation and enrichment
And (3) placing the exchange enrichment liquid 3-1 obtained in the step (V) and the 2 nd part of exchange liquid into a flotation column for extraction, and then carrying out exchange separation to obtain the exchange enrichment liquid. Specifically comprising: and respectively transferring the enriched extraction liquid and the 2 nd exchange liquid into a temperature-controllable flotation column according to the volume ratio of 1:1 by using a liquid transferring gun, opening a cooling circulation tank of the temperature-controllable flotation column, setting the temperature to 272K, opening ventilation (specific gas is nitrogen), adjusting the ventilation volume to 10mL/min, and ventilating for 60min to extract. And (3) placing the mixed solution after the exchange reaction in a centrifugal machine for centrifugal separation to obtain an exchange enrichment solution 3-2.
The isotopic abundance of lithium in exchange enrichment 3-2 was tested, 6 the abundance of Li is 7.80%, 6 the abundance of Li is increased by 0.29%, and the multi-stage separation coefficient of the lithium isotope is 1.042.
7. Fourth-twenty-first air floatation separation and enrichment
Referring to the step six, the 3 rd to 19 th exchange liquids are respectively subjected to air floatation exchange with the exchange enrichment liquid obtained by the air floatation separation enrichment of the previous stage, and the exchange enrichment liquids 3-3, 3-4, 3-5, 3-6, 3-7, 3-8, 3-9, 3-10, 3-11, 3-12, 3-13, 3-14, 3-15, 3-16, 3-17, 3-18, 3-19 and 3-20 are sequentially obtained.
Wherein, the isotope abundance of lithium in the exchange enrichment liquid 3-3 obtained by the fourth-stage air floatation separation enrichment is tested, 6 the abundance of Li is 7.90%, 6 the abundance of Li is increased by 0.39%, and the multi-stage separation coefficient of the lithium isotope is 1.056.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-4 obtained by fifth-stage air floatation separation enrichment, 6 the abundance of Li was 7.97%, 6 the abundance of Li is increased by 0.46%, and the multi-stage separation coefficient of the lithium isotope is 1.067.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-5 obtained by the sixth-stage air floatation separation enrichment, 6 the abundance of Li is 8.05%, 6 the abundance of Li is increased by 0.54%, and the multi-stage separation coefficient of the lithium isotope is 1.078.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-6 obtained by seventh-stage air floatation separation enrichment, 6 the abundance of Li is 8.12%, 6 the abundance of Li is increased by 0.61%, and the multi-stage separation coefficient of the lithium isotope is 1.088.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-7 obtained by eighth-stage air floatation separation enrichment, 6 the abundance of Li is 8.20%, 6 the abundance of Li is increased by 0.69%, and the multi-stage separation coefficient of the lithium isotope is 1.100.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-8 obtained by the ninth-stage air floatation separation enrichment, 6 the abundance of Li is 8.31%, 6 the abundance of Li is increased by 0.80%, and the multi-stage separation coefficient of the lithium isotope is 1.120.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-9 obtained by the tenth-stage air floatation separation enrichment, 6 the abundance of Li is 8.44%, 6 the abundance of Li is increased by 0.93%, and the multi-stage separation coefficient of the lithium isotope is 1.140.
Isotopic abundance of lithium in exchange enrichment liquid 3-10 obtained by eleventh-stage air floatation separation enrichmentThe test was performed in a row and, 6 the abundance of Li is 8.53%, 6 the abundance of Li is improved by 1.02%, and the multi-stage separation coefficient of the lithium isotope is 1.150.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-11 obtained by twelfth-stage air floatation separation enrichment, 6 the abundance of Li is 8.63%, 6 the abundance of Li is improved by 1.12%, and the multi-stage separation coefficient of the lithium isotope is 1.160.
The isotope abundance of lithium in the exchange enrichment liquid 3-12 obtained by the thirteenth-stage air floatation separation enrichment is tested, 6 the abundance of Li is 8.77%, 6 the abundance of Li is improved by 1.26%, and the multi-stage separation coefficient of the lithium isotope is 1.180.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-13 obtained by fourteenth-stage air floatation separation enrichment, 6 the abundance of Li is 8.90%, 6 the abundance of Li is improved by 1.39%, and the multi-stage separation coefficient of the lithium isotope is 1.200.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-14 obtained by fifteenth-stage air floatation separation enrichment, 6 the abundance of Li is 9.05%, 6 the abundance of Li is improved by 1.54%, and the multi-stage separation coefficient of the lithium isotope is 1.230.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-15 obtained by sixteenth-level air floatation separation enrichment, 6 the abundance of Li is 9.19%, 6 the abundance of Li is improved by 1.68%, and the multi-stage separation coefficient of the lithium isotope is 1.250.
The isotope abundance of lithium in the exchange enrichment liquid 3-16 obtained by seventeenth-stage air floatation separation enrichment is tested, 6 the abundance of Li is 9.31%, 6 the abundance of Li is improved by 1.80%, and the multi-stage separation coefficient of the lithium isotope is 1.260.
Testing the isotope abundance of lithium in the exchange enrichment liquid 3-17 obtained by eighteenth-level air floatation separation enrichment, 6 the abundance of Li is 9.42%, 6 the abundance of Li is improved by 1.91%, and the multi-stage separation coefficient of the lithium isotope is 1.280.
The nineteenth stage of air floatation separation and enrichment are carried out to obtain the same lithium in the exchange enrichment liquid 3-18The abundance of the potential element is tested and, 6 the abundance of Li is 9.51%, 6 the abundance of Li is improved by 2.00%, and the multi-stage separation coefficient of the lithium isotope is 1.290.
The isotope abundance of lithium in the exchange enrichment liquid 3-19 obtained by the twentieth air floatation separation enrichment is tested, 6 the abundance of Li is 9.65%, 6 the abundance of Li is improved by 2.14%, and the multi-stage separation coefficient of the lithium isotope is 1.320.
In conclusion, the system for extracting and separating lithium isotopes provided by the embodiment of the invention can effectively improve 6 The separation of Li enriches the abundance.
The foregoing is merely exemplary of the application and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the application and are intended to be comprehended within the scope of the application.
Claims (6)
1. A system for separating lithium isotopes by multistage air-floatation extraction, which is characterized by comprising a floatation column, an organic extraction phase, a lithium salt solution phase and m parts of exchange liquid; wherein, based on the condition of bubbling gas in the flotation column, the organic extraction phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation to obtain an extraction enrichment solution, and m parts of exchange solution are sequentially subjected to m-stage air flotation exchange separation with the extraction enrichment solution to obtain enriched solution 6 An mth exchange enriched liquid of Li;
the organic extraction phase comprises an extracting agent, an ionic liquid and a diluting agent which are mixed with each other, wherein the lithium salt solution phase is an aqueous solution of lithium salt, and the exchange liquid is an aqueous solution of bis (trifluoromethanesulfonyl) imide, sulfuric acid or hydrochloric acid; the concentration of the exchange liquid is 0.4mol/L to 0.6mol/L;
when the organic extraction phase and the lithium salt solution phase are subjected to first-stage air flotation extraction separation in the flotation column or m parts of exchange liquid are sequentially subjected to m-stage air flotation exchange separation with the extraction enrichment liquid, the gas blown into the flotation column is selected from any one of nitrogen, oxygen, carbon dioxide, hydrogen or rare gas, the gas flow is 1 mL/min-25 mL/min, and the gas blowing time is 60 min-90 min; the floatation column is a temperature-controllable floatation column, and the control temperature is 260K-295K when extraction separation or exchange separation is carried out in the floatation column;
wherein m is an integer of 2 or more;
wherein the extractant is selected from any one of the compounds represented by the following formulas 1 to 3,
，/>，the method comprises the steps of carrying out a first treatment on the surface of the In the compounds shown in the formulas 1 to 3, R is selected from alkyl, alkoxy, amino, nitro or phenyl with the carbon number of 0-20, X is N or O, and N is 0, 1 or 2;
the ionic liquid consists of anions and cations; the cation is selected from any one of cations represented by the following formulas 2-1 to 2-10,
、/>、/>、/>、、/>、/>、/>、、/>r, R in the cations of the formulae 2-1 to 2-10 1 、R 2 、R 3 And R is 4 Independently selected from alkyl groups having 0 to 20 carbon atoms; the anion is selected from [ PF ] 6 ] - 、[(SO 2 CF 3 ) 2 N] - 、[(SO 2 CF 2 CF 3 ) 2 N] - 、[CF 3 SO 3 ] - 、[CH 3 COO] - And [ BF ] 4 ] - One or two or more of them;
the diluent is selected from one or more of anisole, dichloromethane, chloroform, 1, 2-dichloroethane, nitrobenzene, 1, 2-trichloroethane, acetone, methyl isobutyl ketone, methyl tert-butyl ketone and kerosene.
2. The system for separating lithium isotopes by multistage air-flotation extraction according to claim 1, characterized in that the volume ratio of the ionic liquid to the diluent in the organic extraction phase is (1-10): (1-15), wherein the concentration of the extractant is 0.1 mol/L-0.5 mol/L.
3. The system for multistage air-floating extraction separation of lithium isotopes of claim 1, wherein the lithium salt in the lithium salt solution phase is selected from LiCl, liBr, liI, liOH, liNO 3 、LiClO 4 、LiSCN、CH 3 COOLi、CF 3 COOLi、CHF 2 COOLi、CH 2 FCOOLi and Li [ NTf 2 ]Any one of them; the concentration of lithium salt in the lithium salt solution phase is 0.2 mol/L-5 mol/L.
4. The system for multistage air-flotation extraction separation of lithium isotopes according to claim 1, characterized in that, based on the first stage air-flotation extraction separation of the organic extract phase and the lithium salt solution phase in the flotation column, the volume ratio of the organic extract phase to the lithium salt solution phase is 1: and (3) placing the mixture in the flotation column according to the proportion of (1-15).
5. The system for separating lithium isotopes by multistage air-flotation extraction according to claim 1, characterized in that when m parts of exchange liquid are sequentially subjected to m stages of air-flotation exchange separation from the extraction enrichment liquid based on the flotation column, the volume ratio of the extraction enrichment liquid to the exchange liquid is 1: and (3) placing the mixture in the flotation column according to the proportion of (1-15).
6. The system for separating lithium isotopes by multistage air-flotation extraction according to any of claims 1-5, wherein m has a value of 4.ltoreq.m.ltoreq.20.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102154563A (en) * | 2010-12-09 | 2011-08-17 | 江南大学 | Flotation method for enriching lithium from brine of salt lake brine |
| CN102671775A (en) * | 2012-06-11 | 2012-09-19 | 江南大学 | Chemical separation floatation column with high enrichment ratio |
| CN104607046A (en) * | 2015-02-11 | 2015-05-13 | 中国科学院上海高等研究院 | Method and device for separating and enriching lithium isotopes by utilizing membrane extraction |
| JP2015536234A (en) * | 2012-11-05 | 2015-12-21 | 上海 インスティテュート オブ オーガニック ケミストリー、チャイニーズ アカデミー オブ サイエンシーズＳｈａｎｇｈａｉ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｏｒｇａｎｉｃ Ｃｈｅｍｉｓｔｒｙ， Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Extraction agent for lithium isotope separation and its application |
| CN105536537A (en) * | 2015-12-17 | 2016-05-04 | 中国科学院青海盐湖研究所 | Method for extracting lithium isotope |
-
2020
- 2020-09-10 CN CN202010950021.5A patent/CN112058090B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102154563A (en) * | 2010-12-09 | 2011-08-17 | 江南大学 | Flotation method for enriching lithium from brine of salt lake brine |
| CN102671775A (en) * | 2012-06-11 | 2012-09-19 | 江南大学 | Chemical separation floatation column with high enrichment ratio |
| JP2015536234A (en) * | 2012-11-05 | 2015-12-21 | 上海 インスティテュート オブ オーガニック ケミストリー、チャイニーズ アカデミー オブ サイエンシーズＳｈａｎｇｈａｉ Ｉｎｓｔｉｔｕｔｅ Ｏｆ Ｏｒｇａｎｉｃ Ｃｈｅｍｉｓｔｒｙ， Ｃｈｉｎｅｓｅ Ａｃａｄｅｍｙ Ｏｆ Ｓｃｉｅｎｃｅｓ | Extraction agent for lithium isotope separation and its application |
| CN104607046A (en) * | 2015-02-11 | 2015-05-13 | 中国科学院上海高等研究院 | Method and device for separating and enriching lithium isotopes by utilizing membrane extraction |
| CN105536537A (en) * | 2015-12-17 | 2016-05-04 | 中国科学院青海盐湖研究所 | Method for extracting lithium isotope |
Non-Patent Citations (2)
| Title |
|---|
| Lithium isotope effect in extraction of lithium chloride by 4-Aminobenzo-15-crow n-5 in water-anisole ionic liquid double solvent system;Bing Liu et al.;《Journal of Radioanalytical and Nuclear Chemistry》;全文 * |
| 苯并-15-冠-5/离子液体体系液液萃取锂;束玉珍;吴继宗;邓惟勤;钱红娟;;核化学与放射化学(02);全文 * |
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