CN113104816B - Method for extracting sulfuric acid by recycling vanadium precipitation wastewater - Google Patents
Method for extracting sulfuric acid by recycling vanadium precipitation wastewater Download PDFInfo
- Publication number
- CN113104816B CN113104816B CN202110405924.XA CN202110405924A CN113104816B CN 113104816 B CN113104816 B CN 113104816B CN 202110405924 A CN202110405924 A CN 202110405924A CN 113104816 B CN113104816 B CN 113104816B
- Authority
- CN
- China
- Prior art keywords
- vanadium
- sulfuric acid
- recycling
- vanadium precipitation
- precipitation wastewater
- 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.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/22—Alkali metal sulfides or polysulfides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G31/00—Compounds of vanadium
- C01G31/02—Oxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Inorganic Compounds Of Heavy Metals (AREA)
- Catalysts (AREA)
Abstract
The invention relates to a method for recycling vanadium precipitation wastewater and extracting sulfuric acid, belonging to the technical field of recycling vanadium extraction tailings. The method for recycling the vanadium precipitation wastewater to extract the sulfuric acid comprises the following steps: extracting V from vanadium slag after vanadium extraction by sodium roasting method 2 O 5 Will extract V 2 O 5 The vanadium precipitation wastewater is subjected to gradient roasting, then a reducing agent is added for mixing, and the mixture reacts at 1000-1150 ℃ for 1.5-2 h for reduction to obtain the product containing Na 2 Solids of S and SO 2 、NH 3 、CO 2 A gas; the gradient roasting is sequentially heated at 1000-1075 ℃ for 0.25-0.3 h, 1085-1135 ℃ for 0.5-0.6 h and 1145-1150 ℃ for 0.75-0.8 h; absorbing said gas with NH 3 Then, the residual gas reacts with oxygen under the action of a catalyst to obtain SO 3 (ii) a Adding SO 3 Absorbed to obtain H 2 SO 4 . The method has high recovery efficiency and saves time and energy cost.
Description
Technical Field
The invention relates to a method for recycling vanadium precipitation wastewater and extracting sulfuric acid, belonging to the technical field of recycling vanadium extraction tailings.
Background
Vanadium is an important rare metal in the industrial field and is mainly used in the steel industry. The vanadium-containing steel has the excellent characteristics of high strength, high toughness, good wear resistance and the like, so the vanadium-containing steel is widely applied to industries such as machinery, automobiles, shipbuilding, railways, aviation, bridges, electronic technology, national defense industry and the like, the consumption of the vanadium-containing steel accounts for about 85 percent of the vanadium consumption, and the consumption of the steel industry accounts for the maximum proportion in the application of the vanadium. The demand of the steel industry directly influences the market quotation of vanadium. About 10% of vanadium is used to produce titanium alloys required by the aerospace industry. Vanadium can be used as a stabilizer and a reinforcer in the titanium alloy, so that the titanium alloy has good ductility and plasticity. In addition, vanadium is used primarily as a catalyst and colorant in the chemical industry. Vanadium has also been used to produce rechargeable hydrogen batteries or vanadium redox batteries. In addition, the new national steel standard regulations require that the vanadium content standard in steel is improved by 25 times. The demand of vanadium is increased sharply due to various reasons, so that the vanadium extraction enterprises can produce the vanadium in full, a large amount of solid waste generated by vanadium extraction is accumulated, and if the solid waste is not treated in time, the vanadium extraction enterprises can not only face the production stop crisis; the accumulation of the vanadium extraction tailings can cause serious pollution to the environment.
The treatment of the vanadium extraction tailings in the prior art is to carry out sodium roasting method on the vanadium extraction tailings to extract V 2 O 5 And accumulating the residual vanadium precipitation wastewater, wherein the residual vanadium precipitation wastewater mainly contains sodium sulfate and ammonium sulfate and other impurities. If proper treatment is not carried out, not only is the waste of resources caused and the requirement of clean production not met, but also the crystal liquid is placed in the environment to generate dust emission, leaching and the like, secondary pollution is formed, and the environment is obviously influenced.
Disclosure of Invention
The invention aims to provide a method for recycling vanadium precipitation wastewater to extract sulfuric acid.
In order to achieve the first object of the invention, the method for recycling the vanadium precipitation wastewater to extract sulfuric acid comprises the following steps:
A. reduction of vanadium-precipitating waste water by sodium salt roasting method, namely extracting V from vanadium slag after vanadium extraction by sodium salt roasting method 2 O 5 Will extract V 2 O 5 The vanadium precipitation waste water is subjected to gradient roasting, then a reducing agent is added and mixed, and the mixture reacts at the temperature of 1000-1150 ℃ for 1.5-2 h to be reduced, so that Na-containing material is obtained 2 Solids of S and SO 2 、NH 3 、CO 2 A gas; the gradient roasting is sequentially heated at 1000-1075 ℃ for 0.25-0.3 h, 1085-1135 ℃ for 0.5-0.6 h and 1145-1150 ℃ for 0.75-0.8 h;
B.SO 2 oxidation of (2): absorbing NH with the gas in the step A 3 Then, the residual gas reacts with oxygen under the action of a catalyst to obtain SO 3 ;
C. Subjecting the SO to 3 Absorbing to obtain H 2 SO 4 ;
The reducing agent is preferably fly ash.
In a specific embodiment, the mass of the vanadium precipitation wastewater subjected to gradient roasting in the step A is M, and the mass ratio of M to the reducing agent is 3-5.
In a specific embodiment, the water content in the vanadium precipitation wastewater in the step A is less than 9.5%, and the water in the vanadium precipitation wastewater after the gradient roasting is completely evaporated.
In one embodiment, the reducing agent has a particle size of less than 7 mesh.
In a specific embodiment, the gradient roasting is firstly heated at 1000-1075 ℃ for 0.25-0.3 h; then heating for 0.5-0.6 h at 1085-1135 ℃; finally heating for 0.75-0.8 h at 1145-1150 ℃.
In one embodiment, the temperature of the reaction in step B is 550 to 650 ℃.
In one embodiment, the catalyst in step C is V 2 O 5 Platinum, iron oxide; preferably V 2 O 5 。
In a specific embodiment, the method further comprises adding Na to the solution containing Na 2 And (3) leaching the solid of the S with an alkali solution, taking supernatant, concentrating and drying to obtain sodium sulfide.
In one embodiment, the alkali is 78-85% NaOH, the leaching temperature is 75-90 ℃, and the leaching time is preferably 4-4.3 h.
In one embodiment, the sodium sulfide is in a yield of 89.5 to 99.2% and in a purity of 98.4 to 99.9%.
Has the advantages that:
the method for recovering, utilizing and extracting the sulfuric acid from the vanadium precipitation wastewater has high recovery efficiency and saves time and energy cost. The invention treats the vanadium precipitation wastewater to ensure that the subsequent yield of sodium sulfide can reach 89.5-99.2%, and the sodium sulfide is easy to leach and purify, and the purity can reach 98.4-99.9% after simple alkali leaching and concentration and drying.
Drawings
FIG. 1 is a diagram of a process for carrying out the present invention.
Detailed Description
In order to achieve the first object of the invention, the method for recycling the vanadium precipitation wastewater to extract sulfuric acid comprises the following steps:
A. reduction of vanadium-precipitating waste water by sodium roasting method, namely extracting V from vanadium slag after vanadium extraction by sodium roasting method 2 O 5 Will extract V 2 O 5 The vanadium precipitation waste water is subjected to gradient roasting, then a reducing agent is added and mixed, and the mixture reacts at the temperature of 1000-1150 ℃ for 1.5-2 h to be reduced, so that Na-containing material is obtained 2 Solids of S and SO 2 、NH 3 、CO 2 A gas; the gradient roasting is sequentially heated at 1000-1075 ℃ for 0.25-0.3 h, 1085-1135 ℃ for 0.5-0.6 h and 1145-1150 ℃ for 0.75-0.8 h;
B.SO 2 oxidation of (2): absorbing NH with the gas in the step A 3 Then, the residual gas reacts with oxygen under the action of a catalyst to obtain SO 3 ;
C. Subjecting the SO to 3 Absorbing to obtain H 2 SO 4 ;
The reducing agent is preferably fly ash.
In a specific embodiment, the mass of the vanadium precipitation wastewater subjected to gradient roasting in the step A is M, and the mass ratio of M to the reducing agent is 3-5.
In a specific embodiment, the water content in the vanadium precipitation wastewater in the step A is less than 9.5%, and the water in the vanadium precipitation wastewater after the gradient roasting is completely evaporated.
In one embodiment, the reducing agent has a particle size of less than 7 mesh.
In a specific embodiment, the gradient roasting is firstly heated at 1000-1075 ℃ for 0.25-0.3 h; then heating for 0.5-0.6 h at 1085-1135 ℃; finally heating for 0.75-0.8 h at 1145-1150 ℃.
In one embodiment, the temperature of the reaction in step B is 550 to 650 ℃.
In one embodiment, the catalyst in step C is V 2 O 5 Platinum, iron oxide; preferably V 2 O 5 。
In a specific embodiment, the method further comprises adding Na to the solution containing Na 2 And leaching the solid of the S with an alkaline solution, taking supernatant, concentrating and drying to obtain sodium sulfide.
In one embodiment, the alkali is 78-85% NaOH, the leaching temperature is 75-90 ℃, and the leaching time is preferably 4-4.3 h.
In one embodiment, the sodium sulfide is in a yield of 89.5 to 99.2% and in a purity of 98.4 to 99.9%.
The following examples are provided to further illustrate the embodiments of the present invention and are not intended to limit the scope of the present invention.
Example 1
And conveying the vanadium precipitation wastewater to a reaction workshop for roasting. And (3) performing step-by-step gradient continuous roasting in a rotary chamber, sequentially roasting at 1054 ℃ for 0.28h, 1100 ℃ for 0.55h and 1148 ℃ for 0.77h, and completely evaporating water in the vanadium precipitation wastewater after the step roasting. The model number of the rotary furnace KY-LQ is 600-10m, and then the rotary furnace KY-LQ is mixed with high-quality coal powder (the granularity of the coal powder is less than 7 meshes) with high carbon content, and the solid mass after the wastewater is dried and the coal powder are 5 in weight ratio. Reacting for 1.8h at 1020 ℃ by taking coal gas as a heat source. The model of the reaction rotary furnace is QC-M1800-18IK. The equipment processing capacity is 5 t/h.
The reduced gas after the reaction in the rotary furnace is directly led to an absorption chamber, and NH generated by the reaction is absorbed by a titanium type catalyst at the temperature of 300 DEG C 3 Then, the residual SO 2 With CO 2 Introducing the mixed gas into a contact chamber, SO 2 At V 2 O 5 Under the catalysis of620 ℃ and O 2 Reaction to form SO 3 SO produced 3 Directly introducing into an absorption tower, and using 98.3% concentrated sulfuric acid as SO 3 Absorption of (2). Generation of H 2 SO 4 The reaction rate of (A) was 1.2 t/stage · h.
Cooling the residual solid after the reaction in the rotary furnace to 700 ℃, putting the solid into 80 ℃ NaOH solution with the concentration of 80 percent for leaching for 4 hours, taking supernatant fluid after leaching, concentrating and drying to obtain the sodium sulfide.
The yield of the obtained sodium sulfide is 99.2%; the purity of the sodium sulfide is detected to be 99.8%.
Example 2
a. 1kg of vanadium precipitation wastewater is continuously roasted by adopting a step gradient, wherein the mass fraction of Na in the vanadium precipitation wastewater is calculated 2 SO 4 68.0%,(NH 4 ) 2 SO 4 20.2%,H 2 O 9.1%,NH 4 0.8 percent of Cl0.9 percent and the rest 1.9 percent. The process of the sectional gradient continuous roasting comprises the following steps: firstly, heating for 0.25h at 1054 ℃; heating at 1100 deg.C for 0.5h; finally heating at 1148 deg.C for 0.75h. After the step gradient continuous roasting and sintering, completely evaporating the water in the vanadium precipitation wastewater;
b. pulverizing coal powder until the particle size is less than 7 meshes;
c. mixing the raw materials subjected to the segmented gradient continuous roasting with coal powder according to the weight ratio of 5 to 1, heating by using coal gas to perform reduction reaction, wherein the reaction temperature is 1000 ℃, and the reaction time is controlled to be 2 hours, so as to obtain a solid pre-product and mixed gas;
d. cooling the pre-product to 700 ℃, putting the pre-product into NaOH solution with the temperature of 80 ℃ and the concentration of 80 percent, leaching for 4 hours, taking supernatant liquor after leaching, concentrating and drying to obtain the sodium sulfide.
The weight of the obtained sodium sulfide was 371.2g, and the yield was 99.2%; the purity of the sodium sulfide is detected to be 99.9%.
The mixed gas passes through a titanium type catalyst to absorb NH 3 Introducing the remaining gas into V 2 O 5 Blowing pure oxygen into a catalyst absorption chamber, controlling the reaction temperature at 620 ℃, and adding SO 2 Oxidation to SO 3 Finally, 98.3% concentrated sulfuric acid is used as SO 3 Is sucked143g of sulfuric acid was obtained.
Comparative example 1
a. Taking 1kg of vanadium precipitation wastewater, wherein Na is contained in the wastewater 2 SO 4 68.0%,(NH 4 ) 2 SO 4 20.2 percent, and after the vanadium precipitation wastewater is heated for 6 hours at the temperature of 1150 ℃, the water content of the vanadium precipitation wastewater is 0 percent.
b. Pulverizing coal powder until the particle size is less than 7 meshes;
c. mixing the dried raw materials and coal powder according to a weight ratio of 5;
d. cooling the pre-product to 700 ℃, putting the pre-product into NaOH solution with the temperature of 80 ℃ and the concentration of 80 percent, leaching for 4 hours, taking supernatant liquor after leaching, concentrating and drying to obtain the sodium sulfide.
The weight of sodium sulfide obtained was 208.3g, the yield was 61.3%, and the purity was found to be 91%.
Absorption of the SO produced 2 : absorption of NH by a titanium-type catalyst 3 SO is prepared by 2 Let in V 2 O 5 Blowing pure oxygen into a catalyst absorption chamber, controlling the reaction temperature at 620 ℃, and adding SO 2 Oxidation to SO 3 Finally, 98.3% concentrated sulfuric acid is used as SO 3 The absorption of (2) produced 86g of sulfuric acid.
Claims (8)
1. The method for recycling the vanadium precipitation wastewater to extract sulfuric acid is characterized by comprising the following steps:
A. reduction of vanadium-precipitating waste water by sodium roasting method, namely extracting V from vanadium slag after vanadium extraction by sodium roasting method 2 O 5 Will extract V 2 O 5 The vanadium precipitation waste water is subjected to gradient roasting, then a reducing agent is added and mixed, and the mixture reacts at the temperature of 1000-1150 ℃ for 1.5-2 h to be reduced, so that Na-containing material is obtained 2 Solids of S and SO 2 、NH 3 、CO 2 A gas; the gradient roasting is sequentially heated at 1000-1075 ℃ for 0.25-0.3 h, 1085-1135 ℃ for 0.5-0.6 h and 1145-1150 ℃ for 0.75-0.8 h; step A, the water content in the vanadium precipitation wastewater is below 9.5 percent, and the water in the vanadium precipitation wastewater is completely removed after the gradient roastingPervaporation;
B. SO 2 oxidation of (2): absorbing NH in the gas in the step A 3 Then, the residual gas reacts with oxygen under the action of a catalyst to obtain SO 3 (ii) a The reaction temperature in the step B is 550-650 ℃, and the catalyst is V 2 O 5 Platinum, iron oxide;
C. subjecting the SO to 3 Absorbed to obtain H 2 SO 4 ;
The reducing agent is fly ash, and the granularity of the reducing agent is less than 7 meshes.
2. The method for recycling and extracting sulfuric acid from vanadium precipitation wastewater according to claim 1, wherein the mass of the vanadium precipitation wastewater subjected to gradient roasting in the step A is M, and the mass ratio of M to the reducing agent is 3-5.
3. The method for recycling the vanadium precipitation wastewater to extract the sulfuric acid according to the claim 1 or 2, characterized in that the gradient roasting is firstly heating for 0.25 to 0.3h at the temperature of 1000 to 1075 ℃; then heating for 0.5-0.6 h at 1085-1135 ℃; finally heating for 0.75-0.8 h at 1145-1150 ℃.
4. The method for recycling and extracting sulfuric acid from vanadium precipitation wastewater according to claim 1 or 2, wherein the catalyst in the step B is V 2 O 5 。
5. The method for recycling and extracting sulfuric acid from vanadium precipitation wastewater according to claim 1 or 2, characterized in that the method further comprises the step of recycling and extracting sulfuric acid from the wastewater containing Na 2 And (3) leaching the solid of the S with an alkali solution, taking supernatant, concentrating and drying to obtain sodium sulfide.
6. The method for recycling and extracting sulfuric acid from vanadium precipitation wastewater according to claim 5, wherein the alkali is 78-85% NaOH, and the leaching temperature is 75-90 ℃.
7. The method for recycling and extracting sulfuric acid from vanadium precipitation wastewater according to claim 6, wherein the leaching time is 4-4.3 h.
8. The method for recycling and extracting sulfuric acid from vanadium precipitation wastewater according to claim 6, wherein the yield of sodium sulfide is 89.5-99.2%, and the purity is 98.4-99.9%.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN202110405924.XA CN113104816B (en) | 2021-04-15 | 2021-04-15 | Method for extracting sulfuric acid by recycling vanadium precipitation wastewater |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN202110405924.XA CN113104816B (en) | 2021-04-15 | 2021-04-15 | Method for extracting sulfuric acid by recycling vanadium precipitation wastewater |
Publications (2)
Publication Number | Publication Date |
---|---|
CN113104816A CN113104816A (en) | 2021-07-13 |
CN113104816B true CN113104816B (en) | 2022-10-18 |
Family
ID=76717291
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN202110405924.XA Active CN113104816B (en) | 2021-04-15 | 2021-04-15 | Method for extracting sulfuric acid by recycling vanadium precipitation wastewater |
Country Status (1)
Country | Link |
---|---|
CN (1) | CN113104816B (en) |
Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB294975A (en) * | 1927-08-03 | 1929-01-10 | Selden Co | Contact sulphuric acid process |
US5082645A (en) * | 1990-08-24 | 1992-01-21 | Chemetics International Company, Ltd. | Waste acid recovery process |
EP0516001A1 (en) * | 1991-05-24 | 1992-12-02 | Haldor Topsoe A/S | Process for the regeneration of spent sulphuric acid |
US5437849A (en) * | 1992-05-21 | 1995-08-01 | Metallgesellschaft Aktiengesellschaft | Method of processing vanadium-containing residues |
CN1406882A (en) * | 2001-09-12 | 2003-04-02 | 攀枝花世纪行实业发展有限公司 | Process for treating acid waste water for depositing vanadium |
CN101224875A (en) * | 2007-12-06 | 2008-07-23 | 昆明理工大学 | Method for reclaiming sulfuric acid from vanadium-containing stone coal oxygen pressure acid drench |
CN101513993A (en) * | 2009-03-21 | 2009-08-26 | 山东军辉建设安装工程有限公司 | Method using magnesium sulphate to produce sulphuric acid |
CN107815549A (en) * | 2017-11-13 | 2018-03-20 | 攀钢集团攀枝花钢铁研究院有限公司 | The Application way of vanadium wastewater |
CN110643838A (en) * | 2019-11-12 | 2020-01-03 | 四川大学 | Method for roasting vanadium slag by adopting calcium sulfate |
CN111704303A (en) * | 2020-07-09 | 2020-09-25 | 攀枝花学院 | Drying method of evaporation crystallization liquid of vanadium precipitation wastewater and method for recycling sodium sulfide |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5427763A (en) * | 1994-04-15 | 1995-06-27 | Mcdonnel Douglas Corp. | Method for making vanadium dioxide powders |
CN101503762B (en) * | 2009-03-20 | 2010-09-08 | 湖南大学 | Desulphurization and vanadium extraction technique for calcinated vanadium ore |
WO2012057794A1 (en) * | 2010-10-29 | 2012-05-03 | Tda Research, Inc. | Low temperature sulphur dioxide oxidation catalyst for sulfuric acid manufacture |
CN104342567B (en) * | 2014-11-05 | 2015-10-14 | 攀枝花兴辰钒钛有限公司 | High calcium is containing the method for vanadium material vanadium extraction |
CN114988473A (en) * | 2018-09-13 | 2022-09-02 | 中钒联科技发展有限公司 | Process for recycling ammonia gas for preparing ammonium and wastewater for vanadium preparation |
-
2021
- 2021-04-15 CN CN202110405924.XA patent/CN113104816B/en active Active
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB294975A (en) * | 1927-08-03 | 1929-01-10 | Selden Co | Contact sulphuric acid process |
US5082645A (en) * | 1990-08-24 | 1992-01-21 | Chemetics International Company, Ltd. | Waste acid recovery process |
EP0516001A1 (en) * | 1991-05-24 | 1992-12-02 | Haldor Topsoe A/S | Process for the regeneration of spent sulphuric acid |
US5437849A (en) * | 1992-05-21 | 1995-08-01 | Metallgesellschaft Aktiengesellschaft | Method of processing vanadium-containing residues |
CN1406882A (en) * | 2001-09-12 | 2003-04-02 | 攀枝花世纪行实业发展有限公司 | Process for treating acid waste water for depositing vanadium |
CN101224875A (en) * | 2007-12-06 | 2008-07-23 | 昆明理工大学 | Method for reclaiming sulfuric acid from vanadium-containing stone coal oxygen pressure acid drench |
CN101513993A (en) * | 2009-03-21 | 2009-08-26 | 山东军辉建设安装工程有限公司 | Method using magnesium sulphate to produce sulphuric acid |
CN107815549A (en) * | 2017-11-13 | 2018-03-20 | 攀钢集团攀枝花钢铁研究院有限公司 | The Application way of vanadium wastewater |
CN110643838A (en) * | 2019-11-12 | 2020-01-03 | 四川大学 | Method for roasting vanadium slag by adopting calcium sulfate |
CN111704303A (en) * | 2020-07-09 | 2020-09-25 | 攀枝花学院 | Drying method of evaporation crystallization liquid of vanadium precipitation wastewater and method for recycling sodium sulfide |
Non-Patent Citations (2)
Title |
---|
"Recovery of vanadium from black shale";Li Cunxiong et al;《Transactions of Nonferrous Metals Society of China》;20010524;第20卷;第S127-S131页 * |
"扩散渗析膜法从石煤提钒浸出液中回收硫酸";李兴彬等;《2008年全国冶金物理化学学术会议专辑(下册)》;20080831;第26卷;第541-544页 * |
Also Published As
Publication number | Publication date |
---|---|
CN113104816A (en) | 2021-07-13 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN108728653B (en) | A method of extracting molybdenum from useless nickel molybdenum catalyst | |
CN109110826B (en) | Production method of battery-grade nickel sulfate | |
CN109987639B (en) | Method for dealkalizing aluminum-reinforced red mud and separating and recovering aluminum and iron | |
CN102828025B (en) | Method for extracting V2O5 from stone coal navajoite | |
CN109055757B (en) | Method for recovering manganese dioxide and lead in anode slag of electrolytic manganese or electrolytic zinc | |
CN107840311B (en) | A kind of method of containing sulphur-slag recycling sulphur | |
CN112760487A (en) | Method for recovering manganese and lead from electrolytic manganese anode slag | |
CN112522512B (en) | Method for preparing battery-grade cobalt sulfate by using organic cobalt slag of zinc smelting plant | |
CN102492858A (en) | Method for separating enriched nickel and cobalt from battery waste leaching solution | |
CN103233125A (en) | Method for extracting tungsten, molybdenum and rhenium from waste high-temperature alloy | |
CN101445446A (en) | Method for producing iron oxalate and by-products chrome metal and chromic acid | |
CN102994746B (en) | Method for producing nickel sulfide ore concentrate by use of industrial waste acid | |
CN102061388A (en) | Method for smelting ferromolybdenum by utilizing molybdenum scrap | |
CN105274341A (en) | Method for leaching metallic vanadium and metallic tungsten in waste selective catalytic reduction (SCR) denitration catalyst | |
CN103074496B (en) | Method for separating and purifying magnesium dioxide from anode mud | |
CN116555592A (en) | Leaching method of chromium and iron in ferrochrome | |
CN101705377B (en) | Method for extracting vanadium from stone coal by wet-process enrichment and pyrogenic-process conversion | |
CN110735039A (en) | Electrolytic manganese metal anode mud treatment method | |
CN112645387A (en) | Method for preparing battery-grade manganese dioxide by using anode slag | |
CN113104816B (en) | Method for extracting sulfuric acid by recycling vanadium precipitation wastewater | |
CN105861836A (en) | Method for collecting noble metal from polymetallic alloy material | |
CN105983707A (en) | Method for preparing high-purity rhenium powder from rhenium-containing high-arsenic copper sulfide | |
CN110028042B (en) | Method for recycling waste cathode carbon blocks of electrolytic aluminum electrolysis cell | |
CN109207742B (en) | Method for efficiently leaching cobalt and nickel from cobalt and nickel sulfide waste | |
CN105543506A (en) | Method for producing high-purity chromium metal |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PB01 | Publication | ||
PB01 | Publication | ||
SE01 | Entry into force of request for substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
GR01 | Patent grant | ||
GR01 | Patent grant |