CN111994928A - Aluminum ash recycling system and processing method thereof - Google Patents
Aluminum ash recycling system and processing method thereof Download PDFInfo
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- CN111994928A CN111994928A CN202010890349.2A CN202010890349A CN111994928A CN 111994928 A CN111994928 A CN 111994928A CN 202010890349 A CN202010890349 A CN 202010890349A CN 111994928 A CN111994928 A CN 111994928A
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- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 129
- 238000004064 recycling Methods 0.000 title claims description 20
- 238000003672 processing method Methods 0.000 title abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims abstract description 114
- 238000003860 storage Methods 0.000 claims abstract description 103
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000000463 material Substances 0.000 claims abstract description 63
- 239000007789 gas Substances 0.000 claims abstract description 50
- 238000001035 drying Methods 0.000 claims abstract description 39
- 238000012216 screening Methods 0.000 claims abstract description 30
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 239000000428 dust Substances 0.000 claims abstract description 27
- 238000000034 method Methods 0.000 claims abstract description 19
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 239000011261 inert gas Substances 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims description 61
- 239000007788 liquid Substances 0.000 claims description 55
- 238000005507 spraying Methods 0.000 claims description 48
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 45
- 238000005406 washing Methods 0.000 claims description 43
- 238000003756 stirring Methods 0.000 claims description 30
- 229910021529 ammonia Inorganic materials 0.000 claims description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 26
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 17
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 17
- 239000012267 brine Substances 0.000 claims description 16
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 16
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 claims description 15
- 239000000243 solution Substances 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 13
- 239000002994 raw material Substances 0.000 claims description 12
- 239000004411 aluminium Substances 0.000 claims description 11
- 238000005096 rolling process Methods 0.000 claims description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 10
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 239000006148 magnetic separator Substances 0.000 claims description 9
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 8
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 8
- 238000002425 crystallisation Methods 0.000 claims description 8
- 230000008025 crystallization Effects 0.000 claims description 8
- 238000001556 precipitation Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000000498 ball milling Methods 0.000 claims description 7
- 238000001704 evaporation Methods 0.000 claims description 7
- 230000008020 evaporation Effects 0.000 claims description 7
- 239000002002 slurry Substances 0.000 claims description 7
- 239000012452 mother liquor Substances 0.000 claims description 6
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 4
- 239000011344 liquid material Substances 0.000 claims description 4
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 238000012432 intermediate storage Methods 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- 239000011343 solid material Substances 0.000 claims description 3
- 239000002699 waste material Substances 0.000 abstract description 10
- 125000004122 cyclic group Chemical group 0.000 abstract description 2
- 239000007921 spray Substances 0.000 description 8
- 238000007599 discharging Methods 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 7
- 239000007787 solid Substances 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000007885 magnetic separation Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- PMHQVHHXPFUNSP-UHFFFAOYSA-M copper(1+);methylsulfanylmethane;bromide Chemical compound Br[Cu].CSC PMHQVHHXPFUNSP-UHFFFAOYSA-M 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- CAVCGVPGBKGDTG-UHFFFAOYSA-N alumanylidynemethyl(alumanylidynemethylalumanylidenemethylidene)alumane Chemical compound [Al]#C[Al]=C=[Al]C#[Al] CAVCGVPGBKGDTG-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- COOGPNLGKIHLSK-UHFFFAOYSA-N aluminium sulfide Chemical compound [Al+3].[Al+3].[S-2].[S-2].[S-2] COOGPNLGKIHLSK-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/58—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C17/00—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls
- B02C17/10—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls with one or a few disintegrating members arranged in the container
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C17/00—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls
- B02C17/18—Details
- B02C17/183—Feeding or discharging devices
- B02C17/1835—Discharging devices combined with sorting or separating of material
- B02C17/184—Discharging devices combined with sorting or separating of material with separator arranged in discharge path of crushing zone
- B02C17/1845—Discharging devices combined with sorting or separating of material with separator arranged in discharge path of crushing zone with return of oversize material to crushing zone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C17/00—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls
- B02C17/18—Details
- B02C17/183—Feeding or discharging devices
- B02C17/1835—Discharging devices combined with sorting or separating of material
- B02C17/185—Discharging devices combined with sorting or separating of material with more than one separator
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/22—Alkali metal sulfides or polysulfides
- C01B17/32—Hydrosulfides of sodium or potassium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/46—Purification of aluminium oxide, aluminium hydroxide or aluminates
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/50—Inorganic acids
- B01D2251/506—Sulfuric acid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/80—Particles consisting of a mixture of two or more inorganic phases
- C01P2004/82—Particles consisting of a mixture of two or more inorganic phases two phases having the same anion, e.g. both oxidic phases
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- Chemical & Material Sciences (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
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- Life Sciences & Earth Sciences (AREA)
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- Materials Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides an aluminum ash recovery processing system and a processing method thereof. The system comprises an aluminum ash screening treatment system, an aluminum ash reaction system connected with the aluminum ash screening treatment system, a reaction material separation and drying system connected with the aluminum ash reaction system, and a finished product storage system connected with the reaction material separation and drying system. This system retrieves the dust in with the processing procedure through the dust collection pipeline, has avoided the influence of dust to the surrounding environment, better avoid the resource loss moreover, improved the resource recovery rate. The safety problem possibly brought in the aluminum ash treatment process is effectively solved by introducing the inert gas. The generated gases such as ammonia gas can be safely and effectively recovered as resources. The system comprehensively treats the waste aluminum ash, effectively recovers various resources, and finally uses the residual gas as a heat source of the system, so that the whole system realizes the cyclic utilization of all resources and has good social and economic benefits.
Description
Technical Field
The invention belongs to the technical field of comprehensive treatment and recycling of waste resources. In particular to an aluminum ash recovery processing system and a processing method thereof.
Background
The aluminum ash is a product of cooling slag generated in the production process of electrolytic aluminum or cast aluminum, and is generated in all production processes of aluminum melting as solid waste, so that the production amount is huge every year. The main components of the material comprise substances with economic value such as aluminum oxide, aluminum nitride, aluminum carbide, aluminum sulfide, soluble salt and the like, and simultaneously contain a certain amount of harmful elements. Therefore, if a large amount of aluminum ash waste cannot be recycled reasonably, not only is the resource wasted, but also the environment is seriously affected. Therefore, the recovery and disposal of aluminum ash and the reuse of resources thereof have been continuously studied in this field.
At present, various recovery processing methods for aluminum ash exist, valuable resources and toxic substances contained in the aluminum ash are easy to generate toxic and harmful gases in the recovery processing process, the generation of the gases can not only cause great influence on the environmental atmosphere, but also easily cause explosion, have great potential safety hazard and bring certain difficulty to the safe and efficient recovery processing of the aluminum ash.
Disclosure of Invention
In order to solve the problems, the invention provides an aluminum ash recycling system and a processing method thereof. The system can efficiently and safely recover various components in the aluminum ash, can effectively avoid the influence of harmful gas on the environment and potential safety hazards, can sufficiently and efficiently recover various components in the aluminum ash, and has good social and economic benefits.
The invention is realized by the following technical scheme
The utility model provides an aluminium ash recovery processing system, this system includes aluminium ash screening processing system, the aluminium ash reaction system who is connected with aluminium ash screening processing system, the reaction material separation drying system who is connected with aluminium ash reaction system, the finished product storage system who is connected with reaction material separation drying system.
Furthermore, the aluminum ash screening treatment system comprises a blanking hopper, a lifting machine connected with a discharge port of the blanking hopper, a raw material bin connected with a discharge port of the lifting machine, a conveying belt positioned right below an outlet of the raw material bin, a ball mill connected with a discharging end of the conveying belt, the lifting machine connected with the ball mill, and a rolling screen connected with the lifting machine, wherein the rolling screen is respectively connected with the magnetic separator, the 60-80 mesh particle storage tank and the particle storage tank smaller than 80 mesh; the discharge port of the magnetic separator is connected with an aluminum particle storage tank, the 60-80-mesh particle storage tank is connected with a ball mill through a material pipeline, a screw conveyor is arranged right below the discharge port of the particle storage tank smaller than 80 meshes, and the material is conveyed to an aluminum ash reaction system through the discharge port of the screw conveyor; the aluminum ash screening treatment system also comprises a plurality of dust collecting pipelines and a bag-type dust collector connected with the outlets of the collecting pipelines; the plurality of collecting pipelines are respectively used for collecting dust in the blanking hopper, the raw material bin, the ball mill, the 60-80 mesh particle storage tank and the particle storage tank smaller than 80 mesh, and then the collected dust is conveyed to the particle storage tank smaller than 80 mesh through the bag-type dust remover.
Furthermore, the aluminum ash reaction system comprises a stirring tank, a slurry pump connected with the stirring tank and a reaction tank connected with the slurry pump; a first gas outlet at the upper end of the stirring tank and a first gas outlet at the upper end of the reaction tank are both connected with a first water-sealed tank, a gas outlet of the first water-sealed tank is communicated with a concentrated ammonia device, a second gas outlet at the upper end of the reaction tank is also connected with a second water-sealed tank, the second water-sealed tank is connected with a dilute ammonia device, and a material outlet at the bottom end of the reaction tank is communicated with a reaction material separation and drying system through a material pipeline; preferably, the aluminum ash reaction system further comprises an emergency treatment pool, wherein an inlet of the emergency treatment pool is connected with a discharge port at the bottom end of the reaction tank, and an outlet of the emergency treatment pool is connected with the stirring tank.
Further, the aluminum ash reaction system also comprises a nitrogen storage tank, wherein the nitrogen storage tank passes through the stirring tank and the reaction tank through gas pipelines respectively.
Further, the dilute ammonia device comprises a washing tower connected with the aluminum ash reaction system, a discharge hole at the bottom end of the washing tower is communicated with a middle storage tank, the middle storage tank is communicated with a discharge pump, and the discharge pump is communicated with an ammonium sulfate storage tank; the device also comprises a sulfuric acid storage tank which is communicated with an inlet at the upper part of the washing tower through a circulating pump; the concentrated ammonia device comprises a hydrogen sulfide reactor, a discharge port at the bottom end of the hydrogen sulfide reactor is communicated with a sodium hydrosulfide storage tank, and an outlet at the top end of the hydrogen sulfide reactor is communicated with an ammonia gas absorption tower; the hydrogen sulfide reactor is also provided with a sodium hydroxide solution inlet, and the sodium hydrosulfide storage tank is also communicated with the hydrogen sulfide reactor through a pipeline and a sodium hydrosulfide circulating pump; the ammonia absorption tower is also communicated with the heat exchanger through a material pipeline and a heat exchanger circulating pump.
Further, the reaction material separation and drying system comprises a five-section vacuum belt conveyor, and a material outlet of the five-section vacuum belt conveyor is connected with the aluminum ash dryer; a liquid outlet of a mother liquid area of the five-section vacuum belt conveyor is communicated with a mother liquid storage tank, a first-stage spraying area is communicated with a first-stage spraying area washing liquid storage tank, a second-stage spraying area is communicated with a second-stage spraying area washing liquid storage tank, a third-stage spraying area is communicated with a third-stage spraying area washing liquid storage tank, and a fourth-stage spraying area and a drying area are communicated with a fourth-stage spraying area washing liquid storage tank; an outlet of the mother liquor storage tank is communicated with a precipitation tank, an outlet of the precipitation tank is communicated with a strong brine tank, and the strong brine tank is communicated with a strong brine evaporation and crystallization system; the first-stage spraying area washing liquid storage tank and the third-stage spraying area washing liquid storage tank are communicated with the saline water mixing tank; the second-stage spraying area cleaning solution storage tank and the fourth-stage spraying area cleaning solution storage tank are communicated with a spraying device of the five-section vacuum belt conveyor through a conveying pipeline; the settling tank is also communicated with a feed inlet of the five-section vacuum belt conveyor through a material pipeline.
The method for treating the aluminum ash by using the aluminum ash recovery treatment system comprises the following steps: collecting aluminum ash, and performing ball milling and screening treatment; the particles with the particle size of less than 80 meshes obtained by screening are placed in an aluminum ash reaction system for reaction; separating and drying the solid-liquid material obtained by the reaction to obtain a finished product; and conveying the mixed gas obtained by the reaction to an ammonia gas treatment device for treatment, and taking the residual gas as a drying heat source.
Further, the reaction in the aluminum ash reaction system is specifically as follows: firstly, introducing inert gas into an aluminum ash reaction system to discharge air in the reaction system, then uniformly mixing aluminum ash particles with a particle size of less than 80 meshes and a sodium hydroxide aqueous solution in the aluminum ash reaction system, and reacting for 8-10 hours at the temperature of 80-120 ℃; preferably, the ratio of the aluminum ash to the sodium hydroxide is 100: 5, the concentration of the sodium hydroxide solution is 32%.
Further, the solid-liquid material is separated by adopting a five-section vacuum belt conveyor.
Further, the moisture content of the solid material obtained by the five-section vacuum belt conveyor is 25-35%, the drying is carried out in an aluminum ash drying machine, the temperature during the drying is 300-600 ℃, and the drying is carried out until the moisture content is less than 1%.
Compared with the prior art, the invention has the following positive beneficial effects
When the system is used for treating the aluminum ash, firstly, the aluminum ash is subjected to ball milling and screening treatment, and aluminum-containing particles obtained by screening are subjected to magnetic separation and then aluminum-containing particles are recovered; recovering the large particles into the ball mill for ball milling again to fully recover the resources in the ball mill, and reacting the powder particles obtained by screening in an aluminum ash reaction system which discharges air through inert gas; liquid obtained after solid-liquid separation of materials generated by reaction is recycled in the whole system, and solid is recovered after being dried and can be used as building materials and the like (the main component of the materials after reaction and drying is alumina which can be used for partially replacing bauxite in industries such as steel, cement, refractory materials and the like); the gas generated by the reaction is combustible gas for the residual gas after ammonia gas recovery, and can be recovered and conveyed to a drying system to be used as a heat source. Therefore, the whole system realizes the full recycling of aluminum ash resources, does not waste resources or generate wastes, greatly reduces the consumption of extra resources and has good social and economic benefits.
This system has retrieved the dust in with the processing procedure through dust collecting tube, has not only avoided the influence of dust to the surrounding environment, better avoid the resource loss moreover, has improved the resource recovery rate. The safety problem possibly brought in the aluminum ash treatment process is effectively solved by introducing the inert gas. The generated gases such as ammonia gas can be safely and effectively recovered as resources.
The system comprehensively treats the waste aluminum ash, effectively recovers various resources in the waste aluminum ash, and finally uses the residual gas as a heat source of the system, so that the whole system realizes the complete cyclic utilization and obviously improves the resource utilization rate.
Drawings
Figure 1 shows one of the schematic diagrams of the aluminum ash screening treatment system,
figure 2 shows a second schematic diagram of the aluminum ash screening treatment system,
FIG. 3 is a schematic view of an aluminum ash reaction system
FIG. 4 shows a second schematic view of an aluminum ash reaction system,
FIG. 5 shows a third schematic view of an aluminum ash reaction system,
FIG. 6 shows a schematic view of a reaction mass separation and drying system,
figure 7 shows a schematic diagram of a lean ammonia plant,
figure 8 shows a schematic diagram of a concentrated ammonia plant,
FIG. 9 shows a schematic view of an aluminum ash recovery processing system,
the symbols in the figures represent: 1 denotes a hopper, 2 denotes a hoist, 3 denotes a raw material silo, 4 denotes a conveyor belt, 5 denotes a ball mill, 6 denotes a rolling screen, 7 denotes a magnetic separator, 8 denotes an aluminum particle storage tank, 9 denotes a 60-80 mesh particle storage tank, 10 denotes a less-than-80 mesh particle storage tank, 11 denotes a screw conveyor, 12 denotes a dust collection pipe, 13 denotes a bag-type dust collector, 14 denotes a stirring tank, 15 denotes a slurry pump, 16 denotes a reaction tank, 17 denotes a first water-sealed tank, 18 denotes a second water-sealed tank, 19 denotes an emergency treatment tank, 20 denotes a nitrogen storage tank, 21 denotes a five-stage vacuum belt conveyor, 2101 denotes a mother liquid zone, 2102 denotes a primary spray zone, 2103 denotes a secondary spray zone, 2104 denotes a tertiary spray zone, 2105 denotes a quaternary spray zone, 2106 denotes an evacuation zone, 22 denotes a mother liquid storage tank, 23 denotes a primary spray zone storage tank, 24 denotes a secondary spray zone washing liquid storage tank, 25 denotes a tertiary spray zone washing liquid storage tank, 26 denotes a quaternary spray zone washing liquid storage tank, 27 denotes a precipitation tank, 28 denotes a concentrated brine tank, 29 denotes a concentrated brine evaporative crystallization system, 30 denotes a brine mixing tank, 31 denotes an aluminum ash dryer, 32 denotes a seal pump, 33 denotes a product tank, 34 denotes a scrubber, 35 denotes an intermediate storage tank, 36 denotes a discharge pump, 37 denotes an ammonium sulfate circulation pump, 38 denotes a hydrogen sulfide reactor, 39 denotes a sodium hydrosulfide intermediate tank, 40 denotes a sodium hydrosulfide circulation pump, 41 denotes an ammonia gas absorption tower, 42 denotes a heat exchanger, and 43 denotes a heat exchanger circulation pump.
Detailed Description
The present invention will be described in more detail with reference to the following embodiments for understanding the technical solutions of the present invention, but the present invention is not limited to the scope of the present invention.
Example 1
The invention provides an aluminum ash recovery processing system, which comprises an aluminum ash screening processing system, an aluminum ash reaction system connected with the aluminum ash screening processing system, a reaction material separation and drying system connected with the aluminum ash reaction system, and a finished product storage system connected with the reaction material separation and drying system;
the aluminum ash screening treatment system comprises a blanking hopper, a lifting machine connected with a discharge port of the blanking hopper, a raw material bin connected with a discharge port of the lifting machine, a conveying belt positioned right below an outlet of the raw material bin, a ball mill connected with a discharging end of the conveying belt, the lifting machine connected with the ball mill, and a rolling screen connected with the lifting machine, wherein a discharge port of the rolling screen is respectively connected with a magnetic separator, a 60-80 mesh particle storage tank and a less than 80 mesh particle storage tank; the discharge port of the magnetic separator is connected with an aluminum particle storage tank, the 60-80-mesh particle storage tank is connected with a ball mill through a material pipeline, a screw conveyor is arranged right below the discharge port of the particle storage tank smaller than 80 meshes, and the material is conveyed to an aluminum ash reaction system through the discharge port of the screw conveyor;
the collected aluminum ash is placed in a raw material bin through a discharging hopper and a lifting machine, then is conveyed to a ball mill through the raw material bin and a conveying belt, and is conveyed to a rolling screen through the ball mill, the rolling screen is used for screening, oversize materials (mainly containing iron and aluminum) are placed in a magnetic separator for magnetic separation, and the residual aluminum particles after the magnetic separation are recovered. And placing the particles of 60-80 meshes obtained by screening with a rolling screen into a particle storage tank of 60-80 meshes, then conveying the particles into the ball mill for ball milling again in the ball mill, and recovering and fully utilizing the particles again. And placing the particles smaller than 80 meshes obtained by screening by the rolling screen into a particle storage tank smaller than 80 meshes, and then conveying the particles into an aluminum ash reaction system by a screw conveyor for reaction treatment.
Preferably, the aluminum ash screening treatment system further comprises a plurality of dust collecting pipelines and a bag-type dust collector connected with outlets of the collecting pipelines; the plurality of collecting pipelines are respectively used for collecting dust in the blanking hopper, the raw material bin, the ball mill, the 60-80 mesh particle storage tank and the particle storage tank smaller than 80 mesh, and then the collected dust is conveyed to the particle storage tank smaller than 80 mesh through the bag-type dust remover.
The dust that produces in this in-process through many dust collecting tube says collects each in-process, then collects the dust of collecting to being less than 80 mesh granule storage jar through the sack cleaner and carries out follow-up use. The process can not generate dust which has great influence on the environment, and materials in the process can be more sufficiently recovered, so that the resource recovery rate is improved.
The aluminum ash reaction system comprises a stirring tank, a slurry pump connected with the stirring tank and a reaction tank connected with the slurry pump; a first gas outlet at the upper end of the stirring tank and a first gas outlet at the upper end of the reaction tank are both connected with a first water-sealed tank, a gas outlet of the first water-sealed tank is communicated with a concentrated ammonia device, a second gas outlet at the upper end of the reaction tank is also connected with a second water-sealed tank, the second water-sealed tank is connected with a dilute ammonia device, and a material outlet at the bottom end of the reaction tank is communicated with a reaction material separation and drying system through a material pipeline; preferably, the retort can be a plurality of, a plurality of retort are established ties, the material after mixing in the agitator tank at first gets into first retort and reacts, then gets into the second retort of establishing ties and reacts, can react as to in a plurality of retort in proper order for the material reaction is more abundant, more abundant retrieves the material in the aluminium ash.
And (3) mixing the granular material smaller than 80 meshes conveyed into the stirring tank with the sodium hydroxide aqueous solution, uniformly stirring, conveying the mixture into the reaction tank through a material pump, reacting for 8-10 hours at the temperature of 80-120 ℃, conveying gas generated in the reaction process into a concentrated ammonia device from the top of the reaction tank for recycling, and conveying the mixed material generated in the reaction into a reaction material separation and drying system through a material pipeline for separation and drying.
Preferably, the aluminum ash reaction system further comprises an emergency treatment pool, wherein an inlet of the emergency treatment pool is connected with a discharge port at the bottom end of the reaction tank, and an outlet of the emergency treatment pool is connected with the stirring tank. When a problem occurs in the reaction process, materials in the reaction tank are conveyed to the stirring tank through the emergency treatment pool to be subjected to recycling treatment again, so that resource waste and environmental pollution caused by reaction material discharge are avoided.
More preferably, the aluminum ash reaction system further comprises a nitrogen storage tank, wherein the nitrogen storage tank passes through the stirring tank and the reaction tank respectively through a gas pipeline. Before the material mixing reaction and at the beginning of the mixing reaction, firstly introducing nitrogen into the stirring tank and the reaction tank, discharging oxygen in the stirring tank and the reaction tank through the nitrogen, conveying the mixed gas discharged from the stirring tank and the reaction tank into the dilute ammonia device through the second water-sealed tank to treat ammonia contained in the mixed gas, and recovering and reusing the residual inert gas after treatment or discharging the residual inert gas outside (no pollution exists to the atmosphere). And after the inert gas is discharged, closing the inert gas inlet valve, fully reacting the materials in the reaction tank to generate a large amount of mixed gas containing ammonia gas, and treating the mixed gas in the ammonia concentration device through the first water seal tank to recover the ammonia gas and other gases.
The reaction material separation and drying system comprises a five-section vacuum belt conveyor, and a material outlet of the five-section vacuum belt conveyor is connected with an aluminum ash dryer; a liquid outlet of a mother liquid area of the five-section vacuum belt conveyor is communicated with a mother liquid storage tank, a first-stage spraying area is communicated with a first-stage spraying area washing liquid storage tank, a second-stage spraying area is communicated with a second-stage spraying area washing liquid storage tank, a third-stage spraying area is communicated with a third-stage spraying area washing liquid storage tank, and a fourth-stage spraying area and a drying area are communicated with a fourth-stage spraying area washing liquid storage tank; an outlet of the mother liquor storage tank is communicated with a precipitation tank, an outlet of the precipitation tank is communicated with a strong brine tank, and the strong brine tank is communicated with a strong brine evaporation and crystallization system;
putting the reaction materials into a five-section vacuum dryer, firstly carrying out solid-liquid separation through a mother liquor zone, conveying the separated liquid into a mother liquor storage tank, precipitating the liquid in the mother liquor storage tank in a precipitation tank, putting the precipitated solid into a concentrated salt water tank, then carrying out evaporation crystallization treatment, recovering the salt in the concentrated salt water tank, and recycling the salt as a resource; the materials passing through the mother liquid zone are washed and subjected to solid-liquid separation through a first-stage spraying zone, a second-stage spraying zone, a third-stage spraying zone and a fourth-stage spraying zone in sequence, liquid generated after separation respectively enters a first-stage spraying zone washing liquid storage tank, a second-stage spraying zone washing liquid storage tank, a third-stage spraying zone washing liquid storage tank and a fourth-stage spraying zone washing liquid storage tank, the solid materials forward enter a drying zone of a five-stage vacuum belt conveyor for solid-liquid separation again, the solid obtained through separation is conveyed to an aluminum ash dryer for drying treatment (the temperature during drying is 300-600 ℃, the water content is less than 1%), and the product materials are obtained after drying. And liquid obtained by solid-liquid separation in the pumping area enters a washing liquid storage tank in the four-stage spraying area. The five-section vacuum belt conveyor and the aluminum ash dryer are well known devices of the technical personnel in the field.
Preferably, the first-stage spraying area washing liquid storage tank and the third-stage spraying area washing liquid storage tank are both communicated with the brine mixing tank, and the solution in the brine mixing tank is conveyed to the stirring tank for recycling; the secondary spraying area washing liquid storage tank and the fourth spraying area washing liquid storage tank are communicated with a spraying device of the five-section type vacuum belt conveyor through a conveying pipeline, so that the materials are recycled; the settling tank is also communicated with a feed inlet of the five-section vacuum belt conveyor through a material pipeline. Realizes the recycling of materials in the whole process, obviously improves the resource utilization rate and reduces the resource consumption.
Further, the dilute ammonia device comprises a washing tower connected with the aluminum ash reaction system, a discharge hole at the bottom end of the washing tower is communicated with a middle storage tank, the middle storage tank is communicated with a discharge pump, and the discharge pump is communicated with an ammonium sulfate storage tank; the device also comprises a sulfuric acid storage tank which is communicated with an inlet at the upper part of the washing tower through a circulating pump.
The concentrated ammonia device comprises a hydrogen sulfide reactor, wherein a discharge port at the bottom end of the hydrogen sulfide reactor is communicated with a sodium hydrosulfide storage tank, and an outlet at the top end of the hydrogen sulfide reactor is communicated with an ammonia gas absorption tower; the hydrogen sulfide reactor is also provided with a sodium hydroxide solution inlet, and the sodium hydrosulfide storage tank is also communicated with the hydrogen sulfide reactor through a pipeline and a sodium hydrosulfide circulating pump; the ammonia absorption tower is also communicated with the heat exchanger through a material pipeline and a heat exchanger circulating pump.
Conveying mixed gas containing inert gas (nitrogen) generated in the initial stirring tank and the reaction tank to a washing tower of a dilute ammonia device, reversely contacting with sulfuric acid in the washing tower to generate ammonium sulfate, and placing the ammonium sulfate in an ammonium sulfate storage tank to realize recycling of ammonia gas; the residual inert gas is discharged from the top end of the washing tower, so that the inert gas can be recycled and reused and can be discharged after reaching the standard.
The mixed gas with larger ammonia concentration generated in the reaction tank is introduced into a concentrated ammonia device, firstly mixed with sodium hydroxide solution to remove hydrogen sulfide gas in the mixed gas, the generated sodium hydrosulfide is placed in a sodium hydrosulfide storage tank for recycling, the rest unreacted gas enters an ammonia gas absorption tower and is in reverse contact with cooling water to generate ammonia water, the ammonia water is discharged from the bottom of the tower for recycling, the rest gas is discharged from the top of the tower and is recycled to an aluminum ash dryer for ignition to be used as a heat source, namely, the whole process realizes the whole recycling of aluminum ash resources, and the operation is simple and safe, thereby having good social application value.
Example 2
The invention also provides a method for recycling the aluminum ash by using the aluminum ash recycling system in the embodiment 1, which comprises the following steps:
(1) collecting aluminum ash, placing the collected aluminum ash into a ball mill for ball milling, and placing the ball-milled materials into a drum screen for screening;
the upper-layer substances obtained by screening (the upper-layer substances are mainly aluminum particles containing iron and aluminum ash, the content of the aluminum simple substance is more than 60 percent) are magnetically separated in a magnetic separator, and the residual aluminum particles after magnetic separation are recovered in an aluminum particle storage tank; the middle layer material obtained by screening is particles with the particle size within the range of 60-80 meshes, and the particles with the particle size of 60-80 meshes are conveyed into a ball mill for ball milling again so as to more fully recover the resources in the particles; conveying the particles with the particle size of less than 80 meshes obtained by screening to an aluminum ash reaction system through a material pipeline for reaction;
(2) conveying the particles with the particle size smaller than 80 meshes obtained in the step (1) into a stirring tank to be mixed with a sodium hydroxide solution in the stirring tank (the mass ratio of the particles to the sodium hydroxide solution is 100: 5, and the mass fraction of the sodium hydroxide solution is 32%), uniformly mixing, conveying into a reaction tank to react, and reacting at 80-120 ℃ until the aluminum ash in the reaction tank is completely reacted (the content of aluminum nitride in the material after the reaction is finished is below 0.5%);
when the aluminum ash particles smaller than 80 meshes are conveyed into the stirring tank and the reaction tank, firstly introducing nitrogen into the stirring tank and the reaction tank to discharge air in the stirring tank and the reaction tank, introducing the nitrogen, the air and a small amount of dispersed reaction gas into a washing tower through a water-sealed tank, washing by using dilute sulfuric acid to obtain ammonium sulfate for recycling, wherein the residual nitrogen can be discharged up to the standard and can also be recycled;
(3) conveying the solid-liquid reaction material obtained after the reaction in the step (2) to a five-section vacuum belt conveyor by a material conveying pump for solid-liquid separation (the water content of the solid obtained after the solid-liquid separation is 25-35%), conveying the solid obtained after the separation to an aluminum ash drying machine for drying (the temperature when the aluminum ash drying machine is used for drying is 300-; the separated liquid is conveyed to a concentrated brine evaporation crystallization system for evaporation crystallization, and salts (the main components of the salts are 70% of sodium chloride and 30% of potassium chloride) in the concentrated brine evaporation crystallization system are recovered;
preferably, the mixed gas can be conveyed to a five-section vacuum belt conveyor to be used as washing liquid, and can also be conveyed to a stirring tank to be reused;
(4) and (3) discharging the mixed gas obtained by the reaction in the step (2) from a gas outlet at the top end of the reaction tank, sealing the mixed gas with water, and then treating the mixed gas in a concentrated ammonia device, wherein the specific steps are as follows: firstly, mixing and reacting the mixed gas with sodium hydroxide (the mass fraction is 10%), and recycling the reacted materials into a sodium hydrosulfide storage tank to recycle the sodium hydrosulfide therein; conveying the residual gas to an ammonia absorption tower to react to generate ammonia water for recycling; and (3) discharging the residual gas after ammonia recovery from the top of the ammonia absorption tower for recovery, and using the residual gas as fuel gas (which can provide a heat source for an aluminum ash dryer).
The system and the method realize the complete recovery of resources in the aluminum ash, have no resource waste and no waste, realize the system circulation in the whole process, have safe and efficient recovery process, are easy to operate and have good social and economic benefits.
Claims (10)
1. The utility model provides an aluminium ash recovery processing system, its characterized in that, this system includes aluminium ash screening processing system, the aluminium ash reaction system who is connected with aluminium ash screening processing system, the reaction material separation drying system who is connected with aluminium ash reaction system, the finished product storage system who is connected with reaction material separation drying system.
2. The treatment system of claim 1, wherein the aluminum ash screening treatment system comprises a blanking hopper, a lifting machine connected with a discharge port of the blanking hopper, a raw material bin connected with a discharge port of the lifting machine, a conveying belt positioned right below an outlet of the raw material bin, a ball mill connected with a discharge end of the conveying belt, the lifting machine connected with the ball mill, and a rolling screen connected with the lifting machine, wherein the rolling screen is respectively connected with the magnetic separator, the 60-80 mesh particle storage tank and the less than 80 mesh particle storage tank; the discharge port of the magnetic separator is connected with an aluminum particle storage tank, the 60-80-mesh particle storage tank is connected with a ball mill through a material pipeline, a screw conveyor is arranged right below the discharge port of the particle storage tank smaller than 80 meshes, and the material is conveyed to an aluminum ash reaction system through the discharge port of the screw conveyor;
the aluminum ash screening treatment system also comprises a plurality of dust collecting pipelines and a bag-type dust collector connected with the outlets of the collecting pipelines; the plurality of collecting pipelines are respectively used for collecting dust in the blanking hopper, the raw material bin, the ball mill, the 60-80 mesh particle storage tank and the particle storage tank smaller than 80 mesh, and then the collected dust is conveyed to the particle storage tank smaller than 80 mesh through the bag-type dust remover.
3. The treatment system according to claim 1, wherein the aluminum ash reaction system comprises a stirring tank, a slurry pump connected with the stirring tank, and a reaction tank connected with the slurry pump; a first gas outlet at the upper end of the stirring tank and a first gas outlet at the upper end of the reaction tank are both connected with a first water-sealed tank, a gas outlet of the first water-sealed tank is communicated with a concentrated ammonia device, a second gas outlet at the upper end of the reaction tank is also connected with a second water-sealed tank, the second water-sealed tank is connected with a dilute ammonia device, and a material outlet at the bottom end of the reaction tank is communicated with a reaction material separation and drying system through a material pipeline;
preferably, the aluminum ash reaction system further comprises an emergency treatment pool, wherein an inlet of the emergency treatment pool is connected with a discharge port at the bottom end of the reaction tank, and an outlet of the emergency treatment pool is connected with the stirring tank.
4. The processing system of claim 3, wherein the aluminum ash reaction system further comprises a nitrogen storage tank, and the nitrogen storage tank passes through the stirring tank and the reaction tank respectively through gas pipelines.
5. The treatment system of claim 3, wherein the dilute ammonia device comprises a washing tower connected with the aluminum ash reaction system, a discharge port at the bottom end of the washing tower is communicated with an intermediate storage tank, the intermediate storage tank is communicated with a discharge pump, and the discharge pump leads to the ammonium sulfate storage tank; the device also comprises a sulfuric acid storage tank which is communicated with an inlet at the upper part of the washing tower through a circulating pump;
the concentrated ammonia device comprises a hydrogen sulfide reactor, a discharge port at the bottom end of the hydrogen sulfide reactor is communicated with a sodium hydrosulfide storage tank, and an outlet at the top end of the hydrogen sulfide reactor is communicated with an ammonia gas absorption tower; the hydrogen sulfide reactor is also provided with a sodium hydroxide solution inlet, and the sodium hydrosulfide storage tank is also communicated with the hydrogen sulfide reactor through a pipeline and a sodium hydrosulfide circulating pump; the ammonia absorption tower is also communicated with the heat exchanger through a material pipeline and a heat exchanger circulating pump.
6. The processing system of claim 1, wherein the reaction material separation and drying system comprises a five-stage vacuum belt conveyor, and a material outlet of the five-stage vacuum belt conveyor is connected with an aluminum ash dryer; a liquid outlet of a mother liquid area of the five-section vacuum belt conveyor is communicated with a mother liquid storage tank, a first-stage spraying area is communicated with a first-stage spraying area washing liquid storage tank, a second-stage spraying area is communicated with a second-stage spraying area washing liquid storage tank, a third-stage spraying area is communicated with a third-stage spraying area washing liquid storage tank, and a fourth-stage spraying area and a drying area are communicated with a fourth-stage spraying area washing liquid storage tank; an outlet of the mother liquor storage tank is communicated with a precipitation tank, an outlet of the precipitation tank is communicated with a strong brine tank, and the strong brine tank is communicated with a strong brine evaporation and crystallization system; the first-stage spraying area washing liquid storage tank and the third-stage spraying area washing liquid storage tank are communicated with the saline water mixing tank;
the second-stage spraying area cleaning solution storage tank and the fourth-stage spraying area cleaning solution storage tank are communicated with a spraying device of the five-section vacuum belt conveyor through a conveying pipeline; the settling tank is also communicated with a feed inlet of the five-section vacuum belt conveyor through a material pipeline.
7. The method for treating aluminum ash by using the aluminum ash recycling system as recited in any one of claims 1 to 6, comprising the steps of:
collecting aluminum ash, and performing ball milling and screening treatment;
the particles with the particle size of less than 80 meshes obtained by screening are placed in an aluminum ash reaction system for reaction;
separating and drying the solid-liquid material obtained by the reaction to obtain a finished product;
and conveying the mixed gas obtained by the reaction to an ammonia gas treatment device for treatment, and taking the residual gas as a drying heat source.
8. The method for treating the aluminum ash according to claim 7, wherein the reaction in the aluminum ash reaction system is as follows: firstly, introducing inert gas into an aluminum ash reaction system to discharge air in the reaction system, then uniformly mixing aluminum ash particles with a particle size of less than 80 meshes and a sodium hydroxide aqueous solution in the aluminum ash reaction system, and reacting for 8-10 hours at the temperature of 80-120 ℃;
preferably, the mass ratio of the aluminum ash to the sodium hydroxide is 100: and 5, the mass fraction of the sodium hydroxide solution is 32%.
9. The method for treating aluminum ash according to claim 7, wherein the solid-liquid material separation is performed by a five-stage vacuum belt conveyor.
10. The method for treating aluminum ash as claimed in claim 7, wherein the moisture content of the solid material separated by the five-stage vacuum belt conveyor is 25-35%, the drying is performed in an aluminum ash dryer at a temperature of 300 ℃ and 600 ℃ until the moisture content is less than 1%.
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