CN104593595A - Method for separating rare earth elements - Google Patents
Method for separating rare earth elements Download PDFInfo
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- CN104593595A CN104593595A CN201510039017.2A CN201510039017A CN104593595A CN 104593595 A CN104593595 A CN 104593595A CN 201510039017 A CN201510039017 A CN 201510039017A CN 104593595 A CN104593595 A CN 104593595A
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- 229910052761 rare earth metal Inorganic materials 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000000605 extraction Methods 0.000 claims abstract description 59
- 238000005406 washing Methods 0.000 claims abstract description 47
- 238000000926 separation method Methods 0.000 claims abstract description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000000463 material Substances 0.000 claims abstract description 18
- 238000001179 sorption measurement Methods 0.000 claims abstract description 17
- 238000010521 absorption reaction Methods 0.000 claims abstract description 9
- 238000002360 preparation method Methods 0.000 claims abstract description 4
- 150000002910 rare earth metals Chemical class 0.000 claims description 30
- 239000007788 liquid Substances 0.000 claims description 23
- 239000012074 organic phase Substances 0.000 claims description 15
- 229910052799 carbon Inorganic materials 0.000 claims description 14
- 238000005342 ion exchange Methods 0.000 claims description 12
- 239000000284 extract Substances 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 8
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 8
- 150000001412 amines Chemical class 0.000 claims description 8
- 238000005194 fractionation Methods 0.000 claims description 8
- 229910052698 phosphorus Inorganic materials 0.000 claims description 8
- 239000011574 phosphorus Substances 0.000 claims description 8
- -1 2-ethyl Chemical group 0.000 claims description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 239000006210 lotion Substances 0.000 claims description 6
- LJKDOMVGKKPJBH-UHFFFAOYSA-N 2-ethylhexyl dihydrogen phosphate Chemical class CCCCC(CC)COP(O)(O)=O LJKDOMVGKKPJBH-UHFFFAOYSA-N 0.000 claims description 5
- 230000002378 acidificating effect Effects 0.000 claims description 5
- 239000003350 kerosene Substances 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000012153 distilled water Substances 0.000 claims description 4
- 150000003512 tertiary amines Chemical class 0.000 claims description 4
- 238000011068 loading method Methods 0.000 claims description 3
- 229910000831 Steel Inorganic materials 0.000 claims description 2
- 239000010959 steel Substances 0.000 claims description 2
- 238000000638 solvent extraction Methods 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 3
- 230000001351 cycling effect Effects 0.000 abstract 1
- 238000010828 elution Methods 0.000 abstract 1
- 238000012856 packing Methods 0.000 abstract 1
- 238000005191 phase separation Methods 0.000 abstract 1
- 230000008092 positive effect Effects 0.000 abstract 1
- 239000000344 soap Substances 0.000 description 3
- 239000011575 calcium Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000007127 saponification reaction Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 229910052779 Neodymium Inorganic materials 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- WFXRJNDIBXZNJK-KVVVOXFISA-N azanium;(z)-octadec-9-enoate Chemical compound N.CCCCCCCC\C=C/CCCCCCCC(O)=O WFXRJNDIBXZNJK-KVVVOXFISA-N 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 229910052747 lanthanoid Inorganic materials 0.000 description 1
- 150000002602 lanthanoids Chemical class 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000013081 microcrystal Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention discloses a method for separating rare earth elements. The method comprises the following steps: (1) preparation of an activated carbon adsorption material, (2) column packing, (3) column separation, (4) column washing and (5) column cycling. The method has the positive effects that activated carbon is used as an adsorption material and has the characteristic of oil absorption, so that the problem of COD pollution caused by extraction wastewater does not exist; the rare earth elements are separated by using the activated carbon adsorption material, thus solving the problem of phase separation difficulty caused by traditional solvent extraction; separation of the rare earth elements by adopting a fractional extraction-elution process is achieved by utilizing a mode of connecting a plurality of columns in series and a new method is provided for separation of the rare earth elements.
Description
Technical field
The present invention relates to rare earths separation technical field, particularly relate to a kind of method of separation of rare earth elements.
Background technology
Rare earth element, because of its similar electron structure and rare earth " lanthanide contraction " phenomenon, causes the ionic radius between rare earth element close, determines the similarity of the physicochemical property of rare earth element, cause the separation difficulty between rare earth element.The separation method of rare earth element is numerous, and separation principle relies on the fine difference between rare earth compound, by certain extraction agent or precipitation agent through repeatedly repeated isolation step by rare earths separation.The multiplex Solvent Extraction Separation rare earth element of current technique, but Solvent Extraction Separation rare earth is because adopting in ammonia soap or soda soap, calcium soap, magnesium soap etc. and saponification organic phase, exchange lower a large amount of inorganic salt waste water containing ammonium or alkalimetal ion, contaminate environment or treatment cost high, the problem of environmental pollution such as simultaneously water body COD also can be brought to exceed standard.The requirement of solvent extration to feed liquid impurity is higher, Ca
2+, Mg
2+, Al
3+, Fe
3+, Si
4+easily there is third phase in foreign matter content height, causes phase-splitting difficulty, and the rare earth feed liquid extraction efficiency of extraction lower concentration is low, affects plant produced efficiency.Progression simultaneously needed for solvent extration is many, and mishmetal separation is obtained single rare earth approximately needs 3,000 multistage extraction tanks, and rare earth indent amount is large, and fixed cost investment is large.In recent years country also been proposed new requirement in the green smelting of rare earth, and therefore the method for the separation of rare earth elements that development research is new is particularly important.
Summary of the invention
For realizing the separation of rare earth, the invention provides a kind of method of separation of rare earth elements.Gac belongs to a kind of unformed Carbon Materials, and it is made up of graphite microcrystal and the hydrocarbon polymer that connects these crystallites.The stable chemical nature of gac, can resistance to strong acid, highly basic, high temperature, High Pressure, and it has flourishing microvoid structure and huge specific surface area, has good absorption property to organic substance and granule foreign.Invention utilizes the adsorbable organic characteristic of gac, adopts pickling process by phosphorus extractant and to H
+the mixed extractant absorption with the amine extractant composition of effect of extracting on the activated carbon, forms active carbon adsorption material thus, then realizes the separation of rare earth element with active carbon adsorption material.
The present invention adopts following technical scheme:
The concrete steps of the method for separation of rare earth elements of the present invention are as follows:
(1) preparation of active carbon adsorption material:
By acidic phosphorus extractant, amine extractant and sulfonated kerosene by volume for the ratio of 1:0.3 ~ 5:0 ~ 8 is mixed to form organic phase, the ratio of to be 5 ~ 500 object gacs by organic phase and granularity be in mass ratio 0.1 ~ 5:1 mixes formation active carbon adsorption material;
(2) post is filled:
Active carbon adsorption material wet method dress post method loading post footpath step (1) obtained is 1 ~ 300cm, aspect ratio is the ion exchange column of 1 ~ 80:1;
(3) post is separated:
The ion exchange column that step (2) dress post obtains carries out multicolumn series connection and obtains separator column, series system is as Fig. 2, separator column is divided into column extractor, washing column and re-extraction column according to pillar jointing, and post trend is along column extractor, washing column and re-extraction column direction; First column extractor is connected with the n-th washing column, and the first washing column is connected with the n-th re-extraction column; Be that the rare earth feed liquid of 3 ~ 5 is with 0.1 ~ 20cmmin by pH value
-1flow velocity flow through separator column from the first column extractor, be that the hydrochloric acid of 0.1 ~ 6mol/L is with 0.1 ~ 20cmmin by concentration
-1flow velocity flow through separator column from the first re-extraction column, from n-th re-extraction column flow out strip liquor with the form of washing lotion with 0.1 ~ 20cmmin
- 1flow velocity flow through separator column from the first washing column; Elapsed time
after, wherein: D
maxfor single pillar rare earth absorption saturation capacity, M
ffor feed liquid mass rate, f
afor feed liquid easily extracts component molar mark, λ was extraction coefficient, and the first column extractor enters washing section, and the first washing column enters stripping section; Obtain rare earth difficulty extraction component at the n-th column extractor place, obtain rare earth at the n-th re-extraction column place and easily extract component;
(4) post washing
Being washed with distilled water to elutant pH value being greater than 3 containing acid separation column after using, obtains blank post;
(5) post circulation
Blank post recirculation step (3) ~ (4) after washing realize adopting fractionation extraction to drench technique separation of rare earth elements.
In step (1), described phosphorus extractant is two (2-ethylhexyl phosphoric acids) or 2-ethylhexyl phosphoric acid single 2-ethyl polyhexamethylene; Described amine extractant is trialkyl tertiary amine.
In step (1), described organic phase is acidic phosphorus extractant, amine extractant with sulfonated kerosene by volume for the ratio of 1:0.3 ~ 5:0 ~ 8 mixes formed organic phase, the granularity of described gac is 5 ~ 500 orders, and organic phase is 0.1 ~ 5:1 with quality of activated carbon ratio.
In step (2), described ion exchange column post footpath is 1 ~ 300cm, aspect ratio is 1 ~ 80:1.
In step (4), the pH value of described rare earth feed liquid is 3 ~ 5.
In step (3), multicolumn series connection adopts fractionation extraction to drench the separation that technique realizes rare earth element; At the first column extractor feeding liquid, shunted by the n-th re-extraction column and flow through the first washing column post with the form of washing lotion, enter back extraction acid at the first re-extraction column; Elapsed time
after, wherein: D
maxfor single pillar rare earth absorption saturation capacity, M
ffor feed liquid mass rate, f
afor feed liquid easily extracts component molar mark, λ was extraction coefficient, first column extractor enters washing section becomes the n-th washing column, and the first washing column post enters stripping section becomes the n-th re-extraction column, obtains rare earth difficulty extraction component respectively, rare earth easily extracts component at the n-th column extractor, the n-th re-extraction column place.
Fractionation extraction is drenched ion exchange column described in process technology scheme and can be substituted with steel basin.
Positively effect of the present invention is as follows:
(1) gac has oil absorption, there is not the COD pollution problem that extraction wastewater produces;
(2) use active carbon adsorption material separation of rare earth elements, eliminate the phase-splitting difficult problem that traditional solvent extraction brings;
(3) utilize trialkyl tertiary amine (N235 resin) to H
+adsorptive power, not producing other positively charged ions when being separated, solving because saponification produces ammonia nitrogen or brine waste pollution problem;
(4) activated carbon property is stablized, and recycle is effective, easy to operate, nontoxic, pollution-free;
(5) mode utilizing multicolumn to connect realizes adopting fractionation extraction to drench technique separation of rare earth elements, and the separation for rare earth element provides a kind of novel method.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the inventive method;
Fig. 2 is the series system figure of the ion exchange column of the inventive method;
In figure, F-column extractor, W-washing column, H-re-extraction column, F
1-the first column extractor, Fn-n-th column extractor, W
1-the first washing column, Wn-n-th washing column, H
1-the first re-extraction column, Hn-n-th re-extraction column, V
f-feed velocity, V
w-washing lotion flow velocity, V
h-back extraction acid flow velocity.
Embodiment
The following examples describe in further detail of the present invention.
As shown in figure 1 and 2, the concrete steps of the method for separation of rare earth elements of the present invention are as follows:
(1) preparation of active carbon adsorption material:
By acidic phosphorus extractant, amine extractant and sulfonated kerosene by volume for the ratio of 1:0.3 ~ 5:0 ~ 8 is mixed to form organic phase, the ratio of to be 5 ~ 500 object gacs by organic phase and granularity be in mass ratio 0.1 ~ 5:1 mixes formation active carbon adsorption material;
(2) post is filled:
Active carbon adsorption material wet method dress post method loading post footpath step (1) obtained is 1 ~ 300cm, aspect ratio is the ion exchange column of 1 ~ 80:1;
(3) post is separated:
The ion exchange column that step (2) dress post obtains carries out multicolumn series connection and obtains separator column, series system is as Fig. 2, separator column is divided into column extractor F, washing column W and re-extraction column H according to pillar jointing, and post trend is along column extractor F, washing column W and re-extraction column H direction; First column extractor F
1be connected with the n-th washing column Wn, the first washing column W
1be connected with the n-th re-extraction column Hn; Be that the rare earth feed liquid of 3 ~ 5 is with 0.1 ~ 20cmmin by pH value
-1flow velocity from the first column extractor F
1place flows through separator column, is that the hydrochloric acid of 0.1 ~ 6mol/L is with 0.1 ~ 20cmmin by concentration
-1flow velocity from the first re-extraction column H
1place flows through separator column, from n-th re-extraction column Hn flow out strip liquor with the form of washing lotion with 0.1 ~ 20cmmin
-1flow velocity from the first washing column W
1flow through separator column; Elapsed time
after, wherein: D
maxfor single pillar rare earth absorption saturation capacity, M
ffor feed liquid mass rate, f
afor feed liquid easily extracts component molar mark, λ was extraction coefficient, the first column extractor F
1enter washing section, the first washing column W
1enter stripping section; At the n-th extraction F
nplace obtains rare earth difficulty extraction component, obtains rare earth easily extract component at the n-th re-extraction column Hn place;
(4) post washing
Being washed with distilled water to elutant pH value being greater than 3 containing acid separation column after using, obtains blank post;
(5) post circulation
Blank post recirculation step (3) ~ (4) after washing realize adopting fractionation extraction to drench technique separation of rare earth elements.
Embodiment 1
2-ethylhexyl phosphoric acid single 2-ethyl polyhexamethylene (P507) is mixed formation organic phase with trialkyl tertiary amine (N235) in the ratio of 1:1, be that 80 ~ 100 object gacs mix formation active carbon adsorption material again with granularity, wherein organic phase and gac are 1:1.5 in mass ratio; Active carbon adsorption material wet method dress post method is loaded post footpath is 20mm, post is high is the ion exchange column of 1000mm, dress post height is 850mm.
Separation circuit contains separator column 15, wherein column extractor 6, washing column 6, re-extraction column 3.Testing rare earth feed liquid concentration used is 0.3mol/L, and partition of rare earth element is Pr
3+: 51.30%, Nd
3+: 48.60%, the equal <0.1% of other elements, material liquid pH is 3.5, and rare earth feed liquid is with 1.06cmmin
-1flow velocity from F
1place flows through separator column, is that the hydrochloric acid of 5.0mol/L is with 5.5cmmin by concentration
-1flow velocity from H
1place flows through separator column, from H
3the back extraction acid moieties that place flows out is with 1.95cmmin
-1flow velocity flow into W
1post.After 3min, F
1post enters washing section, W
1post enters stripping section.At F
6place obtains Pr
3+concentration is 0.053mol/L, and purity is 99.89%, the equal <0.1% of other elements; At H
3place obtains Nd
3+concentration is 0.93mol/L, and purity is 99.90%, the equal <0.1% of other elements.
Be washed with distilled water to elutant pH value containing acid separation column and be greater than the blank post of 3 formation, blank post is used further to the separation of rare earth feed liquid, so recycles separator column.
Although illustrate and describe embodiments of the invention, for the ordinary skill in the art, be appreciated that and can carry out multiple change, amendment, replacement and modification to these embodiments without departing from the principles and spirit of the present invention, scope of the present invention is by claims and equivalents thereof.
Claims (7)
1. a method for separation of rare earth elements, is characterized in that: the concrete steps of described method are as follows:
(1) preparation of active carbon adsorption material:
By acidic phosphorus extractant, amine extractant and sulfonated kerosene by volume for the ratio of 1:0.3 ~ 5:0 ~ 8 is mixed to form organic phase, the ratio of to be 5 ~ 500 object gacs by organic phase and granularity be in mass ratio 0.1 ~ 5:1 mixes formation active carbon adsorption material;
(2) post is filled:
Active carbon adsorption material wet method dress post method loading post footpath step (1) obtained is 1 ~ 300cm, aspect ratio is the ion exchange column of 1 ~ 80:1;
(3) post is separated:
The ion exchange column that step (2) dress post obtains carries out multicolumn series connection and obtains separator column, series system is as Fig. 2, separator column is divided into column extractor (F), washing column (W) and re-extraction column (H) according to pillar jointing, and post trend is along column extractor (F), washing column (W) and re-extraction column (H) direction; First column extractor (F
1) be connected with the n-th washing column (Wn), the first washing column (W
1) be connected with the n-th re-extraction column (Hn); Be that the rare earth feed liquid of 3 ~ 5 is with 0.1 ~ 20cmmin by pH value
-1flow velocity from the first column extractor (F
1) place flows through separator column, is that the hydrochloric acid of 0.1 ~ 6mol/L is with 0.1 ~ 20cmmin by concentration
-1flow velocity from the first re-extraction column (H
1) place flows through separator column, the strip liquor flowed out from the n-th re-extraction column (Hn) with the form of washing lotion with 0.1 ~ 20cmmin
-1flow velocity from the first washing column (W
1) flow through separator column; Elapsed time
after, wherein: D
maxfor single pillar rare earth absorption saturation capacity, M
ffor feed liquid mass rate, f
afor feed liquid easily extracts component molar mark, λ was extraction coefficient, the first column extractor (F
1) enter washing section, the first washing column (W
1) enter stripping section; At the n-th column extractor (F
n) place obtain rare earth difficulty extraction component, obtain rare earth at the n-th re-extraction column (Hn) place and easily extract component;
(4) post washing:
Being washed with distilled water to elutant pH value being greater than 3 containing acid separation column after using, obtains blank post;
(5) post circulation:
Blank post recirculation step (3) ~ (4) after washing realize adopting fractionation extraction to drench technique separation of rare earth elements.
2. the method for a kind of separation of rare earth elements as claimed in claim 1, is characterized in that: in step (1), and described phosphorus extractant is two (2-ethylhexyl phosphoric acids) or 2-ethylhexyl phosphoric acid single 2-ethyl polyhexamethylene; Described amine extractant is trialkyl tertiary amine.
3. the method for a kind of separation of rare earth elements as claimed in claim 1, it is characterized in that: in step (1), described organic phase is acidic phosphorus extractant, amine extractant with sulfonated kerosene by volume for the ratio of 1:0.3 ~ 5:0 ~ 8 mixes formed organic phase, the granularity of described gac is 5 ~ 500 orders, and organic phase is 0.1 ~ 5:1 with quality of activated carbon ratio.
4. the method for a kind of separation of rare earth elements as claimed in claim 1, is characterized in that: in step (2), and described ion exchange column post footpath is 1 ~ 300cm, aspect ratio is 1 ~ 80:1.
5. the method for a kind of separation of rare earth elements as claimed in claim 1, is characterized in that: in step (4), and the pH value of described rare earth feed liquid is 3 ~ 5.
6. the method for a kind of separation of rare earth elements as claimed in claim 1, is characterized in that: in step (3), and multicolumn series connection adopts fractionation extraction to drench the separation that technique realizes rare earth element; At the first column extractor (F
1) feeding liquid, shunted by the n-th re-extraction column (Hn) and flow through the first washing column (W with the form of washing lotion
1) post, at the first re-extraction column (H
1) enter back extraction acid; Elapsed time
after, wherein: D
maxfor single pillar rare earth absorption saturation capacity, M
ffor feed liquid mass rate, f
afor feed liquid easily extracts component molar mark, λ was extraction coefficient, the first column extractor (F
1) enter washing section and become the n-th washing column (Wn), the first washing column (W
1) post enters stripping section becomes the n-th re-extraction column (Hn), at the n-th column extractor (F
n), the n-th re-extraction column (Hn) place obtains rare earth difficulty extraction component, rare earth respectively and easily extracts component.
7. the method for a kind of separation of rare earth elements as described in any one of claim 1-6, is characterized in that: fractionation extraction is drenched ion exchange column steel basin described in process technology scheme and substituted.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85101874A (en) * | 1985-04-01 | 1986-07-30 | 中国科学院长春应用化学研究所 | P507 extration resin chromatography is separated and extraction HIGH PURITY THULIUM OXIDE and lutecium oxide |
| CN102766766A (en) * | 2012-08-16 | 2012-11-07 | 江西理工大学 | Non-saponification rare earth extraction separation process |
| WO2014018421A1 (en) * | 2012-07-21 | 2014-01-30 | K-Technologies, Inc. | Processes for the recovery of fluoride and silica products and phosphoric acid from wet-process phosphoric acid facilities and contaminated waste waters |
| CN104120258A (en) * | 2014-07-25 | 2014-10-29 | 广西师范大学 | Method for non-saponification extraction and separation of light rare earth elements |
-
2015
- 2015-01-26 CN CN201510039017.2A patent/CN104593595B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85101874A (en) * | 1985-04-01 | 1986-07-30 | 中国科学院长春应用化学研究所 | P507 extration resin chromatography is separated and extraction HIGH PURITY THULIUM OXIDE and lutecium oxide |
| WO2014018421A1 (en) * | 2012-07-21 | 2014-01-30 | K-Technologies, Inc. | Processes for the recovery of fluoride and silica products and phosphoric acid from wet-process phosphoric acid facilities and contaminated waste waters |
| CN102766766A (en) * | 2012-08-16 | 2012-11-07 | 江西理工大学 | Non-saponification rare earth extraction separation process |
| CN104120258A (en) * | 2014-07-25 | 2014-10-29 | 广西师范大学 | Method for non-saponification extraction and separation of light rare earth elements |
Non-Patent Citations (1)
| Title |
|---|
| 方家远等: "负载N-1923活性炭富集230Th的快速测定", 《铀矿地质》 * |
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| Publication number | Publication date |
|---|---|
| CN104593595B (en) | 2017-11-03 |
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