CN219682497U - Device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate - Google Patents
Device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate Download PDFInfo
- Publication number
- CN219682497U CN219682497U CN202320379026.6U CN202320379026U CN219682497U CN 219682497 U CN219682497 U CN 219682497U CN 202320379026 U CN202320379026 U CN 202320379026U CN 219682497 U CN219682497 U CN 219682497U
- Authority
- CN
- China
- Prior art keywords
- leaching
- tank
- leaching tank
- secondary leaching
- electric furnace
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000002386 leaching Methods 0.000 title claims abstract description 159
- 239000000428 dust Substances 0.000 title claims abstract description 28
- 229940062993 ferrous oxalate Drugs 0.000 title claims abstract description 24
- OWZIYWAUNZMLRT-UHFFFAOYSA-L iron(2+);oxalate Chemical compound [Fe+2].[O-]C(=O)C([O-])=O OWZIYWAUNZMLRT-UHFFFAOYSA-L 0.000 title claims abstract description 24
- 238000002156 mixing Methods 0.000 claims abstract description 37
- 238000003756 stirring Methods 0.000 claims abstract description 32
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 238000001914 filtration Methods 0.000 claims abstract description 30
- 239000002002 slurry Substances 0.000 claims abstract description 22
- 238000003825 pressing Methods 0.000 claims abstract description 11
- 239000002893 slag Substances 0.000 claims abstract description 7
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 7
- 239000011701 zinc Substances 0.000 claims abstract description 7
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 5
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 27
- 239000000463 material Substances 0.000 claims description 18
- 239000008367 deionised water Substances 0.000 claims description 12
- 229910021641 deionized water Inorganic materials 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 239000002253 acid Substances 0.000 claims description 9
- 235000006408 oxalic acid Nutrition 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 19
- 239000002994 raw material Substances 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000003795 chemical substances by application Substances 0.000 abstract description 3
- 230000035484 reaction time Effects 0.000 abstract description 2
- 238000004513 sizing Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 12
- 230000009471 action Effects 0.000 description 11
- 239000012528 membrane Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 239000006228 supernatant Substances 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- -1 polytetrafluoroethylene Polymers 0.000 description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 3
- 239000004810 polytetrafluoroethylene Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000009854 hydrometallurgy Methods 0.000 description 2
- XMWCXZJXESXBBY-UHFFFAOYSA-L manganese(ii) carbonate Chemical compound [Mn+2].[O-]C([O-])=O XMWCXZJXESXBBY-UHFFFAOYSA-L 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000006004 Quartz sand Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010668 complexation reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000001027 hydrothermal synthesis Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Classifications
-
- 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
Landscapes
- Manufacture And Refinement Of Metals (AREA)
Abstract
The utility model discloses a device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate, and belongs to the technical field of hydrometallurgical equipment. The device comprises a size mixing tank, a secondary leaching tank A, a secondary leaching tank B, a leaching liquid filtering system and a filter pressing system, wherein the secondary leaching tank A and the secondary leaching tank B are connected through a reducing connecting pipe, a feeding bin is arranged at the upper part of the secondary leaching tank B, the sizing agents in the secondary leaching tank A and the secondary leaching tank B enter the filter pressing system through a discharge valve A and a discharge valve B respectively to obtain zinc-rich slag and ferrous oxalate respectively, and tail liquid enters the leaching liquid filtering system through a discharge hole B of the secondary leaching tank B and is sent into the size mixing tank again after purified and decontaminated. Compared with the traditional hydrometallurgical leaching equipment, the device has the advantages that the slurry mixing tank is arranged for stirring and mixing before the formal leaching reaction, so that the reaction time of raw materials in the leaching tank can be effectively reduced; the operation is simple and safe, the leaching rate of the electric furnace dust removal ash is high, and the product yield is high.
Description
Technical Field
The utility model relates to the technical field of hydrometallurgy equipment, in particular to a device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate.
Background
The electric furnace dust is a typical bulk hazardous waste in the metallurgical industry, and contains rich Fe, zn and other resources. The annual production amount of the electric furnace dust removal ash in China is approximately 300 ten thousand tons, and the stocking amount is more approximately ten millions of tons. At present, the electric furnace dust removal ash is mainly utilized in the modes of incineration, stockpiling, landfill treatment and the like, but the defects are obvious: high energy consumption, high equipment investment cost and serious environmental pollution. Therefore, a proper method and device are selected to carry out resource and high-value utilization on the electric furnace dust, so that the problem of the solid waste disposal of the enterprises is solved, and the obtained high-added-value product can bring considerable profits to the enterprises, and has remarkable social benefit and economic benefit.
Hydrometallurgy is used as a method for efficiently and low-cost recovery of valuable elements, generally, the leaching temperature, the leaching time, the liquid-solid ratio, the stirring speed and the pulp concentration in the leaching process are controlled within a certain range, and the purpose of pertinently recovering the valuable elements in the leaching agent is finally achieved by utilizing chemical reaction between the leaching agent and the raw materials. However, the current stage leaching apparatus often suffers from the following drawbacks: (1) The equipment always takes priority of independent processes and working procedures, such as leaching, extraction, filtering and the like, and does not consider all process links, which often causes difficult connection among the working procedures and inconsistent product quality; (2) The system is closed, materials cannot be added in time in the reaction process, and insufficient leaching or excessive leaching is easily caused, so that the leaching effect and the element yield are affected; (3) The leaching solution is not subjected to effective filtration and impurity removal, the impurity content is high, and even the loss of valuable metals and the exceeding of the content of harmful elements can be caused; (4) The tail liquid cannot be fully recycled, the treatment cost of a large amount of tail liquid is high, and the hidden danger of the environment is increased.
The patent 'a device for continuously leaching rhodochrosite (CN 201921647638.9)' designs a device capable of continuously leaching rhodochrosite, which comprises a plurality of leaching tanks which are sequentially and obliquely arranged, so that the leaching rate and the element yield can be effectively improved, but the device does not consider the convenience of material addition and the purification treatment of reaction tail liquid in the reaction process; the patent "continuous leaching apparatus and its application (CN 201610908772.4)" devised a device comprising a mixing tank and a two-stage leaching tank, which can improve the leaching efficiency of powder samples, but which was not fully considered for the treatment of leached tailings and leached tailings. In view of the above, it is important to design a wet leaching device which can achieve both leaching efficiency and leaching process flow and recycle tail liquid.
Disclosure of Invention
The utility model aims to provide a device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate, which solves the problems in the prior art.
In order to achieve the above purpose, the present utility model provides the following technical solutions: the device for continuously and circularly leaching the electric furnace dust removal ash and preparing the ferrous oxalate comprises a pulp mixing tank, a secondary leaching tank A, a secondary leaching tank B, a leaching liquid filtering system and a filter pressing system, wherein a feed inlet A and a discharge outlet A are arranged on the secondary leaching tank A, the height of the feed inlet A is higher than that of the discharge outlet A, a feed inlet B and a discharge outlet B are arranged on the secondary leaching tank B, and the height of the feed inlet B is higher than that of the discharge outlet B; the secondary leaching tank A is connected with the secondary leaching tank B through a reducing connecting pipe, and a discharge hole A of the secondary leaching tank A is higher than a feed hole B of the secondary leaching tank B; the upper part of the secondary leaching tank B is provided with a feeding bin, the slurry in the secondary leaching tank A and the slurry in the secondary leaching tank B enter a filter pressing system through a discharge valve A and a discharge valve B respectively to obtain zinc-rich slag and ferrous oxalate, and the tail liquid enters a leaching liquid filtering system through a discharge port B of the secondary leaching tank B and is sent into a slurry mixing tank again for slurry mixing after being purified and decontaminated.
Preferably, the size mixing tank, the secondary leaching tank A and the secondary leaching tank B are respectively provided with a stirrer, and each stirrer consists of a stirring shaft, blades attached to the stirring shaft and a stirring motor; the stirring speed is controlled by a stirring motor, and the control range is 0-400r/min; the stirring motor drives the stirring shaft to rotate, and then drives the blades of the stirring shaft to rotate.
Preferably, the flow and circulation of the materials are realized between the secondary leaching tank A and the secondary leaching tank B and between the secondary leaching tank B and the leaching liquid filtering system through connecting pipes and the screw pumps A and B, and the flow of the screw pumps A and B for conveying the materials is 0.8-1.5m 3 And/h, the lift is 30-50m.
Preferably, the size mixing tank is provided with a deionized water supply pipe, an electric furnace dust removal feeding bin and an oxalic acid feeding bin; the deionized water supply pipe is provided with a deionized water inlet valve, and the oxalic acid feeding bin is provided with a feeding control valve.
Preferably, the size mixing tank is provided with a circulating acid inlet, the circulating acid inlet is connected with a screw pump C through a pipeline, and the screw pump C is connected with a discharge port C of the leaching liquid filtering system through a material conveying pipeline.
Preferably, the connection pipelines of the pulp mixing tank and the secondary leaching tank A are respectively provided with a discharge valve C and a feed valve A correspondingly, and heating electrodes are arranged in the secondary leaching tank A and the secondary leaching tank B.
Preferably, a filtering pipeline is arranged in the leaching liquid filtering system.
Compared with the prior art, the utility model has the following beneficial effects:
1. compared with the traditional leaching equipment, the device for continuously and circularly leaching the electric furnace dust removal ash and preparing the ferrous oxalate has the advantages that the raw materials are firstly stirred and uniformly mixed in the size mixing tank before entering the leaching tank for reaction, and the reaction time of about 50% of the raw materials in the leaching tank can be saved.
2. The device for continuously and circularly leaching the electric furnace dust and preparing the ferrous oxalate is simple and safe to operate, is uniformly stirred, and has high leaching rate of the electric furnace dust and the ash and high product yield.
3. The device for continuously and circularly leaching the electric furnace dust removal ash and preparing the ferrous oxalate can directly inject the tail liquid into a size mixing tank to serve as a reactant after purifying the tail liquid after preparing the ferrous oxalate by hydrothermal reaction, and the whole reaction process can achieve near zero emission of the tail liquid and has small environmental pressure.
4. The device for continuously and circularly leaching the electric furnace dust and preparing the ferrous oxalate is easier to realize the continuity and automation in production, can effectively shorten the leaching period and reduce the production cost.
Drawings
Fig. 1 is a schematic view of the overall structure of the present utility model.
In the figure: 1. a deionized water inlet valve; 2. a deionized water supply pipe; 3. an electric furnace dedusting ash feeding bin; 4. a stirring motor; 5. oxalic acid feeding bin; 6. a feed control valve; 7. a stirring shaft; 8. a blade; 9. a circulating acid inlet; 10. a discharging valve C; 11. a feed valve A; 12. a feed inlet A; 13. heating the electrode; 14. a discharging valve A; 15. a connecting pipe; 16. a screw pump A; 17. a discharge hole A; 18. a feed inlet B; 19. a discharging valve B; 20. a discharge port B; 21. a feeding bin; 22. a screw pump B; 24. a discharge port C; 25. a filter tube; 26. a material transport pipeline; 27. a screw pump C; 28. a size mixing tank; 29. a secondary leaching tank A; 30. a secondary leaching tank B; 31. a leachate filtration system; 32. and a filter pressing system.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Referring to fig. 1, a device for continuously and circularly leaching electric furnace dust removal ash and preparing ferrous oxalate in the embodiment comprises a pulp mixing tank 28, a secondary leaching tank a29, a secondary leaching tank B30, a leaching liquid filtering system 31 and a filter pressing system 32, wherein a feed port a12 and a discharge port a17 are arranged on the secondary leaching tank a29, the height of the feed port a12 is higher than that of the discharge port a17, a feed port B18 and a discharge port B20 are arranged on the secondary leaching tank B30, and the height of the feed port B18 is higher than that of the discharge port B20; the secondary leaching tank A29 and the secondary leaching tank B30 are connected through a reducing connecting pipe 15, and a discharge hole A17 of the secondary leaching tank A29 is higher than a feed hole B18 of the secondary leaching tank B30; the upper part of the secondary leaching tank B30 is provided with a feeding bin 21, the slurry in the secondary leaching tank A29 and the slurry in the secondary leaching tank B30 respectively enter a filter pressing system 32 through a discharge valve A14 and a discharge valve B19 to respectively obtain zinc-rich slag and ferrous oxalate, the tail liquid of the zinc-rich slag and ferrous oxalate enters a leaching solution filtering system 31 through a discharge port B20 of the secondary leaching tank B30, and the tail liquid is purified and decontaminated and then is sent into a slurry mixing tank 28 again for slurry mixing, so that the aim of continuous and cyclic leaching is finally achieved. The height difference of certain 0.5-1.5m exists among the size mixing tank 28, the secondary leaching tank A29, the secondary leaching tank B30 and the leaching liquid filtering system 31, so that reaction materials can be driven to flow spontaneously in the system, the working time of a screw pump is shortened, the service life is prolonged, and the overall reaction efficiency is improved.
In the embodiment, a size mixing tank 28, a secondary leaching tank A29 and a secondary leaching tank B30 are respectively provided with a stirrer, wherein the stirrer consists of a stirring shaft 7, a blade 8 attached to the stirring shaft 7 and a stirring motor 4; the stirring speed is controlled by a stirring motor 4, and the control range is 0-400r/min; the stirring motor 4 drives the stirring shaft 7 to rotate, so as to drive the blades 8 to rotate; finally, the solvent and the raw materials are fully mixed, and the purposes of shortening the leaching time and improving the leaching efficiency are achieved.
The flow and circulation of the materials are realized between the secondary leaching tank A29 and the secondary leaching tank B30 and between the secondary leaching tank B30 and the leaching liquid filtering system 31 through the connecting pipe 15 and the screw pump A16 and the screw pump B22, and the flow of the screw pump A16 and the screw pump B22 for conveying the materials is 0.8-1.5m 3 And/h, the lift is 30-50m, and after the reaction is finished, the materials are transferred to the next container for reaction under the pushing action of a pump.
The size mixing tank 28 in the embodiment is provided with a deionized water supply pipe 2, an electric furnace dust removal feeding bin 3 and an oxalic acid feeding bin 5; a deionized water inlet valve 1 is arranged on the deionized water supply pipe 2, and a feed control valve 6 is arranged on the oxalic acid feeding bin 5; the size mixing tank 28 is provided with a circulating acid inlet 9, the circulating acid inlet 9 is connected with a screw pump C27 through a pipeline, and the screw pump C27 is connected with a discharge port C24 of a leaching liquid filtering system 31 through a material conveying pipeline 26; the connection pipelines of the pulp mixing tank 28 and the secondary leaching tank A29 are respectively provided with a discharge valve C10 and a feed valve A11 correspondingly, and heating electrodes 13 are arranged in the secondary leaching tank A29 and the secondary leaching tank B30; the inside of the leaching solution filtering system 31 is provided with a filtering pipeline 25, the leaching solution filtering system 31 mainly adopts a separation membrane to achieve the aim of filtering impurities, and the separation membrane can adopt a microfiltration membrane, an ultrafiltration membrane or a nanofiltration membrane, and the specific selection is selected according to the granularity of the powder.
The groove body of the device is internally provided with polytetrafluoroethylene acid-proof layers with the lining thickness of 4-8 mm; the connecting pipes among the devices are polytetrafluoroethylene pipelines; the screw pump for conveying materials is made of polytetrafluoroethylene, and can achieve the purposes of effectively preventing acid and high temperature.
Adopting the device provided by the utility model, uniformly mixing the electric furnace dust, deionized water and oxalic acid in a slurry mixing tank 28 positioned at the forefront according to a certain adding proportion, after all reaction samples are injected into the slurry mixing tank 28, turning on a stirring motor 4, and under the action of the stirring motor 4, driving a stirring shaft 7 to drive a blade 8 attached to the upper part to rotate so as to achieve the purpose of uniformly mixing slurry; after being uniformly mixed for a period of time, a discharge valve C10 and a feed valve A11 between the pulp mixing tank 28 and the secondary leaching tank A29 are opened, and materials flow into the secondary leaching tank A29 from the pulp mixing tank 28 at the front end through a connecting pipe 15 under the action of self gravity; after all materials flow into the secondary leaching tank A29, a feeding valve A11 is closed, a stirring motor 4 and a heating electrode 13 of the secondary leaching tank A29 are opened, and the hydrothermal complexation leaching reaction is completed under the drive of a blade 8 attached to the stirring motor 4; after the reaction is finished, a screw pump A16 is opened, under the pushing action of the screw pump A16, supernatant in a secondary leaching tank A29 enters a secondary leaching tank B30, lower slurry enters a filter pressing system 32 through a discharge valve A14 of the secondary leaching tank A29, and under the dehydration action of a filter press, a product I-zinc-rich slag is finally obtained; after the supernatant in the secondary leaching tank A29 enters the secondary leaching tank B30 through the connecting pipe 15, adding a proper amount of iron powder and oxalic acid into the secondary leaching tank B through the feeding bin 21 according to the content of Fe ions in the supernatant, then opening the stirring motor 4 and the heating electrode 13 to finish the hydrothermal reduction precipitation reaction, and after the reaction is finished, enabling the lower slurry to enter the filter pressing system 32 through the discharging valve B19 of the secondary leaching tank B30, and finally obtaining a product II-zinc-rich slag under the dehydration action of a filter press; the supernatant of the secondary leaching tank B30 is pumped to a leaching solution filtering system 31 through a discharge port B20 under the pushing action of a screw pump B22, and is pumped to a reaction tail liquid through a feed port of the leaching solution filtering system 31, and sequentially passes through structures such as activated carbon, quartz sand, a filter membrane and the like in a filtering pipeline 25 in the equipment, so that the aim of removing impurities is fulfilled; the purified reaction tail liquid flows into the circulating acid inlet 9 of the size mixing tank 28 again through the material conveying pipeline 26 connected to the discharge port C24 of the leaching liquid filtering system 31 under the pushing action of the screw pump C27, and is reused as the raw material of leaching reaction, so that the purposes of circulating leaching and no tail liquid discharge are achieved.
It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.
Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. The utility model provides a device of continuous cycle leaching electric stove dust removal ash and preparation ferrous oxalate, includes size mixing jar (28), second grade leaching tank A (29), second grade leaching tank B (30), leachate filtration system (31) and filter-pressing system (32), its characterized in that: the secondary leaching tank A (29) is provided with a feed inlet A (12) and a discharge outlet A (17), the feed inlet A (12) is higher than the discharge outlet A (17), the secondary leaching tank B (30) is provided with a feed inlet B (18) and a discharge outlet B (20), and the feed inlet B (18) is higher than the discharge outlet B (20); the secondary leaching tank A (29) and the secondary leaching tank B (30) are connected through a reducing connecting pipe (15), and a discharge hole A (17) of the secondary leaching tank A (29) is higher than a feed hole B (18) of the secondary leaching tank B (30); the upper part of the secondary leaching tank B (30) is provided with a feeding bin (21), the slurry in the secondary leaching tank A (29) and the slurry in the secondary leaching tank B (30) enter a filter pressing system (32) through a discharging valve A (14) and a discharging valve B (19) respectively to obtain zinc-rich slag and ferrous oxalate, and the tail liquid enters a leaching liquid filtering system (31) through a discharging hole B (20) of the secondary leaching tank B (30) and is sent into a slurry mixing tank (28) again for slurry mixing after purification and impurity removal.
2. The apparatus for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate according to claim 1, wherein: the slurry mixing tank (28), the secondary leaching tank A (29) and the secondary leaching tank B (30) are respectively provided with a stirrer, and each stirrer consists of a stirring shaft (7), blades (8) attached to the stirring shaft (7) and a stirring motor (4); the stirring speed is controlled by a stirring motor (4) with the control range of 0-400r/min; the stirring motor (4) drives the stirring shaft (7) to rotate, and then drives the blades (8) thereof to rotate.
3. The apparatus for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate according to claim 1, wherein: the flow and circulation of the materials are realized between the secondary leaching tank A (29) and the secondary leaching tank B (30) and between the secondary leaching tank B (30) and the leaching liquid filtering system (31) through the connecting pipe (15) and the screw pump A (16) and the screw pump B (22), and the flow of the screw pump A (16) and the screw pump B (22) for conveying the materials is 0.8-1.5m 3 And/h, the lift is 30-50m.
4. The apparatus for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate according to claim 1, wherein: the slurry mixing tank (28) is provided with a deionized water supply pipe (2), an electric furnace dust removal feeding bin (3) and an oxalic acid feeding bin (5); the deionized water supply pipe (2) is provided with a deionized water inlet valve (1), and the oxalic acid feeding bin (5) is provided with a feeding control valve (6).
5. The apparatus for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate according to claim 4, wherein: the slurry mixing tank (28) is provided with a circulating acid inlet (9), the circulating acid inlet (9) is connected with a screw pump C (27) through a pipeline, and the screw pump C (27) is connected with a discharge port C (24) of a leaching liquid filtering system (31) through a material conveying pipeline (26).
6. A device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate according to claim 3, wherein: the slurry mixing tank (28) and the secondary leaching tank A (29) are respectively and correspondingly provided with a discharge valve C (10) and a feed valve A (11), and heating electrodes (13) are respectively arranged in the secondary leaching tank A (29) and the secondary leaching tank B (30).
7. The apparatus for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate according to claim 1, wherein: the inside of the leaching liquid filtering system (31) is provided with a filtering pipeline (25).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320379026.6U CN219682497U (en) | 2023-03-03 | 2023-03-03 | Device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320379026.6U CN219682497U (en) | 2023-03-03 | 2023-03-03 | Device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219682497U true CN219682497U (en) | 2023-09-15 |
Family
ID=87969576
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320379026.6U Active CN219682497U (en) | 2023-03-03 | 2023-03-03 | Device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219682497U (en) |
-
2023
- 2023-03-03 CN CN202320379026.6U patent/CN219682497U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102011010A (en) | Method for totally extracting vanadium, gallium and scandium by using titanium dioxide hydrolysis waste acid to leach steel slag containing vanadium | |
| CN109112291B (en) | Wet grinding-closed curing vanadium extraction system and method | |
| CN201793760U (en) | Fluid preparation device for producing electrolytic manganese metal by adopting two-ores method | |
| CN102534656A (en) | Process for recycling copper through electrodeposition by treating scrap copper materials by adopting cyclone electrolysis technology | |
| CN103834805A (en) | Method of leaching divalent cobalt from cobalt copper bidery metal | |
| CN108396150A (en) | A kind of secondary recovery product line device of aluminium lime-ash | |
| CN103922552B (en) | A kind of single conditioner multiple pressure filter sludge dewatering system and method for continuing | |
| CN107185386A (en) | A kind of low nickel matte ore pulp absorbs the method for administering nitrous oxides exhaust gas | |
| CN106756003A (en) | The production method that a kind of use potential control is continuously leached | |
| CN219682497U (en) | Device for continuously and circularly leaching electric furnace dust and preparing ferrous oxalate | |
| CN105668641B (en) | A kind of method that sulfuric acid roasting direct pyrolusite prepares manganese sulfate solution | |
| CN219044981U (en) | Device for preparing calcium sulfate whisker by using sintered flue gas desulfurization ash | |
| CN113881843B (en) | Production system and production method for reducing magnesium content in nickel concentrate | |
| CN102181647B (en) | Method for extracting chromated nickel from low-grade stainless steel sludge by using stainless steel acid-washing waste mother liquor | |
| CN210546982U (en) | Causticized slag recovery processing device | |
| CN110482821B (en) | Circulating water type dealkalization system and dealkalization method for red mud by sulfur-containing tailings | |
| CN103834818B (en) | Oxygen adding system and method for reactor iron removing | |
| CN106350668A (en) | Preparation method of V2O5 by vapour carbonizing pretreatment of vanadium-containing stone coal | |
| CN202808644U (en) | Device for continuously recovering acetylene from carbide slag slurry | |
| CN105540705B (en) | A kind of high concentration NPE waste water thermocatalytic prepares the method and its device of solid adsorbent | |
| CN206607301U (en) | Navajoite clinker, which is crushed, leaches filter | |
| CN218872173U (en) | Production system for preparing hydrogen sulfide removing agent from alumina red mud | |
| CN203728905U (en) | Oxygen adding system for iron removal of reactor | |
| CN104562082A (en) | Method for preparing copper-containing solution by dissolving waste copper | |
| CN220335267U (en) | Pilot-scale platform for producing ferrous oxalate and zinc-rich slag by utilizing electric furnace dust |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |