CN107177740B - Method for recovering aluminum from refining slag - Google Patents
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- CN107177740B CN107177740B CN201710347451.6A CN201710347451A CN107177740B CN 107177740 B CN107177740 B CN 107177740B CN 201710347451 A CN201710347451 A CN 201710347451A CN 107177740 B CN107177740 B CN 107177740B
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
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Abstract
The invention provides a method for recovering aluminum from refining slag, which comprises the following steps: mixing the refining slag and NaOH solution to obtain slurry; introducing CO into the slurry2Gas, heating and reactingObtaining solid-liquid mixed slurry; and carrying out solid-liquid separation to obtain a sodium aluminate solution. The method has the advantages of simple process, easy operation and low energy consumption, can realize high-efficiency recovery of aluminum in the refining slag, and the recovery rate of the aluminum can reach more than 90 percent. The invention can utilize CO generated by enterprises2The waste gas is produced, the comprehensive utilization of the waste gas is realized, and meanwhile, micron-sized bubbles are blown into the system by adopting the micropore gas distribution device, so that the carbonation reaction time is shortened, the energy waste is reduced, and the cost is reduced. Is beneficial to popularization in industrial production, and has good economic benefit and wide application prospect.
Description
Technical Field
The invention relates to the field of metallurgy, in particular to a method for recovering aluminum from refining slag.
Background
The refining slag is one of steel slag, and the yield accounts for about 5 percent of the total yield of the steel slag. With the continuous increase of steel output in China, the ladle refining furnace is widely applied as a main external treatment means, so that a large amount of refining waste residues are generated in the steel production process. The refining slag contains a significant amount of the metal being refined, in addition to the impurities being removed and the flux reactants being added. When the refining slag contains less impurity elements, the refining slag can be returned to the pre-smelting operation treatment to recover the refined metal and valuable impurity elements; when the amount of the impurity elements is large, the impurity elements can be treated separately to recover valuable impurity elements.
As a valuable element in refining slag, the recovery of aluminum element is always the focus of research in the steel industry. However, because the components in the refining slag are complex, a plurality of solid phases form a structure which is mutually mixed and wrapped, the recovery of aluminum in the refining slag is difficult, and the aluminum is difficult to be utilized in a large scale. Particularly, in the high-Si refining slag, the recovery of aluminum is more difficult. Therefore, how to utilize the aluminum element in the refining slag with high efficiency is a difficult problem in the field.
CN101402460A discloses a method for preparing aluminum silicate by using LF furnace refining slag, which comprises the steps of adding sulfuric acid with a certain concentration into the crushed, magnetically separated and ground LF furnace refining slag, carrying out acidolysis at 40-70 ℃ under the condition that the mass ratio of slag acid is 1/8-1/10, controlling the acidolysis time at 60min, and separating acidolysis products to remove solid gypsum to obtain a mixed solution mainly containing aluminum salt; then slowly adding the aluminum silicate into a water glass solution with a certain concentration in a streamline mode, continuously stirring in the process, controlling the pH value of the system to 4.0-5.0, aging for 30min at a constant temperature of 40 ℃, then filtering an aging product to obtain a filter cake, washing the filter cake for multiple times by using distilled water until the pH value of the system is about 6.5, then filtering, dissolving a solid isolate in water, adjusting the pH value to about 10.0 by using 11-12 wt% of the standby water glass solution, standing for 20min at a constant temperature of 40 ℃, filtering and drying to obtain the aluminum silicate. However, the acid leaching method has the disadvantages of large acid consumption, low aluminum leaching rate, complex process and complicated operation, and is not beneficial to industrial application.
CN101259969A discloses a preparation process of alumina, which comprises the steps of crushing refining slag of an LF furnace into particles with the particle size of less than 3 mm; after magnetic separation, the particles are crushed into micro powder with the particle size of less than 0.125 mm; then adding sodium carbonate solution, reacting at 70-95 ℃ for not less than 1.5 hours, and filtering to obtain soluble sodium metaaluminate solution and insoluble calcium carbonate precipitate; introducing gas rich in carbon dioxide into the sodium metaaluminate solution to generate an aluminum hydroxide precipitate and a sodium carbonate solution, filtering and drying. The method has the disadvantages that in order to fully expose the aluminum in the refining slag, a secondary crushing step is adopted to crush the refining slag into 0.125mm micro powder, the energy consumption is increased in the crushing process, and the cost is overhigh.
The method has complex process and high energy consumption, is only aiming at the refining slag with high Al content, but not suitable for the refining slag with high Si content, so a new method needs to be developed to realize the aim of simply and efficiently recovering the aluminum from the refining slag.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a method for recovering aluminum from refining slag, which can realize the high-efficiency recovery of the aluminum in the refining slag, and the recovery rate of the aluminum can reach more than 90 percent. The method has the advantages of simple process, easy operation, low cost, good safety and suitability for industrial production.
To achieve the purpose, the invention provides the following technical scheme:
the invention provides a method for recovering aluminum from refining slag, which comprises the following steps:
(1) mixing the refining slag and NaOH solution to obtain slurry;
(2) introducing CO into the slurry obtained in the step (1)2Heating the gas to react to obtain solid-liquid mixed slurry;
(3) and (3) carrying out solid-liquid separation on the solid-liquid mixed slurry obtained in the step (2) to obtain a sodium aluminate solution.
The main existing phase in the refining slag is CaO-CaF2、CaO-Al2O3And CaO-Al2O3-SiO2In which the aluminum phase is encapsulated by the calcium phase and the silicon phase, the exposed portion is small, and it is difficult to directly extract it. And the crushing of the waste water requires higher energy consumption, so that the treatment cost is increased.
In the invention, refining slag and NaOH solution are prepared into slurry, and CO is introduced into the slurry2Heating the gas to a certain temperature, adding NaOH and CO2Under the combined action of the two components, the additive can be mixed with CaO and SiO in the refining slag2And reacting to fully expose the aluminum phase to react with NaOH, thereby obtaining a sodium aluminate solution and realizing the recovery of the aluminum phase in the refining slag.
The equation for the above reaction is:
CaO-Al2O3+NaOH+CO2＝CaCO3+NaAlO2+H2O；
CaO-Al2O3-SiO2+2NaOH＝CaSiO3+2NaAlO2+H2O。
after the reaction is finished, the solid-liquid mixed slurry is subjected to solid-liquid separation to obtain tailings containing calcium carbonate, calcium silicate, magnesium carbonate and the like and a sodium aluminate solution, Ca, Si and other elements in the refining slag are effectively removed, the high-efficiency recovery of aluminum in the refining slag is realized, and the recovery rate of aluminum is over 90 percent.
Some impurity elements also exist in the sodium aluminate solution obtained after the solid-liquid separation in the step (3), and the impurity can be removed by adopting a conventional method in the field to obtain a pure sodium aluminate solution. Illustratively, the obtained sodium aluminate solution can be diluted to the concentration of the sodium hydroxide solution of about 300g/L, added with CaO and reacted in a stirred tank reactor at a temperature of about 85 ℃ for 1.5h to remove Si impurities.
According to the invention, the refining slag is subjected to crushing, iron selection and grinding in sequence before the step (1). The crushing, iron selection and grinding modes are conventional methods in the field, and are not described in detail.
According to the invention, the grain size of the refined slag after crushing is 400-600 meshes, such as 400 meshes, 420 meshes, 440 meshes, 460 meshes, 480 meshes, 500 meshes, 520 meshes, 540 meshes, 560 meshes, 580 meshes or 600 meshes, and the specific values between the above values are limited by space and for the sake of brevity, and the invention is not exhaustive.
According to the invention, the mass ratio of the refining slag to the NaOH solution in step (1) is (2-7):1, and may be, for example, 2:1, 3:1, 4:1, 5:1, 6:1 or 7:1, and the specific values between the above values are not exhaustive, and the invention is not limited to the specific values included in the ranges for brevity and conciseness.
According to the invention, the concentration of the NaOH solution in step (1) is 60-80 wt%, for example 60 wt%, 63 wt%, 65 wt%, 67 wt%, 70 wt%, 72 wt%, 75 wt%, 78 wt% or 80 wt%, and the specific values between the above values, which are limited by space and for the sake of brevity, are not exhaustive and do not list the specific values included in the range.
According to the invention, the operation of step (2) is carried out under stirring conditions, favouring CO2The gas is fully contacted with the slurry, so that the reaction speed is accelerated.
According to the invention, the stirring speed is 200-300r/min, such as 200r/min, 210r/min, 220r/min, 230r/min, 240r/min, 250r/min, 260r/min, 270r/min, 280r/min, 290r/min or 300r/min, and the specific values therebetween are limited for the sake of brevity and brevity, the invention is not exhaustive.
According to the invention, in the step (2), CO is introduced into the slurry through a micropore gas distribution device2The gas is blown into micron-sized bubbles in the system by adopting a micropore gas distribution device, so that CO is greatly increased2Dispersing in alkaline solution medium to increase CO2The opportunity of contact reaction with the refining slag particles shortens the carbonation reaction time and saves the energy consumption.
The microporous aeration head is arranged in the microporous air distribution device, is a conventional aeration head and can be obtained by market purchase. During operation, the aeration is carried out through the microporous aeration head, so that the introduced CO is introduced2The gas forms bubbles.
According to the present invention, the diameter of the micro-pores of the micro-pore aeration head is 1-100 μm, for example, 1 μm, 5 μm, 10 μm, 20 μm, 30 μm, 40 μm, 50 μm, 60 μm, 70 μm, 80 μm, 90 μm or 100 μm, and the specific values therebetween are not exhaustive, and the invention is not limited to the specific values included in the range for brevity and conciseness.
According to the invention, the CO2The gas forms bubbles in the microporous gas distribution means, said bubbles having a diameter of 5-80 μm, for example 5 μm, 10 μm, 20 μm, 30 μm, 40 μm, 50 μm, 60 μm, 70 μm, or 80 μm, and the specific points between the above values, which are not meant to be exhaustive for reasons of space and simplicity, are included in the scope of the invention.
According to the present invention, the heating temperature in step (2) is 160-250 ℃, and may be, for example, 160 ℃, 170 ℃, 180 ℃, 190 ℃, 200 ℃, 210 ℃, 220 ℃, 230 ℃, 240 ℃ or 250 ℃, and the specific values therebetween are not limited to the space and for the sake of brevity, and the present invention is not exhaustive list of the specific values included in the range.
According to the invention, the reaction time of step (2) is 2-6h, for example 2h, 2.5h, 3h, 3.5h, 4h, 4.5h, 5h, 5.5h or 6h, and the specific values between the above values are not exhaustive for the sake of brevity and simplicity.
According to the invention, the reaction of step (2) is carried out at atmospheric pressure. Therefore, the reaction is carried out in an atmospheric reaction vessel.
According to the present invention, the solid-liquid mixed slurry obtained in step (2) is diluted before step (3).
Because the concentration of NaOH in the obtained solid-liquid mixed slurry is high in viscosity and difficult to separate solid from liquid, and the concentration of NaOH is more favorable for desiliconization when the concentration is 300-450g/L, the invention selects to add water to the solid-liquid mixed slurry for dilution. The concentration of NaOH in the diluted solid-liquid mixed slurry is 300-450g/L, such as 300g/L, 330g/L, 350g/L, 370g/L, 400g/L, 420g/L or 450g/L, and the specific values therebetween are limited to the space and for the sake of brevity, and the invention is not exhaustive.
According to the present invention, the temperature of the solid-liquid mixed slurry in the solid-liquid separation in the step (3) is 100-150 ℃, for example, 100 ℃, 105 ℃, 110 ℃, 115 ℃, 120 ℃, 125 ℃, 130 ℃, 135 ℃, 140 ℃, 145 ℃ or 150 ℃, and the specific values between the above values are limited to space and for the sake of brevity, and the present invention is not exhaustive list of the specific values included in the range.
The solid-liquid separation in step (3) of the present invention is performed by a method known in the art, and is not particularly limited, and for example, filtration, suction filtration, etc. may be used, but not limited thereto.
As a preferable technical scheme, the method for recovering the aluminum from the refining slag comprises the following steps:
(1) crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing the refining slag ground in the step (1) and NaOH solution with the concentration of 60-80 wt% into slurry according to the mass ratio of 1 (2-7);
(3) under the stirring condition of 200-300r/min, CO is distributed through a micropore gas distribution device2Forming bubbles with the diameter of 0.5-100 mu m by gas, and introducing the bubbles into the mixture obtained in the step (1)Heating the slurry to 160-250 ℃ under normal pressure to react for 2-6h to obtain solid-liquid mixed slurry;
(4) and (3) diluting the solid-liquid mixed slurry obtained in the step (2) until the concentration of NaOH is 300-450g/L, and then carrying out solid-liquid separation at the temperature of 100-150 ℃ to obtain a sodium aluminate solution.
Compared with the prior art, the invention has at least the following beneficial effects:
(1) effectively destroy calcium phase and silicon phase in the refining slag, realize the high-efficient recovery of aluminum in the refining slag, and the recovery rate reaches more than 90 percent.
(2) Effectively utilize CO generated by enterprises2The waste gas is produced, the comprehensive utilization of the waste gas is realized, the purpose of emission reduction is achieved, and the economic benefit is increased.
(3) Micron-sized bubbles are blown into the system by adopting the micropore gas distribution device, so that the carbonation reaction time is shortened, the energy waste is reduced, the energy consumption is saved, and the cost is reduced.
(4) Simple process, easy operation and good safety, and is beneficial to popularization in industrial production.
Drawings
FIG. 1 is a process flow diagram provided by one embodiment of the present invention.
Detailed Description
In order to better illustrate the present invention and facilitate the understanding of the technical solutions of the present invention, the present invention is further described in detail below. The following examples are merely illustrative of the present invention and do not represent or limit the scope of the claims, which are defined by the claims.
The present invention provides, in a specific embodiment, a method for recovering aluminum from a refining slag, the method comprising the steps of:
(1) mixing the refining slag and NaOH solution to obtain slurry;
(2) introducing CO into the slurry obtained in the step (1)2Heating the gas to react to obtain solid-liquid mixed slurry;
(3) and (3) carrying out solid-liquid separation on the solid-liquid mixed slurry obtained in the step (2) to obtain a sodium aluminate solution.
As shown in fig. 1, a process flow provided by one embodiment of the present invention may be: crushing, selecting iron, ball milling refining slag, adding NaOH solution to prepare slurry, and introducing CO into the prepared slurry through a microporous gas distribution device2Stirring and heating the gas for reaction to obtain solid-liquid mixed slurry, carrying out solid-liquid separation on the solid-liquid mixed slurry to obtain tailings and filtrate, and adding an impurity removing agent into the filtrate for impurity removal to obtain the sodium aluminate solution.
The following are typical, but non-limiting, examples of the invention:
the embodiment of the invention partially adopts a normal-pressure heating and stirring reaction vessel for reaction, and all the raw materials are the refining slag obtained from the same batch in a steel bearing production workshop.
Example 1
(1) Crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing slurry from the ground refining slag and a NaOH solution according to a mass ratio of 7:1, wherein the mass concentration of NaOH is 80%;
(3) selecting an atmospheric pressure reactor as a reaction container, and under the stirring condition of 250r/min, leading CO to pass through a micropore gas distribution device2Forming bubbles with the diameter of 100 mu m by gas, introducing the bubbles into the slurry obtained in the step (2), heating to 250 ℃ and reacting for 6 hours to obtain solid-liquid mixed slurry;
(4) and (4) adding water to dilute the solid-liquid mixed slurry obtained in the step (3) until the concentration of NaOH is 450g/L, filtering at 150 ℃ to obtain tailings containing calcium carbonate, calcium silicate and magnesium carbonate, and removing impurities from the filtrate by adopting a conventional method to obtain a pure sodium aluminate solution.
Through the detection and analysis of the inductively coupled plasma spectrometer, the recovery rate of aluminum in the refining slag in the embodiment is 95.32%.
Example 2
(1) Crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing slurry by the ground refining slag and NaOH solution according to the mass ratio of 2:1, wherein the mass concentration of NaOH is 60%;
(3) selecting an atmospheric pressure reactor as a reaction container, and under the stirring condition of 265r/min, leading CO to pass through a micropore gas distribution device2Forming bubbles with the diameter of 0.5 mu m by gas, introducing the bubbles into the slurry obtained in the step (2), heating to 160 ℃, and reacting for 2 hours to obtain solid-liquid mixed slurry;
(4) and (4) adding water to dilute the solid-liquid mixed slurry obtained in the step (3) until the concentration of NaOH is 300g/L, filtering at 100 ℃ to obtain tailings containing calcium carbonate, calcium silicate and magnesium carbonate, and removing impurities from the filtrate by a conventional method to obtain a pure sodium aluminate solution.
Through the detection and analysis of the inductively coupled plasma spectrometer, the recovery rate of aluminum in the refining slag in the embodiment is 91.37%.
Example 3
(1) Crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing slurry by the ground refining slag and NaOH solution according to the mass ratio of 3:1, wherein the mass concentration of NaOH is 65%;
(3) selecting an atmospheric pressure reactor as a reaction container, and under the stirring condition of 240r/min, leading CO to pass through a micropore gas distribution device2Forming bubbles with the diameter of 20 microns by gas, introducing the bubbles into the slurry obtained in the step (2), heating to 180 ℃, and reacting for 6 hours to obtain solid-liquid mixed slurry;
(4) and (3) adding water to dilute the solid-liquid mixed slurry obtained in the step (3) until the concentration of NaOH is 340g/L, filtering at 110 ℃ to obtain tailings containing calcium carbonate, calcium silicate and magnesium carbonate, and removing impurities from the filtrate by a conventional method to obtain a pure sodium aluminate solution.
Through the detection and analysis of the inductively coupled plasma spectrometer, the recovery rate of aluminum in the refining slag in the embodiment is 92.42%.
Example 4
(1) Crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing slurry by the ground refining slag and NaOH solution according to the mass ratio of 4:1, wherein the mass concentration of NaOH is 70%;
(3) selecting an atmospheric pressure reactor as a reaction vesselUnder the stirring condition of 210r/min, CO is introduced through a micropore gas distribution device2Forming bubbles with the diameter of 60 mu m by gas, introducing the bubbles into the slurry obtained in the step (2), heating to 190 ℃ and reacting for 4h to obtain solid-liquid mixed slurry;
(4) and (4) adding water to dilute the solid-liquid mixed slurry obtained in the step (3) until the concentration of NaOH is 380g/L, filtering at 120 ℃ to obtain tailings containing calcium carbonate, calcium silicate and magnesium carbonate, and removing impurities from the filtrate by a conventional method to obtain a pure sodium aluminate solution.
Through the detection and analysis of the inductively coupled plasma spectrometer, the recovery rate of aluminum in the refining slag in the embodiment is 93.72%.
Example 5
(1) Crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing slurry by the ground refining slag and NaOH solution according to the mass ratio of 6:1, wherein the mass concentration of NaOH is 70%;
(3) selecting an atmospheric pressure reactor as a reaction container, and under the stirring condition of 300r/min, leading CO to pass through a micropore gas distribution device2Forming bubbles with the diameter of 75 microns by gas, introducing the bubbles into the slurry obtained in the step (2), heating to 240 ℃, and reacting for 5 hours to obtain solid-liquid mixed slurry;
(4) and (4) adding water to dilute the solid-liquid mixed slurry obtained in the step (3) until the concentration of NaOH is 410g/L, filtering at 125 ℃ to obtain tailings containing calcium carbonate, calcium silicate and magnesium carbonate, and removing impurities from the filtrate by a conventional method to obtain a pure sodium aluminate solution.
Through the detection and analysis of the inductively coupled plasma spectrometer, the recovery rate of aluminum in the refining slag in the embodiment is 91.90%.
Example 6
(1) Crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing slurry by the ground refining slag and NaOH solution according to the mass ratio of 6:1, wherein the mass concentration of NaOH is 75%;
(3) selecting an atmospheric pressure reactor as a reaction container, and under the stirring condition of 255r/min, using a micropore gas distribution device to distribute CO2Forming bubbles with the diameter of 75 microns by gas, introducing the bubbles into the slurry obtained in the step (2), heating to 235 ℃, and reacting for 5.5 hours to obtain solid-liquid mixed slurry;
(4) and (4) adding water to dilute the solid-liquid mixed slurry obtained in the step (3) until the concentration of NaOH is 430g/L, filtering at 135 ℃ to obtain tailings containing calcium carbonate, calcium silicate and magnesium carbonate, and removing impurities from the filtrate by a conventional method to obtain a pure sodium aluminate solution.
Through the detection and analysis of the inductively coupled plasma spectrometer, the recovery rate of aluminum in the refining slag in the embodiment is 94.02%.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
Claims (13)
1. A method for recovering aluminum from a refining slag, characterized in that the method comprises the following steps:
(1) mixing the refining slag with 60-80 wt% NaOH solution to obtain slurry;
(2) introducing CO into the slurry obtained in the step (1)2Heating the gas to 160-250 ℃ for reaction to obtain solid-liquid mixed slurry;
(3) carrying out solid-liquid separation on the solid-liquid mixed slurry obtained in the step (2) to obtain a sodium aluminate solution;
before the step (3), the solid-liquid mixed slurry obtained in the step (2) is diluted, and the concentration of NaOH in the diluted solid-liquid mixed slurry is 300-450 g/L.
2. The method of claim 1, wherein the refining slag is subjected to crushing, iron selection and grinding in sequence before step (1).
3. The method as claimed in claim 2, wherein the grain size of the refined slag after crushing is 400-600 mesh.
4. The method of claim 1, wherein the mass ratio of the refining slag to the NaOH solution in the step (1) is 1 (2-7).
5. The method of claim 1, wherein the operation of step (2) is performed under agitation.
6. The method as claimed in claim 5, wherein the stirring speed is 200-300 r/min.
7. The method of claim 1, wherein in step (2) CO is introduced into the slurry through a microporous gas distribution device2A gas.
8. The method of claim 7, wherein the CO is present in a gas phase2The gas forms bubbles in the micropore gas distribution device.
9. The method of claim 8, wherein the bubbles have a diameter of 5 to 80 μm.
10. The method of claim 1, wherein the reaction time of step (2) is 2-6 h.
11. The method of claim 1, wherein the reaction of step (2) is carried out at atmospheric pressure.
12. The method as claimed in claim 1, wherein the temperature of the solid-liquid mixed slurry in the solid-liquid separation in the step (3) is 100-150 ℃.
13. The method of claim 1, wherein the method comprises the steps of:
(1) crushing the refining slag to the particle size of 400-sand 600 meshes, and then sequentially carrying out iron selection and grinding;
(2) preparing the refining slag ground in the step (1) and NaOH solution with the concentration of 60-80 wt% into slurry according to the mass ratio of 1 (2-7);
(3) under the stirring condition of 200-300r/min, CO is distributed through a micropore gas distribution device2Forming bubbles with the diameter of 0.5-100 mu m by gas, introducing the bubbles into the slurry obtained in the step (1), heating the bubbles to the temperature of 160-250 ℃ under normal pressure, and reacting for 2-6h to obtain solid-liquid mixed slurry;
(4) and (3) diluting the solid-liquid mixed slurry obtained in the step (2) until the concentration of NaOH is 300-450g/L, and then carrying out solid-liquid separation at the temperature of 100-150 ℃ to obtain a sodium aluminate solution.
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| CN102094123A (en) * | 2011-01-14 | 2011-06-15 | 河北钢铁股份有限公司承德分公司 | Method for extracting vanadium from vanadium-containing steel slag by using highly-alkaline sodium hydroxide medium |
| CN105400967A (en) * | 2015-11-10 | 2016-03-16 | 中国科学院过程工程研究所 | Method for extracting chromium and vanadium from vanadium slag at low temperature and normal pressure |
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