CN115058601A - Method for recovering metal aluminum from aluminum ash - Google Patents
Method for recovering metal aluminum from aluminum ash Download PDFInfo
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- CN115058601A CN115058601A CN202210804442.6A CN202210804442A CN115058601A CN 115058601 A CN115058601 A CN 115058601A CN 202210804442 A CN202210804442 A CN 202210804442A CN 115058601 A CN115058601 A CN 115058601A
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- aluminum
- slag
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- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 450
- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 421
- 238000000034 method Methods 0.000 title claims abstract description 94
- 229910052751 metal Inorganic materials 0.000 title abstract description 24
- 239000002184 metal Substances 0.000 title abstract description 24
- 239000002893 slag Substances 0.000 claims abstract description 137
- 150000003839 salts Chemical class 0.000 claims abstract description 102
- 239000007788 liquid Substances 0.000 claims abstract description 71
- 238000003723 Smelting Methods 0.000 claims abstract description 44
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 42
- 238000000605 extraction Methods 0.000 claims abstract description 31
- 238000003825 pressing Methods 0.000 claims abstract description 30
- 238000002156 mixing Methods 0.000 claims abstract description 21
- 239000012752 auxiliary agent Substances 0.000 claims abstract description 16
- 239000000203 mixture Substances 0.000 claims abstract description 12
- 239000011261 inert gas Substances 0.000 claims abstract description 9
- 238000010926 purge Methods 0.000 claims abstract description 6
- 235000002639 sodium chloride Nutrition 0.000 claims description 102
- 239000000463 material Substances 0.000 claims description 76
- 239000002245 particle Substances 0.000 claims description 58
- 230000008569 process Effects 0.000 claims description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 40
- 238000001816 cooling Methods 0.000 claims description 37
- 238000012216 screening Methods 0.000 claims description 23
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 18
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 claims description 14
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 12
- 239000001103 potassium chloride Substances 0.000 claims description 9
- 235000011164 potassium chloride Nutrition 0.000 claims description 9
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 7
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 7
- 150000003841 chloride salts Chemical class 0.000 claims description 7
- 239000011863 silicon-based powder Substances 0.000 claims description 7
- 239000011592 zinc chloride Substances 0.000 claims description 7
- 235000005074 zinc chloride Nutrition 0.000 claims description 7
- 239000011780 sodium chloride Substances 0.000 claims description 6
- 239000006004 Quartz sand Substances 0.000 claims description 5
- 239000002006 petroleum coke Substances 0.000 claims description 5
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 4
- 229910000720 Silicomanganese Inorganic materials 0.000 claims description 4
- 239000001110 calcium chloride Substances 0.000 claims description 4
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 4
- 235000011148 calcium chloride Nutrition 0.000 claims description 4
- 238000000227 grinding Methods 0.000 claims description 4
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 4
- 235000011147 magnesium chloride Nutrition 0.000 claims description 4
- 239000012778 molding material Substances 0.000 claims description 4
- 229910021487 silica fume Inorganic materials 0.000 claims description 4
- 238000011084 recovery Methods 0.000 abstract description 51
- 230000003647 oxidation Effects 0.000 abstract description 10
- 238000007254 oxidation reaction Methods 0.000 abstract description 10
- 239000002910 solid waste Substances 0.000 abstract description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 34
- 238000010494 dissociation reaction Methods 0.000 description 31
- 238000007664 blowing Methods 0.000 description 22
- 230000005593 dissociations Effects 0.000 description 22
- 230000000052 comparative effect Effects 0.000 description 21
- 238000005266 casting Methods 0.000 description 19
- 229910052786 argon Inorganic materials 0.000 description 17
- 238000010438 heat treatment Methods 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 238000000498 ball milling Methods 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 229910052760 oxygen Inorganic materials 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 239000002699 waste material Substances 0.000 description 7
- 239000001307 helium Substances 0.000 description 6
- 229910052734 helium Inorganic materials 0.000 description 6
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000004411 aluminium Substances 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005868 electrolysis reaction Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 238000005054 agglomeration Methods 0.000 description 3
- 230000002776 aggregation Effects 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000001354 calcination Methods 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- IRPGOXJVTQTAAN-UHFFFAOYSA-N 2,2,3,3,3-pentafluoropropanal Chemical compound FC(F)(F)C(F)(F)C=O IRPGOXJVTQTAAN-UHFFFAOYSA-N 0.000 description 2
- KLZUFWVZNOTSEM-UHFFFAOYSA-K Aluminum fluoride Inorganic materials F[Al](F)F KLZUFWVZNOTSEM-UHFFFAOYSA-K 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PMHQVHHXPFUNSP-UHFFFAOYSA-M copper(1+);methylsulfanylmethane;bromide Chemical compound Br[Cu].CSC PMHQVHHXPFUNSP-UHFFFAOYSA-M 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 238000000465 moulding Methods 0.000 description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 230000001698 pyrogenic effect Effects 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000007873 sieving Methods 0.000 description 2
- 229910052814 silicon oxide Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 238000000748 compression moulding Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- PYLLWONICXJARP-UHFFFAOYSA-N manganese silicon Chemical compound [Si].[Mn] PYLLWONICXJARP-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/04—Working-up slag
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B21/00—Obtaining aluminium
- C22B21/06—Obtaining aluminium refining
- C22B21/062—Obtaining aluminium refining using salt or fluxing agents
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B21/00—Obtaining aluminium
- C22B21/06—Obtaining aluminium refining
- C22B21/064—Obtaining aluminium refining using inert or reactive gases
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/001—Dry processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/001—Dry processes
- C22B7/002—Dry processes by treating with halogens, sulfur or compounds thereof; by carburising, by treating with hydrogen (hydriding)
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention provides a method for recovering metal aluminum from aluminum ash, belonging to the technical field of comprehensive utilization of solid wastes in aluminum industry, comprising the following steps: mixing the thermal state aluminum ash slag with a pressing auxiliary agent to obtain a first mixture; squeezing the first mixture to extract aluminum, and then obtaining a first cold-state aluminum slag block and a first aluminum liquid in an inert gas purging atmosphere; covering a salt separating agent on the surface of the first cold-state aluminum slag block to carry out first smelting aluminum extraction to obtain first hot-state salt slag and second aluminum liquid; wherein, the technological parameters of the first smelting aluminum extraction comprise: the temperature is 650-800 ℃. The method comprises squeezing aluminum extraction and smelting aluminum extraction, reduces the burning loss rate of aluminum by avoiding the oxidation of aluminum, and obtains multi-section recovered aluminum liquid, thereby greatly improving the recovery rate of metal aluminum recovered from aluminum ash.
Description
Technical Field
The application relates to the technical field of comprehensive utilization of solid wastes in the aluminum industry, in particular to a method for recovering metal aluminum from aluminum ash.
Background
The aluminum ash mainly comes from waste residues generated in the maintenance and production of an electrolytic cell in the aluminum electrolysis process, salt residues and scum generated in the aluminum electrolysis process, scum generated on the surface of a melt in the smelting and refining processes of secondary aluminum, and salt residues and aluminum ash generated in the aluminum recovery process. About 10-15 kg of aluminous ash can be generated per ton of electrolytic aluminum, and 100-200 kg of aluminous ash can be generated per ton of aluminum in the whole process of processing application. The main components of the aluminum ash slag comprise metallic aluminum, aluminum oxide, aluminum nitride, aluminum chloride, aluminum fluoride, silicon oxide and the like, wherein the content of metallic aluminum in the aluminum ash slag produced in the processes of electrolytic aluminum production, secondary aluminum production and aluminum ingot casting is about 20-60%, so a large amount of effective aluminum resources exist in the aluminum ash slag.
At present, the process for recovering more metal aluminum is mainly pyrometallurgical recovery. The fire method is mainly used for recovering the metal aluminum after one-time fire method direct smelting by a rotary furnace and an ash frying machine. The simple pyrogenic process can cause severe oxidation of aluminum, so that a large amount of metal aluminum is burnt, the efficiency of recovering the metal aluminum is less than 70%, and a large amount of effective aluminum resources are wasted.
Disclosure of Invention
The embodiment of the application provides a method for recovering metal aluminum from aluminum ash slag, which aims to solve the technical problem of low aluminum recovery rate in the conventional method for recovering metal aluminum from aluminum ash slag.
In a first aspect, embodiments of the present application provide a method for recovering metallic aluminum from aluminum dross, the method including:
mixing the thermal state aluminum ash slag with a pressing auxiliary agent to obtain a first mixture;
squeezing the first mixture to extract aluminum, and then obtaining a first cold-state aluminum slag block and a first aluminum liquid in an inert gas purging atmosphere;
covering a salt separating agent on the surface of the first cold-state aluminum slag block to carry out first smelting aluminum extraction to obtain first hot-state salt slag and second aluminum liquid;
wherein, the technological parameters of the first smelting aluminum extraction comprise: the temperature is 650-800 ℃.
Further, the pressing auxiliary agent comprises at least one of metal silicon powder, silica fume, potassium chloride, quartz sand, petroleum coke and silicon manganese.
Further, the mass ratio of the thermal aluminum ash to the pressing auxiliary agent is (95-99.5): (0.5-5).
Further, the salt separating agent comprises a chloride salt.
Further, the chloride salt includes at least one of potassium chloride, sodium chloride, magnesium chloride, zinc chloride, and calcium chloride.
Furthermore, the mass ratio of the salt separating agent to the cold aluminum slag block is (1-15): 85-99.
Further, the method further comprises:
carrying out water cooling on the first hot salt slag, and dissociating the salt slag to obtain cold ash slag;
performing first screening on the cold-state ash slag to obtain a first oversize material and a first undersize material;
grinding the first screen material, and then carrying out second screening to obtain a second screen material;
mixing the first oversize material, the second oversize material and a salt separating agent, and then pressing and forming to obtain a second cold-state aluminum slag forming material;
carrying out second smelting aluminum extraction on the second cold-state aluminum slag molding material to obtain second hot-state salt slag and third aluminum liquid;
wherein the technological parameters of the second smelting aluminum extraction comprise: the temperature is 650-800 ℃.
Further, the particle size of the first oversize material is larger than 1 mm; the grain size of the second oversize material is 1mm-0.1 mm.
Further, the water cooling time is 3-8 min, and the temperature of the first thermal state salt slag after water cooling is 100-150 ℃.
Furthermore, the mass part ratio of the first oversize material to the second oversize material to the salt separating agent is (20-40) to (30-60) to (5-30).
Compared with the prior art, the technical scheme provided by the embodiment of the application has the following advantages:
the embodiment of the application provides a method for recovering metallic aluminum from aluminum ash, which comprises the steps of squeezing and extracting aluminum and smelting and extracting aluminum, wherein two sections of aluminum extracting modes are combined to extract aluminum for many times, the aluminum burnout rate is reduced by avoiding the aluminum from being oxidized, and multi-section recovered aluminum liquid is obtained, so that the recovery rate of recovering the metallic aluminum from the aluminum ash is greatly improved. Specifically, the method comprises the following steps: on one hand, in the process of squeezing and extracting aluminum, the squeezing auxiliary agent improves the squeezing efficiency and prevents the subsequent calcination loss; the first aluminum liquid is purged by inert gas, so that the surface of the aluminum liquid is protected from generating an alumina film easily, the mobility of the aluminum liquid is reduced, the gas content in the aluminum liquid can be reduced, and the defects caused by subsequent aluminum castings are prevented. On the other hand, the temperature for extracting aluminum by smelting is between 650 and 800 ℃, so that aluminum is molten to the maximum extent and is prevented from oxidation, the aluminum burning loss rate is reduced, and the recovery rate of the second aluminum liquid is improved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the invention and together with the description, serve to explain the principles of the invention.
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present invention, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art to obtain other drawings without inventive labor.
FIG. 1 is a schematic flow chart of a method for recovering metallic aluminum from aluminum dross according to an embodiment of the present disclosure;
fig. 2 is a flow chart of a process for recovering metallic aluminum from aluminum dross according to an embodiment of the present disclosure.
Detailed Description
The present invention will be described in detail below with reference to specific embodiments and examples, and the advantages and various effects of the present invention will be more clearly apparent therefrom. It will be understood by those skilled in the art that these specific embodiments and examples are for the purpose of illustrating the invention and are not to be construed as limiting the invention.
Throughout the specification, unless otherwise specifically noted, terms used herein should be understood as having meanings as commonly used in the art. Accordingly, unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. If there is a conflict, the present specification will control.
Unless otherwise specifically indicated, various raw materials, reagents, instruments, equipment and the like used in the present invention may be commercially available or may be prepared by existing methods.
The aluminum ash mainly comes from waste residues generated in the maintenance and production of an electrolytic cell in the aluminum electrolysis process, salt residues and scum generated in the aluminum electrolysis process, scum generated on the surface of a melt in the smelting and refining processes of secondary aluminum, and salt residues and aluminum ash generated in the aluminum recovery process. About 10-15 kg of aluminum ash can be generated per ton of electrolytic aluminum, and 100-200 kg of aluminum ash can be generated per ton of aluminum in the whole process of the aluminum processing application. The main components of the aluminum ash slag comprise metallic aluminum, aluminum oxide, aluminum nitride, aluminum chloride, aluminum fluoride, silicon oxide and the like, wherein the content of metallic aluminum in the aluminum ash slag produced in the processes of electrolytic aluminum production, secondary aluminum production and aluminum ingot casting is about 20-60%, so a large amount of effective aluminum resources exist in the aluminum ash slag.
At present, the process for recovering more metal aluminum is mainly pyrometallurgical recovery. The fire method is mainly used for recovering the metallic aluminum after one-time fire method direct smelting by a rotary furnace and an ash frying machine. The simple pyrogenic process can cause severe oxidation of aluminum, so that a large amount of metal aluminum is burnt, the efficiency of recovering the metal aluminum is less than 70%, and a large amount of effective aluminum resources are wasted.
In order to solve the technical problems, the embodiment of the invention provides the following general ideas:
in a first aspect, embodiments of the present application provide a method for recovering metallic aluminum from aluminum ash, as shown in fig. 1, the method includes:
mixing the thermal state aluminum ash slag with a pressing auxiliary agent to obtain a first mixture;
squeezing the first mixture to extract aluminum, and then obtaining a first cold-state aluminum slag block and a first aluminum liquid in an inert gas purging atmosphere;
covering a salt separating agent on the surface of the first cold-state aluminum slag block to carry out first smelting aluminum extraction to obtain first hot-state salt slag and second aluminum liquid;
wherein, the technological parameters of the first smelting aluminum extraction comprise: the temperature is 650-800 ℃.
The embodiment of the application provides a method for recovering metallic aluminum from aluminum ash, which comprises the steps of squeezing and extracting aluminum and smelting and extracting aluminum, wherein two sections of aluminum extracting modes are combined to extract aluminum for many times, the aluminum burnout rate is reduced by avoiding the aluminum from being oxidized, and multi-section recovered aluminum liquid is obtained, so that the recovery rate of recovering the metallic aluminum from the aluminum ash is greatly improved. Specifically, the method comprises the following steps: on one hand, in the process of squeezing and extracting aluminum, the squeezing auxiliary agent improves the squeezing efficiency and prevents the subsequent calcination loss; the first aluminum liquid is blown by inert gas, so that the surface of the aluminum liquid is protected from generating an alumina film easily, the mobility of the aluminum liquid is reduced, the gas content in the aluminum liquid can be reduced, and the defects of subsequent aluminum castings are prevented. On the other hand, the temperature for extracting aluminum by smelting is between 650 and 800 ℃, so that aluminum is molten to the maximum extent and is prevented from oxidation, the aluminum burning loss rate is reduced, and the recovery rate of the second aluminum liquid is improved.
In the present application, in some embodiments, the aluminum extraction by pressing specifically refers to the aluminum extraction by pressing hot aluminum ash slag by using a hot aluminum slag press which is commercially available or conventional in the art.
In this application, in some embodiments, the first smelting aluminum extraction process is: throwing the first cold-state aluminum slag block into heat recovery equipment, adding a salt separating agent for covering, performing heat treatment to obtain aluminum liquid and hot-state salt slag, and allowing the aluminum liquid to flow out by a vertical blowing protection method; the technological parameters of the heat treatment comprise: the temperature is 650-800 ℃, and the time is 50-300 min.
In the application, the hot aluminum ash is just taken out of an aluminum smelting furnace, and the temperature is generally over 600 ℃.
In the application, the first thermal state salt slag is the salt-containing hot aluminum ash subjected to the first smelting aluminum extraction treatment by the method, and the temperature is over 600 ℃.
In the present application, the first cold state aluminum slag block refers to aluminum ash slag with the temperature reduced below 100 ℃.
As an implementation manner of the embodiment of the present application, the pressing auxiliary agent includes at least one of metal silicon powder, silica fume, potassium chloride, quartz sand, petroleum coke, and silicomanganese.
In the application, the hot aluminum ash slag is mixed with the pressing auxiliary agents such as metal silicon powder, silica fume, potassium chloride, quartz sand, petroleum coke and silicomanganese, so that the pressing efficiency can be improved, the subsequent calcination loss is prevented, and the aluminum recovery rate is improved.
As an implementation manner of the embodiment of the application, the mass ratio of the hot aluminum ash slag to the pressing auxiliary agent is (95-99.5): (0.5-5).
In the application, the mass ratio of the thermal state aluminum ash residues to the pressing auxiliary agent is controlled to be (95-99.5): (0.5-5), the pressing auxiliary agent is added, the fluidity of the aluminum liquid is improved, the pressing efficiency is improved, the efficiency is not obviously improved due to less addition, and excessive aluminum liquid impurities can be caused due to excessive addition.
As an implementation of the embodiments herein, the salt separating agent comprises a chloride salt.
As an embodiment of the embodiments of the present application, the chloride salt includes at least one of potassium chloride, sodium chloride, magnesium chloride, zinc chloride, and calcium chloride; preferably a combination of sodium chloride and zinc chloride.
In the present application, the main effect of using chloride salts such as potassium chloride, sodium chloride, magnesium chloride, zinc chloride and calcium chloride as salt separating agents is to improve the recovery efficiency of the metallic aluminum. Specifically, sodium chloride can lower the melting point of aluminum ash; the zinc chloride can accelerate the movement of aluminum solution particles and increase the effects of interfacial tension of an aluminum ash liquid aluminum phase and a molten salt slag phase and the like, and because aluminum and salt are not wetted with each other and the density of an aluminum melt is high, the aluminum melt has high fluidity, the aluminum melt is converged at the bottom of a pot, salt floats on the upper part to form separation, and the aluminum melt covers the surface of aluminum, and the zinc chloride also has the effect of preventing oxidation.
As an implementation mode of the embodiment of the application, the mass ratio of the salt separating agent to the cold aluminum slag block is (1-15): 85-99.
In the application, the salt separating agent and the cold aluminum slag block are controlled to be in a mass ratio of (1-15) to (85-99), so that the salt is less, the burning loss is serious, the salt is more, the salt content in the aluminum slag is higher, and the aluminum loss caused by separation is more.
As an implementation manner of the embodiment of the present application, the method further includes:
carrying out water cooling on the first hot salt slag, and dissociating the salt slag to obtain cold ash slag;
performing first screening on the cold-state ash slag to obtain a first oversize material and a first undersize material;
grinding the first sieved material, and then carrying out second sieving to obtain a second sieved material;
mixing the first oversize material, the second oversize material and a salt separating agent, and then pressing and forming to obtain a second cold-state aluminum slag forming material;
carrying out second smelting aluminum extraction on the second cold-state aluminum slag molding material to obtain second hot-state salt slag and third aluminum liquid;
wherein the technological parameters of the second smelting aluminum extraction comprise: the temperature is 650-800 ℃.
In this application, cold state ash refers to aluminous ash with temperature reduced below 100 ℃.
In the application, the first oversize material is specifically coarse aluminum particles obtained after cold-state ash slag is subjected to first screening; and the second oversize material is specifically fine aluminum particles obtained by grinding the first undersize material and then carrying out second screening.
In the application, the first oversize material (coarse aluminum particles), the second oversize material (fine aluminum particles) and a salt separating agent are mixed, then are pressed and formed to obtain a second cold-state aluminum slag forming material, and then are subjected to third-stage aluminum extraction to obtain third aluminum liquid; the method has the advantages that the pressing forming is carried out according to reasonable grain size distribution, the particle agglomeration forming is facilitated, the pores among the particles are reduced, the specific surface area is reduced, the burning loss of aluminum can be reduced in the subsequent smelting link to the maximum extent, the recovery efficiency of the metal aluminum is improved, the high-efficiency resource utilization is realized, the coarse aluminum particles, the fine aluminum particles and the salt separating agent are mixed in different proportions and are smelted after forming, the smoldering state can be formed, oxygen is isolated to the maximum extent, the oxidation is prevented, the burning loss rate of the aluminum is reduced, and the recovery rate of the aluminum is further improved.
In this application, in some embodiments, for aluminum ash in different processing batches, the second cold-state aluminum slag molding material obtained by processing in the first batch can be added to the first aluminum extraction smelting stage in the next batch, and the first aluminum extraction smelting is performed together with the first cold-state aluminum slag block, so that energy consumption is reduced.
As an implementation of the examples herein, the first oversize material has a particle size > 1 mm; the grain size of the second oversize material is 1mm-0.1 mm.
In the application, the pressing forming is carried out according to reasonable grain size distribution, so that the particle agglomeration forming is facilitated, the pores among particles are reduced, the specific surface area is reduced, the burning loss of aluminum in the subsequent smelting link can be reduced to the greatest extent, the recovery efficiency of metal aluminum is improved, and efficient resource utilization is realized.
As an implementation manner of the embodiment of the application, the cooling time of the water cooling is 3-8 min, and the temperature of the first thermal salt slag after the water cooling is 100-150 ℃.
In some embodiments, the cooling time of the water cooling is 3-8 min, the temperature of the first hot salt slag after the water cooling is 100-150 ℃, and the dissociation time of the salt slag after the water cooling is 10-30 min. The specific process of obtaining cold-state ash slag can be carried out by adopting a water-cooling-dissociation two-stage system, wherein the main equipment of the water-cooling-dissociation two-stage system is a roller cooler, and the cooler comprises a barrel, a front roller ring, a gear, a baffle roller, a drag roller, a pinion, a discharging part, a reducer, a motor, an iron chain, cooling water and the like; the working principle process is that materials enter a cylinder of the cooler, the heat supply of a heat carrier is directly and indirectly obtained in the process that the front half section moves forwards along with the rotation of the cylinder, the hot materials are cooled, an iron chain is driven to knock along with the rotation to be dissociated, the rear half section is cooled by a water tank, and then the material conveying end outputs the materials.
As an implementation manner of the embodiment of the application, the mass part ratio of the first oversize material, the second oversize material and the salt separating agent is (20-40): 30-60): 5-30.
In the application, the coarse and fine aluminum particles and the salt separating agent are mixed and molded in different proportions and then smelted, so that a smoldering state can be formed, oxygen is isolated to the maximum extent, oxidation is prevented, the burning loss rate of aluminum is reduced, and the burning loss rate of aluminum (the burning loss rate of aluminum is calculated in a way that the content of metallic aluminum in hot aluminum ash is subtracted from the content of metallic aluminum in salt slag and coarse and fine aluminum sheets and then is divided by the content of metallic aluminum in hot aluminum ash) can reach 0.31% at the lowest extent, so that the recovery rate of aluminum is further improved.
The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The experimental methods of the following examples, which are not specified under specific conditions, are generally determined according to national standards. If there is no corresponding national standard, it is carried out according to the usual international standards, to the conventional conditions or to the conditions recommended by the manufacturer.
Example 1
The embodiment provides a method for low-loss recovery of metal aluminum from aluminum ash, the process flow is shown in fig. 2, and the specific operations are as follows:
firstly, mixing hot aluminum ash and petroleum coke, then squeezing and extracting aluminum through a squeezer, horizontally blowing the residual aluminum slag blocks at low temperature through nitrogen to obtain cold aluminum slag blocks, and vertically blowing aluminum liquid through nitrogen to protect the aluminum liquid to flow out through a splitter box and enter a casting mold to realize pouring of aluminum ingots; then throwing the cold-state aluminum slag blocks and the ball forming materials into heat recovery equipment, adding a salt separating agent for covering, carrying out heat treatment at 650 ℃ for 50min to obtain aluminum liquid and hot-state salt slag, and vertically blowing and protecting the aluminum liquid by adopting nitrogen, flowing out of a splitter box and entering a casting mold to realize the pouring of aluminum ingots; then, the hot salt slag passes through a water cooling-dissociation two-stage system, the water cooling time is 3min, the temperature of the salt slag after water cooling reaches 100-150 ℃, the dissociation time is 10min, and cold ash slag is obtained after dissociation; screening the cold-state ash slag, wherein the oversize material is coarse aluminum particles, and the undersize material is subjected to ball milling and screening to obtain fine aluminum particles and fine ash; and finally, mixing 40% of coarse aluminum particles, 55% of fine aluminum particles and 5% of salt separating agent, pressing into balls, and returning to a smelting aluminum extraction unit for smelting and extracting aluminum.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Example 2
Mixing hot aluminum ash with metal silicon powder, then squeezing and extracting aluminum through a squeezer, horizontally blowing the rest aluminum slag blocks at low temperature through helium to obtain cold aluminum slag blocks, and vertically blowing and protecting aluminum liquid through helium to flow out through a splitter box and enter a casting mold to realize pouring of aluminum ingots; then throwing the cold-state aluminum slag blocks and the ball forming materials into heat recovery equipment, adding a salt separating agent for covering, performing heat treatment at 800 ℃ for 300min to obtain aluminum liquid and hot-state salt slag, and vertically blowing the aluminum liquid by helium gas to protect the aluminum liquid to flow out of a splitter box and enter a casting mold to realize the pouring of aluminum ingots; then, the hot salt slag passes through a water cooling-dissociation two-stage system, the water cooling time is 8min, the temperature of the salt slag after water cooling reaches 100-150 ℃, the dissociation time is 30min, and cold ash slag is obtained after dissociation; screening the cold-state ash slag to obtain oversize materials and undersize materials, wherein the oversize materials are coarse aluminum particles for standby, and performing ball milling and screening on the undersize materials to obtain fine aluminum particles and fine ash; and finally, mixing 40% of coarse aluminum particles, 30% of fine aluminum particles and 30% of salt separating agent, pressing into balls, and returning to a smelting aluminum extraction unit for smelting and extracting aluminum.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Example 3
Mixing hot aluminum ash with metal silicon powder, then squeezing and extracting aluminum through a squeezer, horizontally blowing the rest aluminum slag blocks at low temperature through argon to obtain cold aluminum slag blocks, and vertically blowing and protecting aluminum liquid through argon to flow out through a splitter box and enter a casting mold to realize pouring of aluminum ingots; then throwing the cold-state aluminum slag blocks and the ball forming materials into heat recovery equipment, adding a salt separating agent for covering, performing heat treatment at 700 ℃ for 200min to obtain aluminum liquid and hot-state salt slag, and vertically blowing the aluminum liquid by argon to protect the aluminum liquid to flow out of a splitter box and enter a casting mold to realize the pouring of aluminum ingots; then, the hot salt slag passes through a water cooling-dissociation two-stage system, the water cooling time is 8min, the temperature of the salt slag after water cooling reaches 100-150 ℃, the dissociation time is 30min, and cold ash slag is obtained after dissociation; screening the cold-state ash slag to obtain oversize materials and undersize materials, wherein the oversize materials are coarse aluminum particles for standby, and performing ball milling and screening on the undersize materials to obtain fine aluminum particles and fine ash; and finally, mixing 40% of coarse aluminum particles, 30% of fine aluminum particles and 30% of salt separating agent, pressing into balls, and returning to the smelting aluminum extraction unit.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Example 4
Mixing hot aluminum ash slag and potassium chloride powder, then squeezing and extracting aluminum through a squeezer, horizontally blowing the rest aluminum slag blocks at low temperature through argon to obtain cold aluminum slag blocks, and vertically blowing aluminum liquid through argon to protect the aluminum liquid to flow out of a splitter box and enter a casting mold to realize pouring of aluminum ingots; then throwing the cold-state aluminum slag blocks and the ball forming materials into heat recovery equipment, adding a salt separating agent for covering, performing heat treatment at 700 ℃ for 200min to obtain aluminum liquid and hot-state salt slag, and vertically blowing the aluminum liquid by argon to protect the aluminum liquid to flow out of a splitter box and enter a casting mold to realize the pouring of aluminum ingots; then, the hot salt slag passes through a water cooling-dissociation two-stage system, the water cooling time is 5min, the temperature of the salt slag after water cooling reaches 100-150 ℃, the dissociation time is 20min, and cold ash slag is obtained after dissociation; screening the cold-state ash slag to obtain oversize materials and undersize materials, wherein the oversize materials are coarse aluminum particles for standby, and performing ball milling and screening on the undersize materials to obtain fine aluminum particles and fine ash; and finally, mixing 20% of coarse aluminum particles, 60% of fine aluminum particles and 10% of salt separating agent, pressing into blocks, and then returning to the smelting aluminum extraction unit.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Example 5
Mixing hot aluminum ash slag and quartz sand powder, then squeezing and extracting aluminum through a squeezer, horizontally blowing the rest aluminum slag blocks at low temperature through helium to obtain cold aluminum slag blocks, and vertically blowing and protecting aluminum liquid through argon to flow out through a splitter box and enter a casting mold to realize pouring of aluminum ingots; then throwing the cold-state aluminum slag blocks and the ball forming materials into heat recovery equipment, adding a salt separating agent for covering, carrying out heat treatment at 650 ℃ for 100min to obtain aluminum liquid and hot-state salt slag, and vertically blowing the aluminum liquid by argon to protect the aluminum liquid to flow out of a splitter box and enter a casting mold to realize the pouring of aluminum ingots; then, the hot salt slag passes through a water cooling-dissociation two-stage system, the water cooling time is 3min, the temperature of the salt slag after water cooling reaches 100-150 ℃, the dissociation time is 10min, and cold ash slag is obtained after dissociation; screening the cold-state ash slag to obtain oversize materials and undersize materials, wherein the oversize materials are coarse aluminum particles for standby, and performing ball milling and screening on the undersize materials to obtain fine aluminum particles and fine ash; and finally, mixing 40% of coarse aluminum particles, 55% of fine aluminum particles and 5% of salt separating agent, pressing into balls, and then returning to the smelting aluminum extraction unit.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Example 6
Mixing hot aluminum ash and silicomanganese, then squeezing and extracting aluminum through a squeezer, horizontally blowing the rest aluminum slag blocks at low temperature through argon to obtain cold aluminum slag blocks, and vertically blowing and protecting aluminum liquid through argon to flow out through a splitter box and enter a casting mold to realize pouring of aluminum ingots; then throwing the cold-state aluminum slag blocks and the ball forming materials into heat recovery equipment, adding a salt separating agent for covering, performing heat treatment at 800 ℃ for 300min to obtain aluminum liquid and hot-state salt slag, and vertically blowing the aluminum liquid by argon to protect the aluminum liquid to flow out of a splitter box and enter a casting mold to realize the pouring of aluminum ingots; then, the hot salt slag passes through a water cooling-dissociation two-stage system, the water cooling time is 7min, the temperature of the salt slag after water cooling reaches 100-150 ℃, the dissociation time is 25min, and cold ash slag is obtained after dissociation; screening the cold-state ash slag to obtain oversize materials and undersize materials, wherein the oversize materials are coarse aluminum particles for standby, and performing ball milling and screening on the undersize materials to obtain fine aluminum particles and fine ash; and finally, mixing 30% of coarse aluminum particles, 40% of fine aluminum particles and 30% of salt separating agent, pressing into blocks, and then returning to the smelting aluminum extraction unit.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Example 7
Mixing hot aluminum ash with metal silicon powder, then squeezing and extracting aluminum through a squeezer, horizontally blowing the rest aluminum slag blocks at low temperature through argon to obtain cold aluminum slag blocks, and vertically blowing and protecting aluminum liquid through argon to flow out through a splitter box and enter a casting mold to realize pouring of aluminum ingots; then throwing the cold-state aluminum slag blocks and the ball forming materials into heat recovery equipment, adding a salt separating agent for covering, carrying out heat treatment at 750 ℃ for 200min to obtain aluminum liquid and hot-state salt slag, and vertically blowing the aluminum liquid by argon to protect the aluminum liquid to flow out of a splitter box and enter a casting mold to realize the pouring of aluminum ingots; then, the hot salt slag passes through a water cooling-dissociation two-stage system, the water cooling time is 6min, the temperature of the salt slag after water cooling reaches 100-150 ℃, the dissociation time is 30min, and cold ash slag is obtained after dissociation; screening the cold-state ash slag to obtain oversize materials and undersize materials, wherein the oversize materials are coarse aluminum particles for standby, and performing ball milling and screening on the undersize materials to obtain fine aluminum particles and fine ash; and finally, mixing 40% of coarse aluminum particles, 30% of fine aluminum particles and 30% of salt separating agent, pressing into balls, and returning to the smelting aluminum extraction unit.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Comparative example 1
The comparative example is different from example 7 in that no auxiliary agent is added in the aluminum squeezing unit, and the rest steps are the same as example 7. Because no auxiliary agent is added in the squeezing process, the fluidity is poor, the separation of aluminum liquid is incomplete, and the recovery rate of aluminum is reduced by about 7 percent.
The specific process parameters and aluminum recovery results of this example are shown in table 1.
Comparative example 2
This comparative example differs from example 2 in that the purge gas is air and the rest of the procedure is the same as example 7. Oxygen in the air reacts with the high-temperature aluminum metal, resulting in loss of the aluminum metal.
The specific process parameters and aluminum recovery results of this example are shown in table 1.
Comparative example 3
This comparative example is different from example 7 in that the heat treatment temperature is 600 ℃ and the remaining steps are the same as example 7. Because the temperature is lower, the aluminum burning loss rate is lower, but the recovered aluminum of the aluminum is reduced, and the resource waste is caused.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Comparative example 4
This comparative example is different from example 7 in that the heat treatment temperature is 800 ℃ and the remaining steps are the same as example 7. Because the temperature is higher, the aluminum burning loss rate is higher, and the resource waste is still caused.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Comparative example 5
This comparative example is different from example 7 in that the water cooling process is not performed, and the remaining steps are the same as example 7. Because the water cooling time is insufficient, the aluminum and the salt slag are easily embedded together and are not easy to screen, and the aluminum recovery rate is reduced.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Comparative example 6
This comparative example differs from example 7 in that no dissociation process is performed and the remaining steps are the same as example 7. Because the dissociation time is insufficient, the aluminum and the salt slag are not easy to screen, and the aluminum recovery rate is reduced.
The specific process parameters and aluminum recovery results of this example are shown in table 1.
Comparative example 7
This comparative example differs from example 7 in that 40% coarse aluminum particles, 55% fine aluminum particles, and 5% salt-separating agent were pressed into pellets, and the remaining steps were the same as in example 7. Because the salt separating agent is less, the aluminum burning loss in the smelting process is serious, and the recovery of the aluminum is also influenced.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
Comparative example 8
This comparative example differs from example 7 in that the batch was pressed into briquettes and the rest of the procedure was the same as example 7. As the block specific surface area is larger than the sphere, aluminum contacts more oxygen in the smelting process, so that the burning loss is higher.
The specific process parameters and aluminum recovery results of this example are shown in Table 1.
TABLE 1 comparison of Process parameters and aluminum recovery results for each example
As can be known from comparative example 1, the flowability of the aluminum liquid can be influenced by adding no auxiliary agent in the process of squeezing the aluminum extracting unit, so that the quality of the aluminum liquid separated in the process of squeezing the aluminum is influenced, part of the aluminum liquid remains in slag blocks, and a large amount of salt needs to be correspondingly added in the subsequent smelting process to prevent oxidation and cause a large amount of burning loss. However, a large amount of salt is added, so that negative feedback is increased for subsequent screening, ball milling, ingredient forming, smelting and aluminum extraction, and the recovery rate of aluminum is influenced.
As can be seen from example 1 and comparative example 2, purging with nitrogen or air results in the nitrogen or oxygen reacting with the high temperature aluminum, thereby reducing the recovery of aluminum, and therefore the inert gas shield is selected from argon and helium, and argon is preferred for the inert shield because argon is less expensive than helium.
As can be seen from comparative examples 3 and 4, when the heat treatment temperature is lower, the melting point of aluminum cannot be reached, so that the aluminum cannot be completely changed into aluminum liquid to be separated out, and the waste of aluminum resources is caused; when the heat treatment temperature is higher, the reaction with oxygen is easy to occur, so that the oxidation is caused, and the waste of aluminum resources is caused.
It can be known from comparative examples 5 and 6 that water cooling is the rapid cooling, the purpose is that the molten aluminum is in the process of changing into aluminum particles and contacting with air and oxidizing, make the molten aluminum drop solidify rapidly and reunite into aluminum particles, so the cooling time is the key factor, then the purpose of dissociation technology is to let aluminum particles further separate with the aluminium ash, reduce the adhesion, in order to be favorable to sieving aluminum particles and aluminium ash, therefore water cooling and dissociation time are insufficient, easily cause salt slag and aluminium to inlay together, follow-up screening ball-milling is difficult to select separately thoroughly equally, influence the aluminium rate of recovery and cause the aluminium resource waste.
As can be seen from comparative examples 7 and 8, the salt separating agent was more and the burning loss was less during the compounding ratio. The specific surface area of the mixture is reduced by forming the mixture into a spherical shape, and the large-area contact of oxygen and aluminum can be avoided, so that the burning loss rate of the mixture can be reduced by pressing the mixture into a sphere.
In summary, the method for recovering metallic aluminum from aluminum ash provided by the invention, specifically a method for recovering metallic aluminum from aluminum ash with low loss, has at least the following beneficial effects:
(1) the aluminum liquid is blown by inert gas, so that on one hand, the surface of the aluminum liquid is protected from generating an alumina film easily to reduce the fluidity of the aluminum liquid, on the other hand, the gas content in the aluminum liquid can be reduced, and the defects caused by subsequent aluminum castings are prevented. The hot slag is purged by low-temperature inert gas, so that on one hand, aluminum in the hot slag can be protected from being oxidized, and on the other hand, the quick low-temperature cooling can provide a basis for the subsequent quick dissociation of salt and aluminum;
(2) the rapid water cooling is beneficial to reducing the contact time of the aluminum liquid in the hot salt slag and air in the process of converting the aluminum liquid into aluminum particles and promoting the aluminum liquid drops to be rapidly solidified and agglomerated into aluminum particles; dissociation is beneficial to further separating the aluminum particles from the salt slag, adhesion is reduced, and the aluminum particles and the salt slag are efficiently screened, so that water cooling and dissociation time are accurately controlled, and the maximum recovery rate of aluminum can reach 99.56%;
(3) the coarse and fine aluminum particles and the salt separating agent are subjected to compression molding according to reasonable particle size grading, so that particle agglomeration molding is facilitated, pores among particles are reduced, the specific surface area is reduced, the burning loss of aluminum in a smelting link can be reduced to the maximum extent, the recovery efficiency of metal aluminum is improved, efficient resource utilization is realized, the coarse and fine aluminum particles and the salt separating agent are subjected to batching molding in different proportions and then are smelted, and the burning loss rate of aluminum can reach 0.31% at least;
(4) and part of the salt separating agent is recycled in the treatment process.
It should be understood that the endpoints of the ranges and any values disclosed herein are not limited to the precise range or value and that such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
It is noted that, in this document, relational terms such as "first" and "second," and the like, may be 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. Also, 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. In addition, the term "and/or" appearing herein is merely one type of association that describes an associated object, meaning that three relationships may exist, e.g., a and/or B, may mean: a exists alone, A and B exist simultaneously, and B exists alone.
The foregoing are merely exemplary embodiments of the present invention, which enable those skilled in the art to understand or practice the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A method for recovering metallic aluminum from aluminum dross, the method comprising:
mixing the thermal state aluminum ash slag with a pressing auxiliary agent to obtain a first mixture;
squeezing the first mixture to extract aluminum, and then obtaining a first cold-state aluminum slag block and a first aluminum liquid in an inert gas purging atmosphere;
covering a salt separating agent on the surface of the first cold-state aluminum slag block to carry out first smelting aluminum extraction to obtain first hot-state salt slag and second aluminum liquid;
wherein, the technological parameters of the first smelting aluminum extraction comprise: the temperature is 650-800 ℃.
2. The process for recovering metallic aluminum from aluminous ash according to claim 1, wherein the pressing aid comprises at least one of metallic silicon powder, silica fume, potassium chloride, quartz sand, petroleum coke and silicomanganese.
3. The method for recovering metallic aluminum from aluminous ash according to claim 1, wherein the mass ratio of the hot aluminous ash to the pressing aid is (95-99.5) to (0.5-5).
4. A process for recovering metallic aluminum from aluminous ash according to claim 1 wherein said salt separating agent comprises a chloride salt.
5. The method of claim 4, wherein the chloride salt comprises at least one of potassium chloride, sodium chloride, magnesium chloride, zinc chloride, and calcium chloride.
6. The method for recovering metallic aluminum from aluminous ash according to claim 1, wherein the mass ratio of the salt separating agent to the cold aluminous clinker is (1-15) to (85-99).
7. The method for recovering metallic aluminum from aluminum dross according to any one of claims 1 to 6, further comprising:
carrying out water cooling on the first hot salt slag, and dissociating the salt slag to obtain cold ash slag;
performing first screening on the cold-state ash slag to obtain a first oversize material and a first undersize material;
grinding the first screen material, and then carrying out second screening to obtain a second screen material;
mixing the first oversize material, the second oversize material and a salt separating agent, and then pressing and forming to obtain a second cold-state aluminum slag forming material;
carrying out second smelting aluminum extraction on the second cold-state aluminum slag molding material to obtain second hot-state salt slag and third aluminum liquid;
wherein the technological parameters of the second smelting aluminum extraction comprise: the temperature is 650-800 ℃.
8. The method of claim 7, wherein the first oversize material has a particle size of > 1 mm; the grain size of the second oversize material is 1mm-0.1 mm.
9. The method for recovering metallic aluminum from aluminum ash according to claim 7, wherein the temperature reduction time of water cooling is 3-8 min, and the temperature of the first hot salt slag after water cooling is 100-150 ℃.
10. The method for recovering metallic aluminum from aluminum dross according to claim 7, wherein the ratio of the first oversize material to the second oversize material to the salt-separating agent is (20-40) to (30-60) to (5-30) in parts by mass.
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Effective date of registration: 20240423 Address after: 450041 No. 82, Jiyuan Road, Zhengzhou District, Henan Patentee after: China Aluminum Zhengzhou Research Institute of Nonferrous Metals Co.,Ltd. Country or region after: China Address before: 100082 No. 62 North Main Street, Haidian District, Beijing, Xizhimen Patentee before: ALUMINUM CORPORATION OF CHINA Ltd. Country or region before: China |
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