CN103436717A - Method for enriching gallium and comprehensively utilizing potassium and aluminum from alunite - Google Patents
Method for enriching gallium and comprehensively utilizing potassium and aluminum from alunite Download PDFInfo
- Publication number
- CN103436717A CN103436717A CN2013103886999A CN201310388699A CN103436717A CN 103436717 A CN103436717 A CN 103436717A CN 2013103886999 A CN2013103886999 A CN 2013103886999A CN 201310388699 A CN201310388699 A CN 201310388699A CN 103436717 A CN103436717 A CN 103436717A
- Authority
- CN
- China
- Prior art keywords
- gallium
- solid
- acid leaching
- solution
- liquid separation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
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
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to a method for enriching gallium and comprehensively utilizing potassium and aluminum from alunite. The method comprises the process steps of dewatering, roasting, and conveying the obtained dewatered and roasted clinker aggregate to an acid leaching system through a material conveying machine; carrying out primary acid leaching, and carrying out acid leaching on the dewatered and roasted clinker aggregate by using a sulphuric acid solution to simultaneously leach the potassium, the aluminum and the gallium; carrying out primary gallium enrichment, discontinuously adding primary acid leaching liquor, and controlling the pH of a solution to obtain a primary neutralization solution and gallium-enriched ores 1; carrying out secondary acid leaching, leaching the gallium-enriched ores 1 by using the sulphuric acid solution, and controlling the pH value of the solution so as to simultaneously leach the potassium, the aluminum and the gallium contained in the gallium-enriched ores 1; carrying out secondary gallium enrichment, discontinuously adding the dewatered and roasted clinker aggregate to neutralize secondary acid leaching liquor, and controlling the pH value of the solution to obtain a secondary neutralization solution and gallium-enriched ores 2; naturally cooling and crystallizing the primary and secondary neutralization solutions to obtain an alum product and an alum crystallizing mother solution; and carrying out multiple-effect evaporation and crystallization to obtain a solid aluminum sulfate product and an aluminum sulfate crystallizing mother solution. The method disclosed by the invention has the advantages of simple needed production line equipment, small investment, easiness in raw material sulfuric acid purchasing in the market, simplified process step, easiness in operation, low production cost, good product quality, high gallium enrichment ratio, high recovery rate, and the like and is suitable for chemical enterprises.
Description
Technical field
The present invention relates to a kind of method of enrichment gallium and potassium aluminium comprehensive utilization from alunite, be suitable for the chemical enterprise application.
Background technology
Alunite is a kind of moisture potassium aluminium sulfate class mineral, also contains a certain amount of gallium simultaneously.Gallium is the important member in dissipated metal family, is also the propping material of contemporary new and high technology, and gallium obtains applying more and more widely in fields such as national defence, band optical fiber communication, aerospace, electronic technology.In recent years, along with the raising of scientific and technical develop rapidly and people's lives and health level, also increasing to the demand of gallium.But the recovery of gallium concentrates on the part of enrichment in the base metal metallurgical process, by current state of the art, but the quantity of economic recovery is only the small part of reserves.Therefore, the rate of recovery of reserved resource and raising resource is the gallium main task reclaimed.
Since the thirties, Chinese scholars has been done many research work to alunite comprehensive utilizating research aspect, also obtained the achievement of many stages, the reduction heat solution has been proposed in succession, solvay soda process, card human relations nit acid system, the U.G method, decomposition for ammonium sulfate, tens kinds of technical process such as thermolysis, but these techniques nearly all only relate to potassium in alunite, the comprehensive reutilization of aluminium, the ubiquity product is single, the shortcomings such as added value of product is low, and only there is the reduction heat solution to be able to industrial applications in USSR (Union of Soviet Socialist Republics), and the report that reclaims gallium from alunite is few, just also there are many deficiencies in only a small amount of report at present, as Chinese patent CN103103339A document discloses the method for selective recovery alum and gallium " a kind of from the alunite concentrate ", the method is that the calcining after roasting first leaches aluminium under low sulfuric acid concentration by the alunite concentrate, the metal ions such as potassium, after solid-liquid separation again the filtrate crystallization become alum and crystalline mother solution, crystalline mother solution is returned to low Ore Leaching, leached mud leaches the rare metal gallium after sizing mixing under high sulfuric acid concentration, finally adopt ion-exchange or extraction process to reclaim the gallium in high acid solution, solution crystallisation by cooling alum after the recovery gallium, exploring the method through scientific research exists following not enough: the one, and in the alum crystallisation process, the potassium al mole ratio does not mate, in solution, aluminium is excessive, can't realize the high-efficiency comprehensive utilization of aluminium, the 2nd, low Acid Leaching-out Ratio section is subject to the impact of alunite ore grade and other foreign matter contents very large, condition harshness, performance difficulty.And for example Chinese patent CN102517461A document discloses a kind of " reclaiming the method for gallium from alunite ", the method is at first to the alunite roasting of being dewatered, next is to the acidleach of roasting grog solid-liquid separation, to the pickling liquor crystallization again, obtain alum and contain the gallium crystalline mother solution, finally to containing the gallium crystalline mother solution, returning to the acidleach of roasting grog solid-liquid separation, so circulation, in mother liquor to be crystallized, gallium content therefrom extracts gallium again and obtains the gallium product after reaching 100～300mg/L, exploring the method through scientific research exists following not enough: the one, and in the alum crystallisation process, the potassium al mole ratio does not still mate, in solution, aluminium is excessive, can't realize the high-efficiency comprehensive utilization of aluminium, the 2nd, in the alum crystallisation process, approximately there is 15%～55% gallium to be taken away by alum, cause gallium to lose in a large number, its rate of loss increases with gallium Enrichment in solution, causes the rate of recovery of final gallium extremely low.
China's alunite is quite abundant, and reserves occupy third place in the world, has found out that ore reserves is more than 300,000,000 t.Form the Wenzhou District of Zhejiang Province chemical general factory of scale production, be the enterprise of current second-biggest-in-the-world comprehensive utilization alunite, but this factory's production technique exist that product is single, added value is low, complete processing is backward equally and association is not recycled etc. to shortcoming in the gallium of this resource.
For this reason, seek that a kind of processing cost is low, strong adaptability, the valuable element rate of recovery be high, can the gallium of efficiently concentrating association in alunite, the method that can fully utilize again potassium, aluminium and sulphur etc. in alunite just seems particularly urgent.
Summary of the invention
Task of the present invention is that the product for existing processing alumstone ore is single, added value is low, complete processing is backwards and association do not recycled etc. to problem in the gallium in this ore deposit, proposed a kind of method that enrichment gallium and potassium aluminium fully utilize from alunite.
Task of the present invention completes by the following technical programs:
A kind of method of enrichment gallium and potassium aluminium comprehensive utilization from alunite, realize by following processing steps in sequence and condition:
The first step dehydration roasting: the roasting of being dewatered under temperature is 550 ℃～650 ℃, roasting time 60min～180min condition, gained dehydration roasting grog send the Ore Leaching system through the thermal material transfer roller;
1 Ore Leaching of second step: be that 70 ℃～95 ℃, time 30min～60min, liquid-solid ratio L/S are to adopt sulphuric acid soln acidleach dehydration roasting grog under 5～7 conditions in temperature, the pH that controls solution is 0.8～1.1, the potassium, the aluminium plus gallium that make to dewater in the roasting grog are leached simultaneously, after question response finishes, solid-liquid separation obtains 1 acid leaching liquor and 1 acid leaching slag, and 1 acid leaching slag is discharged;
The rich gallium of the 3rd step 1 time: be 70 ℃～95 ℃ in temperature, under time 90min～150min condition, be interrupted and add acid leaching liquor 1 time, controlling pH value of solution is 3.05～3.30, and after reaction finishes, solid-liquid separation obtains 1 neutralizer and rich gallium ore deposit 1;
The 4th step 2 times Ore Leaching: be that 70 ℃～95 ℃, time 30min～60min, liquid-solid ratio L/S are to adopt sulphuric acid soln to leach the rich gallium ore deposit 1 of the 3rd step gained under 3～5 conditions in temperature, and the pH that controls solution in whole process is 0.6～0.9, potassium, aluminium plus gallium in rich gallium ore deposit 1 are leached simultaneously, after question response finishes, solid-liquid separation obtains 2 acid leaching liquors and 2 acid leaching slags, and 2 acid leaching slags are discharged;
The rich gallium of the 5th step 2 times: at 70 ℃～95 ℃, under time 90min～150min condition, be interrupted in the dehydration roasting grog that adds the first step gained and 2 acid leaching liquors, and to control pH value of solution in the reaction whole process be 3.05～3.30, after question response finishes, solid-liquid separation obtains 2 neutralizers and rich gallium ore deposit 2;
The 6th step natural cooling crystallization: 1 neutralizer, 2 neutralizers and n neutralizer are merged, then carry out natural cooling crystallization, solid-liquid separation obtains alum product and alum crystalline mother solution;
The 7th step multiple-effect evaporation crystallization: send Multi-effect evaporation crystallizer to carry out evaporative crystallization the 7th step gained alum crystalline mother solution, solid-liquid separation obtains solid sulphuric acid aluminium product and Tai-Ace S 150 crystalline mother solution.
Per-cent described in specification sheets all is weight percentage.
Advantage of the present invention:
1. required apparatus for production line is simple, invests littlely, and raw material sulphuric acid market is easily purchased.
2. processing step is brief, easily operation, and production cost is low.
3. good product quality, crystallization alum quality product reaches China's food grade alum quality standard, and crystalline solid Tai-Ace S 150 target level of product quality reaches China's industrial aluminum sulphate III type solid masses standard.
4. the concentration ratio of gallium is large, the rate of recovery is high.
The accompanying drawing explanation
Fig. 1 is a kind of method process flow sheet that enrichment gallium and potassium aluminium fully utilize from alunite proposed according to the present invention.
Below in conjunction with accompanying drawing, explanation is described in further detail, not as limiting the scope of the present invention.
Embodiment
As shown in Figure 1, the method for a kind of enrichment gallium and potassium aluminium comprehensive utilization from alunite of the present invention, processing step and condition are carried out in the following order successively:
The first step dehydration roasting: the roasting of being dewatered under temperature is 550 ℃～650 ℃, roasting time 60min～180min condition, should guarantee that the crystal water in alunite is removed more fully, guarantee that again the sulphur cash in alunite does not decompose as far as possible, gained dehydration roasting grog is delivered to the Ore Leaching system through good operational environment, level of automation is high, thermosteresis is little hot scraper plate thermal material transfer roller and is processed;
1 Ore Leaching of second step: be that 70 ℃～95 ℃, time 30min～60min, liquid-solid ratio L/S are to adopt sulphuric acid soln to leach the dehydration roasting grog of the first step gained under 5～7 conditions in temperature, and the pH that controls solution in the reaction whole process is 0.8～1.1, potassium, aluminium plus gallium in the first step dehydration roasting gained grog are leached simultaneously, and after question response finishes, solid-liquid separation obtains 1 acid leaching liquor and 1 acid leaching slag;
The rich gallium of the 3rd step 1 time: be 70 ℃～95 ℃ in temperature, under time 90min～150min condition, be interrupted in the dehydration roasting grog that adds the first step gained and 1 acid leaching liquor, and the major cause of controlling pH value of solution=3.05～3.30(gallium enrichment energy enrichment in the reaction whole process is: under these conditions, add grog neutralizing acid leach liquor (pH=0.8～1.1) to pH=3.05～3.30, this just both guaranteed gallium in acid leaching liquor with alkali formula gallium sulfate alum salt or other insoluble substances precipitate enter in and in slag, guarantee that again the gallium in neutralization grog used is not leached, and in N-process in grog most potassium and aluminium by leaching, entered in neutralizer, in and the slag rate greatly reduce, many times of enrichments of gallium have been realized), after reaction finishes, solid-liquid separation obtains 1 neutralizer and rich gallium ore deposit 1,
The 4th step 2 times Ore Leaching: be that 70 ℃～95 ℃, time 30min～60min, liquid-solid ratio L/S are to adopt sulphuric acid soln to leach the rich gallium ore deposit 1 of the 3rd step gained under 3～5 conditions in temperature, and the pH that controls solution in whole process is 0.6～0.9, potassium, aluminium plus gallium in rich gallium ore deposit 1 are leached simultaneously, and after question response finishes, solid-liquid separation obtains 2 acid leaching liquors and 2 acid leaching slags;
The rich gallium of the 5th step 2 times: be 70 ℃～95 ℃ in temperature, under time 90min～150min condition, be interrupted in the dehydration roasting grog that adds the first step gained and 2 acid leaching liquors, and to control pH value of solution in the reaction whole process be 3.05～3.30, after question response finishes, solid-liquid separation obtains 2 neutralizers and rich gallium ore deposit 2;
The 6th step natural cooling crystallization: 1 neutralizer, 2 neutralizers and n neutralizer are merged, then carry out natural cooling crystallization, solid-liquid separation obtains alum product and alum crystalline mother solution;
The 7th step multiple-effect evaporation crystallization: send Multi-effect evaporation crystallizer to carry out evaporative crystallization the 7th step gained alum crystalline mother solution, solid-liquid separation obtains solid sulphuric acid aluminium product and Tai-Ace S 150 crystalline mother solution.
Method of the present invention further comprises:
Rich gallium ore deposit 2 after 2 rich gallium solid-liquid separation of described the 5th step is carried out to n Ore Leaching and n rich gallium (n ﹥ 2) again: adopt the condition consistent with the 4th step to process rich gallium ore deposit n-1, solid-liquid separation obtains n acid leaching liquor and n acid leaching slag, n time acid leaching slag is discharged, the dehydration roasting grog that adds the first step gained in interruption is in the condition consistent with the 5th step and n acid leaching liquor, after question response finishes, solid-liquid separation obtains rich gallium ore deposit n and n neutralizer, n time neutralizer returns to the 6th step natural cooling crystallization, obtain alum and alum crystalline mother solution, again the alum crystalline mother solution is delivered to the 7th step multiple-effect evaporation crystallization, obtain Tai-Ace S 150 and Tai-Ace S 150 crystalline mother solution after solid-liquid separation.
The Tai-Ace S 150 crystalline mother solution that described the 7th step multiple-effect evaporation crystallization solid-liquid separation is gone out returns to the 7th step again and carries out the multiple-effect evaporation crystallization, circulation output Tai-Ace S 150 again.
Below in conjunction with embodiment, the inventive method and effect are done to further checking elaboration, the technical process that embodiment adopts is by carrying out shown in Fig. 1.
Embodiment 1
The Zhejiang alunite raw ore of take is raw material, and the main valuable mineral of ore is alunite, and gangue mineral is mainly quartzy, calcedony, and other also has kaolin, sericite, feldspar etc., and its sample ore chemical analysis results is in Table 1.
Certain alunite raw ore chemical composition analysis result of table 1
The method of the comprehensive utilization of alunite potassium and aluminium and gallium efficiently concentrating comprises following processing step and condition successively:
The first step dehydration roasting: certain alunite raw ore is the roasting 150min that dewatered under 550 ℃ of conditions in temperature, the roasting grog that obtains dewatering, and dehydration roasting grog reusable heat scraper plate thermal material transfer roller send the Ore Leaching system to process;
1 Ore Leaching of second step: be that 90 ℃, time 60min, liquid-solid ratio L/S are to adopt valuable element potassium, the aluminium plus gallium of sulphuric acid soln in leaching the dehydration roasting grog of the first step gained under 5 conditions in temperature, and be 0.87 at the pH of reaction Whole Process Control solution, after question response finishes, solid-liquid separation obtains 1 acid leaching liquor and 1 acid leaching slag;
The rich gallium of the 3rd step 1 time: be under 90 ℃ of conditions in temperature, be interrupted in the grog that adds the first step dehydration roasting gained and 1 acid leaching liquor, reaction 90min, and to control pH value of solution in the reaction whole process be 3.27, after question response finishes, solid-liquid separation obtains 1 neutralizer and rich gallium ore deposit 1;
The 4th step 2 times Ore Leaching: be that 90 ℃, time 60min, liquid-solid ratio L/S are to adopt potassium, the aluminium plus gallium of sulphuric acid soln in leaching the rich gallium ore deposit 1 of the 3rd step gained under 4 conditions in temperature, and be 0.74 at the pH of reaction Whole Process Control solution, solid-liquid separation obtains 2 acid leaching liquors and 2 acid leaching slags;
The rich gallium of the 5th step 2 times: be under 90 ℃ of conditions in temperature, be interrupted in the grog add the first step dehydration roasting gained and 2 acid leaching liquors, reaction 150min, and to control pH value of solution in the reaction whole process be 3.24, solid-liquid separation obtains 2 neutralizers and rich gallium ore deposit 2;
The 6th step natural cooling crystallization: 1 neutralizer, 2 neutralizers are merged, then carry out natural cooling crystallization to 30 ℃, solid-liquid separation obtains product alum and alum crystalline mother solution;
The 7th step multiple-effect evaporation crystallization: send Multi-effect evaporation crystallizer to carry out evaporative crystallization the 6th step gained alum crystalline mother solution, solid-liquid separation obtains solid sulphuric acid aluminium product and Tai-Ace S 150 crystalline mother solution.Technical data and technical indicator are in Table 2.
Table 2 embodiment 1 technical data and technical indicator
Embodiment 2
The Fujian copper flotation tailings of take is raw material by flotation gained alunite concentrate again, and the alunite concentrate is mainly alunite, is secondly quartzy, dickite, and other also has kaolin, sericite, feldspar etc., and its sample ore chemical analysis results is in Table 3.
Table 3 alunite flotation concentrate chemical composition analysis result
The method of the comprehensive utilization of alunite potassium and aluminium and gallium efficiently concentrating comprises following processing steps in sequence and condition successively:
The first step dehydration roasting: certain alunite flotation concentrate is the roasting 120min that dewatered under 600 ℃ of conditions in temperature, the roasting grog that obtains dewatering, and dehydration roasting grog send the Ore Leaching system to process through hot scraper plate thermal material transfer roller again;
1 Ore Leaching of second step: potassium, aluminium plus gallium under 80 ℃ of temperature, time 120min, L/S=6 condition in the dehydration roasting grog of employing sulphuric acid soln leaching the first step gained, and be 0.91 at the pH of reaction Whole Process Control solution, after question response finishes, solid-liquid separation obtains 1 acid leaching liquor and 1 acid leaching slag;
The rich gallium of the 3rd step 1 time: under 80 ℃ of conditions, be interrupted in the grog add the first step dehydration roasting gained and 1 acid leaching liquor, reaction 120min, and to control pH value of solution in the reaction whole process be 3.20, solid-liquid separation obtains 1 neutralizer and rich gallium ore deposit 1;
The 4th step 2 times Ore Leaching: potassium, aluminium plus gallium under 80 ℃ of temperature, time 40min, L/S=5 condition in the rich gallium ore deposit 1 of employing sulphuric acid soln leaching the 3rd step gained, and be 0.83 at the pH of reaction Whole Process Control solution, solid-liquid separation obtains 2 acid leaching liquors and 2 acid leaching slags;
The rich gallium of the 5th step 2 times: under 80 ℃ of conditions, be interrupted in the grog add the first step dehydration roasting gained and 2 acid leaching liquors, reaction 120min, and to control pH value of solution in the reaction whole process be 3.15, solid-liquid separation obtains 2 neutralizers and rich gallium ore deposit 2;
The 6th step natural cooling crystallization: 1 neutralizer, 2 neutralizers are merged, then carry out natural cooling crystallization to 30 ℃, solid-liquid separation obtains product alum and alum crystalline mother solution;
The 7th step multiple-effect evaporation crystallization: send Multi-effect evaporation crystallizer to carry out evaporative crystallization the 6th step gained alum crystalline mother solution, solid-liquid separation obtains solid sulphuric acid aluminium product and Tai-Ace S 150 crystalline mother solution.Technical data and technical indicator are in Table 4.
Table 4 embodiment 2 technical datas and technical indicator
Also can further the rich gallium ore deposit 2 after 2 rich gallium solid-liquid separation of described the 5th step be carried out again to n Ore Leaching and n rich gallium (n ﹥ 2) to embodiment 1 and embodiment 2: adopt the condition consistent with the 4th step to process rich gallium ore deposit n-1, solid-liquid separation obtains n acid leaching liquor and n acid leaching slag, n time acid leaching slag is discharged, the dehydration roasting grog that adds the first step gained in interruption is in the condition consistent with the 5th step and n acid leaching liquor, after question response finishes, solid-liquid separation obtains rich gallium ore deposit n and n neutralizer, n time neutralizer returns to the 6th step natural cooling crystallization, obtain alum and alum crystalline mother solution, again the alum crystalline mother solution is delivered to the 7th step multiple-effect evaporation crystallization, obtain Tai-Ace S 150 and Tai-Ace S 150 crystalline mother solution after solid-liquid separation.
The Tai-Ace S 150 crystalline mother solution that described the 7th step multiple-effect evaporation crystallization solid-liquid separation is gone out returns to the 7th step again and carries out the multiple-effect evaporation crystallization, circulation output Tai-Ace S 150.
Claims (3)
1. the method for an enrichment gallium and potassium aluminium comprehensive utilization from alunite, processing step and condition are carried out in the following order successively:
The first step dehydration roasting: the roasting of being dewatered under temperature is 550 ℃～650 ℃, roasting time 60min～180min condition, gained dehydration roasting grog send the Ore Leaching system through the thermal material transfer roller;
1 Ore Leaching of second step: be that 70 ℃～95 ℃, time 30min～60min, liquid-solid ratio L/S are to adopt sulphuric acid soln acidleach dehydration roasting grog under 5～7 conditions in temperature, the pH that controls solution is 0.8～1.1, the potassium, the aluminium plus gallium that make to dewater in the roasting grog are leached simultaneously, after question response finishes, solid-liquid separation obtains 1 acid leaching liquor and 1 acid leaching slag, and 1 acid leaching slag is discharged;
The rich gallium of the 3rd step 1 time: be 70 ℃～95 ℃ in temperature, under time 90min～150min condition, be interrupted and add acid leaching liquor 1 time, controlling pH value of solution is 3.05～3.30, and after reaction finishes, solid-liquid separation obtains 1 neutralizer and rich gallium ore deposit 1;
The 4th step 2 times Ore Leaching: be that 70 ℃～95 ℃, time 30min～60min, liquid-solid ratio L/S are to adopt sulphuric acid soln to leach the rich gallium ore deposit 1 of the 3rd step gained under 3～5 conditions in temperature, and the pH that controls solution in whole process is 0.6～0.9, valuable element potassium, aluminium plus gallium in rich gallium ore deposit 1 are leached simultaneously, after question response finishes, solid-liquid separation obtains 2 acid leaching liquors and 2 acid leaching slags, and 2 acid leaching slags are discharged;
The rich gallium of the 5th step 2 times: at 70 ℃～95 ℃, under time 90min～150min condition, be interrupted in the dehydration roasting grog that adds the first step gained and 2 acid leaching liquors, and to control pH value of solution in the reaction whole process be 3.05～3.30, after question response finishes, solid-liquid separation obtains 2 neutralizers and rich gallium ore deposit 2;
The 6th step natural cooling crystallization: 1 neutralizer, 2 neutralizers and n neutralizer are merged, then carry out natural cooling crystallization, solid-liquid separation obtains alum product and alum crystalline mother solution;
The 7th step multiple-effect evaporation crystallization: send Multi-effect evaporation crystallizer to carry out evaporative crystallization the 7th step gained alum crystalline mother solution, solid-liquid separation obtains solid sulphuric acid aluminium product and Tai-Ace S 150 crystalline mother solution.
2. method according to claim 1, it is characterized in that rich gallium ore deposit 2 after 2 rich gallium solid-liquid separation of described the 5th step carries out n Ore Leaching and n rich gallium again: after adopting the condition consistent with the 4th step to process rich gallium ore deposit n-1, n acid leaching liquor and n acid leaching slag that solid-liquid separation obtains, add n the acid leaching liquor of the dehydration roasting grog of the first step gained in the condition neutralization consistent with the 5th step in interruption, after question response finishes, solid-liquid separation obtains rich gallium ore deposit n and n neutralizer, and n acid leaching slag discharged.
3. method according to claim 1 and 2, is characterized in that Tai-Ace S 150 crystalline mother solution that described the 7th step multiple-effect evaporation crystallization solid-liquid separation goes out returns to the 8th step and carries out the multiple-effect evaporation crystallization again.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310388699.9A CN103436717B (en) | 2013-08-30 | 2013-08-30 | Method for enriching gallium and comprehensively utilizing potassium and aluminum from alunite |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310388699.9A CN103436717B (en) | 2013-08-30 | 2013-08-30 | Method for enriching gallium and comprehensively utilizing potassium and aluminum from alunite |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103436717A true CN103436717A (en) | 2013-12-11 |
| CN103436717B CN103436717B (en) | 2014-10-08 |
Family
ID=49690430
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310388699.9A Active CN103436717B (en) | 2013-08-30 | 2013-08-30 | Method for enriching gallium and comprehensively utilizing potassium and aluminum from alunite |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103436717B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103787396A (en) * | 2014-01-27 | 2014-05-14 | 紫金矿业集团股份有限公司 | Method for preparing high-purity potassium alum and aluminum sulfate from alunite ore |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1519284A (en) * | 1977-03-04 | 1978-07-26 | Novosib Olovyan Kom | Method of producing indium |
| CN101058852A (en) * | 2007-05-30 | 2007-10-24 | 中南大学 | Multistage counter current acid leaching process containing nickel serpentine ore |
| CN102517461A (en) * | 2011-12-16 | 2012-06-27 | 紫金矿业集团股份有限公司 | Method for recycling gallium in alunite concentrate |
| CN103103339A (en) * | 2012-12-19 | 2013-05-15 | 紫金矿业集团股份有限公司 | Method for selectively recovering alum and gallium from alunite concentrate |
| CN103193213A (en) * | 2013-04-24 | 2013-07-10 | 胡雷 | Method for comprehensively utilizing low-grade phosphate ores |
-
2013
- 2013-08-30 CN CN201310388699.9A patent/CN103436717B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1519284A (en) * | 1977-03-04 | 1978-07-26 | Novosib Olovyan Kom | Method of producing indium |
| CN101058852A (en) * | 2007-05-30 | 2007-10-24 | 中南大学 | Multistage counter current acid leaching process containing nickel serpentine ore |
| CN102517461A (en) * | 2011-12-16 | 2012-06-27 | 紫金矿业集团股份有限公司 | Method for recycling gallium in alunite concentrate |
| CN103103339A (en) * | 2012-12-19 | 2013-05-15 | 紫金矿业集团股份有限公司 | Method for selectively recovering alum and gallium from alunite concentrate |
| CN103193213A (en) * | 2013-04-24 | 2013-07-10 | 胡雷 | Method for comprehensively utilizing low-grade phosphate ores |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103787396A (en) * | 2014-01-27 | 2014-05-14 | 紫金矿业集团股份有限公司 | Method for preparing high-purity potassium alum and aluminum sulfate from alunite ore |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103436717B (en) | 2014-10-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Rioyo et al. | Lithium extraction from spodumene by the traditional sulfuric acid process: A review | |
| CN101161596B (en) | A method for resource processing non-ferro metals processing wastewater containing ammonia and sulfate radical | |
| CN101643243B (en) | Method for recycling copper, nickel, chromium, zinc and iron from plating sludge | |
| CN103103339B (en) | Method for selectively recovering alum and gallium from alunite concentrate | |
| CN101586185B (en) | Method for separating and recycling arsenic and iron from biological oxidation solution of sulfide ore | |
| CN102808087B (en) | Method for extracting zinc, potassium and sodium by using secondary dust of rotary hearth furnace | |
| CN101760613B (en) | Method for leaching zinc-containing ores | |
| CN114105171A (en) | Method for recycling and comprehensively utilizing lepidolite and lithium hydroxide prepared by method | |
| CN101058852A (en) | Multistage counter current acid leaching process containing nickel serpentine ore | |
| CN114751434B (en) | Comprehensive recycling method of deposition type lithium resources | |
| CN103073061A (en) | Method for extracting tungsten and molybdenum in high molybdenum scheelite | |
| CN102515220A (en) | Method for extracting alumina and gallium oxide from pulverized fuel ash to prepare aluminum oxide nanometer and polymeric ferric silicate sulfate | |
| CN104261433A (en) | Method for producing potassium sulfate from potassium/chlorine-ion-containing solid waste | |
| CN103589872A (en) | Method for recovering titanium from red mud slag | |
| CN103422119B (en) | A kind of method of utilizing copper-contained sludge to produce tough cathode | |
| CN102517461A (en) | Method for recycling gallium in alunite concentrate | |
| CN105776254A (en) | Technology for preparing lithium carbonate by means of recycling of slag obtained in purifying process of lepidolite | |
| CN104131169B (en) | Flyash acidleach synthetical recovery vanadium, the method for potassium | |
| CN101760614B (en) | Leaching method of nickel-containing ore | |
| CN109022806A (en) | A method of utilizing the vanadium liquid removal of impurities clay standby vanadic anhydride of vanadium | |
| CN108383140A (en) | A kind of clearer production technology and method of lithium sulfate | |
| CN107879929A (en) | A kind of method of comprehensive utilization of rare earth oxalate precipitate mother liquor | |
| CN103787396A (en) | Method for preparing high-purity potassium alum and aluminum sulfate from alunite ore | |
| CN108285975B (en) | A kind of method for extracting lithium from lepidolite by using PVC pyrolysis | |
| CN103436717B (en) | Method for enriching gallium and comprehensively utilizing potassium and aluminum from alunite |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |