CN113584305B - Application and method of N, N-dialkylamide carboxylic acid compounds - Google Patents
Application and method of N, N-dialkylamide carboxylic acid compounds Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 44
- -1 carboxylic acid compounds Chemical class 0.000 title claims abstract description 27
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 181
- 229910052761 rare earth metal Inorganic materials 0.000 claims abstract description 103
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 99
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 95
- 238000000605 extraction Methods 0.000 claims abstract description 81
- 229910052742 iron Inorganic materials 0.000 claims abstract description 80
- 150000002910 rare earth metals Chemical class 0.000 claims abstract description 80
- 239000012074 organic phase Substances 0.000 claims abstract description 79
- 239000003085 diluting agent Substances 0.000 claims abstract description 34
- 238000002156 mixing Methods 0.000 claims abstract description 18
- 239000003513 alkali Substances 0.000 claims abstract description 17
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 72
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 36
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 25
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 22
- 239000008346 aqueous phase Substances 0.000 claims description 17
- 150000007522 mineralic acids Chemical class 0.000 claims description 15
- 239000004411 aluminium Substances 0.000 claims description 13
- 239000002253 acid Substances 0.000 claims description 11
- 239000003350 kerosene Substances 0.000 claims description 9
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 8
- 150000001875 compounds Chemical class 0.000 claims description 8
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 2
- 229910017604 nitric acid Inorganic materials 0.000 claims description 2
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims 1
- 239000000446 fuel Substances 0.000 claims 1
- 229910052500 inorganic mineral Inorganic materials 0.000 claims 1
- 239000011707 mineral Substances 0.000 claims 1
- 238000004945 emulsification Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 4
- 239000000243 solution Substances 0.000 description 91
- 239000007788 liquid Substances 0.000 description 25
- 239000003795 chemical substances by application Substances 0.000 description 24
- 238000000926 separation method Methods 0.000 description 13
- 238000004364 calculation method Methods 0.000 description 9
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 9
- HNNQYHFROJDYHQ-UHFFFAOYSA-N 3-(4-ethylcyclohexyl)propanoic acid 3-(3-ethylcyclopentyl)propanoic acid Chemical compound CCC1CCC(CCC(O)=O)C1.CCC1CCC(CCC(O)=O)CC1 HNNQYHFROJDYHQ-UHFFFAOYSA-N 0.000 description 8
- 239000012071 phase Substances 0.000 description 7
- 230000008929 regeneration Effects 0.000 description 6
- 238000011069 regeneration method Methods 0.000 description 6
- 125000000999 tert-butyl group Chemical group [H]C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 6
- 238000003756 stirring Methods 0.000 description 5
- 125000001436 propyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])[H] 0.000 description 4
- 229910052727 yttrium Inorganic materials 0.000 description 4
- VWQVUPCCIRVNHF-UHFFFAOYSA-N yttrium atom Chemical compound [Y] VWQVUPCCIRVNHF-UHFFFAOYSA-N 0.000 description 4
- 238000007792 addition Methods 0.000 description 3
- 125000000217 alkyl group Chemical group 0.000 description 3
- 125000001995 cyclobutyl group Chemical group [H]C1([H])C([H])([H])C([H])(*)C1([H])[H] 0.000 description 3
- 125000001559 cyclopropyl group Chemical group [H]C1([H])C([H])([H])C1([H])* 0.000 description 3
- 125000001449 isopropyl group Chemical group [H]C([H])([H])C([H])(*)C([H])([H])[H] 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 125000004108 n-butyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- GREAEXCBUOTLNY-UHFFFAOYSA-N butanoic acid;n-ethylethanamine Chemical compound CC[NH2+]CC.CCCC([O-])=O GREAEXCBUOTLNY-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 125000000753 cycloalkyl group Chemical group 0.000 description 2
- 125000001511 cyclopentyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C1([H])[H] 0.000 description 2
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 125000000113 cyclohexyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C([H])([H])C1([H])[H] 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 125000000959 isobutyl group Chemical group [H]C([H])([H])C([H])(C([H])([H])[H])C([H])([H])* 0.000 description 1
- 125000004491 isohexyl group Chemical group C(CCC(C)C)* 0.000 description 1
- 125000001972 isopentyl group Chemical group [H]C([H])([H])C([H])(C([H])([H])[H])C([H])([H])C([H])([H])* 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 125000003136 n-heptyl 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])* 0.000 description 1
- 125000001280 n-hexyl group Chemical group C(CCCCC)* 0.000 description 1
- 125000000740 n-pentyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 125000002914 sec-butyl group Chemical group [H]C([H])([H])C([H])([H])C([H])(*)C([H])([H])[H] 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/04—Solvent extraction of solutions which are liquid
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B59/00—Obtaining rare earth metals
-
- 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)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to an application and a method of N, N-dialkyl amide carboxylic acid compounds, wherein in the structural formula of the N, N-dialkyl amide carboxylic acid compounds, R 1 And R 2 Are respectively independent C1-C9 alkyl, and n is a natural number of 1-6. The method comprises the following steps: mixing the diluent containing the N, N-dialkyl amido carboxylic acid compound and the rare earth solution containing aluminum and/or iron, and then adding alkali liquor for extraction. The N, N-dialkyl amido carboxylic acid compound is used as the extractant to separate iron and/or aluminum in the rare earth solution, so that the method has a good effect of removing the aluminum and the iron in the solution, and no emulsification phenomenon occurs in an organic phase in the extraction process.
Description
Technical Field
The invention relates to the field of metal separation and purification, in particular to application and a method of N, N-dialkyl amide carboxylic acid compounds.
Background
At present, the main method for extracting and removing aluminum and iron from rare earth feed liquid is naphthenic acid extraction.
For example, CN101979680A discloses a method for removing aluminum from rare earth feed liquid, which belongs to rare earth feed liquid treatment technology, and aims to provide a method for removing aluminum from rare earth feed liquid, which has the advantages of good aluminum removal effect, low aluminum removal cost, high rare earth recovery rate, convenient operation and control, simple process and less equipment investment, and the key points of the technical scheme are as follows: (1) Preparing an organic phase from 15-25% of naphthenic acid, 15-25% of alcohol and kerosene according to the volume ratio; (2) Adding the prepared organic phase and the rare earth feed liquid into a stirring tank according to the volume ratio of 2-5: 1, starting stirring, and uniformly mixing; (3) Under the condition of stirring, adding an alkaline solution into the mixed solution obtained in the step (2), wherein the total molar number of the added alkali is 50-100% of the total molar number of the rare earth elements in the rare earth feed liquid; (4) And (3) continuing stirring for a period of time after the alkali is added, stopping stirring, standing for a period of time, and separating the solution into a water phase and an organic phase, wherein the water phase is the rare earth feed liquid after the aluminum is removed.
Meanwhile, CN105200249A also discloses a method for extracting and separating high-purity yttrium from naphthenic acid with high stability, which can ensure that the mixing chamber has proper phase comparison to ensure that the mixing chamber is in a sticky state when the oil-water phase is relatively large or seriously fluctuates in the process of extracting and separating high-purity yttrium from naphthenic acid, so that the mixed phase is quickly clarified and split-phase in the clarification chamber. Compared with a mixing chamber of a high-purity yttrium tank body, the mixing chamber of the high-purity yttrium tank body can be quickly and stably extracted and separated by adjusting naphthenic acid through simple operation steps, a sticky system of the mixing chamber is quickly built again, normal phase splitting of a clarifying chamber is ensured, the operation is simple, the stability is good, the technical requirements on operators are reduced, and stable production of enterprises is facilitated.
Although various means are adopted to optimize the naphthenic acid extraction and separation system in the prior art, the problems of poor aluminum removal effect, organic compatibility, easy emulsification and the like in the extraction process still exist in the existing naphthenic acid extraction and separation.
Disclosure of Invention
In view of the problems in the prior art, the invention aims to provide application and a method of N, N-dialkylamide carboxylic acid compounds, wherein the N, N-dialkylamide carboxylic acid compounds are used as an extracting agent to separate iron and/or aluminum in a rare earth solution, so that the N, N-dialkylamide carboxylic acid compounds have a good effect of removing the aluminum and the iron in the solution, and no emulsification phenomenon occurs in an organic phase in an extraction process.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the invention provides an application of N, N-dialkylamide carboxylic acid compounds, wherein the application is used for extracting iron elements and/or aluminum elements in rare earth solutions.
The N, N-dialkyl amide carboxylic acid compound has the following structure:
in the formula, R 1 And R 2 Are respectively independent C1-C9 alkyl, and n is a natural number of 1-6.
In the invention, the N, N-dialkylaminocarboxylic acid compound is used as the extractant of the iron and/or aluminum elements in the rare earth solution, so that the aluminum and the iron in the solution can be well removed.
In the present invention, R is 1 And R 2 Each independently of the other, a C1-C9 alkyl group, for example, methyl, ethyl, propyl, isopropyl, n-butyl, isobutyl, sec-butyl, tert-butyl, n-pentyl, n-hexyl, n-heptyl, n-octyl, cyclopropyl, cyclobutyl, cyclopentyl, cyclohexyl and the like, may be a chain alkyl group (which may be the same or different), or a cycloalkyl group (which may be the same or different), or a combination of a chain alkyl group and a cycloalkyl group (which may be the same or different in the number of carbon atoms), such as R 1 And R 2 Each being ethyl and ethyl, e.g. R 1 And R 2 Each being ethyl and methyl, e.g. R 1 And R 2 Each being propyl and ethyl, e.g. R 1 And R 2 Each being n-butyl and propyl, e.g. R 1 And R 2 Each of tert-butyl and tert-butyl, e.g. R 1 And R 2 Each being propyl and cyclopropyl, e.g. R 1 And R 2 Each being ethyl and cyclobutyl, e.g. R 1 And R 2 Cyclopropyl and cyclobutyl, respectively, but are not limited to the alkyl groups listed, and other combinations not listed within this range are equally suitable.
In the present invention, n in formula I may be 1, 2, 3, 4, 5 or 6, etc., but is not limited to the recited values, and other combinations not recited within the range are also applicable.
In the invention, the N, N-dialkylaminocarboxylic acid compounds can be synthesized by conventional synthesis methods.
As a preferable technical scheme of the invention, in the structural formula of the N, N-dialkyl amido carboxylic acid compound, N is 2 or 3.
As a preferable technical scheme of the invention, R in the structural formula of the N, N-dialkyl amido carboxylic acid compound 1 And R 2 Each independently a C2-C8 alkyl group.
In a second aspect, the present invention provides a method of extracting iron and/or aluminium from a rare earth solution, the method comprising the steps of:
mixing the diluted solution containing the N, N-dialkyl amide carboxylic acid compound and the rare earth solution containing aluminum and/or iron, and adding alkali liquor for extraction.
In the method for extracting aluminum and/or iron from the solution, the N, N-dialkylamide carboxylic acid compounds are used as the extracting agent, and the aqueous phase and the organic phase are mixed and then added with the alkali liquor to be matched, so that the problem of emulsification of the organic phase in the process of extracting the aluminum and/or iron from the solution is solved.
As a preferred technical scheme of the invention, the diluent in the diluent comprises 1 or at least 2 of n-hexane, n-heptane, toluene, 260# solvent kerosene or aviation kerosene.
As a preferred embodiment of the present invention, the volume ratio of the N, N-dialkylaminocarboxylic acid compound to the diluent is (1-50) (50-99), and may be, for example, 1.
As a preferred embodiment of the present invention, the total concentration of the rare earth elements in the rare earth solution is 0.1 to 2mol/L, and may be, for example, 0.1mol/L, 0.2mol/L, 0.3mol/L, 0.4mol/L, 0.5mol/L, 0.6mol/L, 0.7mol/L, 0.8mol/L, 0.9mol/L, 1mol/L, 1.1mol/L, 1.2mol/L, 1.3mol/L, 1.4mol/L, 1.5mol/L, 1.6mol/L, 1.7mol/L, 1.8mol/L, 1.9mol/L, or 2mol/L, and the like, but is not limited thereto, and other combinations not listed in this range are also applicable.
Preferably, the concentration of aluminum element in the rare earth solution is 0.1 to 10g/L in terms of alumina, and may be, for example, 0.1g/L, 0.2g/L, 0.3g/L, 0.4g/L, 0.5g/L, 0.6g/L, 0.7g/L, 0.8g/L, 0.9g/L, 1g/L, 1.5g/L, 2g/L, 2.5g/L, 3g/L, 3.5g/L, 4g/L, 4.5g/L, 5g/L, 5.5g/L, 6g/L, 6.5g/L, 7g/L, 7.5g/L, 8g/L, 8.5g/L, 9g/L, 9.5g/L, or 10g/L, but not limited to the above, and other combinations are also applicable.
Preferably, the concentration of the iron element in the rare earth solution is 0.01 to 2g/L in terms of iron oxide, and may be, for example, 0.01g/L, 0.02g/L, 0.03g/L, 0.04g/L, 0.05g/L, 0.06g/L, 0.07g/L, 0.08g/L, 0.09g/L, 0.1g/L, 0.2g/L, 0.3g/L, 0.4g/L, 0.5g/L, 0.6g/L, 0.7g/L, 0.8g/L, 0.9g/L, 1g/L, 1.1g/L, 1.2g/L, 1.3g/L, 1.4g/L, 1.5g/L, 1.6g/L, 1.7g/L, 1.8g/L, 1.9g/L, or the like, and other values not listed in combination are applicable.
As a preferable technical scheme of the invention, the alkali liquor comprises 1 or at least 2 of ammonia water, sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution or potassium carbonate solution.
Preferably, the concentration of the alkali solution is 0.5 to 10mol/L, and may be, for example, 0.5mol/L, 0.6mol/L, 0.7mol/L, 0.8mol/L, 0.9mol/L, 1mol/L, 1.5mol/L, 2mol/L, 2.5mol/L, 3mol/L, 3.5mol/L, 4mol/L, 4.5mol/L, 5mol/L, 5.5mol/L, 6mol/L, 6.5mol/L, 7mol/L, 7.5mol/L, 8mol/L, 8.5mol/L, 9mol/L, 9.5mol/L, or 10mol/L, and the like, but is not limited to the recited values, and other combinations not recited in this range are also applicable.
Preferably, the addition amount of the alkali solution is 1 to 20% by volume of the rare earth solution, and may be, for example, 1%, 2%, 3%, 4%, 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%, 15%, 16%, 17%, 18%, 19%, or 20%, and the like, but is not limited to the values listed, and other combinations not listed within this range are also applicable.
Preferably, the volume ratio of the aqueous phase to the organic phase in the extraction is (0.1-10): 1, for example, can be 0.1.
As a preferable technical scheme of the invention, the loaded organic phase is subjected to back extraction by adopting inorganic acid after the extraction is finished.
Preferably, the inorganic acid comprises 1 or a combination of at least 2 of hydrochloric acid, nitric acid or sulfuric acid.
Preferably, the concentration of the inorganic acid is 0.5 to 10mol/L, and may be, for example, 0.5mol/L, 0.6mol/L, 0.7mol/L, 0.8mol/L, 0.9mol/L, 1mol/L, 1.5mol/L, 2mol/L, 2.5mol/L, 3mol/L, 3.5mol/L, 4mol/L, 4.5mol/L, 5mol/L, 5.5mol/L, 6mol/L, 6.5mol/L, 7mol/L, 7.5mol/L, 8mol/L, 8.5mol/L, 9mol/L, 9.5mol/L, or 10mol/L, and the like, but not limited to the values listed, and other combinations not listed in this range are also applicable.
Preferably, the organic phase obtained after the stripping is returned to the extraction process, and the aqueous phase is a solution rich in aluminium and/or iron.
As a preferable technical scheme of the invention, the method comprises the following steps:
mixing the diluent containing the N, N-dialkyl amide carboxylic acid compound and the rare earth solution containing aluminum and/or iron, and then adding alkali liquor for extraction;
the diluent in the diluent comprises 1 or the combination of at least 2 of normal hexane, normal heptane, toluene, 260# solvent kerosene or aviation kerosene; the volume ratio of the N, N-dialkyl amide carboxylic acid compounds to the diluent in the diluent is (1-50) to (50-99); the total concentration of the rare earth elements in the rare earth solution is 0.1-2mol/L; the concentration of the aluminum element in the rare earth solution is 0.1-10g/L calculated by alumina; the concentration of iron element in the rare earth solution is 0.01-2g/L calculated by ferric oxide; the alkali liquor comprises 1 or at least 2 of ammonia water, sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution or potassium carbonate solution; the concentration of the alkali liquor is 0.5-10mol/L; the addition amount of the alkali liquor is 1-20% of the volume of the rare earth solution; the volume ratio of the aqueous phase to the organic phase in the extraction is (0.1-10): 1.
Compared with the prior art, the invention at least has the following beneficial effects:
(1) The N, N-dialkyl amide carboxylic acid extractant has wide chemical raw material source, simple synthesis and low cost.
(2) The N, N-dialkyl amide carboxylic acid extracting agent has high selectivity on impurity aluminum and iron ions, the separation coefficient of aluminum, iron and rare earth is high, and the removal rate of aluminum and iron is high.
(3) After the extractant is used, the extractant is regenerated by inorganic acid and can be recycled.
Detailed Description
To better illustrate the invention and to facilitate the understanding of the technical solutions thereof, typical but non-limiting examples of the invention are as follows:
example 1
The extractant provided in this example was N, N-diethylamide butyric acid, R 1 And R 2 For ethyl, n =2, the formula is as follows:
the separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 20mL of N, N-diethylamide butyric acid extractant was mixed with 80mL of toluene diluent to prepare 100mL of an organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: taking 100mL of rare earth solution containing aluminum and iron elements, mixing the rare earth solution with the organic phase, slowly adding 6.0mol/L sodium hydroxide solution, and extracting. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 25. The total concentration of rare earth elements is 1.85mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 1. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: 25mL of 4.0mol/L hydrochloric acid is taken, and the loaded organic phase is subjected to back extraction, so that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. The back extraction time is 5 minutes, so that the extractant is regenerated.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 2
The extractant is N, N-di-N-octylamide butyric acid, namely R 1 And R 2 N-octyl, n =2, and the formula is as follows:
the separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 50mL of N, N-di-n-octylamidobutyric acid extractant was mixed with 50mL of aviation kerosene diluent to make up 100mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: 10mL of rare earth solution containing aluminum and iron elements is taken to be mixed with the organic phase, and 0.5mol/L sodium hydroxide solution is slowly added for extraction. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 5. The total concentration of rare earth elements is 0.3mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 0.1. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: 25mL of 4mol/L hydrochloric acid is taken, and the loaded organic phase is subjected to back extraction, so that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. The back extraction time is 5 minutes, so that the extractant is regenerated.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 3
The extractant is N, N-dicyclopentylamidobutyric acid, namely R 1 And R 2 The extraction agent is all cyclopentyl, n =2, the structural formula is as follows, the source of the extraction agent is self-made, and the purity and the yield are both more than 98%.
The separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 1mL of extractant was mixed with 9mL of toluene diluent to make up 10mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: taking 100mL of rare earth solution containing aluminum and iron elements, mixing the rare earth solution with the organic phase, slowly adding 8mol/L of sodium hydroxide solution, and extracting. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 10. The total concentration of rare earth elements is 2mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 10. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: 25mL of 4mol/L hydrochloric acid is taken, and the loaded organic phase is subjected to back extraction, so that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. Stripping time 5 minutes, regeneration of extractant.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 4
R in the extractant 1 Is n-butyl, R 2 The extraction agent is ethyl, n =3, the structural formula is as follows, the source of the extraction agent is self-made, and the purity and the yield are both more than 98%.
The separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 30mL of extractant was mixed with 70mL of toluene diluent to make up 100mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 3.
(2) The extraction process comprises the following steps: taking 100mL of rare earth solution containing aluminum and iron elements, mixing the rare earth solution with the organic phase, slowly adding 2mol/L sodium hydroxide solution, and extracting. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 20. The total concentration of rare earth elements is 1.5mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 1. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: 10mL of hydrochloric acid with the concentration of 10mol/L is taken, and the loaded organic phase is subjected to back extraction, so that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. The back extraction time is 5 minutes, so that the extractant is regenerated.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 5
R in the extractant 1 Is isopropyl, R 2 N-butyl, n =4, the structural formula is as follows, the source of the extracting agent is self-made, and the purity and the yield are both more than 98%.
The separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 20mL of extractant was mixed with 80mL of toluene diluent to make up 100mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: 500mL of rare earth solution containing aluminum and iron elements is taken to be mixed with the organic phase, and 1mol/L sodium hydroxide solution is slowly added for extraction. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 25. The total concentration of rare earth elements is 1.85mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 5. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: and taking 15mL of 6mol/L hydrochloric acid, and carrying out back extraction on the loaded organic phase to ensure that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. Stripping time 5 minutes, regeneration of extractant.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 6
R in the extractant 1 Is tert-butyl, R 2 N-amyl, n =5, the structural formula is as follows, the source of the extracting agent is self-made, and the purity and the yield are both more than 98%.
The separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 20mL of extractant was mixed with 80mL of toluene diluent to make up 100mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: taking 100mL of rare earth solution containing aluminum and iron elements, mixing the rare earth solution with the organic phase, slowly adding 3mol/L of sodium hydroxide solution, and extracting. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 25. The total concentration of rare earth elements is 1.85mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 1. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: and (3) taking 20mL of 5mol/L hydrochloric acid, and carrying out back extraction on the loaded organic phase to ensure that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. Stripping time 5 minutes, regeneration of extractant.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 7
R in the extractant 1 Is tert-butyl, R 2 The extraction agent is isopropyl, n =2, the structural formula is as follows, the source of the extraction agent is self-made, and the purity and the yield are both more than 98%.
The separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 20mL of extractant was mixed with 80mL of toluene diluent to make up 100mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: and (3) mixing 20mL of rare earth solution containing aluminum and iron elements with the organic phase, and slowly adding 6mol/L of sodium hydroxide solution for extraction. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 25. The total concentration of rare earth elements is 1.85mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 0.2. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: 25mL of 4mol/L hydrochloric acid is taken, and the loaded organic phase is subjected to back extraction, so that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. Stripping time 5 minutes, regeneration of extractant.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 8
R in the extractant 1 Is tert-butyl, R 2 The extraction agent is isohexyl, n =2, the structural formula is as follows, the source of the extraction agent is self-made, and the purity and the yield are both more than 98%.
The separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 20mL of extractant was mixed with 80mL of toluene diluent to make up 100mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: taking 100mL of rare earth solution containing aluminum and iron elements, mixing the rare earth solution with the organic phase, slowly adding 6mol/L sodium hydroxide solution, and extracting. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 25. The total concentration of rare earth elements is 1.85mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 1. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: and taking 15mL of 6mol/L hydrochloric acid, and carrying out back extraction on the loaded organic phase to ensure that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. Stripping time 5 minutes, regeneration of extractant.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Example 9
R in the extractant 1 Is ethyl, R 2 Is isoamyl, n =2, the structural formula is as follows, the source of the extracting agent is self-made, and the purity and the yield are both more than 98 percent.
The separation of iron and aluminium in the solution was carried out using the following procedure:
(1) Preparing an organic phase. 20mL of extractant was mixed with 80mL of toluene diluent to make up 100mL of organic phase. The volume ratio of the extracting agent to the diluting agent is 1.
(2) The extraction process comprises the following steps: taking 100mL of rare earth solution containing aluminum and iron elements, mixing the rare earth solution with the organic phase, slowly adding 6mol/L of sodium hydroxide solution, and extracting. The extraction time was 30 minutes. The volume ratio of the rare earth feed liquid to the liquid caustic soda is 25. The total concentration of rare earth elements is 1.85mol/L, and the concentration of aluminum elements is 4.025g/L (calculated as Al) 2 O 3 Calculated), the concentration of the iron element is 0.45g/L (calculated as Fe) 2 O 3 Calculation). The volume ratio of the rare earth solution to the organic phase is 1. The aluminum and iron elements are extracted into the organic phase to form a loaded organic phase, while the rare earth remains in solution;
(3) Back extraction process: and (3) taking 20mL of 5mol/L hydrochloric acid, and carrying out back extraction on the loaded organic phase to ensure that the aluminum and iron elements enter the inorganic acid solution. Aluminum and iron elements are effectively separated from rare earth elements. Stripping time 5 minutes, regeneration of extractant.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
Comparative example 1
Naphthenic acid is used as an extracting agent. The other conditions were the same as in example 1.
The changes of the aluminum concentration and the iron concentration in the aqueous phase before and after extraction are determined and shown in table 1.
TABLE 1
From the results of the above examples and comparative examples, it can be seen that the removal rates of aluminum and iron in the solution can be respectively more than 84% and more than 99.2% by separating iron and/or aluminum in the rare earth solution by using the N, N-dialkylamide carboxylic acid compounds as the extractant, and no emulsification phenomenon occurs in the organic phase during the extraction process.
The applicant declares that the present invention illustrates the detailed structural features of the present invention through the above embodiments, but the present invention is not limited to the above detailed structural features, that is, it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be understood by those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, additions of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are all within the protection scope of the present invention.
It should be noted that, in the above embodiments, the various features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, the present invention does not separately describe various possible combinations.
In addition, any combination of the various embodiments of the present invention can be made, and the same should be considered as the disclosure of the present invention as long as the idea of the present invention is not violated.
Claims (18)
1. The application of the N, N-dialkyl amide carboxylic acid compounds is characterized in that the application is used for extracting and separating iron elements and/or aluminum elements in a rare earth solution;
the N, N-dialkyl amide carboxylic acid compound has the following structure:
in the formula, R 1 And R 2 Are respectively independent C1-C9 alkyl, and n is a natural number of 1-6.
2. The use according to claim 1, wherein N in the formula of the N, N-dialkylaminocarboxylic acid compound is 2 or 3.
3. The use according to claim 1 or 2, wherein R in the formula of said N, N-dialkylaminocarboxylic acid compounds 1 And R 2 Each independently a C2-C8 alkyl group.
4. A method for extracting iron and/or aluminium from a rare earth solution, the method comprising the steps of:
mixing the diluted solution containing the N, N-dialkylaminocarboxylic acid compounds according to any one of claims 1 to 3 with a rare earth solution containing aluminum and/or iron, and adding an alkali solution to perform extraction.
5. The method of claim 4, wherein the diluent in the diluent comprises 1 or a combination of at least 2 of n-hexane, n-heptane, toluene, solvent 260# kerosene, or jet fuel.
6. The method according to claim 5, wherein the volume ratio of the N, N-dialkylaminocarboxylic acid compound to the diluent is (1-50) to (50-99).
7. The method of claim 4, wherein the total concentration of rare earth elements in the rare earth solution is 0.1 to 2mol/L.
8. The method according to claim 4, wherein the concentration of the aluminum element in the rare earth solution is 0.1 to 10g/L in terms of alumina.
9. The method according to claim 4, wherein the concentration of the iron element in the rare earth solution is 0.01 to 2g/L in terms of iron oxide.
10. The method of claim 4, wherein the lye comprises a combination of 1 or at least 2 of aqueous ammonia, sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution or potassium carbonate solution.
11. The method of claim 4, wherein the concentration of the lye is 0.5 to 10mol/L.
12. The method of claim 4, wherein the lye is added in an amount of 1 to 20 percent by volume of the rare earth solution.
13. The process according to claim 4, wherein the volume ratio of the aqueous phase to the organic phase in the extraction is (0.1-10): 1.
14. The process according to claim 4, wherein the loaded organic phase is back-extracted with a mineral acid after the extraction is completed.
15. The method of claim 14, wherein the inorganic acid comprises a combination of 1 or at least 2 of hydrochloric acid, nitric acid, or sulfuric acid.
16. The method of claim 14, wherein the concentration of the inorganic acid is 0.5 to 10mol/L.
17. The process according to claim 14, wherein the organic phase obtained after the stripping is returned to the extraction process and the aqueous phase is a solution rich in aluminium and/or iron.
18. A method according to any of claims 4-17, characterized in that the method comprises the steps of:
mixing the diluted solution containing the N, N-dialkylaminocarboxylic acid compound according to any one of claims 1 to 3 and a rare earth solution containing aluminum and/or iron, and adding an alkali solution for extraction;
the diluent in the diluent comprises 1 or the combination of at least 2 of normal hexane, normal heptane, toluene, 260# solvent kerosene or aviation kerosene; the volume ratio of the N, N-dialkyl amide carboxylic acid compounds to the diluent in the diluent is (1-50) to (50-99); the total concentration of rare earth elements in the rare earth solution is 0.1-2mol/L; the concentration of aluminum element in the rare earth solution is 0.1-10g/L calculated by alumina; the concentration of iron element in the rare earth solution is 0.01-2g/L calculated by ferric oxide; the alkali liquor comprises 1 or at least 2 of ammonia water, sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution or potassium carbonate solution; the concentration of the alkali liquor is 0.5-10mol/L; the addition amount of the alkali liquor is 1-20% of the volume of the rare earth solution;
the volume ratio of the aqueous phase to the organic phase in the extraction is (0.1-10): 1.
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