CN1814828A - Method for increasing metal-extracting efficiency of 1,, (2-ethyl-hexyl) phosphate - Google Patents
Method for increasing metal-extracting efficiency of 1,, (2-ethyl-hexyl) phosphate Download PDFInfo
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- CN1814828A CN1814828A CNA2006100106904A CN200610010690A CN1814828A CN 1814828 A CN1814828 A CN 1814828A CN A2006100106904 A CNA2006100106904 A CN A2006100106904A CN 200610010690 A CN200610010690 A CN 200610010690A CN 1814828 A CN1814828 A CN 1814828A
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Abstract
This invention discloses a method for increasing the rate of metal extraction of 2-organic phosphate, which mixes P204 and 260# solvent coal oil in the volume ratio of 5-40% to prepare them to the organic phase, adds acetate in the water with extraction materials as the aids of the P204 in the mol ratio of 0.5:1-3:1, fully mixes the two phases in a tank, then clarifies and separates the rest solution and the load organic phase, which washes out the extracted metals from the back-extraction and returns back to the extraction again, the rest solution is used in soaking materials of the being extracted metal, alkali substances in the material neutralize acid in the solution and the aqueous phase resolves the extracted metal then returns back for further extraction, in which, P204 can be used directly in the extraction without the process of saponification and the extraxtion rate is increased greatly.
Description
Technical field
The present invention relates to the extracting process of metal, more particularly, the present invention relates to a kind of employing two-(2-ethylhexyl) phosphoric acid ester is extraction agent, and metal is carried out method of extraction.
Background technology
At present, carried out extensive studies to adopting two-(2-ethylhexyl) phosphoric acid ester (being called for short: P204 or D2EHPA) as extraction agent extraction separation metal, and in the extraction of metals such as rare earth, nickel, cobalt, zinc, indium, realized industrialization.But, because P204 is an acidic extractant, directly in extraction process, can discharges hydrogen ion and cause solution acidity to raise with its extracting metals, finally make percentage extraction not high, organic phase loaded metal amount is low.
Solution acidity increases in the extraction process, usually employing alkali saponified means neutralize the hydrogen ion among the P204 in advance, bigger variation can not take place in the pH of solution in extraction process like this, extraction process is in the pH scope that helps extracting all the time, thereby reaches the purpose that improves percentage extraction.But load organic phases can be carried hydrogen ion again again after being unloaded carrying metal ion by sour back extraction, and the organic phase after the regeneration is when returning use, must carry out saponification handles, the every circulation primary of organic phase is all wanted saponification once, and alkali consumption is big, the processing cost height.
Someone studied with P204 and P507 (the own ester of 2-ethylhexyl phosphoric acid single 2-ethyl), TOA (trioctylamine) or TBP organic mixtures such as (tributyl phosphates) and extracted some metal, find that mixed extractant is better than the effect of single use extraction agent P204, but the pH value of solution value still there is very big influence to the extraction of metal.
On the other hand, along with the exhaustion day by day of Mineral resources, how making full use of the limited natural resource is the problem that people more and more pay close attention to, and the utilization of low-grade metal mineral wealth has also been put on schedule.The metallurgical technology in low-grade metal ore deposit normally adopts the method for dump leaching to extract metal, metal concentration is not high in the gained leach liquor, should not directly carry out electrolysis and produce metal, generally by extracting obtaining metal behind the metal enrichment again, P204 is applicable to the extraction of multiple metal.
P204 is a kind of weak acid HR, so owing to have the aqueous solution that long carbochain is insoluble in acidity or alkalescence, its molecular formula is:
In the course of the work, the positively charged ion M of it and aqueous phase
N+In conjunction with generating neutral compound MR
n(or M (HR)
nOr other forms), the neutral MR of generation
nDo not contain hydrophilic radical, thereby be insoluble in water and be soluble in organic solvent, hydrogen ion and solution metal ion generation cationic exchange in the reaction of extraction in its structure,
, metal ion enters organic phase, and hydrogen ion enters water, causes the acidity of the aqueous solution to raise.Because the extraction equilibrium constant is relevant with n (metal compound valency) power of hydrogen ion concentration in the aqueous solution, so the variation of pH is sensitive especially to the extraction of metal ion, the influence that pH value of solution extracts several metals to P204 as shown in Figure 1.As seen from the figure, at the percentage extraction height of higher pH scope metal, after extraction agent discharged hydrogen ion, the pH of solution can descend, and the percentage extraction of metal also and then sharply descends.With P204 extracting metals zinc is example, will have following reaction and take place:
Along with the carrying out of extraction, above-mentioned reaction takes place to the right, and H is constantly arranged
+Enter water, water pH rapidly down
Fall, the metal extraction rate also reduces significantly, and the percentage extraction that finally obtains is not high.
Usually the method that addresses this problem is before extraction extraction agent P204 to be carried out saponification to handle, with alkali in advance in and extraction agent in the hydrogen root, make that hydrogen root position is replaced by the positively charged ion in the alkaline solution in the extraction agent, but the extraction agent after handling through saponification does not so contain the free hydrogen ion, the positively charged ion (Na in the alkaline solution that is carried by come together metal ion and extraction agent that takes place in the extraction process
+, K
+, Ca
2+, NH
4 +Deng) between exchange, prevented that aqueous solution acidity in extraction process from rising, thereby improved effect of extracting.
But saponification will consume a large amount of alkali and be used for and hydrogen ion, and organic phase all will be carried out saponification again after each extraction and the back extraction, and production cost is increased greatly, has reduced the competitive power of technology.In addition, the saponification meeting causes extracted organic phase to become milk, is unfavorable for phase-splitting.This is urgency technical barrier to be solved of this professional domain.
Summary of the invention
The objective of the invention is at the deficiencies in the prior art part, a kind of method of raising two-(2-ethylhexyl) phosphoric acid ester extracting metals efficient is provided.This method helps the collection agent in the aqueous phase interpolation that contains by the collection metal, making P204 be directly used in extraction through the saponification processing also can obtain as the effect of extracting through saponification, and the percentage extraction of metal improves greatly, help the collection agent to be repeatedly used, cost is low, can not produce negatively influencing to total system.
Purpose of the present invention is achieved by following technical proposals.
The invention provides a kind of method of raising two-(2-ethylhexyl) phosphoric acid ester extracting metals efficient, this method adopts the step of following order:
(1) commercially available P204 and 260# solvent kerosene are mixed, wherein the volume ratio of P204 is 5%～40%, is made into extracted organic phase.
(2) contain by the aqueous phase of collection metal add acetate as P204 help the collection agent, acetate is selected from a kind of in sodium-acetate, Potassium ethanoate or the ammonium acetate, acetate be 0.5: 1～3: 1 by the mol ratio of collection metal.
(3) in extraction tank two-phase is carried out thorough mixing and extract, raffinate separates in the clarifying tank clarification with load organic phases then.
(4) after load organic phases process back extraction wash-out is come together metal, return and continue on for extraction, go round and begin again, recycle.
(5) raffinate is used to leach the material that contains by the collection metal, the acid in the alkaline matter meeting neutralization solution in leaching process in the material, and water dissolves again and is returned extraction again behind the collection metal, and circulation is used repeatedly.
Above step helps the collection agent except needs add to aqueous phase, and other is all identical with conventional extracting operation method.
Chemical principle of the present invention is as follows: add acetate at the aqueous phase of extracting system and help the collection agent as P204.P204 contacts with acid or weakly acidic water, after adding a certain amount of acetate toward aqueous phase, because aqueous phase contains part free hydrogen ion, they can form and be similar to acetic acid---and the buffered soln of acetate remains within the scope about pH=5.0 solution acidity.With the sodium-acetate is example, reacts as follows:
When hydrogen ion concentration in the solution increased, above-mentioned molecular balance moved right, and the acetate ion binding hydrogen ions generates difficult ionized weak electrolyte acetic acid.Like this, even constantly there is hydrogen ion to change water in the extraction process from organic phase, also can be owing to the shock absorption of acetate, make the pH of solution be unlikely to obviously to reduce and remain in the scope that helps extracting.
When returning, extraction liquid soaks the ore deposit when using, the H in the aqueous solution
+Be consumed with the metal oxide effect, above-mentioned balance regenerates acetate to moving to left, like this, added help the collection agent can be recycled.
Be used for the extraction with respect to P204 not being carried out any pre-treatment, metal extraction rate of the present invention significantly improves, with suitable through the effect of extracting after the saponification, like this for solution acidity concerning metal extraction have a significant effect metal very favourable.And acetate in the aqueous solution, can recycle always, and simple to operate, cost is low.
Compared with prior art, the present invention has following outstanding advantage:
(1) P204 does not use alkali soapization among the present invention, has avoided organic phase emulsification, has saved a large amount of alkali consumption.
(2) in extraction system, add acetate and help the collection agent as what keep pH value of solution, metal extraction rate height, effect can be suitable with saponification.
(3) the present invention is simple to operate, helps the collection agent to stay in the raffinate and can use repeatedly after the extraction, and the saponification cost reduces greatly relatively.
Description of drawings
Fig. 1 is the influence of pH value of solution value to the P204 extracting metals.
Embodiment
By specific embodiment given below, can further be well understood to the present invention.But they are not the qualifications to content of the present invention.
Except as otherwise noted, the percentage ratio that is adopted among the present invention is weight percentage.
Embodiment 1
Commercially available P204,260# kerosene are made into extracted organic phase by 30% and 70% volume ratio, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, contains the zinc dilution heat of sulfuric acid, Zn13.04g/L, and pH=5.0, zinc extraction yield are 72.4%.
Added sodium-acetate by the aqueous phase of collection metal and help collection agent, M containing as P204
Sodium-acetate: M
Zn=2: 1; In the extraction tank two-phase is carried out thorough mixing and extract, raffinate separates in the clarifying tank clarification with load organic phases then.Load organic phases is come together through the back extraction wash-out after the metal, returns and continues on for extraction, goes round and begins again, and recycles.Raffinate is used to leach the material that contains by the collection metal, the acid in the alkaline matter meeting neutralization solution in leaching process in the material, and water dissolves again and is returned extraction again behind the collection metal, and circulation is used repeatedly.The percentage extraction of zinc is 99.2%.
Embodiment 2
Contain the zinc dilution heat of sulfuric acid, Zn12.06g/L, pH=5.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and one-level extracts, and zinc extraction yield is 52.7%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=2: 1), other process is identical with embodiment 1.Zinc extraction yield is 92.9%.
Contain the zinc dilution heat of sulfuric acid, Zn1.24g/L, pH=5.0
Commercially available P204 and 260# kerosene, 5%P204+95% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 88.4%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=1: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 97.2%.
Embodiment 4
Contain the zinc dilution heat of sulfuric acid, Zn3.2g/L, pH=5.0
Commercially available P204 and 260# kerosene, 10%P204+90% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 58.7%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=1: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 89.4%.
Embodiment 5
Contain the zinc dilution heat of sulfuric acid, Zn6.5g/L, pH=5.0
Commercially available P204 and 260# kerosene, 15%P204+85% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 64.6%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=1: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 92.3%.
Embodiment 6
Contain the zinc dilution heat of sulfuric acid, Zn6.2g/L, pH=5.0
Commercially available P204 and 260# kerosene, 20%P204+80% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 84.9%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=1.5: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 95.6%.
Embodiment 7
Contain the zinc dilution heat of sulfuric acid, Zn13.4g/L, pH=5.0
Commercially available P204 and 260# kerosene, 25%P204+75% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 64.7%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=2: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 96.2%.
Embodiment 8
Contain the zinc dilute hydrochloric acid solution, Zn16.2g/L, pH=5.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 64.9%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=2: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 95.6%.
Embodiment 9
Contain the zinc dilute hydrochloric acid solution, Zn25.4g/L, pH=4.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 43.3%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=2.5: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 85.6%.
Embodiment 10
Contain the zinc dilute hydrochloric acid solution, Zn25.4g/L, pH=3.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 35.5%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Zn=3: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 87.5%.
Embodiment 11
Contain the zinc dilution heat of sulfuric acid, Zn13.4g/L, pH=5.0
Commercially available P204 and 260# kerosene, 25%P204+75% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 65.3%.
In the aqueous solution, add Potassium ethanoate (M
Acetate: M
Zn=2: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 96.6%.
Embodiment 12
Contain the zinc dilution heat of sulfuric acid, Zn6.2g/L, pH=5.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 84.5%.
In the aqueous solution, add Potassium ethanoate (M
Acetate: M
Zn=1: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 96.1%.
Embodiment 13
Contain the zinc dilution heat of sulfuric acid, Zn25.4g/L, pH=2.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 23.6%.
In the aqueous solution, add Potassium ethanoate (M
Acetate: M
Zn=2.5: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 85.6%.
Embodiment 14
Contain the zinc dilution heat of sulfuric acid, Zn13.4g/L, pH=4.0
Commercially available P204 and 260# kerosene, 25%P204+75% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 64.7%.
In the aqueous solution, add ammonium acetate (M
Acetate: M
Zn=2: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 94.7%.
Embodiment 15
Contain the zinc dilution heat of sulfuric acid, Zn6.2g/L, pH=4.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 84.9%.
In the aqueous solution, add ammonium acetate (M
Acetate: M
Zn=1: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 95.2%.
Embodiment 16
Contain the zinc dilution heat of sulfuric acid, Zn25.4g/L, pH=4.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and zinc extraction yield is 43.3%.
In the aqueous solution, add ammonium acetate (M
Acetate: M
Zn=2.5: 1), other process is identical with embodiment 1, and the percentage extraction of zinc is 83.8%.
Test-results compares:
Water is the zinc sulfate solution that contains the Different Zinc ionic concn, organic phase is that 30%P204+70% kerosene (volume ratio) is formed, extraction phase compares o/a=1/1, the extraction of three stage countercurrents, other each condition is identical, adds the size that helps collection agent sodium-acetate and do not add the percentage extraction of zinc under the situation that helps the collection agent and relatively lists in table 1.Under low metal concentration condition, because the concentration of hydrogen ion in solution that the displacement extraction agent discharges is not high, pH changes little, little to the extraction influence, so, add and help the collection agent little, under the condition of high metal concentration the percentage extraction influence, the hydrogen ion that discharges is to solution acidity influence when enough big, adds and helps the collection agent than the percentage extraction raising of not adding more than 30%.
Table 1 adds to help and comes together agent and do not have to add the comparison that helps the percentage extraction of zinc under two kinds of situations of collection agent
| Sequence number | Zn concentration (g/L) | M Acetate∶M Zn | Add and help collection agent Zn percentage extraction (%) | Do not add and help collection agent Zn percentage extraction (%) |
| 1 | 1.3 | 0.5∶1 | 99.4 | 99.3 |
| 2 | 4.2 | 1∶1 | 99.3 | 96.7 |
| 3 | 6.2 | 1∶1 | 98.6 | 89.0 |
| 4 | 9.8 | 1.5∶1 | 96.6 | 73.4 |
| 5 | 12.1 | 2∶1 | 98.9 | 67.5 |
| 6 | 17.6 | 2∶1 | 95.2 | 61.7 |
| 7 | 20.5 | 2∶1 | 93.8 | 52.7 |
| 8 | 24.2 | 2.5∶1 | 86.1 | 44.5 |
| 9 | 29.8 | 2.5∶1 | 73.7 | 35.8 |
Embodiment 17
The cupric dilution heat of sulfuric acid, Cu13.5g/L, pH=4.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and the copper percentage extraction is 63.6%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Cu=1: 1), other process is identical with embodiment 1, and the percentage extraction of copper is 99.8%.
Embodiment 18
The cupric dilution heat of sulfuric acid, Cu19.3g/L, pH=4.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and the copper percentage extraction is 51.2%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Cu=2: 1), other process is identical with embodiment 1, and the percentage extraction of copper is 98.4%.
Embodiment 19
The cupric dilution heat of sulfuric acid, Cu25.6g/L, pH=4.0
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the extractions of three stage countercurrents, and the copper percentage extraction is 45.1%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Cu=3: 1), other process is identical with embodiment 1, and the percentage extraction of copper is 84.7%.
Contain the cobalt dilution heat of sulfuric acid, Co21.6g/L, pH=4.5
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the Pyatyi counter-current extraction, and the cobalt percentage extraction is 36.4%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Co=3: 1), other process is identical with embodiment 1, and the percentage extraction of cobalt is 82.5%.
Embodiment 21
Contain the cobalt dilution heat of sulfuric acid, Co18.3g/L, pH=4.5
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the Pyatyi counter-current extraction, and the cobalt percentage extraction is 42.7%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Co=2: 1), other process is identical with embodiment 1, and the percentage extraction of cobalt is 94.3%.
Embodiment 22
Contain the cobalt dilution heat of sulfuric acid, Co18.3g/L, pH=4.5
Commercially available P204 and 260# kerosene, 30%P204++70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the Pyatyi counter-current extraction, and the cobalt percentage extraction is 42.7%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Co=1: 1), other process is identical with embodiment 1, and the percentage extraction of cobalt is 92.6%.
Embodiment 23
Nickeliferous dilute hydrochloric acid solution, Ni17.5g/L, pH=4.5
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the Pyatyi counter-current extraction, and the nickel percentage extraction is 38.7%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Ni=1: 1), other process is identical with embodiment 1, and the percentage extraction of nickel is 78.8%.
Embodiment 24
Nickeliferous dilute hydrochloric acid solution, Ni17.5g/L, pH=3.5
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the Pyatyi counter-current extraction, and the nickel percentage extraction is 35.2%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Ni=2: 1), other process is identical with embodiment 1, and the percentage extraction of nickel is 80.6%.
Embodiment 25
Nickeliferous dilute hydrochloric acid solution, Ni17.5g/L, pH=2.5
Commercially available P204 and 260# kerosene, 30%P204+70% kerosene (volume ratio) is formed organic phase, and extraction phase is than o/a=1/1, and extraction progression is the Pyatyi counter-current extraction, and the nickel percentage extraction is 30.1%.
In the aqueous solution, add sodium-acetate (M
Acetate: M
Ni=3: 1), other process is identical with embodiment 1, and the percentage extraction of nickel is 83.4%.
It is to be noted, technical scheme subject range of the present invention is extensive, for example, metals such as iron, calcium, magnesium, manganese, cadmium can be subjected to the influence of pH value of solution equally when extracting with P204 in weak acidic medium, therefore, interpolation is of the present invention in the extraction process of these metals helps the collection agent that percentage extraction is greatly improved.Because length is limit, an explanation for example here differs.
Claims (2)
1. method that improves two-(2-ethylhexyl) phosphoric acid ester extracting metals efficient, this method adopts the step of following order:
(1) is 5%～40% to mix by volume with commercially available P204 and 260# solvent kerosene, is made into extracted organic phase;
(2) contain by the aqueous phase of collection metal add acetate as P204 help the collection agent, acetate be 0.5: 1～3: 1 by the mol ratio of collection metal;
(3) in extraction tank two-phase is carried out thorough mixing and extract, raffinate separates in the clarifying tank clarification with load organic phases then;
(4) after load organic phases process back extraction wash-out is come together metal, return and continue on for extraction, recycle;
(5) raffinate is used to leach the material that contains by the collection metal, the acid in the alkaline matter neutralization solution in leaching process in the material, and water dissolves again and is returned extraction again behind the collection metal, and circulation is used repeatedly.
2. the method for raising two according to claim 1-(2-ethylhexyl) phosphoric acid ester extracting metals efficient, wherein the described acetate of step (2) is selected from a kind of in sodium-acetate, Potassium ethanoate or the ammonium acetate.
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| CN110616322A (en) * | 2019-09-20 | 2019-12-27 | 华中科技大学 | Non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using acidic extracting agent |
| CN112588274A (en) * | 2020-12-21 | 2021-04-02 | 江苏南方永磁科技有限公司 | Extraction material for separating cerium and preparation method thereof |
| CN113355512A (en) * | 2021-06-03 | 2021-09-07 | 华中科技大学 | Pretreatment method and extraction method of di (2-ethylhexyl) phosphate extractant |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPS51103020A (en) * | 1975-03-07 | 1976-09-11 | Morio Watanabe | RYUSANSANSEIYOEKYORI NI TO CO NO BUNRIHO |
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| CN101787451B (en) * | 2010-01-22 | 2011-10-26 | 内蒙古科技大学 | Method for improving efficiency of acidic organophosphorus extractant for extraction separation of rare-earth elements |
| CN102267770A (en) * | 2011-07-27 | 2011-12-07 | 南京师范大学 | Method for removing lead and zinc elements in ferrous chloride acidic waste water |
| CN102267770B (en) * | 2011-07-27 | 2013-04-03 | 南京师范大学 | Method for removing lead and zinc elements in ferrous chloride acidic waste water |
| CN102628100A (en) * | 2012-04-13 | 2012-08-08 | 宁波金田铜业(集团)股份有限公司 | Device and method for extracting zinc through acid leaching by using acid cyclically |
| CN110616322A (en) * | 2019-09-20 | 2019-12-27 | 华中科技大学 | Non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using acidic extracting agent |
| CN112588274A (en) * | 2020-12-21 | 2021-04-02 | 江苏南方永磁科技有限公司 | Extraction material for separating cerium and preparation method thereof |
| CN112588274B (en) * | 2020-12-21 | 2023-03-28 | 江苏南方永磁科技有限公司 | Extraction material for separating cerium and preparation method thereof |
| CN113355512A (en) * | 2021-06-03 | 2021-09-07 | 华中科技大学 | Pretreatment method and extraction method of di (2-ethylhexyl) phosphate extractant |
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| CN100383262C (en) | 2008-04-23 |
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