CN116497239A - Control method for calcified roasting clinker acid leaching process - Google Patents
Control method for calcified roasting clinker acid leaching process Download PDFInfo
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- CN116497239A CN116497239A CN202310380719.1A CN202310380719A CN116497239A CN 116497239 A CN116497239 A CN 116497239A CN 202310380719 A CN202310380719 A CN 202310380719A CN 116497239 A CN116497239 A CN 116497239A
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- 238000002386 leaching Methods 0.000 title claims abstract description 106
- 238000000034 method Methods 0.000 title claims abstract description 57
- 239000002253 acid Substances 0.000 title claims abstract description 21
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 90
- 229910052720 vanadium Inorganic materials 0.000 claims abstract description 71
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims abstract description 71
- 239000002002 slurry Substances 0.000 claims abstract description 52
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 25
- 239000007787 solid Substances 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 238000007865 diluting Methods 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 20
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 238000000605 extraction Methods 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 13
- 238000004065 wastewater treatment Methods 0.000 claims description 10
- 238000005406 washing Methods 0.000 claims description 7
- 238000004886 process control Methods 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 abstract description 3
- 238000004537 pulping Methods 0.000 abstract description 3
- 238000003756 stirring Methods 0.000 description 16
- 230000000052 comparative effect Effects 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- XHCLAFWTIXFWPH-UHFFFAOYSA-N [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] XHCLAFWTIXFWPH-UHFFFAOYSA-N 0.000 description 3
- 229910001935 vanadium oxide Inorganic materials 0.000 description 3
- 239000000706 filtrate Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000002308 calcification Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000014509 gene expression Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- 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
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a control method for the acid leaching process of calcified roasting clinker, which divides a leaching agent into two parts, wherein one part is used for mixing with calcified roasting clinker to prepare clinker slurry, and the other part is used for diluting concentrated sulfuric acid. The control method for the calcified roasting clinker acid leaching process has low cost and simple and convenient operation, the leaching agent is divided into two parts for pulping clinker, one part is used for leaching and diluted by concentrated sulfuric acid, and the leaching agent containing sulfuric acid is added into clinker slurry, so that the solid ratio of the material slurry is improved, the rapid leaching of vanadium is realized, and the problems of high local acidity, high temperature, high impurity content and the like caused by directly adding the concentrated sulfuric acid are avoided.
Description
Technical Field
The invention relates to the technical field of wet metallurgy of vanadium, in particular to a control method for an acid leaching process of calcified roasting clinker.
Background
Vanadium is used as an important microalloying element, is widely used in the fields of metallurgy, chemical industry, aerospace and the like, can obviously improve the strength, toughness, ductility and the like of steel, and provides important support for guaranteeing the quality of national key engineering. The vanadium titano-magnetite is treated by a blast furnace or an electric furnace at high temperature to obtain vanadium-containing molten iron, and vanadium slag is obtained by selective oxidation from the molten iron, and is used as a vanadium extracting raw material. In the vanadium oxide production process, calcification roasting-acid leaching of vanadium-containing materials is a typical vanadium extraction process.
After the vanadium slag is calcified and roasted, vanadium exists in the form of pentavalent vanadium, and the leaching pH=2.8-3.5 can be controlled by adding sulfuric acid to dissolve the vanadium into the solution, wherein more than about 80% of the vanadium leaching reaction occurs within 15min after the start, and a large amount of sulfuric acid is consumed at the moment. In practice, the local acidity is usually too high due to the rapid addition of sulfuric acid, uneven addition, etc. According to the existence form of vanadium, when the pH of the leaching solution is low and the concentration of pentavalent vanadium is high, the solution system is unstable, and the vanadium is easy to hydrolyze and precipitate to cause loss, so that the content fluctuation of the TV of the vanadium extraction tailings obtained in industrial production is large and is 1.0-1.7%.
In summary, the problem of vanadium loss easily caused by excessive local acidity in the acid leaching process of calcified roasting clinker becomes a technical problem to be solved urgently by those skilled in the art.
Based on this, the prior art still remains to be improved.
Disclosure of Invention
In order to solve the technical problems, the embodiment of the invention provides a control method for the acid leaching process of calcified roasting clinker, which aims to solve the technical problems caused by overlarge local acidity in the acid leaching process of calcified roasting clinker in the prior art.
In order to solve the technical problems, some embodiments of the invention disclose a control method for the acid leaching process of calcified roasting clinker, wherein a leaching agent is divided into two parts, one part is used for being mixed with the calcified roasting clinker to prepare clinker slurry, and the other part is used for diluting concentrated sulfuric acid.
Further, the method comprises the steps of:
step one, mixing calcified roasting clinker with a first leaching agent to obtain clinker slurry;
mixing concentrated sulfuric acid with a second leaching agent to obtain a first solution;
step three, adding the first solution into clinker slurry at a constant speed to obtain a third solution;
and fourthly, controlling the pH value of the third solution to be 2.5-3.5, carrying out leaching reaction, and then carrying out solid-liquid separation to obtain vanadium-containing leaching liquid and vanadium extraction tailings.
Further, in the second step, the amount of the concentrated sulfuric acid is 0.6-0.8 times of the total amount of the concentrated sulfuric acid consumed in the calcified roasting clinker leaching process.
Further, in the first step, the mass ratio of the calcified roasting clinker to the first leaching agent is 1:1 to 2.
Further, in the first step, the first leaching agent is water, wastewater treatment reuse water or vanadium-containing solution.
Further, in the second step, the second leaching agent is water or wastewater treatment reuse water.
Further, in the third step, the first solution is added into the clinker slurry at a constant speed for more than 15 min.
Further, the first solution is added into the clinker slurry at a constant speed for 15-25 min.
Further, the liquid-solid mass ratio of the third solution is (2-10): 1, a step of;
preferably, the liquid-solid mass ratio of the third solution is (2-4): 1.
further, the vanadium-containing solution comprises a washing solution of vanadium extraction tailings.
By adopting the technical scheme, the invention has at least the following beneficial effects:
the control method for the calcified roasting clinker acid leaching process has low cost and simple and convenient operation, the leaching agent is divided into two parts for pulping clinker, one part is used for leaching and diluted by concentrated sulfuric acid, and the leaching agent containing sulfuric acid is added into clinker slurry, so that the solid ratio of the material slurry is improved, the rapid leaching of vanadium is realized, and the problems of high local acidity, high temperature, high impurity content and the like caused by directly adding the concentrated sulfuric acid are avoided.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a flow chart of a method for controlling the acid leaching process of calcified roasting clinker according to some embodiments of the present invention.
Detailed Description
Embodiments of the present disclosure are described in further detail below with reference to the drawings and examples. The following detailed description of the embodiments and the accompanying drawings are provided to illustrate the principles of the disclosure and not to limit the scope of the disclosure, which may be embodied in many different forms and not limited to the specific embodiments disclosed herein, but rather to include all technical solutions falling within the scope of the claims.
The present disclosure provides these embodiments in order to make the present disclosure thorough and complete, and fully convey the scope of the disclosure to those skilled in the art. It should be noted that: the relative arrangement of parts and steps, the composition of materials, numerical expressions and numerical values set forth in these embodiments should be construed as exemplary only and not limiting unless otherwise specifically stated.
In the description of the present disclosure, unless otherwise indicated, the meaning of "plurality" is greater than or equal to two; the terms "upper," "lower," "left," "right," "inner," "outer," and the like indicate an orientation or positional relationship merely for convenience of describing the present disclosure and simplifying the description, and do not indicate or imply that the devices or elements being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus are not to be construed as limiting the present disclosure. When the absolute position of the object to be described is changed, the relative positional relationship may be changed accordingly.
Furthermore, the use of the terms first, second, and the like in this disclosure do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. The "vertical" is not strictly vertical but is within the allowable error range. "parallel" is not strictly parallel but is within the tolerance of the error. The word "comprising" or "comprises" and the like means that elements preceding the word encompass the elements recited after the word, and not exclude the possibility of also encompassing other elements.
It should also be noted that, in the description of the present disclosure, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be directly connected or indirectly connected through an intermediate medium. The specific meaning of the terms in the present disclosure may be understood as appropriate by those of ordinary skill in the art. When a particular device is described as being located between a first device and a second device, there may or may not be an intervening device between the particular device and either the first device or the second device.
All terms used in the present disclosure have the same meaning as understood by one of ordinary skill in the art to which the present disclosure pertains, unless specifically defined otherwise. It will be further understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and will not be interpreted in an idealized or overly formal sense unless expressly so defined herein.
Techniques, methods, and apparatus known to one of ordinary skill in the relevant art may not be discussed in detail, but where appropriate, the techniques, methods, and apparatus should be considered part of the specification.
As shown in fig. 1, some embodiments of the present invention disclose a method of controlling the acid leaching process of calcified-roasting clinker, which divides the leaching agent into two parts, one part for mixing with the calcified-roasting clinker to prepare clinker slurry, and the other part for diluting concentrated sulfuric acid. Specifically, the control process may include the steps of:
step one, mixing calcified roasting clinker with a first leaching agent to obtain clinker slurry; wherein the mass ratio of the calcified roasting clinker to the first leaching agent is preferably 1:1 to 2. The first leaching agent can be water, wastewater treatment reuse water or vanadium-containing solution, the vanadium-containing solution can comprise but is not limited to a washing solution of vanadium extraction tailings, and can also be a vanadium-containing leaching solvent, namely a washing filtrate obtained after acid leaching is finished and filtering and washing, wherein the leaching solvent in the first acid leaching process can be industrial water, the vanadium-containing leaching solvent can be obtained after filtering and washing and is used for the next leaching cycle, and the washing filtrate can be used as the vanadium-containing leaching solvent.
Mixing concentrated sulfuric acid with a second leaching agent to obtain a first solution; wherein, the taking amount of the concentrated sulfuric acid is preferably 0.6-0.8 times of the total amount of the concentrated sulfuric acid consumed in the calcified roasting clinker leaching process. The second leaching agent can be water or wastewater treatment reuse water.
Step three, adding the first solution into clinker slurry at a constant speed in a stirring state to obtain a third solution; the time for adding the first solution into the clinker slurry at a constant speed is preferably controlled to be more than 15 minutes, if the time is too short, local acidity is easily caused to be too high, so that a solution system is unstable, and vanadium is easily hydrolyzed and precipitated to cause loss. Further, the first solution can be added to the clinker slurry at a constant speed for 15 to 25 minutes. The liquid-solid mass ratio of the third solution is preferably (2-10): 1, preferably (2-4): 1.
and fourthly, controlling the pH value of the third solution to be 2.5-3.5, carrying out leaching reaction, and then carrying out solid-liquid separation to obtain vanadium-containing leaching liquid and vanadium extraction tailings. In this step, the control of the pH value can be achieved by dilute sulfuric acid, and the concentration of dilute sulfuric acid can be controlled to about 50%.
The embodiment of the invention divides the leaching agent into two parts for use, one part is used for pulping clinker, the other part is used for leaching and diluting with concentrated sulfuric acid, and then the leaching agent containing sulfuric acid is added into clinker slurry, so that the solid ratio of the slurry is improved, and meanwhile, the rapid leaching of vanadium is realized, and the problems of high local acidity, high temperature, high impurity content and the like caused by directly adding the concentrated sulfuric acid are avoided.
The technical scheme of the present application is further described in detail below by examples.
Comparative example 1:
100g (TV=7.07% and P=0.066%) of calcified roasting clinker is taken, 250mL of water is added, 50% dilute sulfuric acid is adopted to adjust the pH of the system to 3.0 under the stirring state, the reaction is carried out for 60min, and solid-liquid separation is carried out, thus obtaining leaching solution (V=23.82 g/L, P =0.03 g/L) and vanadium extraction tailings (TV=1.14%). The sulfuric acid consumption in the leaching process is reduced to 5.5mL of concentrated sulfuric acid, and the vanadium leaching rate is 84.84%.
Example 1:
(1) Taking 100g (TV=7.07% and P=0.066%) of calcified roasting clinker, adding 100mL of water, and uniformly stirring to obtain clinker slurry A;
(2) Adding 3.3mL of concentrated sulfuric acid into 150mL of water, and uniformly stirring to obtain a solution B;
(3) Adding the solution B into clinker slurry A at a constant speed, wherein the adding time is controlled to be 15min, so as to obtain slurry C, and the liquid-solid ratio of the slurry C is 2.53:1;
(4) The pH value of the slurry C is controlled to be 3.0 by adopting 50% of dilute sulfuric acid by mass percent, after leaching reaction is carried out for 40min, solid-liquid separation is carried out, and vanadium-containing leaching liquid (V=24.22 g/L, P =0.018 g/L) and vanadium-extracting tailings (TV=1.05%) are obtained.
The sulfuric acid consumption in the leaching process is reduced to 5.2mL of concentrated sulfuric acid, and the vanadium leaching rate is 86.03%.
Generally, the liquid-solid ratio of the slurry C is controlled to be 2-4:1, and the slurry C is mainly used for obtaining a vanadium-containing leaching solution (V is more than 20 g/L) with higher vanadium concentration, so that the subsequent further vanadium precipitation is facilitated to prepare a vanadium oxide product. The liquid-solid ratio of the slurry C is a preferred value selected for actual production when the calcified clinker tv=6 to 10%. Theoretically, the liquid-to-solid ratio of this slurry C could be increased to above 10:1, except that the vanadium concentration obtained was below 10g/L.
Comparative example 2:
100g of calcified and roasted clinker (TV=8.54%, P=0.058%) was taken, 300mL of vanadium-containing solution (V=3.15 g/L) was added, the pH of the system was adjusted to 2.8 by 50% dilute sulfuric acid under stirring, the reaction was carried out for 80min, and solid-liquid separation was carried out to obtain a leachate (V=28.31 g/L, P =0.028 g/L) and vanadium extraction tailings (TV=1.08%). The sulfuric acid consumption in the leaching process is reduced to 6.7mL of concentrated sulfuric acid, and the vanadium leaching rate is 88.24%.
Example 2:
(1) Taking 100g of calcified roasting clinker (TV=8.54% and P=0.058%), adding 100mL of vanadium-containing solution (V=3.15 g/L), and uniformly stirring to obtain clinker slurry A;
(2) Adding 5.4mL of concentrated sulfuric acid into 200mL of water, and uniformly stirring to obtain a solution B;
(3) Adding the solution B into clinker slurry A at a constant speed, wherein the adding time is controlled to be 25min, so as to obtain slurry C, and the liquid-solid ratio of the slurry C is 3.05:1;
(4) The pH value of the slurry C is controlled to be 2.8 by adopting 50% of dilute sulfuric acid by mass fraction, leaching reaction is carried out for 60min, and solid-liquid separation is carried out, so that vanadium-containing leaching solution (V= 28.61g/L, P =0.020 g/L) and vanadium-extracting tailings (TV=0.96%) are obtained.
The sulfuric acid consumption in the leaching process is reduced to 6.6mL of concentrated sulfuric acid, and the vanadium leaching rate is 89.43%.
Comparative example 3:
100g of calcified and roasted clinker (TV=8.54%, P=0.058%) is taken, 400mL of wastewater treatment reuse water (V=0.1 g/L) is added, 50% dilute sulfuric acid is adopted to adjust the pH of the system to 2.5 under stirring, the pH is reacted for 80min, and solid-liquid separation is carried out, so as to obtain leaching solution (V=18.57 g/L, P =0.035 g/L) and vanadium extraction tailings (TV=1.21%). The sulfuric acid consumption in the leaching process is reduced to 7.1mL of concentrated sulfuric acid, and the vanadium leaching rate is 86.96%.
Example 3:
(1) Taking 100g of calcified roasting clinker (TV=8.54% and P=0.058%), adding 200mL of wastewater treatment reuse water (V=0.1 g/L), and uniformly stirring to obtain clinker slurry A;
(2) Adding 5.5mL of concentrated sulfuric acid into 200mL of water, and uniformly stirring to obtain a solution B;
(3) Adding the solution B into clinker slurry A at a constant speed, wherein the adding time is controlled to be 25min, so as to obtain slurry C, and the liquid-solid ratio of the slurry C is 4.05:1;
(4) The pH value of the slurry C is controlled to be 2.5 by adopting 50% of dilute sulfuric acid by mass fraction, leaching reaction is carried out for 40min, and solid-liquid separation is carried out, so that vanadium-containing leaching liquid (V=19.28/L, P =0.021 g/L) and vanadium-extracting tailings (TV=0.91%) are obtained.
The sulfuric acid consumption in the leaching process is reduced to 6.8mL of concentrated sulfuric acid, and the vanadium leaching rate is 90.19%.
Comparative example 4:
100g of calcified and roasted clinker (TV=8.54%, P=0.058%) is taken, 600mL of vanadium-containing solution (V=3.15 g/L) is added, 50% dilute sulfuric acid is adopted to adjust the pH of the system to 2.8 under stirring, the reaction is carried out for 80min, and solid-liquid separation is carried out, thus obtaining leaching solution (V=15.70 g/L, P =0.021 g/L) and vanadium extraction tailings (TV=1.06%). The sulfuric acid consumption in the leaching process is reduced to 7.2mL of concentrated sulfuric acid, and the vanadium leaching rate is 88.52%.
Example 4:
(1) Taking 100g of calcified roasting clinker (TV=8.54% and P=0.058%), adding 200mL of vanadium-containing solution (V=3.15 g/L), and uniformly stirring to obtain clinker slurry A;
(2) Adding 5.8mL of concentrated sulfuric acid into 400mL of water, and uniformly stirring to obtain a solution B;
(3) Adding the solution B into clinker slurry A at a constant speed, wherein the adding time is controlled to be 25min, so as to obtain slurry C, and the liquid-solid ratio of the slurry C is 6.06:1;
(4) The pH value of the slurry C is controlled to be 2.8 by adopting 50% of dilute sulfuric acid by mass fraction, leaching reaction is carried out for 60min, and solid-liquid separation is carried out, so that vanadium-containing leaching liquid (V=15.17 g/L, P =0.020 g/L) and vanadium-extracting tailings (TV=0.93%) are obtained.
The sulfuric acid consumption in the leaching process is reduced to 6.8mL of concentrated sulfuric acid, and the vanadium leaching rate is 89.82%.
Comparative example 5:
100g of calcified and roasted clinker (TV=8.54% and P=0.058%) is taken, 1200mL of wastewater treatment reuse water (V=0.1 g/L) is added, 50% dilute sulfuric acid is adopted to adjust the pH of the system to 2.8 under stirring, the reaction is carried out for 80min, and solid-liquid separation is carried out, thus obtaining leaching solution (V=6.31 g/L, P =0.022 g/L) and vanadium extraction tailings (TV=1.04%). The sulfuric acid consumption in the leaching process is reduced to 8.0mL of concentrated sulfuric acid, and the vanadium leaching rate is 88.81%.
Example 5:
(1) Taking 100g of calcified roasting clinker (TV=8.54% and P=0.058%), adding 200mL of wastewater treatment reuse water (V=0.1 g/L), and uniformly stirring to obtain clinker slurry A;
(2) Adding 6.0mL of concentrated sulfuric acid into 1000mL of water, and uniformly stirring to obtain a solution B;
(3) Adding the solution B into clinker slurry A at a constant speed, wherein the adding time is controlled to be 25min, so as to obtain slurry C, and the liquid-solid ratio of the slurry C is 12.06:1;
(4) The pH value of the slurry C is controlled to be 2.8 by adopting 50% of dilute sulfuric acid by mass fraction, leaching reaction is carried out for 40min, and solid-liquid separation is carried out, so that vanadium-containing leaching liquid (V=6.58/L, P =0.021 g/L) and vanadium-extracting tailings (TV=0.90%) are obtained.
The sulfuric acid consumption in the leaching process is reduced to 7.4mL of concentrated sulfuric acid, and the vanadium leaching rate is 90.05%. In the case, the liquid-solid ratio of the slurry C is higher than 10:1, which is favorable for improving the leaching rate of vanadium, but the concentration of vanadium in the obtained leaching solution is lower than 8g/L, which is unfavorable for further extracting vanadium to prepare vanadium oxide products.
Thus, various embodiments of the present disclosure have been described in detail. In order to avoid obscuring the concepts of the present disclosure, some details known in the art are not described. How to implement the solutions disclosed herein will be fully apparent to those skilled in the art from the above description.
Although some specific embodiments of the present disclosure have been described in detail by way of example, it should be understood by those skilled in the art that the above examples are for illustration only and are not intended to limit the scope of the present disclosure. It will be understood by those skilled in the art that the foregoing embodiments may be modified and equivalents substituted for elements thereof without departing from the scope and spirit of the disclosure. In particular, the technical features mentioned in the respective embodiments may be combined in any manner as long as there is no structural conflict.
Claims (10)
1. A control method for the acid leaching process of calcified roasting clinker is characterized in that a leaching agent is divided into two parts, wherein one part is used for being mixed with calcified roasting clinker to prepare clinker slurry, and the other part is used for diluting concentrated sulfuric acid.
2. The method for controlling the acid leaching process of calcified roasting clinker according to claim 1, comprising:
step one, mixing calcified roasting clinker with a first leaching agent to obtain clinker slurry;
mixing concentrated sulfuric acid with a second leaching agent to obtain a first solution;
step three, adding the first solution into clinker slurry at a constant speed to obtain a third solution;
and fourthly, controlling the pH value of the third solution to be 2.5-3.5, carrying out leaching reaction, and then carrying out solid-liquid separation to obtain vanadium-containing leaching liquid and vanadium extraction tailings.
3. The method for controlling the acid leaching process of the calcified roasting clinker according to claim 2, wherein in the second step, the amount of the concentrated sulfuric acid is 0.6-0.8 times the total amount of the concentrated sulfuric acid consumed in the leaching process of the calcified roasting clinker.
4. The method of claim 2, wherein in the first step, the mass ratio of the calcified clinker to the first leaching agent is 1:1 to 2.
5. The method of claim 2, wherein in the first step, the first leaching agent is water, wastewater treatment reuse water or vanadium-containing solution.
6. The method of claim 2, wherein in the second step, the second leaching agent is water or wastewater treatment reuse water.
7. The method according to claim 2, wherein in the third step, the first solution is added to the clinker slurry at a constant speed for 15 minutes or longer.
8. The method of controlling the acid leaching process of calcified roasting clinker according to claim 7, wherein the first solution is added to the clinker slurry at a constant speed for 15 to 25 minutes.
9. The calcified roasting clinker acid leaching process control method according to claim 2, wherein the liquid-solid mass ratio of the third solution is (2-10): 1, a step of;
preferably, the liquid-solid mass ratio of the third solution is (2-4): 1.
10. the method for controlling the acid leaching process of calcified roasting clinker according to claim 5, wherein the vanadium-containing solution comprises a washing solution of vanadium extraction tailings.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310380719.1A CN116497239A (en) | 2023-04-11 | 2023-04-11 | Control method for calcified roasting clinker acid leaching process |
Applications Claiming Priority (1)
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