CN217780770U - System for producing nickel sulfate solution - Google Patents
System for producing nickel sulfate solution Download PDFInfo
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- CN217780770U CN217780770U CN202221829198.0U CN202221829198U CN217780770U CN 217780770 U CN217780770 U CN 217780770U CN 202221829198 U CN202221829198 U CN 202221829198U CN 217780770 U CN217780770 U CN 217780770U
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Abstract
The utility model discloses a system for production nickel sulfate solution, this system leach the unit, fall sour unit and edulcoration unit including the combination. The liquid outlet of the chemical combination leaching unit is communicated with the liquid inlet of the deacidification unit through a first conveying device. And a liquid outlet of the deacidification unit is communicated with a liquid inlet of the impurity removal unit through a second conveying device. And a liquid outlet of the impurity removal unit is communicated with a liquid inlet of the finished product storage tank through a third conveying device. The battery-grade manganese-containing nickel sulfate solution is obtained through concentrated sulfuric acid leaching, deacidification treatment, multiple times of filtering and impurity removal. The nickel powder leaching method has the characteristics of high leaching rate, low nickel sulfate impurity content in the finished product, simple production process and device, safety, environmental protection, low production cost and the like, and has excellent popularization and application values.
Description
Technical Field
The utility model relates to a non ferrous metal production facility, concretely relates to system for producing battery level nickel sulfate solution belongs to non ferrous metal production technical field.
Background
With the rapid development of new energy industries in recent years, the demand of markets for ternary battery materials is rapidly increased, nickel sulfate and manganese sulfate are respectively used as main sources of nickel and manganese elements, the global sales volume of nickel sulfate and manganese sulfate is increased year by year, and the ternary battery material has great production value. The invention introduces a method for industrially producing a battery-grade manganese-containing nickel sulfate solution by using metallic nickel and metallic manganese as main raw materials.
At present, the preparation of nickel sulfate solution mainly comprises methods such as an electrolytic method, wet recovery, a nickel-sulfation method and the like, wherein the electrolytic method and the wet recovery process flow are complex, the energy consumption is high, the production cost is high, and the prepared nickel sulfate solution has high impurity content and can not meet the quality requirement of the existing ternary battery material; the nickel-sulfation method utilizes the direct reaction of the simple substance nickel and the sulfuric acid to prepare the nickel sulfate solution with higher purity, but the leaching efficiency is low, the period is long, and the impurity removal process is inThe problems of difficult deacidification of a system, high price of auxiliary materials containing nickel and the like cause large investment of production equipment, complex production flow and high cost of the auxiliary materials. The invention patent with publication number CN111689530A discloses a method and a device for producing nickel sulfate solution, the method comprises mixing nickel powder and dilute sulfuric acid at normal temperature for 8 days to obtain a first nickel sulfate solution with a certain concentration, then performing solid-liquid separation, adding new nickel powder into the filtrate for mixing, then dropping 27.5% hydrogen peroxide at a certain rate to control the temperature within a certain range, and reacting for 12h to obtain pH of 1.5 and Ni 2+ Adding hydrogen peroxide into the second nickel sulfate solution with the concentration of 122g/L at a certain speed until the pH value is 3.5-4.5, consuming 4 hours, and finally obtaining the leaching residue of the nickel sulfate solution through extraction, saponification, oil removal and filtration. The stirring device has the advantages of low energy consumption, cleanness and environmental protection, and can effectively stir up the nickel powder deposited at the bottom of the kettle and improve the reaction rate. But no external heat source is used in the whole process, the concentration of the used sulfuric acid is low, and the leaching period is overlong; the auxiliary material hydrogen peroxide has higher concentration, lower utilization rate and overlarge consumption, the temperature of the system needs to be strictly monitored and the adding speed of the hydrogen peroxide needs to be adjusted after the hydrogen peroxide is added, and the auxiliary material and labor cost is high; the whole process of leaching, deacidifying and removing impurities is complex, and the production cost is not saved.
SUMMERY OF THE UTILITY MODEL
To the deficiency of the prior art, the utility model provides a system for production nickel sulfate solution leaches, falls sour processing and filters many times and obtains battery level manganese-containing nickel sulfate solution behind the edulcoration process through the concentrated sulfuric acid. The nickel powder leaching method has the characteristics of high leaching rate, low nickel sulfate impurity content in the finished product, simple production process and device, safety, environmental protection, low production cost and the like, and has excellent popularization and application values.
In order to achieve the above object, the utility model adopts the following technical scheme:
a system for producing a nickel sulfate solution comprises a chemical combination leaching unit, an acid reduction unit and an impurity removal unit. The liquid outlet of the chemical combination leaching unit is communicated with the liquid inlet of the deacidification unit through a first conveying device. And a liquid outlet of the deacidification unit is communicated with a liquid inlet of the impurity removal unit through a second conveying device. And a liquid outlet of the impurity removal unit is communicated with a liquid inlet of the finished product storage tank through a third conveying device.
Preferably, the combined leaching unit comprises at least one combined leaching tank. The feed inlet of any one chemical combination leaching barrel is communicated with a nickel block feeding device, a concentrated sulfuric acid feeding pipeline and a high-temperature water feeding pipeline. The liquid discharge ports of all the chemical leaching barrels are communicated with the first conveying device.
Preferably, a hydrogen concentration detection mechanism, a first sulfuric acid concentration detection device and a temperature detection device are further arranged in any one of the chemical leaching tanks.
Preferably, the acid reducing unit comprises at least one acid reducing barrel. The feed inlet of any one of the acid reducing barrels is communicated with a nickel powder feeding device and a first hydrogen peroxide adding pipeline. The feed inlets of all the acid-reducing barrels are communicated with the first conveying device, and the liquid discharge ports of all the acid-reducing barrels are communicated with the second conveying device.
Preferably, a heating mechanism is further arranged in any one of the acid dropping barrels. The heating mechanism is an electric heating wire or an electric heating pipe or a hot water heating device (for example, hot pure water is directly introduced through a pipeline) arranged on the wall and/or the bottom of the deacidification bucket.
Preferably, a stirring mechanism is further arranged in any one of the acid-reducing barrels. The stirring mechanism comprises a stirring motor, a stirring shaft and stirring blades. The stirring motor is arranged on the top cover of the acid-reducing barrel, the upper end of the stirring shaft is connected with the stirring motor, the lower end of the stirring shaft penetrates through the top cover and then extends into the acid-reducing barrel, and the stirring blade is arranged on the stirring shaft positioned in the acid-reducing barrel. The side part of the deacidification bucket is also provided with a circulating clear liquid groove, the bottom of the circulating clear liquid groove is communicated with the deacidification bucket, and a filter screen is arranged on a communication hole between the circulating clear liquid groove and the deacidification bucket. And a pressure pump is also arranged on one side of the top cover of the deacidification bucket, which is positioned on the stirring motor. The stirring shaft and the stirring blade are of hollow cavity structures which are communicated with each other, and the stirring blade is provided with a plurality of spray holes which are communicated with the inner cavity of the stirring blade. The liquid inlet end of the liquid inlet pipe of the pressure pump is thrown below the liquid level of the circulating clear liquid groove, and the liquid outlet of the liquid outlet pipe of the pressure pump is communicated with the cavity of the stirring shaft.
Preferably, a second sulfuric acid concentration detection device and a pH detection mechanism are further provided in any one of the acid-reducing drums.
Preferably, the impurity removing unit comprises a first filtering device, a first impurity removing barrel, a second filtering device, a second impurity removing barrel and a third filtering device. The first filtering device, the first impurity removal barrel, the second filtering device, the second impurity removal barrel and the third filtering device are sequentially communicated in series through a filtrate conveying pipeline. The feed inlet of the first filtering device is communicated with the second conveying device, and the liquid outlet of the third filtering device is communicated with the third conveying device.
Preferably, the feed inlet of the first impurity removing barrel is also communicated with a second hydrogen peroxide adding pipeline. And the feed inlet of the second impurity removing barrel is also communicated with a sodium sulfide feeding device.
Preferably, the system further comprises a control system, wherein the control system is in wired and/or wireless electric signal connection with each component, and the control system controls the start and stop of each component of the system.
The utility model discloses in, the combination leaches the unit and has realized the preliminary leaching of metallic nickel, and the deacidification unit has realized the further leaching of metallic nickel, and the purification unit that edulcoration filter unit has realized containing manganese nickel sulfate solution leaches the unit, deacidification unit and edulcoration filter unit's integrated processing through the combination, has obtained the battery level of high-quality containing manganese nickel sulfate solution.
The utility model discloses in, can add a large amount of fresh metallic nickel powder and low concentration hydrogen peroxide solution in the deacidification bucket, through stirring mixing effect, and then increase the area of contact of solution and metal, and then accelerate leaching and deacidification speed. The device comprises a stirring mechanism, a circulating clear liquid tank, a filter screen, a stirring blade and spray holes, wherein the circulating clear liquid tank is communicated with the inner cavity of the deacidification barrel, the filter screen is arranged at a through hole between the circulating clear liquid tank and the inner cavity of the deacidification barrel, the stirring mechanism in the deacidification barrel and the stirring blade are both of hollow tubular structures, the inner cavity of the stirring shaft is communicated with the inner cavity of the stirring blade, and the stirring blade is also provided with the spray holes which are uniformly distributed and communicated with the inner cavity of the stirring shaft (if necessary, the shaft wall of the stirring shaft can be provided with the spray holes communicated with the inner cavity of the stirring shaft); further, through addding the force pump, in the clear solution via circulation pipeline pump to the inner chamber of (mixing) shaft in the clear solution groove that will circulate, at last from the orifice blowout on the stirring paddle leaf, the rotation of stirring paddle leaf, the solution production whirl in the sour bucket is fallen in the stirring, meanwhile, from the high-speed rotatory rivers of stirring paddle leaf orifice blowout and the whirl solution collision in the sour bucket that falls, and then improved the mixed flow effect of the inside solution of sour bucket that falls greatly, and the high-speed rotatory rivers of injection itself is exactly one part of the interior solution of sour bucket that falls, promptly under the prerequisite that does not change the inside solution composition nature of sour bucket that falls, the utility model discloses a special rabbling mechanism cooperates special sour bucket that falls, has improved metal leaching and has fallen sour speed greatly.
The utility model discloses in, control system can control opening of the component part of each unit and stop to according to predetermineeing the cooperation between them of program control, it is high to have degree of automation, and artifical dependency is low and avoid artificial operation error's advantage.
The utility model discloses in, in the chemical combination leaching barrel is arranged in through cubic metallic nickel (purity > 99%) to add concentrated sulfuric acid solution (purity > 98%), under the condition of 80-150 ℃, carry out preliminary chemical combination reaction, when the residual acid content is less than or equal to 150g/L, shift to the deacidification and deacidification bucket again, add likepowder metallic nickel (purity > 99%) and hydrogen peroxide solution simultaneously, stirring reaction 6-12h, adjust pH value and sulphide at last and carry out the edulcoration, filter through the precision filtration cloth and obtain nickel sulfate solution. The nickel powder leaching agent has the characteristics of high leaching rate, nickel powder, low content of nickel sulfate impurities in a finished product, simple production process and device, safety, environmental protection, low production cost and the like.
Adopt the system of production nickel sulfate solution's concrete step as follows:
chemical leaching: adding a small amount of hot pure water into a chemical combination leaching barrel to bottom, then adding excessive massive metal nickel, and mixing according to a mass ratio (metal nickel: concentrated sulfuric acid = 1.7) Slowly adding concentrated sulfuric acid for multiple times for leaching, wherein the adding amount is not more than 1m each time 3 Synchronously monitoring the hydrogen concentration, timely supplementing hot pure water when the hydrogen concentration exceeds a safe value, continuously reacting for 8-10h after the acid addition is finished, monitoring the temperature in the barrel, timely supplementing the hot pure water when the temperature is lower than 80 ℃, keeping the temperature above 80 ℃, and performing acid reduction operation when the residual acid is lower than 150 g/L.
Acid reduction treatment: transferring the leachate into an acid reduction barrel, adding fresh metal nickel powder according to the acidity of the leachate in a ratio of (2-4T), starting a stirring mechanism and heating until the acidity reaches within 10 g/L; after the acidity of the solution is reduced to a certain range, adding diluted hydrogen peroxide (the content is 12.5-15%) until the pH value is between 3.5 and 4.5, and then carrying out filtration and impurity removal operation.
And (3) filtering and removing impurities: filtering the solution with qualified pH, and filtering the filtrate in an impurity removal unit according to the proportion of adding hydrogen peroxide (the content is more than or equal to 27 percent), filtering and adding Na 2 And S-filtering is carried out in sequence to obtain the manganese-containing nickel sulfate solution which meets the standards of battery-grade nickel sulfate and manganese solution.
Further, the available volume of chemical combination leaching barrel is not less than 50m 3 (preferably) 60m 3 The actual volume is generally 40-45m 3 (ii) a The high-temperature water is boiler steam condensate of 70-90 deg.C (such as about 80 deg.C). The concentrated sulfuric acid is 98% industrial sulfuric acid, the reaction between the acid and nickel is slow, the concentration of the sulfuric acid in the barrel is about 180-240g/L after the charging is finished, and the highest temperature of the system can reach 85 ℃.
In the chemical combination leaching process, the leaching solution containing 130-140g/L of nickel sulfate is obtained after soaking for 15-20h without stirring in the whole process. In the process of transferring the leachate, the amount of the leachate discharged from each chemical combination leaching barrel is about 2/3-3/4 of the total amount of the leachate, and because the nickel beans in the chemical combination barrel do not react completely, the leachate discharged is only the upper layer liquid of the nickel beans in the chemical combination barrel, and the residual nickel beans can be used for next leaching.
In the utility model, in the deacidification treatment process, the amount of the put nickel powder is calculated according to the amount of residual acid in the barrel and the mass ratio (nickel: sulfuric acid = 1.7), and the nickel powder is generally obtained every 30m 3 1.2-1.4t nickel powder (corresponding to residual acid) is added into the leaching solutionThe amount is 70-80 g/L). Meanwhile, the temperature in the barrel needs to be controlled to be about 80 ℃ and the mixture is rapidly stirred so as to accelerate the reaction of the nickel powder and the residual acid; the reaction is carried out until the acidity of the solution is about 30-40g/L, the stirring is decelerated and the temperature rise is stopped. Specifically, the deacidification bucket is provided with a specially-made titanium stirring rod, nickel powder deposited at the bottom of the bucket can be stirred up to increase the reaction contact area and accelerate the deacidification speed, and the time required by the whole deacidification process is about 8-12 h.
The utility model discloses an in the filtration edulcoration: adding hydrogen peroxide into the filtrate to make the pH value reach about 4.5, completely oxidizing and precipitating Fe ions in the filtrate, and removing the Fe ions by filtering (filter pressing); adding Na into the residual heavy metal impurities 2 S can be basically completely precipitated and can be removed by filtration; and finally, the filtrate meets the standard of battery-grade nickel sulfate solution. In particular, it is generally every 30m 3 Only about 200kg of 27.5 mass percent hydrogen peroxide and about 10kg of Na are needed to be added into the filtrate 2 And S, removing impurities.
Compared with the prior art, the utility model discloses a beneficial technological effect as follows:
use the technical scheme of the utility model, on the basis that the quality of guaranteeing the gained product accords with battery level nickel sulfate, manganese solution standard, greatly shortened the production cycle of nickel sulfate solution, reduced the quantity of auxiliary material, simplified production facility and process flow, reduced manufacturing cost to a great extent. Because the reaction rate of nickel and dilute sulfuric acid is greatly slowed down along with the increase of nickel concentration and the decrease of sulfuric acid concentration in the later period, the scheme creates a high-temperature and high-acid reaction environment by adding a safe heat source (high-temperature steam condensate), supplementing high-temperature water at random time and improving the initial sulfuric acid concentration, prevents the leaching from being blocked by too high nickel concentration, can greatly accelerate the reaction rate of a system and shortens the leaching time. The high-temperature distilled cooling water used in the scheme is a boiler power generation byproduct, the energy consumption is low, the production efficiency is high, the safety and the environmental protection are realized, and the comprehensive cost is obviously reduced compared with the prior art.
Drawings
Fig. 1 is a schematic diagram of a system for producing nickel sulfate solution according to the present invention.
Fig. 2 is a schematic diagram of the overall structure of the system for producing nickel sulfate solution according to the present invention.
Fig. 3 is a schematic structural view of the acid-reducing barrel of the present invention.
Fig. 4 is a simplified diagram of the structure of the impurity removing unit of the present invention.
Reference numerals are as follows: 1: a chemical combination leaching unit; 101: a chemical combination leaching barrel; 102: a nickel block feeding device; 103: a concentrated sulfuric acid addition pipeline; 104: a high-temperature water addition pipe; 105: a hydrogen concentration detection mechanism; 106: a first sulfuric acid concentration detection device; 107: a temperature detection device; 2: a deacidification unit; 201: a deacidification bucket; 202: a nickel powder feeding device; 203: a first oxygenated water addition conduit; 204: a heating mechanism; 205: a stirring mechanism; 206: a second sulfuric acid concentration detection device; 207: circulating a clear liquid tank; 210: a pH detection mechanism; 3: an impurity removal unit; 301: a first filtering device; 302: a first impurity removal barrel; 303: a second filtering device; 304: a second impurity removal barrel; 305: a third filtering device; 306: a second oxygenated water addition conduit; 307: a sodium sulfide feeding device; 4: a finished product storage tank; s1: a first conveying device; s2: a second conveying device; s3: and a third conveying device.
Detailed Description
The technical solution of the present invention is illustrated below, and the claimed invention includes but is not limited to the following embodiments.
A system for producing a nickel sulfate solution comprises a chemical combination leaching unit 1, an acid reducing unit 2 and an impurity removing unit 3. The liquid outlet of the chemical combination leaching unit 1 is communicated with the liquid inlet of the deacidification unit 2 through a first conveying device S1. The liquid outlet of the deacidification unit 2 is communicated with the liquid inlet of the impurity removal unit 3 through a second conveying device S2. The liquid outlet of the impurity removing unit 3 is communicated with the liquid inlet of the finished product storage tank 4 through a third conveying device S3.
Preferably, the chemical leaching unit 1 comprises at least one chemical leaching vat 101. The feed inlet of any one of the chemical combination leaching barrels 101 is communicated with a nickel block adding device 102, a concentrated sulfuric acid adding pipeline 103 and a high-temperature water adding pipeline 104. The liquid outlets of all the chemical leaching barrels 101 are communicated with the first conveying device S1.
Preferably, a hydrogen concentration detection mechanism 105, a first sulfuric acid concentration detection device 106 and a temperature detection device 107 are further provided in any one of the chemical leaching tanks 101.
Preferably, the acid reduction unit 2 comprises at least one acid reduction barrel 201. The feed inlet of any one of the acid-reducing barrels 201 is communicated with a nickel powder feeding device 202 and a first hydrogen peroxide adding pipeline 203. The feed inlets of all the acid-reducing barrels 201 are communicated with a first conveying device S1, and the liquid discharge ports of all the acid-reducing barrels 201 are communicated with a second conveying device S2.
Preferably, a heating mechanism 204 is further disposed in any one of the acid-reducing barrels 201. The heating mechanism 204 is an electric heating wire or an electric heating pipe or a hot water heating device arranged on the wall and/or the bottom of the acid-reducing barrel 201.
Preferably, any one of the acid-reducing barrels 201 is further provided with a stirring mechanism 205. The stirring mechanism 205 includes a stirring motor 2051, a stirring shaft 2052, and a stirring blade 2053. The stirring motor 2051 is arranged on the top cover of the deacidification bucket 201, the upper end of the stirring shaft 2052 is connected with the stirring motor 2051, the lower end of the stirring shaft 2052 penetrates through the top cover and then extends into the deacidification bucket 201, and the stirring blades 2053 are arranged on the stirring shaft 2052 positioned in the deacidification bucket 201. The side of the deacidification bucket 201 is also provided with a circulating clear liquid groove 207, the bottom of the circulating clear liquid groove 207 is communicated with the deacidification bucket 201, and a filter screen 208 is arranged on a communication hole between the circulating clear liquid groove 207 and the deacidification bucket 201. A pressure pump 209 is also arranged on the top cover of the deacidification bucket 201 at one side of the stirring motor 2051. The stirring shaft 2052 and the stirring blade 2053 are in communicated cavity structures, and the stirring blade 2053 is provided with a plurality of spray holes 2054 communicated with the inner cavity of the stirring blade. The liquid inlet end of the liquid inlet pipe of the pressure pump 209 is thrown below the liquid level of the circulating clear liquid groove 207, and the liquid outlet of the liquid outlet pipe is communicated with the cavity of the stirring shaft 2052.
Preferably, a second sulfuric acid concentration detection device 206 and a pH detection mechanism 210 are further provided in any one of the acid dropping tanks 201.
Preferably, the trash unit 3 includes a first filtering device 301, a first trash can 302, a second filtering device 303, a second trash can 304, and a third filtering device 305. The first filtering device 301, the first impurity removing barrel 302, the second filtering device 303, the second impurity removing barrel 304 and the third filtering device 305 are sequentially communicated in series through a filtrate conveying pipeline. The feed inlet of the first filtering device 301 is communicated with the second conveying device S2, and the liquid outlet of the third filtering device 305 is communicated with the third conveying device S3.
Preferably, the feed inlet of the first impurity removing barrel 302 is also communicated with a second hydrogen peroxide adding pipeline 306. The feed inlet of the second impurity removing barrel 304 is also communicated with a sodium sulfide feeding device 307.
Preferably, the system further comprises a control system, wherein the control system is in wired and/or wireless electric signal connection with each component, and the control system controls the start and stop of each component of the system.
Example 1
As shown in fig. 1 to 4, a system for producing a nickel sulfate solution includes a combination leaching unit 1, an acid reduction unit 2, and an impurity removal unit 3. The liquid outlet of the chemical combination leaching unit 1 is communicated with the liquid inlet of the deacidification unit 2 through a first conveying device S1. The liquid outlet of the deacidification unit 2 is communicated with the liquid inlet of the impurity removal unit 3 through a second conveying device S2. And a liquid outlet of the impurity removal unit 3 is communicated with a liquid inlet of the finished product storage tank 4 through a third conveying device S3.
Example 2
Example 1 was repeated except that the chemical leaching unit 1 included at least one chemical leaching tank 101. The feed inlet of any one of the compound leaching barrels 101 is communicated with a nickel block adding device 102, a concentrated sulfuric acid adding pipeline 103 and a high-temperature water adding pipeline 104. The liquid discharge ports of all the chemical leaching barrels 101 are communicated with the first conveying device S1.
Example 3
Example 2 was repeated, except that a hydrogen concentration detection means 105, a first sulfuric acid concentration detection device 106 and a temperature detection device 107 were provided in any of the chemical leaching tanks 101.
Example 4
Example 3 is repeated except that the acid reducing unit 2 comprises at least one acid reducing tank 201. The feed inlet of any one of the acid-reducing barrels 201 is communicated with a nickel powder adding device 202 and a first hydrogen peroxide adding pipeline 203. The feed inlets of all the acid-reducing barrels 201 are communicated with the first conveying device S1, and the liquid discharge outlets of all the acid-reducing barrels 201 are communicated with the second conveying device S2.
Example 5
Example 4 is repeated, except that a heating mechanism 204 is further arranged in any one of the acid-reducing barrels 201. The heating mechanism 204 is an electric heating pipe arranged on the wall and the bottom of the acid-reducing barrel 201.
Example 6
Example 5 is repeated except that the heating mechanism 204 is a hot pure water delivery pipeline communicated with the barrel cavity of the deacidification barrel 201.
Example 7
Example 6 is repeated, except that any one of the acid-reducing barrels 201 is also provided with a stirring mechanism 205. The stirring mechanism 205 includes a stirring motor 2051, a stirring shaft 2052, and a stirring blade 2053. The stirring motor 2051 is arranged on the top cover of the deacidification bucket 201, the upper end of the stirring shaft 2052 is connected with the stirring motor 2051, the lower end of the stirring shaft 2052 penetrates through the top cover and then extends into the deacidification bucket 201, and the stirring blade 2053 is arranged on the stirring shaft 2052 positioned in the deacidification bucket 201. The side of the deacidification bucket 201 is also provided with a circulating clear liquid groove 207, the bottom of the circulating clear liquid groove 207 is communicated with the deacidification bucket 201, and a filter screen 208 is arranged on a communication hole between the circulating clear liquid groove 207 and the deacidification bucket 201. A pressure pump 209 is also arranged on the top cover of the deacidification bucket 201 at one side of the stirring motor 2051. The stirring shaft 2052 and the stirring blade 2053 are of a hollow cavity structure communicated with each other, and the stirring blade 2053 is provided with a plurality of spray holes 2054 communicated with the inner cavity thereof. The liquid inlet end of the liquid inlet pipe of the pressure pump 209 is thrown below the liquid level of the circulating clear liquid groove 207, and the liquid outlet of the liquid outlet pipe is communicated with the cavity of the stirring shaft 2052.
Example 8
Example 7 was repeated, except that a second sulfuric acid concentration detection device 206 and a pH detection mechanism 210 were provided in any of the acid-reducing tanks 201.
Example 9
Example 8 is repeated except that the trash unit 3 includes a first filtering device 301, a first trash can 302, a second filtering device 303, a second trash can 304, and a third filtering device 305. The first filtering device 301, the first impurity removing barrel 302, the second filtering device 303, the second impurity removing barrel 304 and the third filtering device 305 are sequentially communicated in series through a filtrate conveying pipeline. The feed inlet of the first filtering device 301 is communicated with the second conveying device S2, and the liquid outlet of the third filtering device 305 is communicated with the third conveying device S3.
Example 10
Example 9 was repeated except that the feed inlet of the first trash can 302 was also connected to a second oxygenated water addition line 306. The feed inlet of the second impurity removing barrel 304 is also communicated with a sodium sulfide feeding device 307.
Example 11
The embodiment 10 is repeated, except that the system further comprises a control system, the control system is in wireless electric signal connection with each component, and the control system is used for controlling the start and stop of each component of the system.
Claims (10)
1. A system for producing a nickel sulfate solution, comprising: the system comprises a chemical combination leaching unit (1), an acid reduction unit (2) and an impurity removal unit (3); a liquid outlet of the chemical combination leaching unit (1) is communicated with a liquid inlet of the deacidification unit (2) through a first conveying device (S1); a liquid outlet of the deacidification unit (2) is communicated with a liquid inlet of the impurity removal unit (3) through a second conveying device (S2); the liquid outlet of the impurity removal unit (3) is communicated with the liquid inlet of the finished product storage tank (4) through a third conveying device (S3).
2. The system of claim 1, wherein: the combined leaching unit (1) comprises at least one combined leaching barrel (101); a feed inlet of any one of the chemical combination leaching barrels (101) is communicated with a nickel block adding device (102), a concentrated sulfuric acid adding pipeline (103) and a high-temperature water adding pipeline (104); the liquid discharge ports of all the chemical compound leaching barrels (101) are communicated with the first conveying device (S1).
3. The system of claim 2, wherein: a hydrogen concentration detection mechanism (105), a first sulfuric acid concentration detection device (106) and a temperature detection device (107) are arranged in any one of the chemical leaching barrels (101).
4. The system according to any one of claims 1-3, wherein: the acid reduction unit (2) comprises at least one acid reduction barrel (201); a feed inlet of any one of the acid reducing barrels (201) is communicated with a nickel powder adding device (202) and a first hydrogen peroxide adding pipeline (203); the feed inlets of all the acid-reducing barrels (201) are communicated with a first conveying device (S1), and the liquid discharge ports of all the acid-reducing barrels (201) are communicated with a second conveying device (S2).
5. The system of claim 4, wherein: a heating mechanism (204) is also arranged in any one of the acid-reducing barrels (201); the heating mechanism (204) is an electric heating wire or an electric heating pipe or a hot water heating device which is arranged on the wall and/or the bottom of the acid-reducing barrel (201).
6. The system of claim 5, wherein: a stirring mechanism (205) is also arranged in any one of the acid-reducing barrels (201); the stirring mechanism (205) comprises a stirring motor (2051), a stirring shaft (2052) and a stirring blade (2053); the stirring motor (2051) is arranged on a top cover of the acid-reducing barrel (201), the upper end of the stirring shaft (2052) is connected with the stirring motor (2051), the lower end of the stirring shaft penetrates through the top cover and then extends into the acid-reducing barrel (201), and the stirring blade (2053) is arranged on the stirring shaft (2052) positioned in the acid-reducing barrel (201); a circulating clear liquid groove (207) is also arranged on the side part of the deacidification barrel (201), the bottom of the circulating clear liquid groove (207) is communicated with the deacidification barrel (201), and a filter screen (208) is arranged on a communication hole between the circulating clear liquid groove (207) and the deacidification barrel (201); a pressure pump (209) is also arranged on one side of the top cover of the deacidification bucket (201) which is positioned at the stirring motor (2051); the stirring shaft (2052) and the stirring blade (2053) are internally provided with cavity structures which are communicated with each other, and the stirring blade (2053) is provided with a plurality of spray holes (2054) which are communicated with the inner cavity of the stirring blade; the liquid inlet end of a liquid inlet pipe of the pressure pump (209) is thrown below the liquid level of the circulating clear liquid groove (207), and the liquid outlet of a liquid outlet pipe of the pressure pump is communicated with the cavity of the stirring shaft (2052).
7. The system according to claim 5 or 6, characterized in that: any one of the acid-reducing barrels (201) is also internally provided with a second sulfuric acid concentration detection device (206) and a pH detection mechanism (210).
8. The system of claim 7, wherein: the impurity removal unit (3) comprises a first filtering device (301), a first impurity removal barrel (302), a second filtering device (303), a second impurity removal barrel (304) and a third filtering device (305); the first filtering device (301), the first impurity removing barrel (302), the second filtering device (303), the second impurity removing barrel (304) and the third filtering device (305) are sequentially communicated in series through a filtrate conveying pipeline; the feed inlet of the first filtering device (301) is communicated with the second conveying device (S2), and the liquid outlet of the third filtering device (305) is communicated with the third conveying device (S3).
9. The system of claim 8, wherein: the feed inlet of the first impurity removing barrel (302) is also communicated with a second hydrogen peroxide adding pipeline (306); the feed inlet of the second impurity removing barrel (304) is also communicated with a sodium sulfide feeding device (307).
10. The system of claim 9, wherein: the system also comprises a control system, wherein the control system is in wired and/or wireless electric signal connection with each component, and the control system controls the start and stop of each component of the system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221829198.0U CN217780770U (en) | 2022-07-15 | 2022-07-15 | System for producing nickel sulfate solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221829198.0U CN217780770U (en) | 2022-07-15 | 2022-07-15 | System for producing nickel sulfate solution |
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| CN116354554A (en) * | 2023-04-04 | 2023-06-30 | 宜兴市艾瑞泽环保科技有限公司 | Landfill leachate treatment process and hydroxyl flocculation composite bed for landfill leachate treatment |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116354554A (en) * | 2023-04-04 | 2023-06-30 | 宜兴市艾瑞泽环保科技有限公司 | Landfill leachate treatment process and hydroxyl flocculation composite bed for landfill leachate treatment |
| CN116354554B (en) * | 2023-04-04 | 2023-11-14 | 浙江埃克钛环境科技有限公司 | Landfill leachate treatment process and hydroxyl flocculation composite bed for landfill leachate treatment |
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