CN104131169A - Technological method for comprehensively recovering vanadium and potassium through acid leaching of pulverized fuel ash - Google Patents
Technological method for comprehensively recovering vanadium and potassium through acid leaching of pulverized fuel ash Download PDFInfo
- Publication number
- CN104131169A CN104131169A CN201410386426.5A CN201410386426A CN104131169A CN 104131169 A CN104131169 A CN 104131169A CN 201410386426 A CN201410386426 A CN 201410386426A CN 104131169 A CN104131169 A CN 104131169A
- Authority
- CN
- China
- Prior art keywords
- crystallization
- flyash
- vanadium
- leaching
- extraction
- 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
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)
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to a technological method for comprehensively recovering vanadium and potassium through acid leaching of pulverized fuel ash. The technological method comprises the following steps: (1) leaching-flying ash neutralization operation; (2) aluminum potassium sulfate crystallization operation; (3) lime neutralization operation; (4) reduction operation; (5) extraction-reextraction operation; (6) crystallization-vanadium precipitation operation; and (7) bichromate calcination operation. Potassium can be recovered by crystallization through using leached supernate, and partial impurity aluminum can be effectively utilized; ammonium alum can be prepared from return water through crystallization, thus further recovering impurity aluminum and also providing a guarantee for quality of finally produced up-to-standard refined vanadium; an extraction raffinate returns to the leaching operation after being treated, no waste water is emitted, and simultaneously the recovery rate of potassium can also be improved. The method is low in running cost, capable of guaranteeing the smoothness of the whole vanadium extraction technology, and less in environmental pollution.
Description
Technical field
The invention belongs to hydrometallurgy field, be specifically related to comprehensively reclaim containing the generating of vanadium type stone coal combustion, flyash acidleach the method for vanadium, potassium technique.
Background technology
Extracting vanadium from stone coal is an importance of bone coal comprehensive utilization of resources, correlative study and the production of China's extracting vanadium from stone coal since the sixties, extracting vanadium from stone coal state of the art has obtained very large lifting, but in process for extracting vanadium, exists the problems such as vanadium total yield is low, reagent consumption is large, cost is high, easy generation pollution still more outstanding; And extracting vanadium from stone coal theoretical investigation is less, and research method is single, especially weaker for the correlation theory research of roasting process, leaching process, this has seriously restricted the development of vanadium extraction technology.
Bone coal resource is very abundant in Ankang Prefecture, Shaanxi Province, compares with domestic similar resource, and its feature shows as: 1. calorific value is high, is used for the thermo-efficiency of coal fired power generation high; 2. burned-coal fly ash vanadium, potassium content are high, can have valency to extract this element; 3. the waste residue after extracting also can partly be used as the industries such as building materials.4. the processing technology routine of whole project meets " resources conservation is strategy preferentially; strengthen Mineral resources saving and comprehensive utilization; raising resources development and utilization efficiency and level " spirit that " 12 " planning > > was saved and fully utilized to national < < Mineral resources, and main project field category.
The whole nation utilizes bone coal type navajoite to refine the producer of Vanadium Pentoxide in FLAKES at present, and its technological process of production is that raw ore is directly smelted, raw ore Vanadium Pentoxide in FLAKES grade 0.9-1%, smelting recovery is in 60% left and right, and the rate of recovery is low, and the wasting of resources is larger, the material consuming is many, and cost is higher.If bone coal type navajoite is carried out to high Ore Leaching, the Vanadium Pentoxide in FLAKES rate of recovery is brought up to more than 80%, there will be again foreign ion and the enrichment in leach liquor of association Hubeiwan, further removal of impurities and comprehensively reclaim the series of problems such as Hubeiwan.
Summary of the invention
The present invention is directed in flyash vanadium extraction technique the series of problems must high Ore Leaching bringing, a kind of method that provides flyash acidleach comprehensively to reclaim vanadium, potassium technique, it makes technique smooth, reclaims other valuable element potassium simultaneously.
Technical solution of the present invention is: the method for vanadium, potassium technique is comprehensively reclaimed in flyash acidleach, comprises the following steps:
(1) in leaching-flyash and operation
Sulfuric acid and the direct acidleach of leaching agent Calcium Fluoride (Fluorspan) for flyash, sulfuric acid consumption is and flyash quality per-cent 30%～50%, and leaching agent Calcium Fluoride (Fluorspan) consumption is with flyash quality per-cent 3.5～5%, extraction time 7～12h, 90 ± 5 ℃ of extraction temperatures, leaches the ratio 2.5～3:1 of liquid volume and solid weight; Leach operation and complete and filters solid-liquid separation, leach supernatant liquor and adopt flyash neutralization, its consumption is 30～60% of acidleach flyash consumption, 50～60 ℃ of flyash neutral temperatures, in and time 3～4h; Leached mud is carried out to adverse current pulping and washing four times, and each leaching requirement is identical with leaching operation liquid volume, and the 4th time washing water are lime and wash water preparation, and each wash water adverse current is returned, and soaks slag filtration and stores up;
(2) potassium aluminium sulfate crystallization operation
In flyash, with supernatant liquor stirred crystallization, obtain Potassium aluminum sulfate dodecahydrate crystallization, 5～10 ℃ of Tcs;
(3) in lime and operation
Under potassium aluminium sulfate crystallization tail washings normal temperature, carry out lime neutralization, pH=1.8 ± 0.2, merges in lime and enters restore job with supernatant liquor and a wash water; In and slag muck deposit;
(4) restore job
In lime, add iron reduction time 1.5～2h with supernatant liquor, iron filings add-on is V in reducing solution
2o
55.5～6 times of amount of metal, 38～42 ℃ of temperature ±, current potential 305～315mv left and right, adds polyacrylamide flocculation agent consumption 20～30g/t-flyash, sedimentation standing 2～3h, and solid-liquid separation, reduction supernatant liquor is as extraction stoste, and reducing slag is stored up;
(5) extraction-reextraction operation
Neutralizer extraction adopts 7 stage countercurrent extractions, 8 stage countercurrent back extractions, 3 stage countercurrent regeneration, 1 stage countercurrent washing, organic phase forms 12.5%2-ethylhexyl phosphoric acid+5% tributyl phosphate+82.5% sulfonated kerosene, the sulphuric acid soln that reverse-extraction agent is 1.5mol, the sulphuric acid soln that regenerator is 3mol; The wastewater treatment of raffinate is to obtain lime mud and reuse water with lime neutralization, and reuse water returns to leaching operation, and after back extraction, lean organic phase is regenerated and returned in extraction operation through organic phase;
(6) crystallization-precipitation operation
Under strip liquor normal temperature, add the crystallization of ammoniacal liquor adjust pH to 2.0～2.2, crystallization time 4～5h, crystallization tschermigite, solid-liquid separation post crystallization tail washings adds sodium chlorate and is oxidizing to solution potential 1050～1100mV, 60 ± 5 ℃ of oxidizing temperatures, oxidization time 1～2h, add ammoniacal liquor to 2.2～2.5 precipitations of pH value, 92～95 ℃ of precipitation temperature, precipitation time 2～4h, obtains red vanadium;
(7) red vanadium calcining operation
The calcining furnace that enters after red vanadium is dried is calcined 2～3h at 530～560 ℃, output essence vanadium product.
Described flyash is that low heat value 3500 kilocalories are below containing the flying dust after vanadium type stone coal mine or the burning of the following bone coal type of low heat value 2000 kilocalorie navajoite.
Advantage of the present invention and positively effect are: the present invention uses and leaches supernatant liquor crystallization recovery potassium, effectively utilizes partial impurities aluminium; Crystalline tschermigite from turn one's coat, except further recycling impurity aluminum, is also the guarantee of the qualified smart vanadium quality of final output; Raffinate is treated returns to leaching operation, outside non-wastewater discharge, has also improved the rate of recovery of potassium simultaneously.Adopt after present method:
(1) in the situation that sulfuric acid consumption is constant, add appropriate leaching agent amount, improve V
2o
5leaching yield; Leaching supernatant liquor is adopted flyash neutralization reduces lime consumption amount greatly.
(2) from flyash neutralizer extract Potassium aluminum sulfate dodecahydrate, the byproduct such as extraction ten sulfate dihydrate aluminium ammoniums from turn one's coat, this set has not only been guaranteed the unimpeded of whole technique, main vanadium product qualified, also obtains byproduct in this link, has improved the profit margin of product.
(3) crystallization-precipitation operation can guarantee the smart vanadium product that output is qualified.
(4) technological process non-wastewater discharge.Raffinate purifying regeneration returns vanadium extraction index is not exerted an influence, and also can improve the rate of recovery of potassium.
(5) precipitation tail water neutralization, in and slag muck deposit, neutral water can be recycled; The chlorine of precipitation oxidation, leaching evolving gas can be up to standard through alkali liquor absorption.Environmental pollution is very little.
Accompanying drawing explanation
Accompanying drawing is process flow sheet of the present invention.
Embodiment
Following examples are intended to further illustrate the present invention, and unrestricted the present invention.
Embodiment:
Adopt somewhere, present method Shaanxi flyash.This ore deposit essential mineral is quartzy, clay mineral, V
2o
5content 0.92%.Described flyash is that low heat value 3500 kilocalories are below containing the flying dust after vanadium type stone coal mine or the burning of the following bone coal type of low heat value 2000 kilocalorie navajoite.
(1) in leaching-flying dust and operation
Add the sulfuric acid of flyash 40% and 3.50% leaching agent Calcium Fluoride (Fluorspan), liquid-solid ratio (leaching the ratio of liquid volume and solid weight) 2.5:1, at 90 ℃, Leaching reaction 7h.Leach operation and complete and carries out solid-liquid separation, leach supernatant liquor and adopt flyash neutralization, its consumption is for leaching 55% of flyash consumption, 50 ℃ of flyash neutral temperatures, in and time 4h.Solid-liquid separation is unobstructed.Neutralizer is containing V
2o
5content 5.5g/L left and right.V
2o
5leaching yield is 82.90%, K
2o leaching yield 51.30%.
Leached mud carries out adverse current pulping and washing four times, and each leaching requirement is identical with leaching operation liquid volume, and the 4th washing is liming, and wash water adverse current is returned, and soaks slag muck to deposit; With raffinate reuse water, washing and add lime for the 4th time is neutralized to pH and is greater than 5.V in leached mud
2o
5containing 0.15%, slag productive rate is 102%.
(2) potassium aluminium sulfate crystallization operation
Leach supernatant liquor and add flyash neutralization, its consumption, for leaching 30-60% of flyash consumption, with supernatant liquor stirred crystallization, obtains Potassium aluminum sulfate dodecahydrate crystallization, 5-10 ℃ of Tcs in flyash.In flying dust, carrying out potassium aluminium sulfate crystallization with supernatant liquor is to ensure the unimpeded prerequisite of whole process for extracting vanadium, 5-10 ℃ of Tcs, and in crystalline product, the potassium oxide rate of recovery accounts in flying dust and the more than 45% of rear liquid amount of metal.Product Potassium aluminum sulfate dodecahydrate meets GB.
(3) in lime and operation
Under potassium aluminium sulfate crystallization tail washings normal temperature, carry out lime neutralization, pH=1.8 ± 0.2.Merge in lime and enter lower step operation with supernatant liquor and a wash water.In lime and operation vanadium recovery is 97.09%, slag productive rate 4.7%.In lime N-process, must strictly control pH value of solution < 2, otherwise V
2o
5loss fast rise.
(4) restore job
With about 2h of machining iron reduction time, iron filings add-on is V in reducing solution
2o
56 times of amount of metal, 40 ℃ of temperature ±, current potential 310mv left and right, adds flocculating agent A L9020, flocculation agent consumption 20-30g/t-flyash, sedimentation standing 2-3h.Adopt a minute bucket solid-liquid separation, reduction supernatant liquor is as extraction stoste, and reducing slag is stored up.Restore job vanadium recovery is 99.65%.(5) extraction-reextraction operation
Extraction adopts 7 stage countercurrent extractions, 8 stage countercurrent back extractions, 3 stage countercurrent regeneration, 1 stage countercurrent washing.Organic phase forms 12.5% (2-ethylhexyl phosphoric acid)+5% (tributyl phosphate)+82.5% (sulfonated kerosene), reverse-extraction agent is the sulphuric acid soln of 1.5mol, regenerator is the sulphuric acid soln of 3mol, raffinate wastewater treatment is to obtain lime mud and reuse water with lime neutralization, reuse water returns to leaching operation, and after back extraction, lean organic phase is regenerated and returned in extraction operation through organic phase; Extract reextraction output product for turning one's coat, its V
2o
5content 40g/l left and right, total iron content is 0.30g/l left and right.Expanding test extraction and stripping rate are 97.21%.
(6) crystallization-precipitation operation
Under strip liquor normal temperature, add the crystallization of ammoniacal liquor adjust pH to 2.0, crystallization time 4h, crystallization tschermigite, after solid-liquid separation, crystallization tail washings adds sodium chlorate and is oxidizing to solution potential 1050-1100mV, 60 ℃ of oxidizing temperatures, oxidization time 1h, add ammoniacal liquor to 2.5 precipitations of pH value, 93 ℃ of precipitation temperature, precipitation time 2h; Obtain red vanadium, crystallization wash water (0.5 times of amount of turning one's coat) returns to configuration reverse-extraction agent.Crystallization tschermigite in crystallization-precipitation process, crystallisation process V
2o
5the rate of recovery 99.44%, precipitation rate 98.34%.Crystallization-precipitation operation V
2o
5the rate of recovery 97.76%.(7) red vanadium calcining operation
Red vanadium after oven dry enters calcining furnace and calcine 3.0h at 530～560 ℃, output product V
2o
5grade is 98.13%, and quality has reached GB1895-2004 standard, and red vanadium calcining output ammonia-contaminated gas, absorbs with precipitation second wash water+tri-time washing water.
From raw material powder coal ash to smart vanadium product, V
2o
5total yield is 76.52%, and the total yield of potassium oxide is more than 39.57%.
The feature that technique of the present invention embodies:
While 1, leaching, sulfuric acid concentration and leaching agent are to guarantee V
2o
5the leaching yield most important condition.
2, use the scheme of lime neutralization for the general acid leaching process of coal ash instead instead, not only effectively reduce lime consumption amount, also avoided the loss of vanadium.
3, raffinate purifying regeneration water is returned to extracting stage, not only water obtains recycle, and has improved the total yield of potassium.
4, from flying dust neutralizer extract potassium aluminium sulfate, from turn one's coat the byproduct such as extraction tschermigite, the unimpeded of whole technique guaranteed in this technique setting, the finished product qualified.In this link, obtain byproduct, reduced production cost, improved to greatest extent the profit margin of byproduct.
5, waste water: more than 90% water is recycled, 10% the treated meet the requirement of environmental protection of waste water; Waste water is without discharge.
6, waste residue is through preliminary textual criticism and test, and part slag can be used as building material.
Claims (2)
1. the method for vanadium, potassium technique is comprehensively reclaimed in flyash acidleach, it is characterized in that, comprises the following steps:
(1) in leaching-flyash and operation
Sulfuric acid and the direct acidleach of leaching agent Calcium Fluoride (Fluorspan) for flyash, sulfuric acid consumption is and flyash quality per-cent 30%～50%, and leaching agent Calcium Fluoride (Fluorspan) consumption is with flyash quality per-cent 3.5～5%, extraction time 7～12h, 90 ± 5 ℃ of extraction temperatures, leaches the ratio 2.5～3:1 of liquid volume and solid weight; Leach operation and complete and filters solid-liquid separation, leach supernatant liquor and adopt flyash neutralization, its consumption is 30～60% of acidleach flyash consumption, 50～60 ℃ of flyash neutral temperatures, in and time 3～4h; Leached mud is carried out to adverse current pulping and washing four times, and each leaching requirement is identical with leaching operation liquid volume, and the 4th time washing water are lime and wash water preparation, and each wash water adverse current is returned, and soaks slag filtration and stores up;
(2) potassium aluminium sulfate crystallization operation
In flyash, with supernatant liquor stirred crystallization, obtain Potassium aluminum sulfate dodecahydrate crystallization, 5～10 ℃ of Tcs;
(3) in lime and operation
Under potassium aluminium sulfate crystallization tail washings normal temperature, carry out lime neutralization, pH=1.8 ± 0.2, merges in lime and enters restore job with supernatant liquor and a wash water; In and slag muck deposit;
(4) restore job
In lime, add iron reduction time 1.5～2h with supernatant liquor, iron filings add-on is V in reducing solution
2o
55.5～6 times of amount of metal, 38～42 ℃ of temperature ±, current potential 305～315mv left and right, adds polyacrylamide flocculation agent consumption 20～30g/t-flyash, sedimentation standing 2～3h, and solid-liquid separation, reduction supernatant liquor is as extraction stoste, and reducing slag is stored up;
(5) extraction-reextraction operation
Neutralizer extraction adopts 7 stage countercurrent extractions, 8 stage countercurrent back extractions, 3 stage countercurrent regeneration, 1 stage countercurrent washing, organic phase forms 12.5%2-ethylhexyl phosphoric acid+5% tributyl phosphate+82.5% sulfonated kerosene, the sulphuric acid soln that reverse-extraction agent is 1.5mol, the sulphuric acid soln that regenerator is 3mol; The wastewater treatment of raffinate is to obtain lime mud and reuse water with lime neutralization, and reuse water returns to leaching operation, and after back extraction, lean organic phase is regenerated and returned in extraction operation through organic phase;
(6) crystallization-precipitation operation
Under strip liquor normal temperature, add the crystallization of ammoniacal liquor adjust pH to 2.0～2.2, crystallization time 4～5h, crystallization tschermigite, solid-liquid separation post crystallization tail washings adds sodium chlorate and is oxidizing to solution potential 1050～1100mV, 60 ± 5 ℃ of oxidizing temperatures, oxidization time 1～2h, add ammoniacal liquor to 2.2～2.5 precipitations of pH value, 92～95 ℃ of precipitation temperature, precipitation time 2～4h, obtains red vanadium;
(7) red vanadium calcining operation
The calcining furnace that enters after red vanadium is dried is calcined 2～3h at 530～560 ℃, output essence vanadium product.
2. flyash acid leaching process according to claim 1 comprehensively reclaims the method for vanadium, potassium technique, it is characterized in that, described flyash is that low heat value 3500 kilocalories are below containing the flying dust after vanadium type stone coal mine or the burning of the following bone coal type of low heat value 2000 kilocalorie navajoite.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410386426.5A CN104131169B (en) | 2014-08-07 | 2014-08-07 | Flyash acidleach synthetical recovery vanadium, the method for potassium |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410386426.5A CN104131169B (en) | 2014-08-07 | 2014-08-07 | Flyash acidleach synthetical recovery vanadium, the method for potassium |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104131169A true CN104131169A (en) | 2014-11-05 |
| CN104131169B CN104131169B (en) | 2016-08-24 |
Family
ID=51804018
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410386426.5A Active CN104131169B (en) | 2014-08-07 | 2014-08-07 | Flyash acidleach synthetical recovery vanadium, the method for potassium |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104131169B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106277005A (en) * | 2016-08-27 | 2017-01-04 | 盛隆资源再生（无锡）有限公司 | A kind of recovery cryolite, calcium carbonate and method of sodium sulfate from calcium fluoride sludge resource |
| CN109706329A (en) * | 2018-12-27 | 2019-05-03 | 大连博融新材料有限公司 | A kind of method that extracting vanadium from stone coal prepares ammonium metavanadate |
| CN110624933A (en) * | 2019-09-24 | 2019-12-31 | 中国恩菲工程技术有限公司 | Method for washing and removing ammonia from metallurgical waste residues |
| CN115161476A (en) * | 2022-07-20 | 2022-10-11 | 万宝矿产有限公司 | Method for reducing iron concentration in secondary copper sulfide ore biological heap leaching system |
| CN115505759A (en) * | 2022-09-07 | 2022-12-23 | 北京华能长江环保科技研究院有限公司 | Fluidized bed system for comprehensive utilization of stone coal for extracting selenium and vanadium and comprehensive utilization method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101239740A (en) * | 2008-03-07 | 2008-08-13 | 昆明理工大学 | Method for coproducing vanadium pentoxide from vanadium-containing stone coal ore and fluorite |
| CN102399976A (en) * | 2011-11-30 | 2012-04-04 | 长沙矿冶研究院有限责任公司 | Roasting pretreatment process for extracting vanadium pentoxide from high-carbon scherbinaite-containing coal mine and vanadium pentoxide extracting method |
-
2014
- 2014-08-07 CN CN201410386426.5A patent/CN104131169B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101239740A (en) * | 2008-03-07 | 2008-08-13 | 昆明理工大学 | Method for coproducing vanadium pentoxide from vanadium-containing stone coal ore and fluorite |
| CN102399976A (en) * | 2011-11-30 | 2012-04-04 | 长沙矿冶研究院有限责任公司 | Roasting pretreatment process for extracting vanadium pentoxide from high-carbon scherbinaite-containing coal mine and vanadium pentoxide extracting method |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106277005A (en) * | 2016-08-27 | 2017-01-04 | 盛隆资源再生（无锡）有限公司 | A kind of recovery cryolite, calcium carbonate and method of sodium sulfate from calcium fluoride sludge resource |
| CN109706329A (en) * | 2018-12-27 | 2019-05-03 | 大连博融新材料有限公司 | A kind of method that extracting vanadium from stone coal prepares ammonium metavanadate |
| CN110624933A (en) * | 2019-09-24 | 2019-12-31 | 中国恩菲工程技术有限公司 | Method for washing and removing ammonia from metallurgical waste residues |
| CN110624933B (en) * | 2019-09-24 | 2021-05-07 | 中国恩菲工程技术有限公司 | Method for washing and removing ammonia from metallurgical waste residues |
| CN115161476A (en) * | 2022-07-20 | 2022-10-11 | 万宝矿产有限公司 | Method for reducing iron concentration in secondary copper sulfide ore biological heap leaching system |
| CN115161476B (en) * | 2022-07-20 | 2023-06-02 | 万宝矿产有限公司 | Method for reducing concentration of ferric acid in secondary copper sulfide ore biological heap leaching system |
| CN115505759A (en) * | 2022-09-07 | 2022-12-23 | 北京华能长江环保科技研究院有限公司 | Fluidized bed system for comprehensive utilization of stone coal for extracting selenium and vanadium and comprehensive utilization method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104131169B (en) | 2016-08-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103131854B (en) | Method for comprehensively recovering scandium and titanium by leaching red mud with titanium white waste acid | |
| CN100413981C (en) | Method for extracting aluminum from high-silicon aluminum-containing mineral raw material by acid process | |
| AU2013351773B2 (en) | Monazite ballast separation and recovery method | |
| CN100482814C (en) | Extraction of vanadium and molybdenum compound from refused materials containing vanadium and molybdenum etc. multiple elements | |
| CN102244309B (en) | Method for recovering lithium from lithium power battery of electric automobile | |
| CN103526057B (en) | Method of comprehensive recovery of rare precious metals in rare earth smelting slag | |
| CN102277483B (en) | Method for preparing rare earth chloride by using Baiyunebo rare earth concentrate | |
| CN103014333B (en) | Separation and recovery method of uranium, thorium and rare earth in monazite slag | |
| CN101914695B (en) | Method for recycling vanadium from vanadium ore containing high silicon and high carbon via wet process | |
| CN104711424B (en) | A kind of method of recovering rare earth and aluminium in removal of impurities slag from weathered superficial leaching rare-earth ore leachate | |
| CN104131169A (en) | Technological method for comprehensively recovering vanadium and potassium through acid leaching of pulverized fuel ash | |
| CN102897810B (en) | Method for producing aluminum oxide by using fly ash | |
| CN103468975B (en) | Method for extracting beryllium from aureobasite type beryllium concentrate with low beneficiation enrichment ratio | |
| CN101092248A (en) | Technique for producing vanadium pentoxide | |
| CN103045851A (en) | Technique for decomposing Baotou rare-earth ores | |
| CN108584994A (en) | A kind of method of lepidolite calcined by rotary kiln lithium carbonate | |
| CN105039699A (en) | Method for treatment and resource utilization of alkali metal slag extracted through lepidolite solid fluorine reconstruction | |
| CN106745130A (en) | A kind of method that aluminium lime-ash prepares aluminum oxide | |
| CN101450814A (en) | Novel method for extracting vanadic anhydride from stone coal vanadium ore | |
| CN101857919A (en) | Method for preparing lead nitrate and lead oxide by using lead plaster of waste lead accumulator | |
| CN104178632A (en) | Method for comprehensively utilizing titanium white waste acid | |
| CN104046786A (en) | Method for recovering metals from vanadium slag | |
| CN104294061A (en) | Technology for extraction of vanadium pentoxide from stone coal mine | |
| CN106337135A (en) | Novel method for producing vanadium pentoxide through ammonium-free vanadium precipitation | |
| CN101250622B (en) | Complete wet way comprehensive processing method for serpentine mine |
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 | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200930 Address after: 710021 podium building No.18, EE Kangcheng, Fengcheng 8th Road, economic development zone, Xi'an City, Shaanxi Province Patentee after: SHAANXI COAL CHEMICAL INDUSTRY CONSTRUCTION (Group) Co.,Ltd. Patentee after: XI'AN NORTHWEST INSTITUTE FOR NONFERROUS METAL RESEARCH Co.,Ltd. Address before: 9 building, building 66, China Construction Bank, 725000 Jiangbei Road, Ankang, Shaanxi Patentee before: SHAANXI COAL AND CHEMICAL INDUSTRY GROUP SHANNAN INVESTMENT AND DEVELOPMENT Co.,Ltd. Patentee before: NORTHWEST GEOLOGICAL INSTITUTE OF NONFERROUS METALS |