CN111321311A - Method for extracting vanadium by converting vanadium slag into salt twice - Google Patents
Method for extracting vanadium by converting vanadium slag into salt twice Download PDFInfo
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- CN111321311A CN111321311A CN202010339708.5A CN202010339708A CN111321311A CN 111321311 A CN111321311 A CN 111321311A CN 202010339708 A CN202010339708 A CN 202010339708A CN 111321311 A CN111321311 A CN 111321311A
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B34/00—Obtaining refractory metals
- C22B34/20—Obtaining niobium, tantalum or vanadium
- C22B34/22—Obtaining vanadium
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/04—Working-up slag
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Abstract
The invention belongs to the technical field of vanadium metallurgy, and particularly relates to a method for extracting vanadium by converting vanadium slag into salts twice. The invention aims to solve the technical problem of providing a method for extracting vanadium by converting vanadium slag into salts twice. The method comprises the following steps: a. oxidizing and roasting the vanadium slag to obtain a first clinker, and performing first carbonation leaching to obtain a first leaching residue and a first leaching solution; b. oxidizing the first leaching residue into salt, converting and roasting to obtain a second clinker, and performing second carbonation leaching to obtain a second leaching residue and a second leaching solution; c. adjusting the pH value of the first leaching solution, crystallizing and separating ammonium metavanadate/sodium metavanadate, and returning the mother solution as a leaching agent to the second carbonation leaching for recycling; the second leaching liquid is used as a leaching agent and returns to the first carbonation leaching for recycling. The method does not need to prepare a salt additive, can reduce the vanadium content in the leaching residue, improves the vanadium leaching rate, and has small vanadium leaching rate fluctuation.
Description
Technical Field
The invention belongs to the technical field of vanadium metallurgy, and particularly relates to a method for extracting vanadium by converting vanadium slag into salts twice.
Background
Vanadium slag is a main raw material for extracting vanadium oxide, and at present, two main industrial processes for extracting vanadium are vanadium slag sodium roasting conversion-water leaching-ammonium vanadate precipitation (sodium treatment process), vanadium slag calcification roasting conversion-sulfuric acid leaching-vanadate precipitation (calcification process). The vanadium extraction tailings generated in the sodium treatment process are high in sodium oxide content and difficult to reutilize, and the vanadium precipitation wastewater is treated to obtain by-products, namely solid waste sodium sulfate and vanadium-chromium reduction filter cakes, which are large in quantity and difficult to treat. The tailings generated by the calcification process have high sulfur content and are difficult to be reused, and a large amount of gypsum slag containing vanadium and manganese is generated by treating the vanadium precipitation wastewater and is difficult to be utilized.
The Master's thesis published by Li Jing in 2014 4/1 discloses a laboratory study on low-calcification vanadium extraction from steel vanadium slag, which uses vanadium slag (component V)2O517.03 percent, CaO1.85 percent, MgO3.27 percent and MnO6.00 percent) as raw materials, and the raw materials are blank roasted at the temperature of 850 ℃, and the vanadium leaching rate of the clinker carbonation leaching is 77.20 percent. The 'vanadium slag blank roasting cleaning vanadium extraction process' published in 2019, 8 months, volume 40, No. 4, of 'iron vanadium titanium', and the vanadium slag (component V)2O517.05 percent, CaO2.48 percent, MgO2.19 percent and MnO10.34 percent) as raw materials, and roasting the raw materials at the temperature of 860-900 ℃ in a blank way, wherein the vanadium leaching rate of the clinker carbonation leaching is 90.49-92.12 percent.
The two vanadium slag vanadium extraction processes solve the problem of high content of alkali metal/sulfur in the residue, but cannot fundamentally solve the problem of large fluctuation of vanadium leaching rate caused by the inherent quality difference of the vanadium slag, and are difficult to popularize and apply on an industrial production line.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method for extracting vanadium by converting vanadium slag into salts twice. The method comprises the following steps:
a. oxidizing and roasting the vanadium slag to obtain a first clinker, and performing first carbonation leaching to obtain a first leaching residue and a first leaching solution;
b. oxidizing the first leaching residue into salt, converting and roasting to obtain a second clinker, and performing second carbonation leaching to obtain a second leaching residue and a second leaching solution;
c. adjusting the pH value of the first leaching solution, crystallizing and separating ammonium metavanadate/sodium metavanadate, and returning the mother solution as a leaching agent to the second carbonation leaching for recycling; the second leaching liquid is used as a leaching agent and returns to the first carbonation leaching for recycling.
Further, in the step a, the oxidizing roasting temperature is 800-850 ℃; the roasting time is 60-120 min.
Further, in step a, the leaching agent adopted in the first carbonation leaching and the second carbonation leaching is an aqueous solution prepared from at least one of sodium carbonate or sodium bicarbonate; the mass concentration of sodium ions in the leaching agent is 38-48 g/L.
Further, the leaching temperature of the first carbonation leaching and the second carbonation leaching is 70-100 ℃; the leaching time is 20-180 min.
Further, in the step a, the vanadium slag is oxidation slag obtained by oxidizing and blowing vanadium-containing molten iron in a converter or a shaking ladle; the particle size of the vanadium slag is less than or equal to 0.125 mm.
Further, in the step b, the temperature of the oxidation salt conversion roasting is 850-900 ℃; the roasting time is 60-120 min.
Further, the liquid-solid ratio of the first carbonation leaching and the second carbonation leaching is 1.5-3 mL:1 g.
Further, the ammonium salt used for crystallizing and separating the ammonium metavanadate/sodium metavanadate from the first leaching solution is at least one of ammonium carbonate, ammonium bicarbonate or ammonia water.
Further, mother liquor obtained after crystallization separation of ammonium metavanadate/sodium metavanadate and secondary leachate are adopted in the primary leachate, sodium carbonate or sodium bicarbonate is supplemented to the secondary leachate until the mass concentration of sodium ions is 38-48 g/L, and then the primary leachate is used as a leaching agent for recycling.
Further, in the step c, carbon dioxide is adopted to adjust the pH value of the first leaching solution to 8-9.
The invention has the beneficial effects that:
the invention provides a method suitable for extracting vanadium from vanadium slag obtained by oxidizing and converting vanadium-containing molten iron, which converts vanadium in the vanadium slag into vanadate through two salt-forming conversions, and separates the vanadate into a vanadium solution by utilizing a carbonation leaching process to realize extraction of the vanadium in the vanadium slag. The invention fully utilizes salifying components carried by the vanadium slag, does not need to be prepared into salt additives, and omits the technical process of mixing ingredients. The salification conversion process is carried out by two times, so that the problem of thermal balance of salification conversion overshoot can be solved, and the salification process is smooth. The mother liquor obtained after the crystallization separation of the ammonium metavanadate/sodium metavanadate in the vanadium solution is circularly used for leaching vanadate, so that the problem of recycling of a leaching medium is solved. The method can greatly reduce the vanadium content in the leaching residue, thereby improving the vanadium leaching rate with small fluctuation. The invention fundamentally solves the problems of high alkali metal/sulfur content in the leaching residue, large consumption of the leaching agent, large secondary solid waste amount, high cost and the like, and has wide application prospect.
Detailed Description
Specifically, the invention provides a method for extracting vanadium by converting vanadium slag into salts twice. The method comprises the following steps:
a. oxidizing and roasting vanadium slag with the particle size of less than or equal to 0.125mm at 800-850 ℃ for 60-120 min to obtain first clinker, crushing the first clinker to the particle size of less than or equal to 0.096mm, taking an aqueous solution prepared from at least one of sodium carbonate or sodium bicarbonate as a leaching agent, controlling the mass concentration of sodium ions in the leaching agent to be 38-48 g/L, and performing primary carbonation leaching on the leaching agent and the first clinker at 70-100 ℃ for 20-180 min according to the liquid-solid ratio of 1.5-3 mL:1g to obtain first leaching residue and first leaching liquid;
b. oxidizing the first leaching residue at 850-900 ℃ to form a salt, converting and roasting for 60-120 min to obtain a second clinker, crushing the second clinker to a granularity of less than or equal to 0.096mm, taking an aqueous solution prepared from at least one of sodium carbonate or sodium bicarbonate as a leaching agent, controlling the mass concentration of sodium ions in the leaching agent to be 38-48 g/L, and performing secondary carbonation leaching for 20-180 min at 70-100 ℃ on the leaching agent and the second clinker according to a liquid-solid ratio of 1.5-3 mL:1g to obtain a second leaching residue and a second leaching solution;
c. adjusting the pH value of the primary leachate to 8-9 by using carbon dioxide, crystallizing and separating ammonium metavanadate/sodium metavanadate, supplementing sodium carbonate or sodium bicarbonate to the mother liquor until the mass concentration of sodium ions is 38-48 g/L, and returning the mother liquor as a leaching agent to the secondary carbonation leaching for recycling; and supplementing sodium carbonate or sodium bicarbonate to the second leaching solution until the mass concentration of sodium ions is 38-48 g/L, and returning the second leaching solution as a leaching agent to the first carbonation leaching for recycling.
The vanadium slag is oxidized slag obtained by oxidizing and blowing vanadium-containing molten iron through a converter or a shaking ladle; the main component in the vanadium slag is 10-25% V2O5、13～19％SiO2、5～10％MnO、1～5％MgO、1.5～3.5％CaO、35～55％FeO、8～12％TiO2. The purpose of controlling the particle size of the vanadium slag to be less than or equal to 0.125mm is to fully expose vanadium-containing spinel in the vanadium slag and facilitate the oxidation and salt formation conversion of the vanadium-containing spinel.
The basic principle of the reaction of the invention is as follows:
a first salt forming reaction:
4FeV2O4+4CaO+5O2＝4Ca(VO3)2+2Fe2O3
4FeV2O4+4MnO+5O2＝4Mn(VO3)2+2Fe2O3
4FeV2O4+4MgO+5O2＝4Mg(VO3)2+2Fe2O3
first carbonation leaching reaction:
Ca(VO3)2+Na2CO3＝2NaVO3(aq)+CaCO3↓
Mn(VO3)2+Na2CO3＝2NaVO3(aq)+MnCO3↓
Mg(VO3)2+Na2CO3＝2NaVO3(aq)+MgCO3↓
in the first oxidation roasting salt-forming reaction process, vanadium in the vanadium slag and salt-forming components CaO, MnO and MgO of the vanadium slag generate corresponding vanadate Ca (VO)3)2、Mn(VO3)2、Mg(VO3)2(ii) a In the first carbonation leaching process, double decomposition reaction of vanadate and leaching agent is carried out to generate water-soluble sodium vanadate and water-insoluble carbonate, and the water-insoluble carbonate enters the first leaching residue. When the content of salt forming components carried by the vanadium slag is enough, vanadium in the vanadium slag can be fully converted into vanadate, and the leaching rate of the vanadium is high during carbonation leaching; on the contrary, when the content of the salt-forming component of the vanadium slag is insufficient, only part of vanadium in the vanadium slag can be converted into vanadate, and the leaching rate of the vanadium is low during carbonation leaching.
And (3) secondary salt forming reaction:
4FeV2O4+4CaCO3+5O2＝4Ca(VO3)2+2Fe2O3+4CO2↑
4FeV2O4+4MnCO3+5O2＝4Mn(VO3)2+2Fe2O3+4CO2↑
4FeV2O4+4MgCO3+5O2＝4Mg(VO3)2+2Fe2O3+4CO2↑
and (3) second carbonation leaching reaction:
Ca(VO3)2+Na2CO3＝2NaVO3(aq)+CaCO3↓
Mn(VO3)2+Na2CO3＝2NaVO3(aq)+MnCO3↓
Mg(VO3)2+Na2CO3＝2NaVO3(aq)+MgCO3↓
during the second salt-forming reaction, the CaCO produced by the first carbonation leaching3、MnCO3、MgCO3Utilized as a salt-forming component to generate corresponding vanadate Ca (VO)3)2、Mn(VO3)2、Mg(VO3)2. Therefore, no matter the content of the salt-forming components of the vanadium slag is high or low, the vanadium slag leaching residue is subjected to secondary treatment, vanadium in the vanadium slag can be fully converted into vanadate, and the vanadium leaching rate in carbonation leaching is improved. After the second carbonating leaching, the salified component is CaCO3、MnCO3、MgCO3The mixture enters a residue to be discharged out of the system.
Salt-forming components carried by the vanadium slag participate in salt-forming reaction twice, so that the full conversion of vanadium is ensured, the problem of insufficient vanadium conversion caused by insufficient salt-forming components carried by the vanadium slag in the existing blank roasting process of the vanadium slag is solved, and the conversion leaching rate of the vanadium is improved. Meanwhile, the conversion is carried out in two steps, which is beneficial to controlling the conversion temperature and enables the conversion process to be stable and controlled.
The leaching temperature is controlled to be 70-100 ℃ during the leaching reaction so as to be beneficial to the dissolution of vanadate. The carbonate leaching is utilized because the carbonate solubility of calcium, magnesium and manganese is lower than that of vanadate, calcium, magnesium and manganese ions are combined with carbonate and remain in slag, and vanadium enters a solution in the form of vanadate.
The mass concentration of sodium ions in the leaching agent is controlled to be 38-48 g/L, so that a vanadium solution with better sodium vanadium is obtained, and the leaching agent is beneficial to leaching vanadium and crystallization separation of ammonium metavanadate/sodium metavanadate.
The invention aims to obtain the better vanadium concentration by controlling the solid-to-solid ratio of the leaching solution to be 1.5-3 mL:1 g.
The method utilizes the carbon dioxide to reduce the pH value of the vanadium solution and convert the carbon dioxide into anions of the leaching agent.
The invention crushes the first clinker and the first clinker to the granularity of less than or equal to 0.096mm, which aims to increase the specific surface area of the clinker and improve the dynamics of the vanadate during carbonation leaching.
The present invention will be further illustrated by the following specific examples.
Example 1
Taking vanadium slag (containing V) with the particle size less than or equal to 0.125mm2O518.95 percent, CaO1.94 percent, MgO1.76 percent and MnO7.53 percent) of the total weight of the raw materials are put into a muffle furnace, oxidized and autorotation roasting is carried out for 120min at 800 ℃ under the condition of introducing air to obtain first clinker, the first clinker is crushed to the granularity of less than or equal to 0.096mm and then added into 300mL of first carbonation leaching agent, stirring and leaching are carried out for 20min at the slurry temperature of 100 ℃, solid-liquid separation is carried out to obtain first leachate and first leaching residue, and V is contained in the first leaching residue2O56.03 wt%. Oxidizing the first leaching residue in a muffle furnace at the roasting temperature of 900 ℃ and introducing air for conversion roasting for 120 min; pulverizing the second clinker to particle size of 0.096mm or less, adding into 300mL of second carbonation leaching agent, leaching at slurry temperature of 100 deg.C under stirring for 100min, performing solid-liquid separation to obtain second leachate and second leaching residue, and separating the second leaching residue V2O50.82wt％。
Sodium bicarbonate was added to the second leach solution to a sodium ion concentration of 38-48 g/L, and the second leach solution was used as the first carbonation leach agent in example 2. The pH value of the first leachate is adjusted to 8 by using carbon dioxide, ammonium metavanadate is crystallized by using ammonium bicarbonate, and sodium bicarbonate is supplemented to the crystallization mother liquor until the sodium ion concentration is 38-48 g/L, so that the first leachate is used as a second carbonation leaching agent for example 2.
Example 2
Taking vanadium slag (containing V) with the particle size less than or equal to 0.125mm2O518.95 percent, CaO1.94 percent, MgO1.76 percent and MnO7.53 percent) of the raw materials are put into a muffle furnace, oxidized and converted and roasted for 80min at 850 ℃ under the condition of introducing air to obtain first clinker, the first clinker is crushed to the granularity of less than or equal to 0.096mm and then added into 250mL of the leaching agent obtained in the example 1, the mixture is stirred and leached for 180min under the condition that the slurry temperature is 70 ℃, solid-liquid separation is carried out to obtain first leachate and first leaching residue, and V in the first leaching residue2O55.48 wt%. Oxidizing the first leaching residue in a muffle furnace at the roasting temperature of 850 ℃ and introducing air for salt conversion roasting for 100min, crushing the second clinker until the granularity is less than or equal to 0.096mm, adding the crushed second clinker into 250mL of the leaching agent obtained in the example 1, and heating the slurry to a temperature of belowLeaching at 100 deg.C for 100min under stirring, separating solid and liquid to obtain second leaching solution and second leaching residue, and collecting second leaching residue V2O50.75wt％。
The second leach solution was supplemented with sodium carbonate to a sodium ion concentration of 38-48 g/L and used as the first carbonation leach in example 3. The pH value of the first leachate is adjusted to 9 by using carbon dioxide, ammonium metavanadate is crystallized by using ammonium carbonate, sodium carbonate is supplemented to the crystallization mother liquor until the concentration of sodium ions is 38-48 g/L, and the first leachate is used as a second carbonation leaching agent for example 3.
Example 3
Taking vanadium slag (containing V) with the particle size less than or equal to 0.125mm2O518.95 percent, CaO1.94 percent, MgO1.76 percent and MnO7.53 percent) of the total weight of the raw materials are put into a muffle furnace, oxidized and self-converted roasting is carried out for 100min at 830 ℃ under the condition of introducing air to obtain first clinker, the first clinker is crushed to the granularity of less than or equal to 0.096mm and then added into 150mL of the leaching agent obtained in the example 2, stirring and leaching are carried out for 120min at the slurry temperature of 100 ℃, solid-liquid separation is carried out to obtain first leachate and first leaching residue, and V in the first leaching residue is2O55.63 wt%. Oxidizing the first leaching residue in a muffle furnace at a roasting temperature of 880 ℃ and introducing air to convert into salt and roast for 70 min; crushing the second clinker to a particle size of less than or equal to 0.096mm, adding the crushed second clinker into 150mL of the leaching agent obtained in the example 2, stirring and leaching for 100min at the slurry temperature of 100 ℃, performing solid-liquid separation to obtain a second leaching solution and a second leaching residue, and performing secondary leaching residue V2O50.73wt％。
The second leach solution was supplemented with sodium carbonate to a sodium ion concentration of 38-48 g/L and used as the first carbonation leach agent in example 4. The pH value of the first leachate is adjusted to 8.5 by using carbon dioxide, ammonium metavanadate is crystallized by using ammonium carbonate, sodium carbonate is supplemented to the crystallization mother liquor until the concentration of sodium ions is 38-48 g/L, and the first leachate is used as a second carbonation leaching agent for example 4.
Example 4
Taking vanadium slag (containing V) with the particle size less than or equal to 0.125mm2O518.95%, CaO1.94%, MgO1.76%, MnO7.53%), put in a muffle furnace, and introduced into a furnaceOxidizing and self-converting roasting at 830 deg.C for 120min under the condition of air to obtain first clinker, pulverizing the first clinker to-0.096 mm, adding into 150mL of leaching agent obtained in example 3, stirring and leaching at slurry temperature of 100 deg.C for 120min, performing solid-liquid separation to obtain first leachate and first leaching residue, and separating V from the first leaching residue2O55.68 wt%. Oxidizing the first leaching residue in a muffle furnace at a roasting temperature of 880 ℃ and introducing air to convert into salt and roast for 80 min; crushing the second clinker to a particle size of less than or equal to 0.096mm, adding the crushed second clinker into 150mL of the leaching agent obtained in the example 3, stirring and leaching for 100min at the slurry temperature of 100 ℃, performing solid-liquid separation to obtain a second leaching solution and a second leaching residue, and performing second leaching residue V2O50.75wt％。
And supplementing sodium carbonate to the second leaching solution until the concentration of sodium ions is 38-48 g/L, and recycling the second leaching solution as a first carbonation leaching agent. Adjusting the pH value of the first leaching solution to 8 by using carbon dioxide, concentrating and crystallizing sodium metavanadate, supplementing sodium carbonate to the crystallization mother solution until the concentration of sodium ions is 38-48 g/L, and recycling the sodium metavanadate as a second carbonation leaching agent.
Claims (10)
1. The method for extracting vanadium by converting vanadium slag into salts twice is characterized by comprising the following steps: the method comprises the following steps:
a. oxidizing and roasting the vanadium slag to obtain a first clinker, and performing first carbonation leaching to obtain a first leaching residue and a first leaching solution;
b. oxidizing the first leaching residue into salt, converting and roasting to obtain a second clinker, and performing second carbonation leaching to obtain a second leaching residue and a second leaching solution;
c. adjusting the pH value of the first leaching solution, crystallizing and separating ammonium metavanadate/sodium metavanadate, and returning the mother solution as a leaching agent to the second carbonation leaching for recycling; the second leaching liquid is used as a leaching agent and returns to the first carbonation leaching for recycling.
2. The method for extracting vanadium by twice converting vanadium slag into salts according to claim 1, is characterized in that: in the step a, the oxidizing roasting temperature is 800-850 ℃; the roasting time is 60-120 min.
3. The method for extracting vanadium by twice converting vanadium slag into salts according to claim 1 or 2, characterized by comprising the following steps: in the step a, the leaching agent adopted in the first carbonation leaching and the second carbonation leaching is an aqueous solution prepared from at least one of sodium carbonate or sodium bicarbonate; the mass concentration of sodium ions in the leaching agent is 38-48 g/L.
4. The method for extracting vanadium by twice conversion of vanadium slag into salts according to any one of claims 1 to 3, characterized by comprising the following steps: the leaching temperature of the first carbonation leaching and the second carbonation leaching is 70-100 ℃; the leaching time is 20-180 min.
5. The method for extracting vanadium by twice conversion of vanadium slag into salts according to any one of claims 1 to 4, characterized by comprising the following steps: in the step a, the vanadium slag is oxidation slag obtained by oxidizing and blowing vanadium-containing molten iron through a converter or a shaking ladle; the particle size of the vanadium slag is less than or equal to 0.125 mm.
6. The method for extracting vanadium by twice conversion of vanadium slag into salts according to any one of claims 1 to 5, characterized by comprising the following steps: in the step b, the temperature of the oxidation salt-forming conversion roasting is 850-900 ℃; the roasting time is 60-120 min.
7. The method for extracting vanadium by twice conversion of vanadium slag into salts according to any one of claims 1 to 6, characterized by comprising the following steps: the liquid-solid ratio of the first carbonation leaching and the second carbonation leaching is 1.5-3 mL:1 g.
8. The method for extracting vanadium by twice conversion of vanadium slag into salts according to any one of claims 1 to 7, characterized by comprising the following steps: and the ammonium salt adopted by crystallizing and separating the ammonium metavanadate/sodium metavanadate in the first leaching solution is at least one of ammonium carbonate, ammonium bicarbonate or ammonia water.
9. The method for extracting vanadium by twice conversion of vanadium slag into salts according to any one of claims 1 to 8, characterized by comprising the following steps: and the first leaching solution adopts mother liquor obtained after crystallization separation of ammonium metavanadate/sodium metavanadate and the second leaching solution to supplement sodium carbonate or sodium bicarbonate until the mass concentration of sodium ions is 38-48 g/L, and then the first leaching solution and the second leaching solution are used as leaching agents for recycling.
10. The method for extracting vanadium by twice converting vanadium slag into salts according to claims 1 to 9, which is characterized by comprising the following steps: in the step c, adjusting the pH value of the first leaching solution to 8-9 by using carbon dioxide.
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Cited By (2)
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| CN114134346A (en) * | 2021-11-30 | 2022-03-04 | 大连理工大学 | Continuous ionic membrane sodium removal-vanadium precipitation method |
| WO2023279142A1 (en) * | 2021-07-08 | 2023-01-12 | Avanti Materials Ltd | Recovery of vanadium from leach residues using combined hydrometallurgical and pyrometallurgical process |
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| CN114134346B (en) * | 2021-11-30 | 2022-08-12 | 大连理工大学 | Continuous ionic membrane sodium removal-vanadium precipitation method |
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Application publication date: 20200623 |