CN116144950B - Method for leaching vanadium in waste denitration catalyst - Google Patents
Method for leaching vanadium in waste denitration catalyst Download PDFInfo
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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
- C22B34/225—Obtaining vanadium from spent catalysts
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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
- C22B7/007—Wet processes by acid leaching
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- 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
Abstract
The invention relates to the field of recovery of waste denitration catalysts, and discloses a method for leaching vanadium in the waste denitration catalysts, which comprises the following steps: (1) Placing the waste denitration catalyst into a first treatment liquid for soaking; (2) Drying and crushing the soaked waste denitration catalyst to obtain crushed materials with the granularity less than or equal to 100 meshes; (3) Mixing the crushed material with a second treatment liquid, performing ultrasonic treatment, reacting for 4-24 hours at 60-100 ℃, and performing solid-liquid separation; the first treatment liquid and the second treatment liquid are respectively titanium white waste acid or mixed liquid obtained by treating the titanium white waste acid; in the first treatment liquid, the concentration of sulfuric acid is less than or equal to 80g/L; in the second treatment liquid, the concentration of sulfuric acid is more than or equal to 150g/L, the concentration of Fe is less than or equal to 40g/L, and the concentration of Ca is less than or equal to 1.2g/L. In the invention, the titanium white waste acid is used for leaching the vanadium in the waste denitration catalyst, so that the acid consumption required by extracting the vanadium is saved, the vanadium extracting effect is excellent, and the leaching rate of the vanadium is up to more than 89%.
Description
Technical Field
The invention relates to the technical field of recovery of waste denitration catalysts, in particular to a method for leaching vanadium in waste denitration catalysts.
Background
The vanadium-titanium denitration catalyst is the denitration catalyst which is most widely applied at present, and is widely applied to the field of large coal denitration mainly in coal-fired power plants. However, the denitration catalyst is deactivated and discarded after long-term use, the discarded denitration catalyst contains a large amount of valuable metal elements, vanadium is the element with the highest value in the denitration catalyst, and separation of vanadium has important significance for recycling the discarded denitration catalyst.
The titanium white waste acid is the waste acid produced by producing titanium dioxide by adopting a sulfuric acid method, about 500 ten thousand t titanium white waste acid is produced annually in China, the quantity is huge, and the environment is seriously polluted if the titanium white waste acid is directly discharged. At present, the treatment method of the titanium white waste acid mainly comprises lime neutralization and sulfuric acid preparation by blending with pyrite, wherein the lime neutralization method is to neutralize the titanium white waste acid with lime to reach the standard of gypsum and then discharge the gypsum, and the method is to stack the waste acid into waste residue, is not a real green treatment mode and has high treatment cost; the method for preparing sulfuric acid by blending with pyrite consumes a very limited amount of titanium white waste acid, and has complex operation and high cost. Therefore, the treatment problem of titanium white waste acid is still very serious at present.
Disclosure of Invention
The invention aims to solve the problems that vanadium in a waste denitration catalyst needs to be separated out and the treatment capacity and the treatment cost of titanium white waste acid are huge in the prior art, and provides a method for leaching vanadium in the waste denitration catalyst.
In order to achieve the above object, the present invention provides a method for leaching vanadium in a waste denitration catalyst, comprising the steps of:
(1) Placing the waste denitration catalyst into a first treatment liquid for soaking;
(2) Drying and crushing the soaked waste denitration catalyst to obtain crushed materials with the granularity less than or equal to 100 meshes;
(3) Mixing the crushed material with a second treatment liquid, performing ultrasonic treatment, reacting for 4-24 hours at 60-100 ℃, and performing solid-liquid separation to obtain vanadium-containing leaching liquid;
the first treatment liquid and the second treatment liquid are respectively titanium white waste acid or mixed liquid obtained by treating the titanium white waste acid;
in the first treatment liquid, the concentration of sulfuric acid is less than or equal to 80g/L;
in the second treatment liquid, the concentration of sulfuric acid is more than or equal to 150g/L, the concentration of Fe is less than or equal to 40g/L, and the concentration of Ca is less than or equal to 1.2g/L.
Preferably, in the step (1), the waste denitration catalyst is prepared by a method comprising the following steps of 2 O 5 The content of the calculated vanadium element is more than or equal to 0.2 weight percent.
Preferably, in the step (1), the liquid-solid ratio of the first treatment liquid to the waste denitration catalyst is not less than 10mL/g.
Preferably, in the step (1), the soaking time is 10-120 min.
Preferably, in the step (2), the drying temperature is 80-140 ℃.
Preferably, in the step (2), the granularity of the crushed material is less than or equal to 100 meshes.
Preferably, in the step (3), the concentration of sulfuric acid in the second treatment solution is 150-600 g/L, the concentration of Fe is 20-40 g/L, and the concentration of Ca is 0.4-1.2 g/L.
Preferably, in the step (3), the liquid-solid ratio of the second treatment liquid and the crushed material is not less than 10mL/g.
Preferably, in the step (3), the ultrasonic time is more than or equal to 1h.
Preferably, in the step (3), the reaction temperature is 80-100 ℃.
And/or in the step (3), the reaction time is 6-20 h.
In the invention, the titanium white waste acid is used for leaching the vanadium in the waste denitration catalyst, so that the acid consumption required by extracting the vanadium is saved, the purpose of neutralizing the waste acid can be achieved, the waste is treated by waste, and the method has a good development prospect. The leaching rate of vanadium is more than 89% by adopting the method to leach the waste denitration catalyst.
Detailed Description
The following describes specific embodiments of the present invention in detail. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
The invention provides a method for leaching vanadium in a waste denitration catalyst, which comprises the following steps of:
(1) Placing the waste denitration catalyst into a first treatment liquid for soaking;
(2) Drying and crushing the soaked waste denitration catalyst to obtain crushed materials with the granularity less than or equal to 100 meshes;
(3) And mixing the crushed material with the second treatment liquid, performing ultrasonic treatment, reacting for 4-24 hours at the temperature of 60-100 ℃, and performing solid-liquid separation to obtain vanadium-containing leaching liquid.
In the invention, the first treatment liquid and the second treatment liquid are respectively titanium white waste acid or mixed liquid obtained by treating the titanium white waste acid.
In one embodiment, in the step (1), the concentration of sulfuric acid in the first treatment liquid is equal to or less than 80g/L. It is understood that when the sulfuric acid concentration in the titanium white waste acid is less than or equal to 80g/L, the titanium white waste acid can be directly used as the first treatment liquid; when the sulfuric acid concentration in the titanium white waste acid is more than 80g/L, the titanium white waste acid needs to be diluted to be less than or equal to 80g/L, namely, the first treatment liquid is a mixed liquid obtained by diluting the titanium white waste acid. However, the concentration of sulfuric acid in the titanium white waste acid is generally high and is generally about 200g/L, so in the invention, the first treatment liquid is a mixed liquid obtained by diluting the titanium white waste acid.
In the present invention, the concentration of sulfuric acid in the first treatment liquid is preferably 10 to 80g/L.
In a specific embodiment, in step (1), the waste denitration catalyst is treated with V 2 O 5 The content of the calculated vanadium element is more than or equal to 0.2 weight percent.
In the present invention, in the step (1), in the soaking step, the liquid-solid ratio of the first treatment liquid to the waste denitration catalyst may be equal to or greater than 10mL/g, preferably 20 to 50mL/g, and specifically, may be, for example, 10mL/g, 15mL/g, 20mL/g, 25mL/g, 30mL/g, 35mL/g, 40mL/g, or 50mL/g. That is, in the step (1), the amount of the first treatment liquid is 10mL or more, preferably 20 to 50mL, relative to 1g of the waste denitration catalyst.
The soaking time in the step (1) is not limited, and may be 10 to 120min, preferably 20 to 60min.
According to the invention, the waste denitration catalyst is soaked by using the first treatment liquid, so that the leaching rate of vanadium can be improved, presumably, due to the acid permeation effect, some ash on the surface is removed, so that vanadium is better exposed, meanwhile, calcium in the ash on the surface can be effectively removed in the first stage process to avoid the combination of the subsequent leaching process and vanadium, and the concentration of sulfuric acid in the first treatment liquid and conditions are insufficient to enable the vanadium to be leached, so that vanadium elements are collected in the subsequent vanadium-containing leaching liquid, and the vanadium can be purified and reused conveniently.
The denitration catalyst works in the flue gas environment of the coal-fired power plant for a long time, so that a large amount of dust in the flue gas is enriched on the surface of the waste denitration catalyst. In order to reduce the impurities in the finally obtained vanadium-containing leaching solution, in the invention, the waste denitration catalyst is subjected to physical ash removal before the step (1). Specifically, the physical ash removal method may be a purge method.
In the invention, the waste denitration catalyst dried in the step (2) is crushed, so that the leaching rate of vanadium can be improved, and the treatment cost can be reduced. In a preferred embodiment, in step (2), the particle size of the crushed material is 200 mesh or less.
The drying temperature in the step (2) is not limited, as long as the waste denitration catalyst taken out in the step (1) can be dried to a constant weight. In a specific embodiment, the drying temperature is 80 to 140 ℃, preferably 100 to 120 ℃.
In the invention, the concentration of sulfuric acid in the second treatment liquid is one of important factors influencing the leaching effect of vanadium, and if the concentration of sulfuric acid is too low, most of vanadium cannot be leached, and in the invention, the concentration of sulfuric acid in the second treatment liquid is more than or equal to 150g/L.
The present inventors have also found that if the concentration of Fe and Ca in the second treatment liquid is too high, the leaching rate of vanadium is reduced, presumably because these metal ions combine with vanadium to form a polymer or precipitate, which cannot be effectively separated into the liquid. In the invention, in the step (3), the concentration of Fe in the second treatment liquid is less than or equal to 40g/L and the concentration of Ca is less than or equal to 1.2g/L.
In a preferred embodiment, in the step (3), the concentration of sulfuric acid in the second treatment liquid is equal to or more than 150g/L, the concentration of Fe is equal to or less than 40g/L, and the concentration of Ca is equal to or less than 1.2g/L. It is understood that when the concentration of sulfuric acid, fe and Ca in the titanium white waste acid meets the above requirements, the titanium white waste acid can be directly used as the second treatment liquid; when the concentration of sulfuric acid, fe and Ca in the titanium white waste acid does not meet the above requirements, the titanium white waste acid needs to be subjected to concentration, impurity removal (Fe and/or Ca) and the like, thereby obtaining a second treatment liquid.
Further preferably, in the step (3), the concentration of sulfuric acid in the second treatment solution is 150-600 g/L, the concentration of Fe is 20-40 g/L, and the concentration of Ca is 0.4-1.2 g/L.
In a specific embodiment, the concentration of Fe in the titanium white waste acid is higher than 40g/L, and the titanium white waste acid needs to be treated to remove Fe, so as to obtain a second treatment liquid. The present invention is not limited to a specific method of removing Fe, and in one specific embodiment, the second treatment liquid is prepared according to the following steps: an oxidizing agent is added to the titanium white waste acid, the pH of the solution is adjusted to 2 by ammonia water, and then the solution is left to stand, and the supernatant is left to remove iron precipitate. In order to save the amount of ammonia, in a preferred embodiment, the second treatment liquid is prepared according to the following procedure: dividing titanium white waste acid into two parts, diluting one part to obtain a first treatment liquid, using the first treatment liquid for soaking a waste denitration catalyst, adding an oxidant, regulating the pH value of the solution to 2 by using ammonia water, standing, and leaving a supernatant to obtain waste acid a; and mixing the waste acid a with the rest part of titanium white waste acid to obtain a second treatment liquid.
In the invention, the oxidant is selected from one or more of hydrogen peroxide, potassium permanganate and potassium dichromate.
In a preferred embodiment, in the step (3), the liquid-solid ratio of the second treatment liquid to the pulverized material is not less than 10mL/g, more preferably 10 to 20mL/g, and specifically, for example, 10mL/g, 12mL/g, 15mL/g, 17mL/g, 18mL/g, or 20mL/g.
In a preferred embodiment, in the step (3), the time of the ultrasonic treatment is not less than 1h, preferably 2-4 h, specifically, for example, 2h, 2.5h, 3h, 3.5h or 4h.
In a preferred embodiment, in the step (3), the reaction temperature is 80 to 100 ℃, specifically, for example, 80 ℃, 82 ℃, 85 ℃, 87 ℃, 90 ℃, 92 ℃, 94 ℃, 95 ℃, 97 ℃, or 100 ℃.
In a preferred embodiment, in the step (3), the reaction time is 6 to 20h, specifically, for example, 6h, 7h, 7.5h, 10h, 12h, 14h, 16h, 18h or 20h.
In the method, the waste denitration catalyst is soaked in the first treatment liquid, then dried, crushed, ultrasonically mixed, reacted and the like, so that the leaching rate of vanadium is high and is more than 89%, and vanadium elements are collected in the vanadium-containing leaching liquid, so that the subsequent purification and utilization are facilitated.
The present invention will be described in detail by way of examples, but the scope of the present invention is not limited thereto. In the following examples 1 to 5, the titanium white waste acid used was obtained from titanium white waste acid produced by sulfuric acid method in a certain titanium dioxide factory in Yunnan, wherein the content (g/L) of each main component in the titanium white waste acid is shown in the following Table 1.
TABLE 1
Example 1
The waste denitration catalyst to be treated is a waste denitration catalyst of a certain power plant and is subjected to physical ash removal, wherein TiO is used in the waste denitration catalyst after the physical ash removal 2 Titanium elementIs 71.44wt%, as in WO 3 The content of tungsten element was 4.11wt% in terms of V 2 O 5 The content of the vanadium element was 1.01wt%.
(1) Placing 200g of waste denitration catalyst subjected to physical ash removal in a first treatment liquid, and soaking for 30min to obtain a first leaching liquid and the soaked waste denitration catalyst, wherein the first treatment liquid is obtained by diluting titanium white waste acid with water, the sulfuric acid content in the first treatment liquid is 61.33g/L, and the liquid-solid ratio of the first treatment liquid to the waste denitration catalyst is 25mL/g;
(2) Drying the waste denitration catalyst soaked in the step (1) to constant weight at 110 ℃, then crushing, and sieving with a 200-mesh sieve to obtain crushed materials;
(3) Adding an oxidant (potassium permanganate) into the titanium white waste acid, wherein 10g of the oxidant is correspondingly added into each 500mL of titanium white waste acid, regulating the pH to 2 by using ammonia water, then standing, and leaving a supernatant, so that Fe precipitate is removed, and a second treatment liquid meeting the requirements is obtained; in the second treatment liquid, the content of sulfuric acid is 262.34g/L, the content of Fe is 32.17g/L, the content of Ca is 0.54g/L, the content of Ti is 4.51g/L, the content of Al is 0.45g/L, the content of Mg is 5.73g/L, and the content of V is 0.45g/L;
(4) And mixing the crushed material with the second treatment liquid, performing ultrasonic treatment for 3 hours, then placing the obtained mixture into a reaction kettle for reaction, wherein the reaction temperature is 80 ℃, the liquid-solid ratio is 20mL/g, the reaction time is 8 hours, and washing and filtering after the reaction is completed to obtain vanadium-containing leaching liquid and residues.
Example 2
The waste denitration catalyst to be treated is a waste denitration catalyst of a certain power plant and is subjected to physical ash removal, wherein TiO is used in the waste denitration catalyst after the physical ash removal 2 The content of titanium element is 71.44wt%, as in WO 3 The content of tungsten element was 4.11wt% in terms of V 2 O 5 The content of the vanadium element was 1.01wt%.
(1) Placing 200g of waste denitration catalyst subjected to physical ash removal in a first treatment liquid, and soaking for 30min to obtain a first leaching liquid and the soaked waste denitration catalyst, wherein the first treatment liquid is obtained by diluting titanium white waste acid with water, the sulfuric acid content in the first treatment liquid is 54.33g/L, and the liquid-solid ratio of the first treatment liquid to the waste denitration catalyst is 25mL/g;
(2) Drying the waste denitration catalyst soaked in the step (1) to constant weight at 110 ℃, then crushing, and sieving with a 200-mesh sieve to obtain crushed materials;
(3) Mixing the crushed material with titanium white waste acid (namely second treatment liquid) and then carrying out ultrasonic treatment for 3 hours, then placing the obtained mixture into a reaction kettle for reaction, wherein the reaction temperature is 80 ℃, the liquid-solid ratio is 20mL/g, the reaction time is 8 hours, and washing and filtering are carried out after the reaction is completed, so that vanadium-containing leaching liquid and residues are obtained.
Example 3
The waste denitration catalyst to be treated is a waste denitration catalyst of a certain power plant and is subjected to physical ash removal, wherein TiO is used in the waste denitration catalyst after the physical ash removal 2 The content of titanium element is 70.96wt%, as in WO 3 The content of tungsten element was 3.46wt% in terms of V 2 O 5 The content of the vanadium element was 0.89wt%.
(1) Placing 200g of waste denitration catalyst subjected to physical ash removal in a first treatment liquid, and soaking for 30min to obtain a first leaching liquid and the soaked waste denitration catalyst, wherein the first treatment liquid is obtained by diluting titanium white waste acid with water, the sulfuric acid content in the first treatment liquid is 47.33g/L, and the liquid-solid ratio of the first treatment liquid to the waste denitration catalyst is 25mL/g;
(2) Drying the waste denitration catalyst soaked in the step (1) to constant weight at 110 ℃, then crushing, and sieving with a 200-mesh sieve to obtain crushed materials;
(3) Mixing the crushed material with titanium white waste acid (namely second treatment liquid) and then carrying out ultrasonic treatment for 3 hours, then placing the obtained mixture into a reaction kettle for reaction, wherein the reaction temperature is 80 ℃, the liquid-solid ratio is 20mL/g, the reaction time is 8 hours, and washing and filtering are carried out after the reaction is completed, so that vanadium-containing leaching liquid and residues are obtained.
Example 4
Waste to be treatedThe denitration catalyst is a waste denitration catalyst of a certain power plant and is subjected to physical ash removal, wherein TiO is used in the waste denitration catalyst after the physical ash removal 2 The content of titanium element is 70.96wt%, as in WO 3 The content of tungsten element was 3.46wt% in terms of V 2 O 5 The content of the vanadium element was 0.89wt%.
(1) Placing 200g of waste denitration catalyst subjected to physical ash removal in a first treatment liquid, and soaking for 30min to obtain a first leaching liquid and the soaked waste denitration catalyst, wherein the first treatment liquid is obtained by diluting titanium white waste acid with water, the sulfuric acid content in the first treatment liquid is 50.22 g/L, and the liquid-solid ratio of the first treatment liquid to the waste denitration catalyst is 30mL/g;
(2) Drying the waste denitration catalyst soaked in the step (1) to constant weight at the temperature of 100 ℃, then crushing, and sieving with a 200-mesh sieve to obtain crushed materials;
(3) Adding sodium metasilicate into titanium white waste acid (wherein 10g of sodium metasilicate is correspondingly added into each 500ml of titanium white waste acid), and removing part of Ca in the titanium white waste acid through flocculation and chemical reaction to obtain a second treatment liquid which meets the requirements, wherein the content of sulfuric acid in the second treatment liquid is 213.20g/L, the content of Fe in the second treatment liquid is 32.11g/L, the content of Ca in the second treatment liquid is 0.56g/L, the content of Ti in the second treatment liquid is 3.47g/L, the content of Al in the second treatment liquid is 0.42g/L, the content of Mg in the second treatment liquid is 3.12g/L, and the content of V in the second treatment liquid is 0.31g/L;
(4) And mixing the crushed material with the second treatment liquid, performing ultrasonic treatment for 2 hours, then placing the obtained mixture into a reaction kettle for reaction, wherein the reaction temperature is 90 ℃, the liquid-solid ratio is 15mL/g, the reaction time is 12 hours, and washing and filtering after the reaction is completed to obtain vanadium-containing leaching liquid and residues.
Example 5
The process was carried out as described in example 1, except that in step (3), 20g of an oxidizing agent was added per 500mL of titanium white waste acid, the pH was adjusted to 2 with ammonia water, and then the mixture was allowed to stand to leave a supernatant, thereby removing Fe precipitate and obtaining a satisfactory second treatment solution; in the second treatment liquid, the content of sulfuric acid is 203.45g/L, the content of Fe is 18.56g/L, the content of Ca is 0.52g/L, the content of Ti is 3.21g/L, the content of Al is 0.31g/L, the content of Mg is 5.62g/L, and the content of V is 0.32g/L.
Comparative example 1
The procedure was followed as described in example 1, except that the first treatment liquid was not added to soak;
specifically, the method comprises the following steps:
(1) Drying 200g of waste denitration catalyst subjected to physical ash removal to constant weight at 110 ℃, crushing, and sieving with a 200-mesh sieve to obtain a crushed material with granularity less than or equal to 200 meshes;
(2) Adding an oxidant (potassium permanganate) into the titanium white waste acid, wherein 10g of the oxidant is correspondingly added into each 500mL of titanium white waste acid, regulating the pH to 2 by using ammonia water, then standing, and leaving a supernatant, so that Fe precipitate is removed, and a second treatment liquid meeting the requirements is obtained; in the second treatment liquid, the content of sulfuric acid is 262.34g/L, the content of Fe is 32.17g/L, the content of Ca is 0.54g/L, the content of Ti is 4.51g/L, the content of Al is 0.45g/L, the content of Mg is 5.73g/L, and the content of V is 0.45g/L;
(3) And mixing the crushed material with the second treatment liquid, performing ultrasonic treatment for 3 hours, then placing the obtained mixture into a reaction kettle for reaction, wherein the reaction temperature is 80 ℃, the liquid-solid ratio is 20mL/g, the reaction time is 8 hours, and washing and filtering after the reaction is completed to obtain vanadium-containing leaching liquid and residues.
Comparative example 2
The procedure of example 1 was followed, except that the titanium white waste acid was directly used as the second treatment liquid, that is, the second treatment liquid, and the Fe content was 69.01g/L.
Comparative example 3
The procedure of example 1 was followed, except that in step (2), 80-mesh sieve was used to obtain a pulverized material.
Comparative example 4
The procedure was followed as described in example 1, except that in step (4), the reaction temperature was 30 ℃.
Comparative example 5
The procedure of example 1 was followed, except that in step (3), the second treatment solution was a sulfuric acid solution of the same concentration, specifically, a sulfuric acid solution of a concentration of 262.34 g/L.
Comparative example 6
The procedure was followed as described in example 2, except that in step (3), the reaction time was 30 minutes.
Comparative example 7
The procedure of example 4 was followed, except that the titanium white waste acid was directly used as the second treatment liquid, that is, the second treatment liquid, and the Ca content was 1.37g/L.
Test case
The leaching rate of vanadium after treatment by the methods described in examples 1 to 5 and comparative examples 1 to 7 was calculated according to the following formula (I), and the calculation results are shown in Table 2 below.
Leaching rate=1- [ (c) 0 ×m 0 )/(c 1 ×m 1 )]×100%（Ⅰ）
Wherein c 1 Vanadium content in the waste denitration catalyst after physical deashing;
m 1 the quality of the waste denitration catalyst after physical deashing;
c 0 is the vanadium content in the residue;
m 0 the quality of the residue.
TABLE 2
As can be seen from Table 2, the method provided by the invention has the advantages that through the ingenious design of experimental steps and experimental conditions, the leaching rate of vanadium is high, so that the effective utilization of titanium white waste acid is realized, the purpose of treating waste by waste is achieved, and the recovered vanadium is collected in the vanadium-containing leaching solution, so that the purification and the reutilization of the vanadium are facilitated.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (9)
1. A method for leaching vanadium from a waste denitration catalyst, which is characterized by comprising the following steps:
(1) Placing the waste denitration catalyst into a first treatment liquid for soaking;
(2) Drying and crushing the soaked waste denitration catalyst to obtain crushed materials with the granularity less than or equal to 100 meshes;
(3) Mixing the crushed material with a second treatment liquid, performing ultrasonic treatment, then reacting for 4-24 hours at 60-100 ℃, and performing solid-liquid separation to obtain vanadium-containing leaching liquid;
the first treatment liquid and the second treatment liquid are respectively titanium white waste acid or mixed liquid obtained by treating the titanium white waste acid;
the concentration of sulfuric acid in the first treatment liquid is 10-80 g/L;
in the second treatment solution, the concentration of sulfuric acid is 150-600 g/L, the concentration of Fe is 20-40 g/L, and the concentration of Ca is 0.4-1.2 g/L.
2. The method of claim 1, wherein in step (1), the waste denitration catalyst is treated with V 2 O 5 The content of the calculated vanadium element is more than or equal to 0.2 weight percent.
3. The method according to claim 1, wherein in the step (1), the liquid-solid ratio of the first treatment liquid to the waste denitration catalyst is not less than 10mL/g.
4. The method of claim 1, wherein in step (1), the soaking time is 10 to 120 minutes.
5. The method according to claim 1, wherein in step (2), the drying temperature is 80 to 140 ℃.
6. The method according to claim 1, wherein in the step (2), the particle size of the crushed material is not more than 200 mesh.
7. The method according to claim 1, wherein in step (3), the liquid-solid ratio of the second treatment liquid and the pulverized material is not less than 10mL/g.
8. The method of claim 1, wherein in step (3), the time of the ultrasound is not less than 1h.
9. The method according to claim 1, wherein in step (3), the temperature of the reaction is 80 to 100 ℃;
and/or in the step (3), the reaction time is 6-20 h.
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| GB1517888A (en) * | 1975-05-01 | 1978-07-19 | Mizusawa Industrial Chem | Method of treating raw materials containing components of titanium and/or zirconium |
| CA1210746A (en) * | 1983-05-16 | 1986-09-02 | Partha S. Ganguli | Recovering metal compounds from used catalysts obtained from hydroprocessing hydrocarbon feedstocks |
| CN101397150A (en) * | 2007-09-25 | 2009-04-01 | 攀钢集团攀枝花钢铁研究院 | Method for extracting vanadium pentoxide from vanadium-containing rotary furnace steel slag |
| CN102936049B (en) * | 2012-11-26 | 2014-06-04 | 西南民族大学 | Method for extracting tungsten, titanium and vanadium from waste SCR (selective catalytic reduction) catalyst |
| CN105969991A (en) * | 2016-06-18 | 2016-09-28 | 浙江天蓝环保技术股份有限公司 | Method for extracting titanium, vanadium and tungsten metallic oxide from failed SCR catalyst |
| CN111470534A (en) * | 2020-05-20 | 2020-07-31 | 胡琳 | Preparation process of vanadium pentoxide |
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