CN115679129A - Method for extracting and separating gallium from aluminum-containing sulfuric acid leaching solution - Google Patents
Method for extracting and separating gallium from aluminum-containing sulfuric acid leaching solution Download PDFInfo
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- CN115679129A CN115679129A CN202211338204.7A CN202211338204A CN115679129A CN 115679129 A CN115679129 A CN 115679129A CN 202211338204 A CN202211338204 A CN 202211338204A CN 115679129 A CN115679129 A CN 115679129A
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 64
- 229910052733 gallium Inorganic materials 0.000 title claims abstract description 55
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 238000002386 leaching Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 27
- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 25
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 239000003350 kerosene Substances 0.000 claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 7
- -1 carbon primary amine Chemical group 0.000 claims abstract description 7
- 238000000605 extraction Methods 0.000 claims description 52
- 239000012074 organic phase Substances 0.000 claims description 31
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 20
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 claims description 18
- STCOOQWBFONSKY-UHFFFAOYSA-N tributyl phosphate Chemical compound CCCCOP(=O)(OCCCC)OCCCC STCOOQWBFONSKY-UHFFFAOYSA-N 0.000 claims description 18
- 238000005406 washing Methods 0.000 claims description 13
- CHPZKNULDCNCBW-UHFFFAOYSA-N gallium nitrate Chemical compound [Ga+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O CHPZKNULDCNCBW-UHFFFAOYSA-N 0.000 claims description 12
- 239000012071 phase Substances 0.000 claims description 12
- 239000011701 zinc Substances 0.000 claims description 11
- 235000010344 sodium nitrate Nutrition 0.000 claims description 9
- 239000004317 sodium nitrate Substances 0.000 claims description 9
- 239000002893 slag Substances 0.000 claims description 8
- 229940044658 gallium nitrate Drugs 0.000 claims description 6
- 239000006227 byproduct Substances 0.000 claims description 5
- JQJCSZOEVBFDKO-UHFFFAOYSA-N lead zinc Chemical compound [Zn].[Pb] JQJCSZOEVBFDKO-UHFFFAOYSA-N 0.000 claims description 4
- 239000008346 aqueous phase Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 abstract description 23
- 150000002500 ions Chemical class 0.000 abstract description 17
- 239000012535 impurity Substances 0.000 abstract description 14
- 238000000926 separation method Methods 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 4
- 229910002651 NO3 Inorganic materials 0.000 abstract description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 abstract description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract 1
- 230000000052 comparative effect Effects 0.000 description 9
- 238000010828 elution Methods 0.000 description 9
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 229910052725 zinc Inorganic materials 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 150000002739 metals Chemical class 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- XTEGARKTQYYJKE-UHFFFAOYSA-M Chlorate Chemical compound [O-]Cl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-M 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000001117 sulphuric acid Substances 0.000 description 2
- 235000011149 sulphuric acid Nutrition 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000008204 material by function Substances 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
Classifications
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- 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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- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a method for extracting and separating gallium from an aluminum-containing sulfuric acid leaching solution, which skillfully utilizes a secondary carbon primary amine extractant (N1923) -tributyl phosphate-sulfonated kerosene mixed extractant to treat Ga in a sulfate system, a chloride system and a nitrate system 3+ And Al 3+ And other impurities, and finally Ga 3+ With Al 3+ And other impurity ions are completely separated, and gallium is extracted and separated from the aluminum-containing sulfuric acid leaching solution, so that the method is simple to operate, good in separation effect and high in recovery efficiency.
Description
The technical field is as follows:
the invention relates to the technical field of hydrometallurgy, in particular to a method for extracting and separating gallium from an aluminum-containing sulfuric acid leaching solution.
Background art:
gallium belongs to strategic metal resources, and is a series of compound semiconductor materials, electronic optical materials, novel functional materials, special alloys, organic metal compounds and the like prepared by taking gallium metal as a matrix, and is an important support material for high and new technologies of modern electronic computers, communication, space navigation, new energy, medicine, health, military industry and the like.
Gallium is used as a rare metal, basically has no independent deposit in nature, mainly accompanies with main metals such as aluminum, zinc and the like in mineral deposits such as lignite, bauxite, lead-zinc ore and the like, and enters by-product slag to be recovered in the smelting process of the main metals. The extraction and separation of the by-product slag after sulfuric acid leaching is one of the main ideas of gallium recovery, and the obtained gallium sulfuric acid leaching solution often contains Al with a certain concentration 3+ And Zn 2+ 、Cu 2+ And other impurity metals, the difficulty of extracting and separating gallium is higher. Especially due to Al 3+ And Ga 3+ The chemical properties of the two are very similar, and the high-efficiency separation of the two is difficult to realize by the existing extraction system or technology.
The invention content is as follows:
the invention aims to provide a method for extracting and separating gallium from an aluminum-containing sulfuric acid leaching solution.
The invention is realized by the following technical scheme:
a process for the extractive separation of gallium from an aluminous sulphuric acid leach solution, the process comprising the steps of:
1) Extracting an aluminum-containing sulfuric acid leaching solution by using a secondary carbon primary amine extractant (N1923) -tributyl phosphate (TBP) -sulfonated kerosene mixed extractant to obtain a gallium-containing loaded organic phase and a raffinate aqueous phase; wherein the aluminum-containing sulfuric acid leaching solution is derived from a sulfuric acid leaching solution of a byproduct slag in a lead-zinc ore wet process and contains Ga 3+ 1～2g/L、Al 3+ 1～3g/L、Zn 2+ 10～20g/L、Cu 2+ 10-20 g/L and Cd 2+ 1-5 g/L; the secondary carbon primary amine extractant (N1923) -tributyl phosphate (TBP) -sulfonated kerosene mixed extractant is prepared from the secondary carbon primary amine extractant (N1923), tributyl phosphate (TBP) and sulfonated kerosene with the volume ratio of 1-3;
2) Washing the gallium-containing loaded organic phase obtained in the step 1) by hydrochloric acid to obtain a pure gallium-loaded organic phase;
3) And (3) carrying out back extraction on the pure gallium loaded organic phase obtained in the step 2) by using sodium nitrate to obtain a separated gallium nitrate solution.
Preferably, the aluminiferous sulphuric acid leach liquor has a pH =0.5 to 1.5.
Preferably, the step 1) adopts countercurrent extraction; the extraction ratio of O/A is (1-3) to 1; the extraction stage number is 1-3; the extraction time is 5-10 min.
Preferably, the gallium-containing loaded organic phase is washed by hydrochloric acid in the step 2) in a cross flow manner, the concentration of the hydrochloric acid is 6-12 mol/L, and the washing ratio O/A is 1 (1-3); the number of stages of cross-flow washing is 1-3; the cross-flow washing time is 5-10 min.
Preferably, sodium nitrate is adopted to perform cross-flow back extraction on the pure gallium loaded organic phase in the step 3), the concentration of the sodium nitrate is 1-3 mol/L, and the back extraction ratio O/A is 1: (1-3); the stage number of the cross-flow back extraction is 3-5; the cross-flow back extraction time is 5-10 min.
The invention has the following beneficial effects: the invention skillfully utilizes the mixed extractant of N1923-TBP-sulfonated kerosene to react Ga in a sulfate system, a chlorate system and a nitrate system 3+ And Al 3+ And other impurities to finally realize Ga 3+ With Al 3+ And other impurity ions are completely separated, and gallium is extracted and separated from the aluminum-containing sulfuric acid leaching solution, so that the method is simple to operate, good in separation effect and high in recovery efficiency.
The specific implementation mode is as follows:
the following is a further description of the invention and is not intended to be limiting.
Example 1: method for extracting and separating gallium from aluminum-containing sulfuric acid leaching solution
The aluminum-containing sulfuric acid leaching solution is derived from a sulfuric acid leaching solution of a byproduct slag in a lead-zinc ore wet process, and mainly comprises the following components: ga 3+ 1.51g/L，Al 3+ 2.28g/L，Zn 2+ 10.22g/L，Cu 2+ 19.83g/L，Cd 2+ 4.29g/L，pH＝1.0。
Mixing 10% N1923, 10% TBP and 80% sulfonated kerosene by volume to obtain a mixed extractant. And (3) carrying out 1-stage extraction on the aluminum-containing sulfuric acid leaching solution and the mixed extracting agent according to the ratio O/A of 3, and extracting for 10min to obtain a gallium-containing loaded organic phase and a raffinate water phase. Ga 3+ Extraction rate 97.75%, al 3+ The extraction rate is 37.23%, and other ions are not extracted basically.
The gallium-containing loaded organic phase was subjected to 3-stage cross-flow washing with 8mol/L hydrochloric acid according to a phase ratio (O/A) 1 3+ The ion is not washed basically, and the elution rate of other ions is 100 percent; pure gallium-loaded organic phase is obtained, 2mol/L sodium nitrate is used for carrying out 5-stage cross-flow back extraction according to a phase ratio (O/A) 1, back extraction is carried out for 10min, ga is obtained 3+ The back extraction rate is 98.63%; obtaining the separated gallium nitrate solution, and calculating the total recovery rate to be 96.41%.
Example 2: method for extracting and separating gallium from aluminum-containing sulfuric acid leaching solution
The aluminum-containing sulfuric acid leaching solution mainly comprises the following components: ga 3+ 1.51g/L，Al 3+ 2.28g/L，Zn 2+ 10.22g/L，Cu 2+ 19.83g/L，Cd 2+ 4.29g/L，pH＝1.5。
Mixed extractants were prepared from 15% N1923, 10% TBP and 75% sulfonated kerosene by volume. And (3) carrying out 3-stage countercurrent extraction on the sulfuric acid leaching solution of the zinc replacement slag and the mixed extracting agent according to the ratio of O/A of 1 for 5min to obtain a gallium-containing load organic phase and a raffinate aqueous phase. Ga 3+ Extraction rate 93.81%, al 3+ The extraction rate is 30.77%, and other impurity ions are not extracted basically.
And (3) carrying out 2-stage cross-flow washing on the gallium-containing loaded organic phase by using 12mol/L hydrochloric acid according to a phase ratio (O/A) 1 3+ The ion is not basically washed, and the elution rate of other ions is 100 percent; pure gallium-loaded organic phase is obtained, 1mol/L sodium nitrate is used for carrying out 5-stage cross-flow back extraction according to a phase ratio (O/A) 1 3+ Stripping rate 98.73 percent; obtaining the separated gallium nitrate solution, and calculating the total recovery rate to be 92.62%.
Example 3: method for extracting and separating gallium from aluminum-containing sulfuric acid leaching solution
The aluminum-containing sulfuric acid leaching solution mainly comprises the following components: ga 3+ 1.51g/L，Al 3+ 2.28g/L，Zn 2+ 10.22g/L，Cu 2+ 19.83g/L，Cd 2+ 4.29g/L, pH =0.5. 20% N1923, 20% TBP and 60% sulfonated kerosene by volume were prepared as a mixed extractant. And (3) carrying out 2-stage countercurrent extraction on the zinc replacement slag sulfuric acid leaching solution and the mixed extracting agent according to the ratio of O/A to O/A of 3, and extracting for 10min to obtain a gallium-containing loaded organic phase and a raffinate water phase. Ga 3+ Extraction rate 98.93%, al 3+ The extraction rate is 39.78%, and other impurity ions are not extracted basically. The gallium-containing loaded organic phase was subjected to 1-stage cross-flow washing with 10mol/L hydrochloric acid in accordance with a phase ratio (O/A) 1 3+ The ion is not washed basically, and the elution rate of other ions is 100 percent; obtaining a pure gallium-loaded organic phase, carrying out 3-stage cross-flow back extraction by using 1mol/L sodium nitrate according to a phase ratio (O/A) 1 3+ The back extraction rate is 96.13%; obtaining the separated gallium nitrate solution, and calculating the total recovery rate to be 95.10%.
Example 4: method for extracting and separating gallium from aluminum-containing sulfuric acid leaching solution
The aluminum-containing sulfuric acid leaching solution comprises the following components: ga 3+ 1.87g/L，Al 3+ 2.90g/L，Zn 2+ 19.27g/L，Cu 2+ 11.53g/L，Cd 2+ 1.67g/L，pH＝0.5。
30% N1923, 30% TBP and 40% sulfonated kerosene by volume to prepare a mixed extractant. And (3) carrying out 3-stage countercurrent extraction on the sulfuric acid leaching solution of the zinc replacement slag and the mixed extracting agent according to the ratio O/A of 2, and extracting for 10min to obtain a gallium-containing load organic phase and a raffinate water phase. Ga 3+ Extraction rate 98.57%, al 3+ The extraction rate is 38.61%, and other impurity ions are not extracted basically.
And (3) carrying out 3-stage cross-flow washing on the gallium-containing load organic phase by using 6mol/L hydrochloric acid according to a phase ratio (O/A) 1 3+ The ion is not washed basically, and the elution rate of other ions is 100 percent; obtaining pure gallium-loaded organic phase with 3mol/LSodium nitrate was subjected to 3-stage cross-flow back extraction according to a phase ratio (O/A) 1, back extraction for 10min 3+ The back extraction rate is 97.78%; obtaining the separated gallium nitrate solution, and calculating the total recovery rate to be 96.38%.
Comparative example 1
Reference example 1, the only differences are: the mixed extractant was selected without adding TBP, by volume, 10% N1923 and 90% sulfonated kerosene. Ga 3+ Extraction rate of 98.92% and Al content 3+ The extraction rate is 42.79%, and other ions are not extracted basically. Ga 3 + 、Al 3+ The elution rate is 100 percent, the pure gallium loaded organic phase can not be obtained by recovery, and Ga is calculated 3+ The overall recovery was 0%.
Comparative example 2
Reference example 1, the only difference is that: when the mixed extractant is selected, N1923 is not added, and the content of the sulfonated kerosene is 10% or TBP +90% according to the volume ratio. Ga 3+ Other impurities are not extracted, pure gallium loaded organic phase can not be obtained by recovery, and Ga is calculated 3+ The overall recovery was 0%.
Comparative example 3
Reference example 1, the only differences are: when the mixed extractant is selected, N1923 and TBP are not added, and sulfonated kerosene is 100% in volume ratio. Ga 3+ Other impurities are not extracted, pure gallium loaded organic phase can not be obtained by recovery, and Ga is calculated 3+ The overall recovery was 0%.
Comparative example 4
Reference example 2, the only differences are: the mixed extractant selected using the analogous extractant N235 instead of N1923, by volume, 15% N235, 10% TBP and 75% sulfonated kerosene. Ga 3+ Other impurities are not extracted, pure gallium loaded organic phase can not be obtained by recovery, and Ga is calculated 3+ The overall recovery was 0%.
Comparative example 5
Reference example 3, the only difference is that: the mixed extractant selected, replacing N1923 with the analogous extractant N263, 20% N263 and 20% TBP and 60% sulfonated kerosene, by volume. Ga 3+ Other impurities are not extracted, pure gallium loaded organic phase can not be obtained by recovery, and Ga is calculated 3+ Total recoveryThe ratio was 0%.
Comparative example 6
Reference example 4, the only difference is that: the mixed extractant selected, replacing TBP with the similar extractant P350, 30% by volume, N1923 and 30% P350+40% sulfonated kerosene. Ga 3+ Extraction rate of 92.39% and Al 3+ The extraction rate was 28.53%, and other ions were not extracted substantially. Ga 3+ Elution Rate 42.87%, al 3+ The elution rate was 100%. Ga 3+ The back extraction rate is 0.53%, and Ga is calculated 3+ The total recovery rate is 0.28%.
Comparative example 7
Reference example 4 differs only in that: when the mixed extractant is selected, the homogeneous extractant N235 is used for replacing N1923, and the homogeneous extractant P350 is used for replacing TBP, and the percentage by volume of the sulfonated kerosene is 30% N235 and 30% by volume, namely P350+ 40%. Ga 3+ Other impurities are not extracted, pure gallium loaded organic phase can not be obtained by recovery, and Ga is calculated 3+ The overall recovery was 0%.
Comparative example 8
Reference example 4 differs only in that: mixing the extractants, using N263 instead of N1923, P350 instead of TBP, 30% N263 and 30% P350+40% sulfonated kerosene by volume ratio. Ga 3+ Other impurities are not extracted, pure gallium loaded organic phase can not be obtained by recovery, and Ga is calculated 3+ The overall recovery was 0%.
Comparative example 9
Reference example 4, the only difference is that: when the mixed extractant is selected, the same extractant N235 is used for replacing N1923, and the acidic phosphorus extractant P204 is used for replacing TBP, and the percentage by volume is 30 percent, namely N235 and 30 percent, P204+40 percent of sulfonated kerosene. Ga 3+ Extraction rate 68.15%, al 3+ Extraction rate 21.73%, zn 2+ 14.31％，Cu 2+ 8.14％、Cd 2+ Substantially without extraction. Ga 3+ The elution rate was 3.19%, and the elution rate of other ions was 100%. Ga 3+ The back extraction rate is 0%, and Ga is calculated 3+ The overall recovery was 0%.
By comparing the examples with the respective proportions, it can be seen that the extraction separation effect on gallium in the respective proportions is far inferior to that in the examples, and therefore, the adoption of the N1923-TBP-sulfonated kerosene mixed extractant for extracting and separating gallium in the aluminum-containing sulfuric acid system is not a simple extractant combination or the like conventional replacement, and has an unexpected synergistic and significant gain effect; and when the extraction mode, the stage number, the time and the like are in the range required by the application, the extraction rate and the separation recovery rate of the gallium can be further ensured.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for extracting and separating gallium from an aluminum-containing sulfuric acid leaching solution is characterized by comprising the following steps:
1) Extracting an aluminum-containing sulfuric acid leaching solution by adopting a secondary carbon primary amine extractant-tributyl phosphate-sulfonated kerosene mixed extractant to obtain a gallium-containing load organic phase and a raffinate aqueous phase; wherein the aluminum-containing sulfuric acid leaching solution is derived from sulfuric acid leaching solution of byproduct slag of lead-zinc ore wet process and contains Ga 3+ 1～2g/L、Al 3+ 1～3g/L、Zn 2+ 10～20g/L、Cu 2+ 10-20 g/L and Cd 2+ 1-5 g/L; the secondary carbon primary amine extractant-tributyl phosphate-sulfonated kerosene mixed extractant is prepared from a secondary carbon primary amine extractant, tributyl phosphate and sulfonated kerosene with the volume ratio of 1-3;
2) Washing the gallium-containing loaded organic phase obtained in the step 1) by hydrochloric acid to obtain a pure gallium-loaded organic phase;
3) And (3) carrying out back extraction on the pure gallium loaded organic phase obtained in the step 2) by using sodium nitrate to obtain a separated gallium nitrate solution.
2. The method of claim 1, wherein the aluminous sulfuric acid leach liquor has a pH = 0.5-1.5.
3. The method of claim 1, wherein the step 1) extraction is counter-current extraction; the extraction ratio of O/A is (1-3) to 1; the extraction stage number is 1-3; the extraction time is 5-10 min.
4. The process according to claim 1, wherein step 2) comprises washing the gallium-containing loaded organic phase with hydrochloric acid in a cross-flow.
5. The method of claim 4, wherein the concentration of hydrochloric acid is 6 to 12mol/L, and the washing phase ratio O/A is 1 (1 to 3).
6. The process of claim 4, wherein the number of stages of the cross-flow washing is 1 to 3 stages.
7. The method of claim 4, wherein the cross-flow washing time is 5 to 10min.
8. The process according to claim 1, wherein step 3) comprises back-extracting the pure gallium-loaded organic phase with sodium nitrate cross-current.
9. The method of claim 8, wherein the concentration of sodium nitrate is 1 to 3mol/L and the stripping ratio O/A is 1 (1 to 3).
10. The method of claim 8, wherein the number of stages of the cross-flow back extraction is 3 to 5; the cross-flow back extraction time is 5-10 min.
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| CN117965914A (en) * | 2024-03-28 | 2024-05-03 | 赣南科技学院 | Method for extracting and separating gallium and germanium from zinc replacement slag sulfuric acid leaching solution |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117947274A (en) * | 2024-03-26 | 2024-04-30 | 赣南科技学院 | Method for separating metal elements in sulfuric acid leaching solution of waste ternary lithium battery by full extraction |
| CN117947274B (en) * | 2024-03-26 | 2024-06-25 | 赣南科技学院 | Method for separating metal elements in sulfuric acid leaching solution of waste ternary lithium battery by full extraction |
| CN117965914A (en) * | 2024-03-28 | 2024-05-03 | 赣南科技学院 | Method for extracting and separating gallium and germanium from zinc replacement slag sulfuric acid leaching solution |
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