CN114293034A - Method for extracting vanadium from sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater - Google Patents
Method for extracting vanadium from sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater Download PDFInfo
- Publication number
- CN114293034A CN114293034A CN202111430781.4A CN202111430781A CN114293034A CN 114293034 A CN114293034 A CN 114293034A CN 202111430781 A CN202111430781 A CN 202111430781A CN 114293034 A CN114293034 A CN 114293034A
- Authority
- CN
- China
- Prior art keywords
- vanadium
- sodium
- filtrate
- precipitation wastewater
- modified
- 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)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Inorganic Compounds Of Heavy Metals (AREA)
Abstract
The invention relates to the field of chemical industry, and discloses a method for extracting vanadium from sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater. The method comprises the following steps: (1) concentrating the vanadium precipitation wastewater to 3/4-2/3 times of the original volume, adding a reducing agent for reaction, adjusting the pH value to 6-6.5 after the reaction is finished, and filtering to obtain chromium reduction slag and filtrate A; (2) adding ammonium salt into the filtrate A, stirring and filtering to obtain filter residue and filtrate B, and diluting the filtrate B to be the same as the volume of the vanadium precipitation wastewater in the step (1); (3) adding the diluted filtrate B obtained in the step (2) into a sodium-modified vanadium-containing clinker, leaching at 90-97 ℃, filtering to obtain vanadium extraction residues and a leachate, adjusting the pH value of the leachate to 1.8-2.3, precipitating vanadium, and calcining to obtain vanadium pentoxide. The method not only recovers the vanadium in the vanadium precipitation wastewater, but also reduces the high-temperature reaction time in the vanadium precipitation process, and saves energy.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a method for extracting vanadium from sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater.
Background
At present, in the vanadium slag sodium salt roasting-water leaching vanadium process, sodium salt is adopted as a roasting additive, roasting is carried out under the high-temperature aerobic condition to generate sodium vanadate dissolved in water, a sodium vanadate solution is obtained after water leaching, vanadium is further precipitated to obtain a vanadium product, and vanadium precipitation wastewater contains a large amount of sodium sulfate. In the prior art, the leaching effect is influenced by the high content of sodium sulfate in the vanadium precipitation wastewater, so that the obtained leaching solution has high sodium sulfate, and the vanadium precipitation effect and the quality of a vanadium product are influenced; in the prior art, the vanadium precipitation wastewater is generally subjected to evaporation concentration after deamination, and ammonium sulfate is carried in the obtained sodium sulfate, so that the treatment is difficult, and the accumulation causes huge environmental protection management cost.
The literature, "technical research on recycling of acidic vanadium precipitation wastewater" mainly studies that vanadium precipitation wastewater is directly recycled, and considers the influence rule of ammonium ions and sodium sulfate on vanadium precipitation rate and products, so as to obtain that the optimal vanadium precipitation wastewater recycled is 50%, and in addition, 50% of fresh water is subjected to composite leaching, and vanadium precipitation is performed by adjusting pH value at high temperature and adding ammonium at high temperature to precipitate vanadium. The document only aims at the proportion of the used wastewater which can be recycled and leached, does not relate to the use of the wastewater which can be recycled, only obtains the vanadium-containing leaching solution after the wastewater is recycled, and can obtain the vanadium product after the vanadium-containing leaching solution is subjected to a vanadium precipitation process.
Disclosure of Invention
The invention aims to solve the problems that the wastewater can not be completely recycled, the step-by-step treatment time of leaching vanadium precipitation is long, and the operation is complicated in the prior art, and provides a method for extracting vanadium from sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater.
In order to achieve the aim, the invention provides a method for extracting vanadium from a sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater, which comprises the following steps:
(1) concentrating the vanadium precipitation wastewater to 3/4-2/3 times of the original volume, adding a reducing agent for reaction, adjusting the pH value to 6-6.5 after the reaction is finished, and filtering to obtain chromium reduction slag and filtrate A;
(2) adding ammonium salt into the filtrate A, stirring and filtering to obtain filter residue and filtrate B, and diluting the filtrate B to be the same as the volume of the vanadium precipitation wastewater in the step (1);
(3) adding the diluted filtrate B obtained in the step (2) into a sodium-modified vanadium-containing clinker, leaching at 90-97 ℃, filtering to obtain vanadium extraction residues and a leachate, adjusting the pH value of the leachate to 1.8-2.3, precipitating vanadium, and calcining to obtain vanadium pentoxide.
Preferably, in the step (1), the content of sodium element in the vanadium precipitation wastewater is 23-60 g/L, and the content of chromium element is 0.3-3 g/L.
Preferably, in step (1), the reducing agent is sodium metabisulfite.
Preferably, in the step (1), the weight ratio of the reducing agent to the chromium element in the vanadium precipitation wastewater is (1.2-1.5): 1.
preferably, in the step (1), the reaction temperature is 70-85 ℃, and the reaction time is 20-40 min.
Preferably, in step (2), the ammonium salt is ammonium bicarbonate and/or ammonium carbonate.
Preferably, in the step (2), the ratio of the ammonium ions in the ammonium salt to the amount of the substance of the sodium element in the filtrate a is (0.5-0.75): 1.
preferably, in the step (2), the stirring temperature is 25-45 ℃, and the stirring time is 60-120 min.
Preferably, in the step (3), the liquid-solid ratio of the diluted filtrate B to the sodium-modified vanadium-containing clinker is 2-2.5 mL/g.
Preferably, in the step (3), the content of vanadium element in the sodium-modified vanadium-containing clinker is 5-12 wt%.
Preferably, in the step (3), the leaching time is 30-50 min.
According to the invention, the vanadium precipitation wastewater is concentrated to a certain volume, ammonium salt is added to remove partial sodium, the influence of high sodium is eliminated, the converted ammonium is used as a vanadium binding agent, no ammonium salt needs to be added in the vanadium precipitation process, the ammonium and vanadium are combined by utilizing the leaching process, the pH value can be adjusted subsequently to directly precipitate vanadium, the vanadium in the vanadium precipitation wastewater is recovered, the high temperature reaction time in the vanadium precipitation process is reduced, and the energy is saved.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The invention provides a method for extracting vanadium from a sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater, which comprises the following steps:
(1) concentrating the vanadium precipitation wastewater to 3/4-2/3 times of the original volume, adding a reducing agent for reaction, adjusting the pH value to 6-6.5 after the reaction is finished, and filtering to obtain chromium reduction slag and filtrate A;
(2) adding ammonium salt into the filtrate A, stirring and filtering to obtain filter residue and filtrate B, and diluting the filtrate B to be the same as the volume of the vanadium precipitation wastewater in the step (1);
(3) adding the diluted filtrate B obtained in the step (2) into a sodium-modified vanadium-containing clinker, leaching at 90-97 ℃, filtering to obtain vanadium extraction residues and a leachate, adjusting the pH value of the leachate to 1.8-2.3, precipitating vanadium, and calcining to obtain vanadium pentoxide.
In the invention, in the step (1), the content of sodium element in the vanadium precipitation wastewater is 23-60 g/L, and the content of chromium element is 0.3-3 g/L. Specifically, the content of sodium element in the vanadium precipitation wastewater can be 23g/L, 25g/L, 30g/L, 35g/L, 40g/L, 45g/L, 50g/L, 55g/L or 60g/L, and the content of chromium element in the vanadium precipitation wastewater can be 0.3g/L, 0.5g/L, 0.7g/L, 1g/L, 1.3g/L, 1.5g/L, 1.8g/L, 2g/L, 2.3g/L, 2.5g/L, 2.8g/L or 3 g/L.
In a preferred embodiment, in step (1), the reducing agent is sodium metabisulfite.
Preferably, in the step (1), the weight ratio of the reducing agent to the chromium element in the vanadium precipitation wastewater is (1.2-1.5): 1. specifically, the weight ratio of the reducing agent to the chromium element in the vanadium precipitation wastewater may be 1.2: 1. 1.25: 1. 1.3: 1. 1.35: 1. 1.4: 1. 1.45: 1 or 1.5: 1.
in the invention, in the step (1), the reaction temperature is 70-85 ℃, and the reaction time is 20-40 min. Specifically, the reaction temperature may be 70 ℃, 71 ℃, 72 ℃, 73 ℃, 74 ℃, 75 ℃, 76 ℃, 77 ℃, 78 ℃, 79 ℃, 80 ℃, 81 ℃, 82 ℃, 83 ℃, 84 ℃ or 85 ℃, and the reaction time may be 20min, 22min, 25min, 27min, 30min, 33min, 35min, 38min or 40 min.
In a specific embodiment, in step (1), the pH of the system after the reaction is completed may be adjusted to 6.1, 6.2, 6.3, 6.4, or 6.5.
Preferably, in step (2), the ammonium salt is ammonium bicarbonate and/or ammonium carbonate.
In a preferred embodiment, in the step (2), the ratio of the ammonium ions in the ammonium salt to the amount of the substance of the sodium element in the filtrate a is (0.5 to 0.75): 1. specifically, the ratio of the ammonium ions in the ammonium salt to the amount of the substance of sodium element in the filtrate a may be 0.5: 1. 0.52: 1. 0.55: 1. 0.57: 1. 0.6: 1. 0.62: 1. 0.65: 1. 0.68: 1. 0.7: 1. 0.72: 1 or 0.75: 1.
in the invention, after the ammonium salt is added into the filtrate A, the sodium bicarbonate is separated out by utilizing the difference of solubility, so that the wastewater needs to be concentrated to 3/4-2/3, the temperature needs to be controlled not to exceed 45 ℃ in the stirring process, and the volatilization of the ammonium salt can be prevented.
Preferably, in the step (2), the stirring temperature is 25-45 ℃, and the stirring time is 60-120 min. Specifically, the stirring temperature can be 25 ℃, 27 ℃, 30 ℃, 33 ℃, 35 ℃, 38 ℃, 40 ℃, 43 ℃ or 45 ℃, and the stirring time can be 60min, 70min, 80min, 90min, 100min, 110min or 120 min.
In the invention, in the step (2), the main component in the filter residue is sodium salt, and the sodium salt is mainly sodium bicarbonate.
In the invention, in the step (3), the liquid-solid ratio of the diluted filtrate B to the sodium-modified vanadium-containing clinker is 2-2.5 mL/g. Specifically, the liquid-solid ratio of the diluted filtrate B to the sodium-modified vanadium-containing clinker can be 2mL/g, 2.1mL/g, 2.2mL/g, 2.3mL/g, 2.4mL/g or 2.5 mL/g.
In the invention, the sodium-modified vanadium-containing clinker is vanadium-containing slag obtained after converting vanadium-containing molten iron.
Preferably, in the step (3), the content of vanadium element in the sodium-modified vanadium-containing clinker is 5-12 wt%. Specifically, the content of vanadium element in the sodium-modified vanadium-containing clinker may be 5 wt%, 6 wt%, 7 wt%, 8 wt%, 9 wt%, 10 wt%, 11 wt% or 12 wt%.
In specific embodiments, in step (3), the temperature of the leaching may be 90 ℃, 91 ℃, 92 ℃, 93 ℃, 94 ℃, 95 ℃, 96 ℃ or 97 ℃.
Preferably, in the step (3), the leaching time is 30-50 min. Specifically, the leaching time may be 30min, 33min, 35min, 37min, 40min, 42min, 45min, 47min, or 50 min.
In the invention, in the step (3), the calcination temperature is 500-550 ℃, and the calcination time is 120-240 min. Specifically, the calcination temperature may be 500 ℃, 510 ℃, 520 ℃, 530 ℃, 540 ℃ or 550 ℃, and the calcination time may be 120min, 140min, 160min, 180min, 200min, 220min or 240 min.
According to the invention, vanadium precipitation wastewater is concentrated to a certain volume, ammonium salt is added to remove part of sodium, the influence of high sodium is eliminated, after filtration, filtrate is diluted and returned to leach clinker, the converted ammonium salt is used as a vanadium binding agent, the obtained leachate is directly acidified to precipitate vanadium, no ammonium salt needs to be added in the vanadium precipitation process, the combination of ammonium and vanadium is completed by utilizing the leaching process, the pH value can be subsequently adjusted to directly precipitate vanadium, the vanadium in the vanadium precipitation wastewater is recovered, the vanadium precipitation wastewater is recycled, the vanadium precipitation wastewater does not need to be completely evaporated, the leaching and the vanadium precipitation are completed in one step, the acid precipitation is directly performed after the leaching, and compared with the conventional vanadium precipitation method, the high temperature reaction time in the vanadium precipitation process is reduced, and energy is saved.
The present invention will be described in detail below by way of examples, but the method of the present invention is not limited thereto.
In the embodiment of the invention, the used vanadium precipitation wastewater is from a vanadium slag sodium salt roasting-water leaching vanadium process, the main components are shown in table 1, the used sodium salt vanadium-containing clinker is vanadium-containing slag obtained after blowing in vanadium-containing molten iron, and the main components are shown in table 2.
TABLE 1 vanadium precipitation wastewater principal Components (g/L)
TABLE 2 sodium-modified vanadium-containing clinker principal component (% by weight)
Example 1
(1) 500mL of vanadium precipitation wastewater in Table 1 was concentrated to 3/4 times (375mL) of the original volume, and then the weight ratio of sodium metabisulfite to chromium in the vanadium precipitation wastewater was 1.2: 1, adding 1.74g of sodium metabisulfite, reacting for 20min at 70 ℃, adjusting the pH value to 6 after the reaction is finished, and filtering to obtain chromium reducing slag and 368mL of filtrate A (the filtrate A contains 0.545mol of sodium element in total);
(2) adding 0.2725mol of ammonium bicarbonate (the ratio of ammonium ions in the ammonium bicarbonate to sodium in the filtrate A is 0.5: 1), stirring at 45 deg.C for 60min, filtering to obtain 22.89g of filter residue and 352mL of filtrate B, and diluting the filtrate B to 500 mL;
(3) adding the diluted filtrate B obtained in the step (2) into 250g of the sodium-modified vanadium-containing clinker in the table 2, wherein the liquid-solid ratio of the diluted filtrate B to the sodium-modified vanadium-containing clinker is 2mL/g, leaching for 30min at 90 ℃, then filtering to obtain vanadium extraction residues and leachate, adjusting the pH value of the leachate to 1.8 for vanadium precipitation, and then calcining for 120min at 500 ℃ to obtain vanadium pentoxide.
Example 2
(1) 200mL of vanadium precipitation wastewater in Table 1 was concentrated to 7/10 times (140mL) of the original volume, and then the weight ratio of sodium metabisulfite to chromium in the vanadium precipitation wastewater was 1.3: 1, adding 0.754g of sodium metabisulfite, reacting at 75 ℃ for 30min, adjusting the pH value to 6.2 after the reaction is finished, and filtering to obtain chromium reducing slag and 138mL of filtrate A (total 0.2189mol of sodium element in the filtrate A);
(2) adding 0.0657mol of ammonium carbonate (the amount ratio of ammonium ions in the ammonium carbonate to sodium elements in the filtrate A is 0.6: 1) into the filtrate A, stirring at 35 ℃ for 90min, filtering to obtain 11.038g of filter residue and 124mL of filtrate B, and diluting the filtrate B to 200 mL;
(3) adding the diluted filtrate B obtained in the step (2) into 90.9g of the sodium-modified vanadium-containing clinker in the table 2, wherein the liquid-solid ratio of the diluted filtrate B to the sodium-modified vanadium-containing clinker is 2.2mL/g, leaching for 40min at the temperature of 92 ℃, filtering to obtain vanadium extraction residues and leachate, adjusting the pH value of the leachate to 2.0 for vanadium precipitation, and calcining for 180min at the temperature of 520 ℃ to obtain vanadium pentoxide.
Example 3
(1) 1000mL of vanadium precipitation wastewater in Table 1 was concentrated to 2/3 times (666.67mL) of the original volume, and then the weight ratio of sodium metabisulfite to chromium in the vanadium precipitation wastewater was 1.5: 1, adding 4.35g of sodium metabisulfite, reacting at 85 ℃ for 40min, adjusting the pH value to 6.5 after the reaction is finished, and filtering to obtain chromium reducing slag and 664mL of filtrate A (the filtrate A contains 1.101mol of sodium element in total);
(2) adding 0.826mol of ammonium bicarbonate (the ratio of ammonium ions in the ammonium bicarbonate to sodium element in the filtrate A is 0.75: 1) into the filtrate A, stirring at 25 deg.C for 120min, filtering to obtain 83.26g of filter residue and 643mL of filtrate B, and diluting the filtrate B to 1000 mL;
(3) adding the diluted filtrate B obtained in the step (2) into 400g of the sodium-modified vanadium-containing clinker in the table 2, wherein the liquid-solid ratio of the diluted filtrate B to the sodium-modified vanadium-containing clinker is 2.5mL/g, leaching for 50min at 97 ℃, filtering to obtain vanadium extraction residues and leachate, adjusting the pH value of the leachate to 2.3 for vanadium precipitation, and calcining for 240min at 550 ℃ to obtain vanadium pentoxide.
Comparative example 1
The process was carried out as described in example 1, except that in step (3), the temperature of the leaching was 80 ℃.
Comparative example 2
The process was carried out as described in example 3, except that in step (3), the temperature of the leaching was 110 ℃.
Test example
The vanadium extraction residue, the leachate and the obtained vanadium pentoxide in step (3) in examples 1 to 3 and comparative examples 1 to 2 were each examined for their composition.
The results are shown in tables 3 to 5, respectively.
TABLE 3 vanadium extraction residue main Components
| Numbering | V/weight% | Cr/weight% | Fe/weight% | SO4 2-Per weight percent | Na2O/weight% |
| Example 1 | 0.70 | 1.01 | 30.11 | 0.8 | 5.2 |
| Example 2 | 0.60 | 1.21 | 30.23 | 0.76 | 5.13 |
| Example 3 | 0.54 | 1.12 | 30.35 | 0.65 | 4.76 |
| Comparative example 1 | 2.46 | 1.23 | 29.52 | 0.54 | 6.23 |
| Comparative example 2 | 0.45 | 0.95 | 31.13 | 2.54 | 5.63 |
TABLE 4 major ingredients of leachate
| Numbering | NH4 +(g/L) | Na(g/L) | Cr(g/L) | SO4 2-(g/L) | V(g/L) |
| Example 1 | 17.81 | 35.42 | 2.70 | 91.40 | 36.85 |
| Example 2 | 19.83 | 31.76 | 2.15 | 91.94 | 33.93 |
| Example 3 | 22.87 | 27.50 | 2.25 | 92.80 | 30.10 |
| Comparative example 1 | 17.81 | 30.78 | 2.09 | 92.70 | 28.68 |
| Comparative example 2 | 15.35 | 29.10 | 2.97 | 85.24 | 30.47 |
TABLE 5 vanadium pentoxide major constituent
The results show that by adopting the method disclosed by the invention, vanadium extraction is carried out on the sodium-modified vanadium-containing clinker after the vanadium precipitation wastewater is treated, the vanadium and sulfate radicals in the vanadium extraction residue are both less than 1 wt%, the sodium oxide content is less than 5.5 wt%, when the leaching temperature is low, part of sodium vanadate in the clinker is not leached sufficiently, the vanadium and sodium contents in the residue are both high, when the leaching temperature is high, a small part of sodium and other impurities in the residue can form sodium ferric silicate, sodium calcium silicate and the like which are difficult to dissolve in water and are left in the residue, sulfate radicals can form insoluble impurities with the sodium ferric silicate and the sodium calcium silicate and the like and are left in the residue, so that the sulfate radical content in the vanadium extraction residue is high, and compared with a common vanadium extraction method, the method reduces the time of high-temperature reaction in the vanadium precipitation process, and the obtained vanadium pentoxide can meet the YB/T5304-2011 quality standard requirements.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (10)
1. A method for extracting vanadium from a sodium-modified vanadium-containing clinker by using vanadium precipitation wastewater is characterized by comprising the following steps:
(1) concentrating the vanadium precipitation wastewater to 3/4-2/3 times of the original volume, adding a reducing agent for reaction, adjusting the pH value to 6-6.5 after the reaction is finished, and filtering to obtain chromium reduction slag and filtrate A;
(2) adding ammonium salt into the filtrate A, stirring and filtering to obtain filter residue and filtrate B, and diluting the filtrate B to be the same as the volume of the vanadium precipitation wastewater in the step (1);
(3) adding the diluted filtrate B obtained in the step (2) into a sodium-modified vanadium-containing clinker, leaching at 90-97 ℃, filtering to obtain vanadium extraction residues and a leachate, adjusting the pH value of the leachate to 1.8-2.3, precipitating vanadium, and calcining to obtain vanadium pentoxide.
2. The method according to claim 1, wherein in the step (1), the content of sodium element in the vanadium precipitation wastewater is 23-60 g/L, and the content of chromium element in the vanadium precipitation wastewater is 0.3-3 g/L.
3. The method according to claim 1, wherein, in step (1), the reducing agent is sodium metabisulfite;
preferably, the weight ratio of the reducing agent to the chromium element in the vanadium precipitation wastewater is (1.2-1.5): 1.
4. the method according to claim 1, wherein in the step (1), the temperature of the reaction is 70-85 ℃, and the time of the reaction is 20-40 min.
5. The method according to claim 1, wherein in step (2), the ammonium salt is ammonium bicarbonate and/or ammonium carbonate.
6. The method according to claim 1, wherein in step (2), the ratio of the amount of ammonium ions in the ammonium salt to the amount of the substance of sodium element in the filtrate A is (0.5-0.75): 1.
7. the method according to claim 1, wherein in the step (2), the stirring temperature is 25 to 45 ℃ and the stirring time is 60 to 120 min.
8. The method according to claim 1, wherein in the step (3), the liquid-solid ratio of the diluted filtrate B to the sodium-modified vanadium-containing clinker is 2-2.5 mL/g.
9. The method of claim 8, wherein in step (3), the content of vanadium element in the sodium-modified vanadium-containing clinker is 5-12 wt%.
10. The method according to claim 8, wherein in the step (3), the leaching time is 30-50 min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111430781.4A CN114293034B (en) | 2021-11-29 | 2021-11-29 | Method for extracting vanadium from sodium-modified vanadium-containing clinker by utilizing vanadium precipitation wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111430781.4A CN114293034B (en) | 2021-11-29 | 2021-11-29 | Method for extracting vanadium from sodium-modified vanadium-containing clinker by utilizing vanadium precipitation wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114293034A true CN114293034A (en) | 2022-04-08 |
| CN114293034B CN114293034B (en) | 2023-09-05 |
Family
ID=80966176
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111430781.4A Active CN114293034B (en) | 2021-11-29 | 2021-11-29 | Method for extracting vanadium from sodium-modified vanadium-containing clinker by utilizing vanadium precipitation wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114293034B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5279804A (en) * | 1991-04-26 | 1994-01-18 | Occidental Chemical Corporation | Vanadium removal in aqueous streams |
| CN102198992A (en) * | 2011-04-08 | 2011-09-28 | 史永军 | Treatment method for vanadium precipitation mother liquor wastewater |
| CN104086032A (en) * | 2014-07-30 | 2014-10-08 | 攀钢集团攀枝花钢钒有限公司 | Method for recycling vanadium precipitating wastewater |
| CN105950865A (en) * | 2016-05-17 | 2016-09-21 | 沈阳理工大学 | Method for separating and extracting vanadium and chromium from high-chromium vanadium leaching liquid |
| CN108911237A (en) * | 2018-07-11 | 2018-11-30 | 成都先进金属材料产业技术研究院有限公司 | The method of sodium vanadium extracting waste water resource utilization |
| CN111500867A (en) * | 2020-06-09 | 2020-08-07 | 攀钢集团攀枝花钢铁研究院有限公司 | Recovery treatment and utilization method of vanadium precipitation wastewater and vanadium trioxide dedusting and leaching water |
-
2021
- 2021-11-29 CN CN202111430781.4A patent/CN114293034B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5279804A (en) * | 1991-04-26 | 1994-01-18 | Occidental Chemical Corporation | Vanadium removal in aqueous streams |
| CN102198992A (en) * | 2011-04-08 | 2011-09-28 | 史永军 | Treatment method for vanadium precipitation mother liquor wastewater |
| CN104086032A (en) * | 2014-07-30 | 2014-10-08 | 攀钢集团攀枝花钢钒有限公司 | Method for recycling vanadium precipitating wastewater |
| CN105950865A (en) * | 2016-05-17 | 2016-09-21 | 沈阳理工大学 | Method for separating and extracting vanadium and chromium from high-chromium vanadium leaching liquid |
| CN108911237A (en) * | 2018-07-11 | 2018-11-30 | 成都先进金属材料产业技术研究院有限公司 | The method of sodium vanadium extracting waste water resource utilization |
| CN111500867A (en) * | 2020-06-09 | 2020-08-07 | 攀钢集团攀枝花钢铁研究院有限公司 | Recovery treatment and utilization method of vanadium precipitation wastewater and vanadium trioxide dedusting and leaching water |
Non-Patent Citations (1)
| Title |
|---|
| 蒋道利;王丹;王海元;: "分步结晶技术在酸性铵盐沉钒废水处理中的应用" * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114293034B (en) | 2023-09-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3473738B1 (en) | Process for recovering components from pickling acid residue | |
| CN108559843B (en) | Method for treating stone coal pickle liquor | |
| DE2558160B2 (en) | Process for cleaning technical molybdenum oxide | |
| US3458277A (en) | Process for the recovery of molybdenum values as high purity ammonium paramolybdate from impure molybdenum-bearing solution,with optional recovery of rhenium values if present | |
| DE2743812B1 (en) | Process for processing non-ferrous metal hydroxide sludge waste | |
| CN108754191A (en) | A method of processing bone coal pickle liquor | |
| DE112022002565T5 (en) | METHOD FOR THE SELECTIVE RECOVERY OF VALUABLE METALS IN WASTE LITHIUM BATTERIES | |
| CN110423901B (en) | Method for separating sodium vanadium chromium from vanadium chromium solution | |
| US11071967B2 (en) | Method of preparation and application of ion-keeper adsorbent | |
| CN103964624A (en) | Recycling method of ammonium salt precipitating vanadium wastewater | |
| CN111485105B (en) | Method for recovering acid liquor and separating vanadium in process of reducing, acid leaching and vanadium-containing waste catalyst | |
| CN110627179A (en) | Method for treating arsenic-containing wastewater by using recyclable composite salt precipitator | |
| DE2546425A1 (en) | HYDROMETALLURGICAL EXTRACTION OF TECHNICAL MOLYBDAENITE TRIOXIDE FROM MOLYBDAENITE CONCENTRATES | |
| CN114293034B (en) | Method for extracting vanadium from sodium-modified vanadium-containing clinker by utilizing vanadium precipitation wastewater | |
| AU2006260586B2 (en) | Chemical beneficiation of raw material, containing tantalum-niobium | |
| CN116715270A (en) | Method for removing impurity ions in sodium dichromate mother solution by hydration of chromium oxide | |
| CN112320847B (en) | Method for extracting vanadium from high-phosphate vanadium solution and recycling wastewater | |
| CN110983054B (en) | Method for separating and recovering cobalt and nickel from manganese sulfate solution | |
| RU2398902C1 (en) | Procedure for hydro-metallurgical treatment of rhenium containing molybdenum concentrate | |
| CN112575189B (en) | Treatment method of high-chromium high-magnesium platinum group metal ore dressing concentrate strengthening leaching solution | |
| DE2229256B2 (en) | Extraction of materials containing refractory metals | |
| CH677921A5 (en) | ||
| JP3780358B2 (en) | Treatment method for petroleum combustion ash | |
| CN114350933A (en) | Sodium removal method for vanadium extraction residue by sodium method | |
| DE3148227A1 (en) | RECOVERY OF COPPER FROM ARSENOUS SLAG |
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 |