CN115351046A - Aluminum ash harmless and recycling treatment system and operation regulation and control method - Google Patents
Aluminum ash harmless and recycling treatment system and operation regulation and control method Download PDFInfo
- Publication number
- CN115351046A CN115351046A CN202211115430.9A CN202211115430A CN115351046A CN 115351046 A CN115351046 A CN 115351046A CN 202211115430 A CN202211115430 A CN 202211115430A CN 115351046 A CN115351046 A CN 115351046A
- Authority
- CN
- China
- Prior art keywords
- aluminum ash
- reaction kettle
- ammonia
- aluminum
- ash
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 229910052782 aluminium Inorganic materials 0.000 title claims abstract description 180
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 title claims abstract description 172
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000004064 recycling Methods 0.000 title claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 96
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 88
- 239000000463 material Substances 0.000 claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 238000011084 recovery Methods 0.000 claims abstract description 35
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 33
- 239000007787 solid Substances 0.000 claims abstract description 28
- 238000005406 washing Methods 0.000 claims abstract description 24
- 238000002386 leaching Methods 0.000 claims abstract description 21
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 19
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 15
- 239000003513 alkali Substances 0.000 claims description 41
- 238000003860 storage Methods 0.000 claims description 29
- 239000007788 liquid Substances 0.000 claims description 27
- 238000002156 mixing Methods 0.000 claims description 21
- 238000010517 secondary reaction Methods 0.000 claims description 17
- 238000003828 vacuum filtration Methods 0.000 claims description 16
- 238000001914 filtration Methods 0.000 claims description 14
- 239000004411 aluminium Substances 0.000 claims description 13
- 239000012267 brine Substances 0.000 claims description 13
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 11
- 238000012216 screening Methods 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 8
- 239000012065 filter cake Substances 0.000 claims description 7
- 239000002904 solvent Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 4
- 238000000227 grinding Methods 0.000 claims description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 60
- 239000007789 gas Substances 0.000 abstract description 33
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 30
- 229910052751 metal Inorganic materials 0.000 abstract description 6
- 239000002184 metal Substances 0.000 abstract description 6
- 238000004134 energy conservation Methods 0.000 abstract description 3
- 239000007791 liquid phase Substances 0.000 abstract description 3
- 239000012071 phase Substances 0.000 abstract description 3
- 230000002035 prolonged effect Effects 0.000 abstract description 3
- 230000035484 reaction time Effects 0.000 abstract description 3
- 239000007790 solid phase Substances 0.000 abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 43
- 230000008569 process Effects 0.000 description 8
- 150000003839 salts Chemical class 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 5
- PMHQVHHXPFUNSP-UHFFFAOYSA-M copper(1+);methylsulfanylmethane;bromide Chemical compound Br[Cu].CSC PMHQVHHXPFUNSP-UHFFFAOYSA-M 0.000 description 5
- 239000002689 soil Substances 0.000 description 5
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 4
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 4
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229910052731 fluorine Inorganic materials 0.000 description 4
- 239000011737 fluorine Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000001988 toxicity Effects 0.000 description 4
- 231100000419 toxicity Toxicity 0.000 description 4
- CAVCGVPGBKGDTG-UHFFFAOYSA-N alumanylidynemethyl(alumanylidynemethylalumanylidenemethylidene)alumane Chemical compound [Al]#C[Al]=C=[Al]C#[Al] CAVCGVPGBKGDTG-UHFFFAOYSA-N 0.000 description 3
- 239000002585 base Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 229910018626 Al(OH) Inorganic materials 0.000 description 2
- 229910020068 MgAl Inorganic materials 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 239000004566 building material Substances 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- -1 compound salt Chemical class 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 150000004673 fluoride salts Chemical class 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000011241 protective layer Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 239000011819 refractory material Substances 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 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
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000013401 experimental design Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 150000002222 fluorine compounds Chemical class 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/30—Destroying solid waste or transforming solid waste into something useful or harmless involving mechanical treatment
- B09B3/35—Shredding, crushing or cutting
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/30—Destroying solid waste or transforming solid waste into something useful or harmless involving mechanical treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/70—Chemical treatment, e.g. pH adjustment or oxidation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses an aluminum ash harmless and recycling treatment system, which comprises: the system comprises an aluminum ash pretreatment system, a reaction kettle system, an ammonia recovery system and a water washing system. On the basis of extracting metal aluminum to the maximum extent, dangerous characteristic factors in aluminum ash are treated, active components are deeply dissociated, ammonia water and combustible gas are recovered from a gas phase, solid-phase inertia is converted into a high-aluminum material, and a liquid phase can be evaporated and crystallized subsequently. The aluminum ash wet leaching is divided into two stages, a first-stage reaction kettle and a second-stage reaction kettle corresponding to the reaction kettle system are arranged, the first-stage reaction kettle fully utilizes the exothermic characteristic of reaction, energy conservation and high reaction efficiency are realized, the second-stage reaction kettle carries out the subsequent reaction of the first-stage reaction kettle, the time and the space utilization rate of the first-stage reaction kettle are improved, the reaction time is prolonged, the liquid-solid ratio is adjusted, and the total nitrogen removal rate of the aluminum ash, which is one of key indexes of aluminum ash harmlessness, is particularly ensured to reach more than 90%. The invention also provides an operation regulation and control method of the aluminum ash harmless and recycling treatment system.
Description
Technical Field
The invention relates to the technical field of industrial waste recycling treatment, in particular to an aluminum ash harmless and recycling treatment system and an operation regulation and control method.
Background
With the great development of the aluminum industry, the contradiction of energy and resource shortage is increasingly prominent, and the environmental protection problem is increasingly severe. It is statistically estimated that about 30-50kg of aluminum ash is discharged per 1 ton of aluminum produced and cast. The traditional disposal method is basically landfill or open-air stacking, the disposal measure not only occupies a large amount of land, but also soluble salt contained in the disposal measure and ammonia gas generated by reaction can be transferred under the action of wind blowing, solarization and rain, or volatilize into the atmosphere, or be mixed into rivers along with rainwater, permeate into underground polluted soil and underground water, generate great damage to growth of animals and plants and human bodies, destroy the ecological environment and influence the ecological balance.
According to different aluminum contents, the aluminum ash can be divided into primary aluminum ash and secondary aluminum ash: (1) primary aluminum ash: mainly a mixture of metal aluminum and aluminum oxide, the aluminum content can reach 15 percent to 70 percent, and the aluminum oxide is generated in the processes of electrolyzing original aluminum, casting and the like without adding salt flux and is in a grey white color, also called as aluminum lime; (2) secondary aluminum ash: the mixture resulting after the primary refining of the aluminium ash or alloy is recovered by means of a salt bath treatment and is also called a salt cake as it solidifies into a mass. The main components comprise a small amount of metal aluminum and aluminum oxide and a certain amount of NaCl, KCl and other salts. The content of metallic aluminum is lower than that of primary aluminum ash.
The environmental hazard of the aluminum ash is mainly embodied in the following three points: (1) the leaching toxicity of fluoride in the secondary aluminum ash is beyond the standard, the corrosivity is high, the direct stockpiling can cause the pH value of the surrounding underground water and soil to be increased, and fluorine pollution is caused; (2) the secondary aluminum ash contains aluminum nitride, metallic aluminum, aluminum carbide and the like, can release a large amount of ammonia when meeting water, generates hydrogen, methane and other flammable and explosive gases, pollutes the atmospheric environment and has potential safety hazards; (3) the secondary aluminum ash contains a large amount of soluble salts, and the dissolution, seepage and accumulation can cause soil salinization and water body pollution.
The secondary aluminum ash has low aluminum content, complex impurity components, high treatment cost and difficult comprehensive utilization. At present, secondary aluminum ash generated by most enterprises is mainly subjected to harmless treatment by vehicle outward transportation, and the resource utilization rate is very low.
Disclosure of Invention
The invention aims to provide a harmless and recycling treatment system for aluminum ash and an operation regulation and control method, which are used for treating dangerous characteristic factors in the aluminum ash on the basis of maximally extracting metal aluminum, deeply dissociating active components, recycling ammonia water and combustible gas from a gas phase, converting solid-phase inertia into a high-aluminum material, and subsequently evaporating and crystallizing a liquid phase.
The aluminum ash wet leaching is divided into two stages, a first-stage reaction kettle and a second-stage reaction kettle corresponding to the reaction kettle system are arranged, the first-stage reaction kettle fully utilizes the exothermic characteristic of reaction, energy conservation and high reaction efficiency are realized, the second-stage reaction kettle carries out the subsequent reaction of the first-stage reaction kettle, the time and the space utilization rate of the first-stage reaction kettle are improved, the reaction time is prolonged, the liquid-solid ratio is adjusted, and the total nitrogen removal rate of the aluminum ash, which is one of key indexes of aluminum ash harmlessness, is particularly ensured to reach more than 90%.
To achieve the purpose, the invention adopts the following technical scheme.
An aluminum ash innocent and recycling treatment system comprises: the system comprises an aluminum ash pretreatment system, a reaction kettle system, an ammonia recovery system and a water washing system.
The aluminum ash material pretreatment system comprises an aluminum ash discharging bin, a rotary screen, a fine aluminum ash feeding bin and a ball mill, wherein the aluminum ash discharging bin output end is connected with the input end of the rotary screen through a pipeline, the rotary screen forms two output ends through a two-way material separating valve, and the two output ends are respectively connected with the fine aluminum ash feeding bin input end and the ball mill input end through independent pipelines.
And the output end pipeline of the ball mill is connected with the input end of the aluminum ash blanking bin.
The reation kettle system includes that alkali lye supplies storehouse, aluminium ash alkali lye blending bunker, one-level reation kettle, second grade reation kettle, fine aluminium ash supplies storehouse output pipe connection aluminium ash alkali lye blending bunker input, alkali lye supplies storehouse output pipe connection aluminium ash alkali lye blending bunker input, aluminium ash alkali lye blending bunker output pipe connection one-level reation kettle top material mouth.
And the material port at the bottom of the first-stage reaction kettle is connected with the material port at the top of the second-stage reaction kettle through a pipeline.
The ammonia recovery system comprises a gas buffer tank, an ammonia recovery jet tower set and an ammonia water storage tank, wherein top material openings of a first-stage reaction kettle and a second-stage reaction kettle are respectively connected with an independent air passage through an input end of the gas buffer tank, an output end air passage of the gas buffer tank is connected with an input end of the ammonia recovery jet tower set, a liquid output end pipeline of the ammonia recovery jet tower set is connected with an input end of the ammonia water storage tank, and an air output end air passage of the ammonia recovery jet tower set is connected with an external processing device of a follow-up system.
The washing system includes vacuum filtration belt feeder, strong brine storage tank, second grade reation kettle bottom material mouth pipe connection the vacuum filtration belt feeder input, vacuum filtration belt feeder liquid output end pipe connection the strong brine storage tank, follow-up system's outer storage equipment is connected to vacuum filtration belt feeder filter cake output.
Preferably, the number ratio of the first-stage reaction kettle to the second-stage reaction kettle is 1.
Preferably, the ammonia recovery jet tower set can be composed of a plurality of ammonia recovery jet towers which are repeatedly connected in series.
The invention also provides an operation regulation and control method of the aluminum ash harmless and recycling treatment system, which comprises the following steps.
And step A, in the stage of pretreating and screening the aluminum ash, feeding the aluminum ash into the drum sieve for screening, directly conveying fine aluminum ash under the sieve to the fine aluminum ash feeding bin through a pipeline, feeding coarse aluminum ash on the sieve into the ball mill, grinding the coarse aluminum ash, and feeding the coarse aluminum ash into the drum sieve for secondary screening.
And step B, in the first stage of wet leaching of the aluminum ash, screened fine aluminum ash enters the aluminum ash alkali liquor mixing bin through the fine aluminum ash feeding bin, alkali liquor enters the aluminum ash alkali liquor mixing bin through the alkali liquor feeding bin and is mixed with the fine aluminum ash and then enters the first-stage reaction kettle, water is added into the first-stage reaction kettle, the liquid-solid ratio is adjusted, and the temperature is adjusted.
And step C, performing wet leaching of aluminum ash, wherein the solid-liquid mixture generated in the step B enters a secondary reaction kettle through a material opening at the bottom of the primary reaction kettle, water is added into the secondary reaction kettle, the liquid-solid ratio is adjusted, and the temperature is adjusted.
And D1, an ammonia gas recovery stage, wherein the ammonia-containing gas generated in the step B and the step C independently enters the input end of the gas buffer tank through top material ports of the primary reaction kettle and the secondary reaction kettle respectively, the ammonia-containing gas enters the ammonia gas recovery jet flow tower set from the gas buffer tank, and the ammonia gas is stored in the ammonia water storage tank in an ammonia water form.
And D2, in a water washing stage, enabling the solid-liquid mixture after the reaction in the step C to enter the vacuum filtration belt conveyor through a material port at the bottom of the secondary reaction kettle, completing solid-liquid separation and four times of clean water washing on the vacuum filtration belt conveyor, connecting a liquid output end pipeline of the vacuum filtration belt conveyor with the strong brine storage tank, and enabling a filter cake after filtering and washing to enter subsequent system external storage equipment as a high-aluminum material.
Preferably, the liquid-solid ratio in the step B is 2.
Preferably, the liquid-solid ratio in the step C is 4.
Preferably, the reaction temperature of the step B and the step C is controlled between 70 and 80 ℃.
Preferably, the solvent of the alkali liquor added in the step B is CaO.
Preferably, the added mass fraction of the CaO solvent is greater than or equal to 6%.
The invention has the beneficial effects of.
1. On the basis of maximally extracting metal aluminum, dangerous characteristic factors in aluminum ash are treated, active components are deeply dissociated, ammonia water and combustible gas are recovered from a gas phase, solid-phase inertia is converted into a high-aluminum material, and a liquid phase can be subsequently evaporated and crystallized.
2. The aluminum ash wet leaching is divided into two stages, a first-grade reaction kettle and a second-grade reaction kettle corresponding to the reaction kettle system are arranged, the first-grade reaction kettle fully utilizes the exothermic characteristic of reaction, energy conservation and high reaction efficiency are realized, the second-grade reaction kettle accepts the subsequent reaction of the first-grade reaction kettle, the time and the space utilization rate of the first-grade reaction kettle are improved, the reaction time is prolonged, the liquid-solid ratio is adjusted, and the total nitrogen removal rate of the aluminum ash is ensured to reach more than 90%.
Drawings
FIG. 1 is a process flow diagram of an embodiment of the present invention.
FIG. 2 is a graph of the result of a single-factor experiment for determining the total nitrogen removal rate by the operation control method of the aluminum ash harmless and recycling treatment system.
Wherein, an aluminum ash discharging bin 1; a drum screen 2; a fine aluminum ash feeding bin 4; a ball mill 5; an alkali liquor feeding bin 6; an aluminum ash alkali liquor mixing bin 7; a first-stage reaction kettle 8; a secondary reaction kettle 9; a gas buffer tank 10; an ammonia recovery jet tower set 11; an ammonia storage tank 12; a vacuum filtration belt conveyor 13; a strong brine storage tank 14; two-way material distributing valve 15.
Detailed Description
The technical scheme of the invention is further explained by combining the attached drawings and the detailed implementation mode.
The environmental hazard of the aluminum ash is mainly reflected in the following three points: (1) the leaching toxicity of fluoride in the secondary aluminum ash exceeds the standard, the corrosivity is high, the direct stockpiling can cause the pH value of surrounding underground water and soil to be increased, and fluorine pollution is caused; (2) the secondary aluminum ash contains aluminum nitride, metallic aluminum, aluminum carbide and the like, and can release a large amount of ammonia when meeting water, so that the atmospheric environment is polluted, and potential safety hazards exist; (3) the secondary aluminum ash contains a large amount of soluble salts (chloride salts and fluoride salts), and the dissolution, seepage and accumulation can cause soil salinization and water body pollution.
Therefore, the harmless and resource treatment of fluorine and nitrogen in the secondary aluminum ash is realized, so that the fluorine and nitrogen are converted into usable substances, or at least stably exist (ammonia gas is not released to the outside, fluoride, chloride and fluoride are not leached out), which is the core target of the harmless and resource treatment of the aluminum ash.
The invention adopts a wet leaching process, and can realize the high-efficiency hydrolysis of active components such as metal aluminum, aluminum carbide, aluminum nitride and the like and the quick leaching of soluble salt by efficiently strengthening continuous multi-stage reaction. Ammonia gas released by decomposition is absorbed to prepare ammonia water with the concentration of about 9%, and combustible gas such as hydrogen, methane and the like is collected and sold as a product; the strong brine can be made into compound salt by evaporation and crystallization, and the inert oxide is made into the alumina content by filtration, washing and drying>70 percent of high-aluminum material. The main component of the high-aluminum material is Al 2 O 3 、CaAl 2 O 4 、MgAl 2 O 4 、Al(OH) 3 Etc. to convert into dry Al 2 O 3 Content (c) of>70 percent, the high-aluminum material has no reactivity and leaching toxicity, meets the requirements of common industry on solid wastes, can be used as a substitute raw material of products such as ceramics, refractory materials, metallurgical auxiliary materials, building materials and the like, widens the resource utilization channel of the products, and realizes the value-added utilization of the aluminum ash.
The main reaction principle.
Al+H 2 O + alkali → Al (OH) 3 +H 2 ↑。
Al 4 C 3 +H 2 O + base → Al (OH) 3 +CH 4 ↑。
AlN+H 2 O + alkali → Al (OH) 3 +NH 3 ↑。
HF + base → poorly soluble fluoride salt + H 2 0。
In order to achieve full resource utilization of the wet leaching process, condition factors (liquid-solid ratio, temperature, time and water washing agent) having potential influence on the secondary aluminum ash wet leaching process are tested according to a single-factor experimental design rule.
As shown in fig. 2, the effect of different liquid-solid ratios on secondary aluminum ash nitrogen content and total nitrogen removal is shown in fig. 2. According to the detection result, the total nitrogen removal rate is 76.22% -84.76%, the liquid-solid ratio is increased from 3 to 7, the total nitrogen removal rate is increased by 8.54%, and the increase degree is small. And improve the liquid-solid ratio and can lead to the violent intensity reduction of wet process leaching reaction, in order to compromise reaction efficiency, utilize and release heat, guarantee that total nitrogen is got rid of, aluminium ash innocent treatment and resourceful treatment system adopt one, the second grade reation kettle arranges, the one-level reation kettle liquid-solid ratio is relatively low, improve reaction efficiency and can utilize and release heat to reach energy-conserving effect, the second grade reation kettle liquid-solid ratio is relatively high, according to the figure 2 result, can better improve total nitrogen clearance, and the design of second grade reation kettle vacates the space for the one-level reation kettle, be favorable to continuous processing.
As can be seen from FIG. 2, the effect of the water wash temperature on the total nitrogen removal is significant. At 40 ℃, the total nitrogen removal rate is only 64.94%; at 80 ℃, the nitrogen content removal rate reaches 85.37 percent. The higher the removal rate of nitrogen content with the increase of temperature, the main reason is that under the alkaline solution environment, the increase of the solution temperature is beneficial to removing the protective layer on the surface of the aluminum nitride and quickening the reaction rate of the aluminum nitride. So, the temperature regulation is all needed to first, second grade reation kettle for this reason, because the reaction is violent relatively in the one-level reation kettle, has produced a large amount of heats, so the one-level reation kettle only need heat a little can satisfy preferred temperature, and second grade reation kettle can be with the help of self exothermic less.
The results of the water washing time on the total nitrogen removal of the aluminum ash are shown in FIG. 2. It can be seen from the graph that as the water wash time increases, the total nitrogen removal increases by 7.92%, which is less than 20.43% when the water wash temperature is changed, and slightly less than 8.54% when the liquid-solid ratio is changed. Meanwhile, it was found that a small amount of water loss occurred in the samples with the increase of time during the experiment. Since the total nitrogen removal rate tends to decrease with decreasing liquid-solid ratio, the total nitrogen removal rate after 3 hours is reduced by 1.83% compared to 2 hours. Therefore, 2 h was chosen as the optimum water wash time.
As shown in fig. 2, the salts in the secondary aluminum ash are mainly sodium salts, and the secondary aluminum ash contains fluorides, which have important influence on the safe disposal of the secondary aluminum ash. Therefore, four kinds of water-washing agents (CaO, ca (OH)) were selected 2 、NaOH、Na 2 CO 3 ) The water wash experiments were performed and the total nitrogen removal results are shown in figure 2. As can be seen from the results, the total nitrogen removal increased gradually with increasing concentrations of the different water washes. Wherein, ca (OH) 2 The total nitrogen removal rate is lowest, and is only 79.27 at the highest; the highest total nitrogen removal rate of NaOH can reach 92.27%. Secondly, the total nitrogen removal rate difference of NaOH is small and is 4.47%; ca (OH) 2 The total nitrogen removal was most fluctuating, with a difference of 22.88%. The total nitrogen removal effectiveness of the four water washes is arranged as: naOH>CaO>Na 2 CO 3 >Ca(OH) 2 . The main reason for this is that NaOH is a strong base, and has a higher solubility in water than the other three water-washing agents, and can form more OH in aqueous solution - Reacting with nitrogen element in the secondary aluminum ash. In the reaction process, the reaction intensity of NaOH is higher, the reaction of CaO is milder, and the cost of CaO is lower than that of NaOH in industry. In summary, caO is selected as the optimal water scrubbing agent, and when the input amount of CaO is greater than or equal to 6%, the total nitrogen removal rate is in a stable state.
According to the analysis of the results in fig. 2, the optimization of the condition factors (liquid-solid ratio, temperature, time and water washing agent) with potential influence is obtained for the full resource utilization of the wet leaching process. With the method as a guide, the technical scheme of the aluminum ash harmless and recycling treatment system is obtained.
An aluminum ash harmless and resource treatment system comprises: the system comprises an aluminum ash pretreatment system, a reaction kettle system, an ammonia gas recovery system and a water washing system.
The aluminum ash material pretreatment system comprises an aluminum ash discharging bin 1, a rotary screen 2, a fine aluminum ash feeding bin 4 and a ball mill 5, wherein an output end of the aluminum ash discharging bin 1 is connected with an input end of the rotary screen 2 through a pipeline, the rotary screen 2 forms two output ends through a two-way material distributing valve 15, and the two output ends are respectively connected with the input end of the fine aluminum ash feeding bin 4 and the input end of the ball mill 5 through independent pipelines.
And the output end of the ball mill 5 is connected with the input end of the aluminum ash discharging bin 1 through a pipeline.
The reation kettle system includes that alkali lye supplies storehouse 6, aluminium ash alkali lye blending bunker 7, one-level reation kettle 8, second grade reation kettle 9, 4 output end pipe connections in thin aluminium ash supplies storehouse 7 input ends of aluminium ash alkali lye blending bunker, 6 output end pipe connections in alkali lye supply bunker 7 input ends of aluminium ash alkali lye blending bunker, 7 output end pipe connections in aluminium ash alkali lye blending bunker 8 top material mouths.
And the bottom material port pipeline of the first-stage reaction kettle 8 is connected with the top material port of the second-stage reaction kettle 9.
The ammonia gas recovery system comprises a gas buffer tank 10, an ammonia gas recovery jet flow tower set 11 and an ammonia water storage tank 12, top material ports of a first-stage reaction kettle 8 and a second-stage reaction kettle 9 are respectively connected with an independent air passage at the input end of the gas buffer tank 12, and the gas buffer tank 12 mainly acts to homogenize gas production. Because the gas yield of chemical reaction has certain fluctuation, has had gas buffer tank 12, can suitable gas yield carry out the crest of a wave and trough and adjust, gas buffer tank 12 output gas flue is connected 11 input ends of ammonia recovery efflux tower system, 11 liquid output end pipe connections of ammonia recovery efflux tower system 11 liquid output end pipe connection 12 input ends of aqueous ammonia storage tank, the outer treatment facility of follow-up system is connected to 11 gas output end gas flue of ammonia recovery efflux tower system.
The washing system includes vacuum filtration belt feeder 13, strong brine storage tank 14, 9 bottom material mouths pipe connection of second grade reation kettle the 13 inputs of vacuum filtration belt feeder, 13 liquid output end pipe connection of vacuum filtration belt feeder the strong brine storage tank 14, the outer storage facilities of follow-up system is connected to 13 filter cake outputs of vacuum filtration belt feeder.
Preferably, the number ratio of the first-stage reaction kettle 8 to the second-stage reaction kettle 9 is 1.
Preferably, the ammonia gas recovery jet tower set 11 may be composed of a plurality of ammonia gas recovery jet towers which are repeatedly connected in series. The ammonia recovery jet tower set 11 formed by repeatedly connecting the four ammonia recovery jet towers in series can realize the production of 9% ammonia water.
The invention also provides an operation regulation and control method of the aluminum ash harmless and recycling treatment system, which comprises the following steps.
Step A, in the stage of pretreating and screening the aluminum ash, the aluminum ash enters the drum screen 2 for screening, fine aluminum ash under the screen is directly conveyed to the fine aluminum ash feeding bin 4 through a pipeline, coarse aluminum ash on the screen enters the ball mill 5, and the coarse aluminum ash enters the drum screen 2 again for screening after being ground. The small-granularity aluminum ash is beneficial to improving the reaction speed of the wet leaching process, and the larger reaction surface area reduces the influence of the formed aluminum oxide or aluminum hydroxide protective layer on the wet leaching reaction.
And step B, in the first stage of wet leaching of the aluminum ash, screened fine aluminum ash enters the aluminum ash alkali liquor mixing bin 7 through the fine aluminum ash feeding bin 4, alkali liquor enters the aluminum ash alkali liquor mixing bin 7 through the alkali liquor feeding bin 6 and is mixed with the fine aluminum ash to enter the first-stage reaction kettle 8, water is added into the first-stage reaction kettle 8, the liquid-solid ratio is adjusted, and the temperature is adjusted. The solid ratio of the first-stage reaction kettle liquid 8 is relatively low, the reaction efficiency is improved, and the energy-saving effect can be achieved by utilizing heat release.
And step C, performing wet leaching of aluminum ash, wherein the solid-liquid mixture generated in the step B enters a secondary reaction kettle 9 through a material opening at the bottom of the primary reaction kettle 8, water is added into the secondary reaction kettle 9, the liquid-solid ratio is adjusted, and the temperature is adjusted. The liquid-solid ratio of the second-stage reaction kettle 9 is relatively high, the total nitrogen removal rate can be better improved according to the result shown in fig. 2, and the design of the second-stage reaction kettle 9 vacates a space for the first-stage reaction kettle 8, which is favorable for continuous treatment.
And D1, in an ammonia gas recovery stage, the ammonia-containing gas generated in the step B and the step C independently enters the input end of the gas buffer tank 10 through top material openings of the primary reaction kettle 8 and the secondary reaction kettle 9 respectively, the ammonia-containing gas enters the ammonia gas recovery jet flow tower set 11 through the gas buffer tank 10, and the ammonia gas is stored in an ammonia water form to the ammonia water storage tank 12.
And D2, a water washing stage, wherein the solid-liquid mixture after the reaction in the step C enters the vacuum filtering belt conveyor 13 through a material port at the bottom of the secondary reaction kettle 9, the vacuum filtering belt conveyor 13 finishes solid-liquid separation and four times of clear water washing, a liquid output end of the vacuum filtering belt conveyor 13 is connected with the concentrated brine storage tank 14 through a pipeline, and filter cakes after filtering and washing enter subsequent system external storage equipment as high-aluminum materials. The main component of the high-aluminum material is Al 2 O 3 、CaAl 2 O 4 、MgAl 2 O 4 、Al(OH) 3 Etc. converting to dry Al 2 O 3 Content (wt.)>70% higherThe aluminum material has no reactivity and leaching toxicity, meets the general industrial solid waste requirement, and can be used as a substitute raw material of products such as ceramics, refractory materials, metallurgical auxiliary materials, building materials and the like. The concentrated brine can be prepared into compound salt through evaporation and crystallization.
Preferably, the liquid-solid ratio in the step B is 2.
Preferably, the liquid-solid ratio in the step C is 4.
Preferably, the reaction temperature of the step B and the step C is controlled between 70 and 80 ℃.
Preferably, the solvent of the alkali liquor added in the step B is CaO.
Preferably, the added mass fraction of the CaO solvent is greater than or equal to 6%.
Example (b): and the secondary aluminum ash enters the aluminum ash feeding bin 1 from the outside, then enters the drum screen 2 for screening, the fine aluminum ash under the screen is directly conveyed to the fine aluminum ash feeding bin 4 through a pipeline, the coarse aluminum ash on the screen enters the ball mill 5, the coarse aluminum ash enters the drum screen 2 again for screening after grinding, and finally all the aluminum ash is ground until all the fine aluminum ash enters the fine aluminum ash feeding bin 4. Then the mixture enters an aluminum ash alkali liquid mixing bin 7, caO alkali liquid with the mass fraction of 6% is added and enters the aluminum ash alkali liquid mixing bin 7 through an alkali liquid feeding bin 6 to be mixed with fine aluminum ash and then enters a first-stage reaction kettle 8, water is added into the first-stage reaction kettle 8, the liquid-solid ratio is adjusted to be 2. And then the mixture enters a secondary reaction kettle 9, water is added into the secondary reaction kettle 9, the liquid-solid ratio is adjusted to be 4. The gaseous passing through of the ammonia that contains that one-level reation kettle 8, second grade reation kettle 9 produced the top material mouth of one-level reation kettle 8, second grade reation kettle 9 independently gets into respectively 10 input ends of gas buffer tank, contain ammonia gas by gas buffer tank 10 gets into the ammonia recovery efflux tower system 11, ammonia store extremely with the aqueous ammonia form aqueous ammonia storage tank 12. And a solid-liquid mixture after the reaction of the second-stage reaction kettle 9 enters the vacuum filtering belt conveyor 13 through a bottom material port of the second-stage reaction kettle 9, the vacuum filtering belt conveyor 13 completes solid-liquid separation and four times of clean water washing, a liquid output end pipeline of the vacuum filtering belt conveyor 13 is connected with the strong brine storage tank 14, and a filter cake after filtering and washing enters subsequent system external storage equipment as a high-aluminum material.
The technical principles of the present invention have been described above with reference to specific embodiments. The description is made for the purpose of illustrating the principles of the invention and should not be construed in any way as limiting the scope of the invention. Based on the explanations herein, those skilled in the art will be able to conceive of other embodiments of the present invention without inventive effort, which would fall within the scope of the present invention.
Claims (9)
1. The utility model provides an aluminium ash innocent treatment and resourceful treatment system which characterized in that includes: the system comprises an aluminum ash pretreatment system, a reaction kettle system, an ammonia recovery system and a water washing system;
the aluminum ash pretreatment system comprises an aluminum ash discharging bin, a rotary screen, a fine aluminum ash feeding bin and a ball mill, wherein an output end of the aluminum ash discharging bin is connected with an input end of the rotary screen through a pipeline, the rotary screen forms two output ends through a two-way material separating valve, and the two output ends are respectively connected with an input end of the fine aluminum ash feeding bin and an input end of the ball mill through independent pipelines;
the output end pipeline of the ball mill is connected with the input end of the aluminum ash blanking bin;
the reaction kettle system comprises an alkali liquor feeding bin, an aluminum ash alkali liquor mixing bin, a first-stage reaction kettle and a second-stage reaction kettle, wherein the output end of the fine aluminum ash feeding bin is connected with the input end of the aluminum ash alkali liquor mixing bin through a pipeline, the output end of the alkali liquor feeding bin is connected with the input end of the aluminum ash alkali liquor mixing bin through a pipeline, and the output end of the aluminum ash alkali liquor mixing bin is connected with a material port at the top of the first-stage reaction kettle through a pipeline;
the material port at the bottom of the primary reaction kettle is connected with the material port at the top of the secondary reaction kettle through a pipeline;
the ammonia recovery system comprises a gas buffer tank, an ammonia recovery jet flow tower set and an ammonia water storage tank, wherein top material openings of a primary reaction kettle and a secondary reaction kettle are respectively and independently connected with an input end of the gas buffer tank through an air passage, an output end of the gas buffer tank is connected with an input end of the ammonia recovery jet flow tower set through an air passage, a liquid output end of the ammonia recovery jet flow tower set is connected with an input end of the ammonia water storage tank through a pipeline, and an air passage at a gas output end of the ammonia recovery jet flow tower set is connected with subsequent system external treatment equipment;
the washing system includes vacuum filtration belt feeder, strong brine storage tank, second grade reation kettle bottom material mouth pipe connection the vacuum filtration belt feeder input, vacuum filtration belt feeder liquid output end pipe connection the strong brine storage tank, follow-up system's outer storage equipment is connected to vacuum filtration belt feeder filter cake output.
2. The aluminum ash harmless and resource treatment system according to claim 1, wherein the number ratio of the first-stage reaction kettle to the second-stage reaction kettle is 1.
3. The aluminum ash harmless and recycling treatment system according to claim 1, wherein said ammonia gas recovery jet tower set can be composed of a plurality of said ammonia gas recovery jet towers which are repeatedly connected in series.
4. An operation control method using the aluminum ash harmless and recycling treatment system as set forth in any one of claims 1 to 3, characterized by comprising the steps of:
step A, in an aluminum ash pretreatment screening stage, feeding aluminum ash into the drum screen for screening, directly conveying fine aluminum ash under the screen to the fine aluminum ash feeding bin through a pipeline, feeding coarse aluminum ash on the screen into the ball mill, grinding the coarse aluminum ash, and feeding the coarse aluminum ash into the drum screen again for screening;
b, in the first stage of wet leaching of the aluminum ash, screened fine aluminum ash enters the aluminum ash alkali liquor mixing bin through the fine aluminum ash feeding bin, alkali liquor enters the aluminum ash alkali liquor mixing bin through the alkali liquor feeding bin and is mixed with the fine aluminum ash and then enters the first-stage reaction kettle, water is added into the first-stage reaction kettle, the liquid-solid ratio is adjusted, and the temperature is adjusted;
step C, performing wet leaching of aluminum ash, wherein the solid-liquid mixture generated in the step B enters a secondary reaction kettle through a material port at the bottom of the primary reaction kettle, water is added into the secondary reaction kettle, the liquid-solid ratio is adjusted, and the temperature is adjusted;
step D1, in an ammonia gas recovery stage, the ammonia-containing gas generated in the step B and the step C independently enters the input end of the gas buffer tank through top material openings of the primary reaction kettle and the secondary reaction kettle respectively, the ammonia-containing gas enters the ammonia gas recovery jet flow tower set from the gas buffer tank, and the ammonia gas is stored to the ammonia water storage tank in an ammonia water form;
and D2, a water washing stage, wherein the solid-liquid mixture after the reaction in the step C enters the vacuum filtering belt conveyor through a material port at the bottom of the secondary reaction kettle, the vacuum filtering belt conveyor finishes solid-liquid separation and four times of clear water washing, the liquid output end of the vacuum filtering belt conveyor is connected with the strong brine storage tank through a pipeline, and filter cakes after filtering and washing enter subsequent system external storage equipment as high-aluminum materials.
5. The operation control method of the aluminum ash harmless and recycling treatment system according to claim 4, wherein the liquid-solid ratio in the step B is 2.
6. The operation control method of the aluminum ash harmless and recycling treatment system according to claim 4, wherein the liquid-solid ratio in the step C is 4.
7. The operation control method for the aluminum ash harmless and recycling treatment system according to claim 4, wherein the reaction temperature of the step B and the step C is controlled to be 70-80 ℃.
8. The method for controlling the operation of the aluminum ash harmless and recycling treatment system according to claim 4, wherein the solvent of the alkali liquor added in the step B is CaO.
9. The operation regulation and control method of the aluminum ash harmless and recycling treatment system according to claim 8, wherein the added mass fraction of the CaO solvent is greater than or equal to 6%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211115430.9A CN115351046A (en) | 2022-09-14 | 2022-09-14 | Aluminum ash harmless and recycling treatment system and operation regulation and control method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211115430.9A CN115351046A (en) | 2022-09-14 | 2022-09-14 | Aluminum ash harmless and recycling treatment system and operation regulation and control method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115351046A true CN115351046A (en) | 2022-11-18 |
Family
ID=84006560
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211115430.9A Pending CN115351046A (en) | 2022-09-14 | 2022-09-14 | Aluminum ash harmless and recycling treatment system and operation regulation and control method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115351046A (en) |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11189410A (en) * | 1997-12-25 | 1999-07-13 | Taiheiyo Cement Corp | Production of hauyne |
| US20120289396A1 (en) * | 2011-05-12 | 2012-11-15 | Atomic Energy Council-Institute Of Nuclear Energy Research | Method for Producing a Refractory Material from Aluminum residues |
| CN109746249A (en) * | 2019-01-22 | 2019-05-14 | 湖南绿脉环保科技有限公司 | A kind of aluminium ash deamination method |
| CN111167830A (en) * | 2019-12-30 | 2020-05-19 | 兴化市永泰铝业有限公司 | Comprehensive treatment and utilization process of secondary aluminum ash |
| CN111874931A (en) * | 2020-07-23 | 2020-11-03 | 辽宁忠旺集团有限公司 | Harmless treatment process for secondary aluminum ash |
| CN111994928A (en) * | 2020-08-29 | 2020-11-27 | 河南明泰科技发展有限公司 | Aluminum ash recycling system and processing method thereof |
| CN212597852U (en) * | 2020-04-03 | 2021-02-26 | 河南绿泽环保科技有限公司 | Explosion-proof type aluminum ash innocent treatment system |
| CN215713433U (en) * | 2021-09-26 | 2022-02-01 | 北京科技大学 | System for preparing aluminum alloy |
| CN216155494U (en) * | 2021-07-28 | 2022-04-01 | 杭州逐真科技有限公司 | System for harmless and full element resource of secondary aluminium ash |
| CN114671636A (en) * | 2022-05-07 | 2022-06-28 | 济南大学 | Method for harmless treatment of secondary aluminum ash by alkalescent water washing |
| CN217251528U (en) * | 2022-04-19 | 2022-08-23 | 巩义市鑫华机械厂 | Secondary aluminum ash hydrolysis gas solid resource utilization device |
| CN115028151A (en) * | 2022-06-27 | 2022-09-09 | 中国铝业股份有限公司 | Method for comprehensively utilizing secondary aluminum ash |
-
2022
- 2022-09-14 CN CN202211115430.9A patent/CN115351046A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11189410A (en) * | 1997-12-25 | 1999-07-13 | Taiheiyo Cement Corp | Production of hauyne |
| US20120289396A1 (en) * | 2011-05-12 | 2012-11-15 | Atomic Energy Council-Institute Of Nuclear Energy Research | Method for Producing a Refractory Material from Aluminum residues |
| CN109746249A (en) * | 2019-01-22 | 2019-05-14 | 湖南绿脉环保科技有限公司 | A kind of aluminium ash deamination method |
| CN111167830A (en) * | 2019-12-30 | 2020-05-19 | 兴化市永泰铝业有限公司 | Comprehensive treatment and utilization process of secondary aluminum ash |
| CN212597852U (en) * | 2020-04-03 | 2021-02-26 | 河南绿泽环保科技有限公司 | Explosion-proof type aluminum ash innocent treatment system |
| CN111874931A (en) * | 2020-07-23 | 2020-11-03 | 辽宁忠旺集团有限公司 | Harmless treatment process for secondary aluminum ash |
| CN111994928A (en) * | 2020-08-29 | 2020-11-27 | 河南明泰科技发展有限公司 | Aluminum ash recycling system and processing method thereof |
| CN216155494U (en) * | 2021-07-28 | 2022-04-01 | 杭州逐真科技有限公司 | System for harmless and full element resource of secondary aluminium ash |
| CN215713433U (en) * | 2021-09-26 | 2022-02-01 | 北京科技大学 | System for preparing aluminum alloy |
| CN217251528U (en) * | 2022-04-19 | 2022-08-23 | 巩义市鑫华机械厂 | Secondary aluminum ash hydrolysis gas solid resource utilization device |
| CN114671636A (en) * | 2022-05-07 | 2022-06-28 | 济南大学 | Method for harmless treatment of secondary aluminum ash by alkalescent water washing |
| CN115028151A (en) * | 2022-06-27 | 2022-09-09 | 中国铝业股份有限公司 | Method for comprehensively utilizing secondary aluminum ash |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113426796B (en) | Electrolytic aluminum overhaul slag, method for recycling overhaul slag leachate and application method of recycled materials | |
| CN110217810B (en) | Method for efficiently recovering valuable elements in aluminum ash | |
| CN113955954B (en) | Carbon dioxide high-pressure leaching decalcification process for fly ash | |
| CN101475194B (en) | Method for recycling ammonia from low concentration ammonium chloride wastewater | |
| JP2000512687A (en) | Treatment of fly ash / APC residue including lead salt recovery | |
| CN114892010B (en) | Secondary aluminum ash treatment method for enhanced denitrification and desalination | |
| CN113941580B (en) | Multistage reverse pulping fly ash water washing process | |
| CN113955889A (en) | Resource recovery process of fly ash washing liquid | |
| CN109821857A (en) | A kind of Innocent treatment method of electrolytic manganese slag and its device | |
| CN104762478A (en) | Method for production and recovery of precious metals on the basis of pickling sludge | |
| CN209886372U (en) | Industrial waste salt treatment device | |
| CN114147047B (en) | Resource recovery process for fly ash water-washing slag | |
| CN109465277A (en) | A kind of daily-life garbage without environmental pollution recycling treatment system utilized with effluent cycle | |
| CN115351046A (en) | Aluminum ash harmless and recycling treatment system and operation regulation and control method | |
| CN115155279B (en) | Flue gas deacidification coupling fly ash treatment method | |
| CN102153127B (en) | Method for preparing gypsum by removing sulfate radicals from mineral salts with waste distillation liquid from ammonia alkali factory | |
| CN111994928A (en) | Aluminum ash recycling system and processing method thereof | |
| CN115974184A (en) | Preparation method and application of water purifying agent produced by using aluminum ash | |
| CN215713433U (en) | System for preparing aluminum alloy | |
| CN212450663U (en) | Aluminum ash recovery processing system | |
| CN109761514B (en) | Beryllium slag detoxification and cement kiln cooperative recycling treatment system and process | |
| CN108559851B (en) | System and method for cooperatively disposing rare earth polishing powder waste by cement kiln | |
| CN109437316A (en) | A kind of preparation method of nanometer level superfine iron zinc composite oxide material | |
| CN215249605U (en) | System for recovering cryolite by combined treatment of aluminum electrolysis overhaul residues and aluminum ash | |
| CN220970348U (en) | Secondary aluminum ash cooperated waste acid and waste alkali recycling continuous treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20221118 |