A purification system for vanadium residue sodium salt calcine leaching solution

Abstract

The utility model relates to the field of metallurgical equipment, concretely relates to a kind of purification system of vanadium residue sodium salt calcination clinker leaching solution, including high buffer tank, vacuum separator, centrifugal separator, purification tank, storage tank, underflow tank and pressurized separator.High buffer tank's output end is connected the input end of vacuum separator, vacuum separator is set to wash and solid-liquid separation to vanadium residue sodiumization calcination clinker, obtain vanadium leaching solution;The output end of vacuum separator is connected the input end of centrifugal separator, the output end of centrifugal separator is connected the input end of purification tank, the output end of purification tank is connected the input end of storage tank and underflow tank, the output end of underflow tank is connected the input end of pressurized separator.The utility model can realize the purification of vanadium leaching solution without complex process, and avoid fine particle residue mixing into phosphorus removal residue, realize the separate recycling of residue and phosphorus removal residue, reduce the cost of vanadium-containing solid waste treatment.

Description

Technical Field

[0001] This utility model relates to the field of metallurgical equipment, specifically to a purification system for leaching liquid from vanadium slag sodium salt roasting clinker. Background Technology

[0002] To remove phosphorus impurities from the leaching solution of vanadium slag sodium salt roasted clinker, the following procedure is performed: calcium chloride is added to the vanadium leaching solution, causing calcium to combine with phosphorus to form calcium phosphate, which enters the underflow slag, thus separating vanadium from phosphorus impurities. However, during solid-liquid separation after leaching of the roasted clinker, the filter medium passes through the filter, resulting in a large amount of fine particulate residue in the separated vanadium leaching solution. This residue enters the underflow slag along with the phosphorus removal slag during the calcium chloride impurity removal process, increasing the amount of phosphorus removal slag generated. Due to the large volume, complex composition, and low vanadium content of the vanadium-containing underflow slag, the subsequent vanadium recovery cost is high.

[0003] The method of reducing vanadium loss in the vanadium-containing underflow slag by filtering the vanadium-containing leachate obtained by solid-liquid separation of vanadium slag calcified clinker after acid leaching using a belt filter is characterized by high filtration resistance and filtration difficulties in actual operation. Utility Model Content

[0004] This utility model provides a purification system for the leachate from vanadium slag sodium salt roasting clinker, comprising:

[0005] High-level buffer tanks, vacuum separators, centrifugal separators, purification tanks, storage tanks, underflow tanks, and pressurized separators;

[0006] The output end of the high-level buffer tank is connected to the input end of the vacuum separator, which is configured to wash and separate the solid and liquid components of the sodium-roasted vanadium slag clinker to obtain vanadium leachate.

[0007] The output end of the vacuum separator is connected to the input end of the centrifugal separator, and the centrifugal separator is configured to perform solid-liquid separation on the vanadium leaching solution again.

[0008] The output end of the centrifuge is connected to the input end of the purification tank, which is configured to add calcium chloride to the vanadium leaching solution to obtain a vanadium solution and a bottom slag.

[0009] The output end of the purification tank is connected to the input end of the storage tank and the underflow tank. The storage tank is configured to store vanadium solution, and the underflow tank is configured to store underflow slag.

[0010] The output end of the underflow tank is connected to the input end of the pressurized separator, which is configured to process underflow slag.

[0011] The purification system for vanadium slag sodium salt roasted clinker leachate according to claim 1 is characterized in that the input end of the high-level buffer tank is also connected to the output end of the vacuum separator.

[0012] In some embodiments, the high-level buffer tank is configured to store a mixture slurry of vanadium slag sodium salt roasting clinker and a low-vanadium-concentration dilute liquid produced by multi-stage washing in a vacuum separator.

[0013] In some embodiments, the elevated buffer tank includes a spiral stirring mechanism.

[0014] In some embodiments, the vacuum separator is configured to add water and a dilute liquid, wherein the weight ratio of water to vanadium slag sodium salt roasted clinker ranges from 1 to 2.5, and the weight ratio of the dilute liquid to vanadium slag sodium salt roasted clinker ranges from 0.5 to 1.5.

[0015] In some embodiments, the centrifuge is composed of a horizontal spiral centrifugal sedimentation unit.

[0016] In some embodiments, the purification tank includes a fan-shaped stirring mechanism.

[0017] In some embodiments, the output end of the purification tank is an overflow port.

[0018] In some embodiments, the storage tank is provided with an insulation layer, and the temperature is not lower than 60°C.

[0019] In some embodiments, the output end of the pressure separator is connected to the input end of the storage tank, and is configured to store the filtrate of the underflow residue into the storage tank.

[0020] The beneficial effects of this utility model are as follows:

[0021] This invention achieves the purification and phosphorus removal of vanadium leaching solution without complicated procedures, and avoids the mixing of fine particulate residues with the phosphorus removal slag, enabling the separate recycling of residues and phosphorus removal slag, thereby reducing the cost of treating vanadium-containing solid waste.

[0022] Vacuum filtration technology enables rapid and efficient solid-liquid separation of vanadium slag sodium salt roasted clinker and slurry obtained after leaching with low-concentration vanadium-containing dilute solution. Compared to traditional gravity sedimentation or pressure filtration methods, vacuum separators can significantly shorten separation time, improve production efficiency, and reduce the amount of solid residue in the slurry, ensuring the smooth progress of subsequent leaching processes.

[0023] By combining vacuum separators and centrifugal separators, the amount of solid waste generated can be significantly reduced. At the same time, the phosphorus removal slag produced in the purification tank has a relatively simple composition, making it easy to process and utilize as a resource. Attached Figure Description

[0024] To better understand this invention, reference can be made to the embodiments shown in the following figures. Components in the figures are not necessarily drawn to scale, and related elements may be omitted, or in some cases the scale may have been enlarged to emphasize and clearly illustrate the novel features described herein. Additionally, as is known in the art, system components may be arranged differently. Furthermore, in the figures, the same reference numerals denote corresponding parts throughout several views.

[0025] Figure 1 A reference schematic diagram of a purification system for vanadium slag sodium salt roasting clinker leachate according to the present invention is shown.

[0026] Figure 2 A schematic diagram of the process of a purification system for vanadium slag sodium salt roasting clinker leachate according to the present invention is shown.

[0027] Explanation of reference numerals in the attached drawings: 11. High-level buffer tank; 12. Vacuum separator; 2. Centrifugal separator; 3. Purification tank; 4. Storage tank; 51. Underflow tank; 52. Pressurized separator. Detailed Implementation

[0028] It should be understood that the embodiments of the present invention shown in the exemplary embodiments are merely illustrative. Although only a few embodiments have been described in detail in this invention, those skilled in the art will readily recognize that various modifications are possible without substantially departing from the teachings of the present invention. Accordingly, all such modifications should be included within the scope of this invention. Other substitutions, modifications, variations, and deletions can be made to the design, operating conditions, and parameters of the following exemplary embodiments without departing from the spirit of the present invention.

[0029] This utility model provides a purification system for the leachate from vanadium slag sodium salt roasting clinker. Please refer to [link to relevant documentation]. Figure 1 ,include:

[0030] High-level buffer tank 11, vacuum separator 12, centrifugal separator 2, purification tank 3, storage tank 4, underflow tank 51, and pressurized separator 52;

[0031] The output end of the high-level buffer tank 11 is connected to the input end of the vacuum separator 12. The vacuum separator 12 is configured to wash and separate the solid and liquid components of the sodium-roasted vanadium slag clinker to obtain vanadium leachate.

[0032] The output end of the vacuum separator 12 is connected to the input end of the centrifugal separator 2, and the centrifugal separator 2 is configured to perform solid-liquid separation on the vanadium leaching solution again.

[0033] The output end of the centrifuge 2 is connected to the input end of the purification tank 3. The purification tank 3 is configured to add calcium chloride to the vanadium leaching solution to obtain vanadium solution and underflow slag.

[0034] The output end of the purification tank 3 is connected to the input end of the storage tank 4 and the underflow tank 51. The storage tank 4 is configured to store vanadium solution, and the underflow tank 51 is configured to store underflow slag.

[0035] The output end of the underflow tank 51 is connected to the input end of the pressurized separator 52, which is configured to process underflow slag.

[0036] Vacuum filtration technology enables rapid and efficient solid-liquid separation of vanadium slag sodium salt roasted clinker and slurry obtained after leaching with low-concentration vanadium-containing dilute solution. Compared to traditional gravity sedimentation or pressure filtration methods, the vacuum separator 12 can significantly shorten the separation time, improve production efficiency, and reduce the amount of solid residue in the slurry, ensuring the smooth progress of subsequent leaching processes.

[0037] Centrifuge 2: The vanadium leaching solution produced by the vacuum separator is centrifuged again to further remove tiny solid particles and suspended matter, resulting in a vanadium leaching solution with low solid content. This not only improves the purity of the vanadium leaching solution, but also provides more favorable conditions for subsequent purification treatment and reduces the impact of impurities on the purification effect.

[0038] Purification Tank 3: Calcium chloride is added to the low-solids vanadium leaching solution produced by the centrifuge for phosphorus removal. Calcium chloride reacts with phosphate ions in the vanadium leaching solution to form calcium phosphate precipitate, effectively removing phosphorus through precipitation separation. This method is simple to operate, low in cost, and can significantly reduce the phosphorus content in vanadium products, improving product quality and added value.

[0039] The combined use of vacuum separator 12 and centrifugal separator 2 significantly reduces the amount of solid waste generated. Simultaneously, the phosphorus-removing slag produced in purification tank 3 has a relatively simple composition, facilitating subsequent processing and resource utilization. The reduction in solid waste directly lowers solid waste treatment costs. Furthermore, due to the increased purity of the vanadium leaching solution and the reduced phosphorus content, the subsequent purification and processing costs of vanadium products are also correspondingly reduced.

[0040] In some embodiments, please refer to Figure 1 The input end of the high-level buffer tank 11 is also connected to the output end of the vacuum separator 12.

[0041] The low-vanadium-concentration dilute solution produced by the vacuum separator 12, containing a small amount of unreacted vanadium slag, can be returned to the high-level buffer tank 11, mixed with new raw materials, and then reintroduced into the leaching process. This reduces the amount of fresh vanadium slag and dilute solution used, thereby lowering raw material costs.

[0042] In some embodiments, please refer to Figure 1 The high-level buffer tank 11 is configured to store a mixture slurry of vanadium slag sodium salt roasting clinker and low-vanadium concentration dilute liquid generated by multi-stage washing in a vacuum separator.

[0043] In some embodiments, please refer to Figure 1 The high-level buffer tank 11 includes a spiral stirring mechanism.

[0044] When the spiral blades rotate, they turn the bottom material upwards and the top material downwards, forming a three-dimensional circulating flow.

[0045] In some embodiments, please refer to Figure 1 The vacuum separator 12 is configured to add water and dilute liquid, with the weight ratio of water to vanadium slag sodium salt roasted clinker ranging from 1 to 2.5, and the weight ratio of dilute liquid to vanadium slag sodium salt roasted clinker ranging from 0.5 to 1.5.

[0046] By controlling the water ratio, excessive evaporation caused by an overly dilute slurry can be avoided. This reduces the amount of fresh diluent used, lowering costs. Maintaining a stable Na+ concentration in the slurry also reduces particle size inconsistencies in the crystalline product.

[0047] In some embodiments, the centrifuge 2 is composed of a horizontal spiral centrifugal sedimentation mechanism.

[0048] Horizontal screw centrifuges enable continuous feeding, continuous slag discharge, and continuous liquid discharge without requiring shutdown for cleaning. They achieve efficient separation at lower speeds, reducing energy consumption. The separated solid phase has a low liquid content and can be directly transported or further processed, reducing solid waste volume and disposal costs.

[0049] In some embodiments, the purification tank 3 includes a fan-shaped stirring mechanism.

[0050] When the fan-shaped blades rotate, they create radial, axial, and tangential flows that cover the entire tank area, preventing local concentrations from being too high or too low.

[0051] In some embodiments, the output end of the purification tank 3 is an overflow port.

[0052] When the slurry enters purification tank 3 and reaches the overflow port height, excess liquid automatically overflows, maintaining a constant liquid level inside the tank. This avoids drastic changes in liquid level caused by fluctuations in the feed flow, ensuring that subsequent equipment receives a stable amount of slurry. The overflow port is located at the top of the tank and outputs the fully mixed and settled upper clear liquid.

[0053] In some embodiments, the storage tank 4 is provided with an insulation layer, and the temperature is not lower than 60°C.

[0054] High-concentration sodium vanadate solutions are prone to crystallization or solidification at low temperatures. The material in the storage tank is kept at a high temperature, so no additional preheating is required when it is transported to subsequent processes.

[0055] In some embodiments, the output end of the pressure separator 52 is connected to the input end of the storage tank 4, and is configured to store the filtrate of the underflow residue in the storage tank.

[0056] The underflow filtrate produced by the pressure separator 52 often contains recyclable substances and is directly transported to the storage tank 4 to avoid external discharge or secondary treatment, thereby improving the resource recovery rate. After storage, the filtrate can be centrally treated to achieve compliant discharge or resource utilization.

[0057] In some embodiments, the purpose of this utility model is to provide a purification system for vanadium slag sodium salt roasted clinker leachate, configured to separate residue and dephosphorized slag from phosphorus-containing vanadium leachate. The purification system comprises: a vacuum separator for washing and solid-liquid separation of the slurry after leaching the vanadium slag sodium salt roasted clinker with a dilute solution, allowing vanadium to enter the leachate; a centrifugal separator for further solid-liquid separation of the vanadium leachate separated by the vacuum separator, removing fine particulate residue; a purification tank for adding calcium chloride to the vanadium leachate separated by the centrifugal separator, causing it to react with phosphorus; a storage tank for storing the vanadium solution in the purification tank before proceeding to the vanadium recovery process; and a pressure separator for solid-liquid separation of the underflow slag in the purification tank. According to the above system, before the vanadium leaching solution is purified and dephosphorized, the vanadium leaching solution is separated from the fine particulate residue therein. The separated residue, along with the leaching residue, is treated as a low-grade vanadium resource. The dephosphorization slag formed by adding calcium chloride to the clarified vanadium leaching solution is small in quantity, simple in composition, and high in vanadium content. Therefore, the purification and dephosphorization of the vanadium leaching solution can be achieved without complex processes, and the mixing of fine particulate residue with the dephosphorization slag is avoided. This allows for the separate recycling of the residue and the dephosphorization slag, reducing the cost of treating vanadium-containing solid waste.

[0058] Figure 2 This is a schematic diagram illustrating the processing steps in the vanadium slag roasted clinker leaching solution purification system of this invention. The roasted clinker, the processing target of the system in this embodiment, can be roasted clinker obtained from vanadium slag through sodium salt roasting, or roasted clinker obtained from further vanadium extraction from vanadium-containing raw materials such as steel slag and ferrophosphate. The sodium salt can be one or a mixture of sodium chloride and sodium carbonate.

[0059] like Figure 2As shown, the processing system in this embodiment includes: a vacuum separation process P1, which leaches, washes, and separates solids and liquids from the roasted clinker, allowing vanadium in the roasted clinker to enter the solution and obtain vanadium leachate; a centrifugal separation process P2, which centrifuges the fine particulate residue in the vanadium leachate to further reduce the solid content in the vanadium leachate; a purification process P3, which adds calcium chloride to the centrifuged vanadium leachate to remove phosphorus, allowing phosphorus to enter the underflow slag; a storage process P4, where the purified and phosphorus-removed vanadium leachate is stored in a storage device for subsequent vanadium recovery processing; and a pressure separation process P5, which washes, presses, and separates the underflow slag generated after the purification and phosphorus removal of the vanadium leachate, with the phosphorus-removed slag being used for further vanadium extraction, thereby improving the system's vanadium yield at a lower cost.

[0060] First, the vacuum separation process P1 will be described. Vacuum separation process P1 includes a high-level buffer tank 11 and a vacuum separator 12. The high-level buffer tank stores the roasted clinker slurry. The high-level buffer tank 11 contains a mixture of roasted clinker and a low-vanadium-concentration dilute solution produced by multi-stage washing in the vacuum separator. The roasted clinker slurry is continuously fed from the high-level buffer tank 11 to the vacuum separator 12. The high-level buffer tank 11 is equipped with a stirring mechanism. After the roasted clinker slurry is washed with water in the vacuum separator, most of the vanadium enters the vanadium leaching solution. The residue produced by the vacuum separator has a low vanadium content and can be further processed for vanadium extraction or used as other resources. The amount of water added to the vacuum separator 12 is set to be 1.0 to 2.5 times the weight of the roasted clinker, and the amount of dilute solution added is set to be 0.5 to 1.5 times the weight of the roasted clinker.

[0061] Next, the centrifugal separation process P2 will be described. Centrifugal separation process P2 further separates the fine particulate residue from the vanadium leaching solution produced by the vacuum separator P1, ensuring minimal inclusions in the subsequent dephosphorization slag. For this purpose, the centrifugal separator 2 can be composed of a horizontal spiral centrifugal sedimentation unit. The centrifugal separator 2 separates the vanadium leaching solution from the fine particulate residue within it. The fine particulate residue can be utilized together with the residue produced by the vacuum separator 1. It should be noted that the centrifugal separator is equipped with an automatic control system, including automatic cleaning.

[0062] Next, the purification process P3 will be explained. Purification process P3 is for dephosphorizing the vanadium leaching solution produced by centrifugal separation process P2. For this purpose, purification tank 3 is equipped with a stirring mechanism and an overflow port. In purification process P3, calcium chloride is added to purification tank 3. As a result, dephosphorized slag is generated in purification tank 3. The following two reactions occur in purification tank 3 where calcium chloride has been introduced:

[0063] Ca 2+ +PO4 3- →Ca3(PO4)2……(1)

[0064] Ca 2++VO3 3- →Ca(VO3)3……(2)

[0065] As shown in reaction 1, the phosphorus concentration in the vanadium solution decreases by generating calcium phosphate. Simultaneously, a side reaction, as shown in reaction 2, occurs, generating calcium vanadate. Because calcium phosphate is less soluble than calcium vanadate, the vanadium loss during phosphorus removal is relatively small.

[0066] Next, the storage process P4 will be described. Storage process P4 involves aging the vanadium leachate obtained from the overflow of purification tank 3 in purification process P3 to obtain a clarified vanadium leachate, which is then transported to the vanadium recovery process. For this purpose, storage tank 4 is equipped with an insulation layer to ensure that the temperature of the vanadium leachate is not lower than 60°C. It should be noted that the filtrate from the underflow slag produced in purification process P3, after solid-liquid separation, can also enter storage tank 4.

[0067] Finally, the pressure separation process P5 will be described. Pressure separation process P5 performs solid-liquid separation on the underflow slag obtained after treatment in purification process P3. For this purpose, pressure separation process P5 consists of an underflow tank 51 and a pressure separator 52. The underflow slag in underflow tank 51 is washed and subjected to solid-liquid separation by pressure filter press 52. Water-soluble vanadium is removed from the underflow slag, and after pressing, dephosphorized slag is obtained. The filtrate enters storage tank 4. The amount of water added to pressure separator 52 is set to be 0.5 to 1.0 times the weight ratio of the dephosphorized slag.

[0068] As described above, according to this embodiment, the vanadium leachate, after being washed and separated in vacuum separator 12, is further separated in centrifugal separator 2, significantly reducing the solid content in the vanadium leachate. Therefore, in the subsequent purification tank 3, less calcium chloride can be added to achieve sedimentation, and the amount of dephosphorization slag generated is significantly reduced, as well as the vanadium loss rate is lowered. Furthermore, the dephosphorization slag is small in volume, simple in composition, and high in vanadium content, making it easy to recover the high-value vanadium from it at low cost.

[0069] The above embodiments are possible examples of implementations of this utility model, and are provided only to enable those skilled in the art to clearly understand the principles of this utility model. Those skilled in the art should understand that the above discussion of any embodiment is merely exemplary and is not intended to imply that the scope of the disclosed embodiments of this utility model includes claims limited to these examples. Under the overall concept of this utility model, the technical features of the above embodiments or different embodiments can also be combined with each other, resulting in many other variations of different aspects of the embodiments of this utility model as described above. For the sake of brevity, these variations are not provided in the specific embodiments. Therefore, any omissions, modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the embodiments of this utility model should be included within the protection scope claimed by this utility model.

Claims

1. A purification system for vanadium slag sodium salt roasting clinker leachate, characterized in that, include: High-level buffer tank (11), vacuum separator (12), centrifugal separator (2), purification tank (3), storage tank (4), underflow tank (51) and pressurized separator (52); The output end of the high-level buffer tank (11) is connected to the input end of the vacuum separator (12), which is configured to wash and separate the solid and liquid of the sodium-roasted vanadium slag clinker to obtain vanadium leachate. The output end of the vacuum separator (12) is connected to the input end of the centrifugal separator (2), and the centrifugal separator (2) is configured to perform solid-liquid separation on the vanadium leaching solution again; The output end of the centrifuge (2) is connected to the input end of the purification tank (3), which is configured to add calcium chloride to the vanadium leaching solution to obtain vanadium solution and underflow residue. The output end of the purification tank (3) is connected to the input end of the storage tank (4) and the underflow tank (51). The storage tank (4) is configured to store vanadium solution, and the underflow tank (51) is configured to store underflow slag. The output end of the underflow tank (51) is connected to the input end of the pressurized separator (52), which is configured to process underflow slag.

2. The purification system for the vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The input end of the high-level buffer tank (11) is also connected to the output end of the vacuum separator (12).

3. The purification system for vanadium slag sodium salt roasting clinker leachate according to claim 2, characterized in that, The high-level buffer tank (11) is configured to store a mixture slurry of vanadium slag sodium salt roasted clinker and dilute liquid with low vanadium concentration generated by multi-stage washing in a vacuum separator.

4. The purification system for the vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The high-level buffer tank (11) includes a spiral stirring mechanism.

5. The purification system for the vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The vacuum separator (12) is configured to add water and dilute liquid, with the weight ratio of water to vanadium slag sodium salt roasted clinker ranging from 1 to 2.5, and the weight ratio of dilute liquid to vanadium slag sodium salt roasted clinker ranging from 0.5 to 1.

5.

6. The purification system for vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The centrifuge (2) is composed of a horizontal spiral centrifugal sedimentation mechanism.

7. The purification system for vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The purification tank (3) includes a fan-shaped stirring mechanism.

8. The purification system for the vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The output end of the purification tank (3) is an overflow port.

9. The purification system for the vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The storage tank (4) is equipped with an insulation layer with a temperature not lower than 60°C.

10. The purification system for vanadium slag sodium salt roasting clinker leachate according to claim 1, characterized in that, The output end of the pressurized separator (52) is connected to the input end of the storage tank (4), and is configured to store the filtrate of the underflow sludge in the storage tank.

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