CN115228885A - Method for treating fly ash generated by waste incineration - Google Patents
Method for treating fly ash generated by waste incineration Download PDFInfo
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- CN115228885A CN115228885A CN202210733428.1A CN202210733428A CN115228885A CN 115228885 A CN115228885 A CN 115228885A CN 202210733428 A CN202210733428 A CN 202210733428A CN 115228885 A CN115228885 A CN 115228885A
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- fly ash
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- waste liquid
- soluble salt
- filter residue
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- 239000010881 fly ash Substances 0.000 title claims abstract description 99
- 238000000034 method Methods 0.000 title claims abstract description 54
- 238000004056 waste incineration Methods 0.000 title claims abstract description 12
- 150000003839 salts Chemical class 0.000 claims abstract description 95
- 238000005406 washing Methods 0.000 claims abstract description 69
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000007788 liquid Substances 0.000 claims abstract description 63
- 239000002699 waste material Substances 0.000 claims abstract description 62
- 230000008018 melting Effects 0.000 claims abstract description 51
- 238000002844 melting Methods 0.000 claims abstract description 51
- 239000002002 slurry Substances 0.000 claims abstract description 30
- 238000002386 leaching Methods 0.000 claims abstract description 14
- 239000002893 slag Substances 0.000 claims abstract description 14
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 13
- 231100000419 toxicity Toxicity 0.000 claims abstract description 13
- 230000001988 toxicity Effects 0.000 claims abstract description 13
- 238000001704 evaporation Methods 0.000 claims abstract description 12
- 238000001914 filtration Methods 0.000 claims abstract description 9
- 208000005156 Dehydration Diseases 0.000 claims abstract description 8
- 230000018044 dehydration Effects 0.000 claims abstract description 8
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 28
- 239000003546 flue gas Substances 0.000 claims description 28
- 229910001385 heavy metal Inorganic materials 0.000 claims description 25
- 230000008569 process Effects 0.000 claims description 23
- 239000000460 chlorine Substances 0.000 claims description 15
- 229910052801 chlorine Inorganic materials 0.000 claims description 14
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 13
- 150000002500 ions Chemical class 0.000 claims description 9
- 230000009467 reduction Effects 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
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- 239000011707 mineral Substances 0.000 claims description 4
- 238000009388 chemical precipitation Methods 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 238000000108 ultra-filtration Methods 0.000 claims description 3
- 235000002639 sodium chloride Nutrition 0.000 description 77
- 210000002381 plasma Anatomy 0.000 description 37
- 239000011552 falling film Substances 0.000 description 7
- 238000006722 reduction reaction Methods 0.000 description 7
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- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 3
- 235000011941 Tilia x europaea Nutrition 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- -1 chlorine ions Chemical class 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 235000010755 mineral Nutrition 0.000 description 3
- 231100000614 poison Toxicity 0.000 description 3
- 239000001103 potassium chloride Substances 0.000 description 3
- 235000011164 potassium chloride Nutrition 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 239000003440 toxic substance Substances 0.000 description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 229910045601 alloy Inorganic materials 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 229910001424 calcium ion Inorganic materials 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 230000009920 chelation Effects 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 150000002739 metals Chemical group 0.000 description 2
- 239000006060 molten glass Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- LIVNPJMFVYWSIS-UHFFFAOYSA-N silicon monoxide Inorganic materials [Si-]#[O+] LIVNPJMFVYWSIS-UHFFFAOYSA-N 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 229910018557 Si O Inorganic materials 0.000 description 1
- 238000003723 Smelting Methods 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
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000004182 chemical digestion Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000010806 kitchen waste Substances 0.000 description 1
- 229910001338 liquidmetal Inorganic materials 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010128 melt processing Methods 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 231100000783 metal toxicity Toxicity 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000011151 potassium sulphates Nutrition 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229910052604 silicate mineral Inorganic materials 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000012360 testing method Methods 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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/02—Working-up flue dust
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- General Chemical & Material Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Health & Medical Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The application discloses a fly ash treatment method generated by waste incineration, which comprises the following steps: performing water washing pretreatment on fly ash generated by burning garbage to obtain fly ash slurry; washing and filtering the fly ash slurry in sequence to obtain soluble salt waste liquid and filter residue; evaporating the soluble salt waste liquid to obtain industrial salt; and (3) sequentially carrying out dehydration treatment and plasma melting treatment on the filter residue to obtain the glassy state slag with the leaching toxicity reaching the standard. The product leaching toxicity of the application meets the standard, the treatment cost is low, and the stable operation can be realized.
Description
Technical Field
The application relates to the field of fly ash treatment, in particular to a fly ash treatment method generated by waste incineration.
Background
The main treatment mode of the fly ash at present is a fly ash plasma melting treatment technology, and the fly ash treatment capacity is large when the fly ash is subjected to high-temperature plasma melting treatment; the melting point of the soluble salt is extremely low, and the soluble salt is very easy to volatilize and block a rear end flue of the plasma melting furnace and needs to be cleaned regularly; and the volatile soluble salt is washed after the high-temperature melting treatment, so that the plasma melting treatment process is long; the above causes the cost of the plasma fusion treatment process to be high.
Therefore, the prior art has the technical problem of high treatment cost.
Disclosure of Invention
The application mainly aims to provide a method for treating fly ash generated by waste incineration, and aims to solve the technical problem of high treatment cost in the prior art.
In order to achieve the above object, the present application provides a method for treating fly ash generated by burning garbage, the method comprising:
illustratively, the method for treating the fly ash generated by the incineration of the garbage comprises the following steps:
performing water washing pretreatment on fly ash generated by burning garbage to obtain fly ash slurry;
washing and filtering the fly ash slurry in sequence to obtain soluble salt waste liquid and filter residue;
evaporating the soluble salt waste liquid to obtain industrial salt;
and (3) sequentially carrying out dehydration treatment and plasma melting treatment on the filter residue to obtain the glassy state slag with the leaching toxicity reaching the standard.
Illustratively, the washing treatment process employs a multi-stage counter-current washing process, the number of washing stages of which is determined based on the chlorine content in the fly ash slurry.
Illustratively, before the last stage of water washing in the multistage countercurrent water washing process, the soluble salt waste liquid obtained from the last stage of water washing is subjected to water purification treatment and chemical precipitation treatment in sequence to remove mineral ions and heavy metal ions in the soluble salt waste liquid.
Illustratively, the amount of waste salt in the filter residue after dehydration treatment is 2% to 5%.
Illustratively, the step of evaporating the soluble salt waste liquid to obtain industrial salt comprises:
flashing the soluble salt waste liquid to a saturated state to obtain concentrated soluble salt waste liquid;
sequentially cooling, crystallizing and centrifugally dewatering the concentrated soluble salt waste liquid to obtain solid crystalline salt;
the solid crystalline salt is used as industrial salt.
Illustratively, before the step of subjecting the soluble salt waste liquid to evaporation treatment to obtain industrial salt, the method further comprises:
and carrying out chemical conditioning treatment and ultrafiltration treatment on the soluble salt waste liquid to ensure that the hardness of the soluble salt waste liquid is less than 50mg/L and the turbidity is less than 5NTU.
Illustratively, the plasma melting treatment process comprises controlling the retention time of the filter residue in a reduction zone of the plasma melting furnace so as to reduce the heavy metal in the filter residue.
The residence time of the filter residue in the plasma furnace is, for example, 60 to 150 minutes.
Illustratively, flue gas generated in the plasma melting treatment process is treated by flue gas and then is discharged after reaching standards.
Illustratively, the plasma melt processing temperature is 1200 to 1400 degrees celsius.
The application provides a method for treating fly ash generated by waste incineration. Compared with the prior art that the fly ash treatment product has high leaching toxicity, high fly ash treatment cost and unstable operation, the fly ash slurry is sequentially subjected to water washing treatment and filtering treatment to obtain soluble salt waste liquid and filter residue, so that the fly ash can be subjected to reduction treatment before plasma melting treatment; soluble salt water in the fly ash is washed away by water, acid-base balance treatment is not needed to be carried out on filter residues in the plasma melting treatment process, the plasma melting treatment process is optimized, and the treatment cost is reduced; the soluble salt waste liquid is evaporated to obtain industrial salt, so that the recycling of the soluble salt waste liquid is realized, and the treatment cost is further reduced; and (3) sequentially carrying out dehydration treatment and plasma melting treatment on the filter residue to remove toxic substances contained in the filter residue to obtain the glassy slag with the leaching toxicity reaching the standard, and ending the whole process flow. Therefore, the present application can reduce the processing cost.
Drawings
FIG. 1 is a schematic flow chart showing a first embodiment of a method for treating fly ash generated by incineration of garbage according to the present invention;
the implementation, functional features and advantages of the objectives of the present application will be further explained with reference to the accompanying drawings.
Detailed Description
It should be understood that the specific embodiments described herein are merely illustrative of the present application and are not intended to limit the present application.
Referring to fig. 1, fig. 1 is a schematic flow diagram illustrating a first embodiment of a method for treating fly ash generated by burning garbage.
In this embodiment, the method for treating fly ash generated by burning garbage includes the following steps:
step S10, carrying out water washing pretreatment on fly ash generated by waste incineration to obtain fly ash slurry;
in this embodiment, the fly ash generated by burning garbage is mainly composed of SiO, which is an acidic oxide 2 And basic oxide Al 2 O 3 CaO is taken as the main component, and the total proportion is 56 percent; as the flue gas desulfurization is carried out by using a calcium spraying method in the waste incineration process, more Ca is carried in the fly ash, and the melting temperature is increased due to the increase of the Ca content. The Cl content in the waste incineration fly ash reaches 4.88%, chlorine in the fly ash mainly comes from kitchen waste and chloride in plastic bags, and the chloride is decomposed and attached to the fly ash due to low boiling point in the combustion process of the waste, and the fly ash also contains toxic substances such as heavy metals, so that chlorine ions, mineral ions and heavy metal ions in the fly ash generated by waste incineration are mainly removed in the embodiment.
In this embodiment, before the fly ash generated by burning the garbage is subjected to the water washing treatment, if the chlorine content in the fly ash can be determined, the water consumption in the water washing process can be determined according to the chlorine content; but before the fly ash generated by waste incineration is introduced into water washing treatment equipment through a pipeline, the measurement of the chlorine content in the fly ash existing in the form of fine particles is difficult; and the fly ash amount of each batch of water washing treatment is not convenient to determine, therefore, the fly ash generated by the garbage incineration is subjected to water washing pretreatment to obtain fly ash slurry, and the process of the water washing pretreatment is to mix the fly ash and water according to the ratio of 1:10, and uniformly stirring the mixture to be viscous to obtain fly ash slurry, namely measuring the weight of the fly ash slurry, and stopping introducing the fly ash when the weight of the fly ash slurry reaches a preset threshold value.
In the prior art, when the fly ash is subjected to plasma melting treatment, the fly ash exists in the form of fine particles, so that the treatment capacity of the fly ash is large, and the treatment cost is high.
Step S20, sequentially carrying out water washing treatment and filtering treatment on the fly ash slurry to obtain soluble salt waste liquid and filter residue;
in this embodiment, after obtaining the fly ash slurry, detecting the chlorine content in the fly ash slurry, introducing the detected chlorine content into a water washing treatment device, and sequentially performing water washing treatment and filtration treatment on the fly ash slurry to obtain a soluble salt waste liquid and a filter residue.
Specifically, the washing treatment process adopts a multi-stage countercurrent washing process, and the washing process is to wash potassium, sodium, sulfur and chlorine plasmas in the fly ash to separate the plasmas from the fly ash; the washing stage number of the multistage countercurrent washing process is determined based on the chlorine content in the fly ash slurry, and if the measured chlorine content in the fly ash slurry reaches 200-500 milligrams per standard cubic meter, the three-stage countercurrent washing process is adopted.
The fly ash slurry is sequentially subjected to water washing treatment and filtering treatment, and the steps are as follows: introducing the fly ash slurry into a first-stage water washing reactor and a water washing separator for solid-liquid separation to obtain first-stage soluble salt waste liquid and first-stage filter residue, wherein the waste salt content in the first-stage filter residue reaches 12-15%; washing water for storing the first-stage soluble salt waste liquid, and washing filter residues in the next stage; and (3) introducing the first-stage soluble salt waste liquid into a second-stage washing reactor and a second-stage washing separator for second washing and solid-liquid separation to obtain second-stage soluble salt waste liquid and second-stage filter residue, wherein the waste salt content in the second-stage filter residue reaches 4-6%.
And after the second-stage countercurrent washing treatment, introducing the second-stage soluble salt waste liquid into water quality purification treatment equipment, and performing chemical precipitation treatment to remove mineral ions and heavy metal ions in the soluble salt waste liquid so as to achieve the purpose of removing impurities and heavy metal ions in the fly ash slurry.
And (3) introducing the second-stage soluble salt waste liquid subjected to water quality purification treatment into a third-stage washing reactor and a washing separator for third washing and solid-liquid separation to obtain third-stage soluble salt waste liquid and third-stage filter residue. And (4) the waste salt content in the filter residue after the dehydration treatment is 2-5%, and the three-stage countercurrent washing process flow is finished.
During tertiary washing, wash through the external filter residue that the water that leads to produces the washing of last one-level, obtain last one-level soluble salt waste liquid, will last one-level soluble salt waste liquid is as the washing water of last one-level washing, and the soluble salt waste liquid after adopting multistage countercurrent washing water washing technology to handle all is as the washing water of last one-level washing, and concrete step is: firstly, introducing water from the outside in the third stage of countercurrent washing process, and taking soluble salt waste liquid generated by the third stage of countercurrent washing as washing water of the second stage of countercurrent washing; wherein, the water consumption of the external introduced water is determined based on the chlorine content in the fly ash slurry, and the soluble salt waste liquid generated by the soluble salt waste liquid after the second-stage water washing is used as the water for preparing the fly ash slurry before the first-stage water washing; the fly ash slurry is directly subjected to first-stage countercurrent washing after being prepared, the mass loss of the fly ash after the three-stage countercurrent washing is about 40 percent, and soluble salts KCl and CaCl in the fly ash 2 、NaCl、MgCl 2 Are all dissolved in water.
Wherein, the water consumption of the external introduced water can be analyzed by sampling, the chlorine content in the fly ash slurry is measured, and the water consumption is determined according to the measurement result and the slurry ratio of 2-3.
Compared with the fly ash plasma melting treatment process in the prior art, the fly ash is not subjected to reduction treatment, so that the treatment cost is higher; the fly ash contains about 25% of acidic soluble salts such as sodium chloride, potassium chloride, sodium sulfate, potassium sulfate and the like, when the fly ash is subjected to plasma melting treatment, alkaline substances such as calcium oxide are required to be added to adjust the pH value of the fly ash, so that the treatment cost is increased, the melting point of the soluble salts is extremely low, the soluble salts are very easy to volatilize and block a rear end flue of a plasma melting furnace, and the volatilized soluble salts are required to be subjected to water washing treatment after high-temperature melting, so that the treatment process flow is very long, and the treatment cost is increased. Before the fly ash is subjected to plasma melting treatment, the fly ash is washed by water to achieve the purpose of reduction, the treatment cost is reduced, most of soluble salt is washed away in the washing process, a flue at the rear end of a plasma melting furnace is not blocked, the volatile soluble salt does not need to be washed after high-temperature melting, and most of fly ash needs to be pretreated when being subjected to plasma melting treatment at present, the ratio of calcium oxide and silicon dioxide in the fly ash is adjusted to carry out granulation pretreatment on the fly ash.
S30, evaporating the soluble salt waste liquid to obtain industrial salt;
in this embodiment, before the soluble salt waste liquid is subjected to evaporation treatment, chemical conditioning and ultrafiltration treatment need to be performed on the soluble salt waste liquid to meet the conditions for evaporation; adding lime or alkaline water and a flocculating agent into the soluble salt waste liquid for softening, adjusting the hardness and the alkalinity, softening and clarifying, wherein the hardness of the effluent is less than 50mg/L, the alkalinity is less than 3mmol/L, the turbidity is less than 5NTU (turbidity standard unit), the temperature and the pressure of chemical conditioning are normal temperature and normal pressure, and the lime or alkaline water is added for removing Ca2 in the concentrated salt water + And Mg2 + The dosage of the plasma, lime or alkaline water depends on the total alkalinity of the concentrated brine and free Ca2 in the concentrated brine + And Mg2 + Hardness and other parameters.
In this embodiment, the soluble salt waste liquid is introduced into an MVR (mechanical vapor recompression) evaporator, and the soluble salt waste liquid is flashed to a saturated state, so as to obtain a concentrated soluble salt waste liquid; the MVR evaporator consists of a multi-effect falling film evaporator, concentrated soluble salt waste liquid obtained by evaporation of the last-effect falling film evaporator is sent to cooling crystallization equipment, crystals are subjected to centrifugal dehydration treatment, solid crystal salt is obtained, the main components of the solid crystal salt are sodium chloride and potassium chloride, and the solid crystal salt is used as industrial salt.
Specifically, the temperature of a material liquid in a one-effect falling-film evaporator of the MVR evaporator is the highest and is 120-130 ℃, when the soluble salt waste liquid reaches a preset concentration value, the soluble salt waste liquid is sequentially led into a two-effect falling-film evaporator and a next one-effect falling-film evaporator, the temperature of the material liquid in the two-effect falling-film evaporator is reduced to be 95-105 ℃, the temperature of the last one-effect falling-film evaporator is 65-75 ℃, and water is sequentially evaporated.
And S40, sequentially dehydrating the filter residue and carrying out plasma melting treatment to obtain the glassy state slag with the leaching toxicity reaching the standard.
In this embodiment, the filter residue is sequentially dehydrated, the dehydrated filter residue is sent into a plasma melting furnace, the filter residue is melted at 1200 to 1400 ℃, organic matters in the filter residue are decomposed, combusted and gasified, silicon ions and calcium ions in the inorganic matters form a Si-O network structure after the melting treatment, and heavy metals in the filter residue are encapsulated and solidified in the network structure to form a rigid amorphous molten slag glass state; after the melting treatment, organic matters such as dioxin and the like in the filter residue are thoroughly decomposed and destroyed by heating, the high-temperature pyrolysis rate of the dioxin is 99.5 to 99.9 percent, and heavy metal salts with lower boiling points in the filter residue are volatilized, transferred into gas and captured in the form of fly ash. Most heavy metals form alloy and sink at the furnace bottom, the alloy is separated from slag, and a small amount of metals are transferred into vitreous slag, so that the leaching rate of the heavy metals is greatly reduced; in the prior art, a coupling landfill technology capable of stably operating by utilizing fly ash chelation is utilized, the treated fly ash is buried by cement solidification or chemical agent chelation treatment, but the leaching toxicity of heavy metal and dioxin in the fly ash is found to exceed the national regulation standard when the buried fly ash is subjected to sampling inspection; in the embodiment, the leaching content of the heavy metal is less than 0.01g/L through the toxicity leaching characteristic experiment result, which indicates that the heavy metal replaces part of calcium ions and aluminum ions in the silicate mineral to be encapsulated in the network lattices of the silicate and is very stably dissolved in the glass phase. After the fly ash is subjected to melting treatment, the density is greatly increased, the volume of filter residue is reduced by more than half, and the obtained amorphous glassy slag, namely glassy slag, can be used as a roadbed material.
In the embodiment, the filter residues enter the pretreatment chamber of the plasma melting furnace once every half hour, after the air in the pretreatment chamber is replaced by argon, the argon is sent into a melting pool of the plasma melting furnace, the slag is continuously discharged, and the hourly treatment capacity reaches 2.5 to 3 tons.
In this embodiment, after the plasma melting treatment of the filter residue, when the melting temperature in the furnace is controlled at 1350 ℃, the filter residue is allowed to stay in the reduction zone of the plasma melting furnace for 60 to 150 minutes and then the product is discharged, the heavy metal and the carbon element of the filter residue undergo a reduction reaction to separate the heavy metal from the molten glass, the heavy metal and the molten glass are recovered at the bottom and the side of the melting furnace through the water quenching cooling mode at the glass flow outlets, the heavy metal can be used as a raw material for non-ferrous metal smelting, the water quenching glassy slag can be used as microcrystalline glass, a building base material and the like, and the residue is returned to the melting furnace as a batch.
Specifically, the flue gas that produces among the plasma melting treatment process carries out the thermal conversion through waste heat recovery device, and the steam of production is used for waste heat power generation device to generate electricity, and the electric power that produces supplies plasma melting furnace to use as the energy, carries out flue gas treatment back discharge to harmful substance such as particulate matter, volatile heavy metal, acid gas and dioxin in the flue gas up to standard, the step of flue gas treatment is: the method comprises the following steps of dedusting flue gas, leading generated secondary fly ash back to preparation equipment of fly ash slurry, treating the secondary fly ash together when fly ash is treated next time, carrying out desulfurization and dechlorination on the dedusted flue gas through flue gas purification treatment equipment, carrying out dehumidification filtration, and further removing moisture and dust in the flue gas, wherein a flue gas sample collection module is used for detecting the current flue gas emission state of a flue gas emission source and collecting a flue gas sample from the flue gas emission source according to the flue gas emission state; the method comprises the steps of preprocessing a flue gas sample to obtain a corresponding flue gas solution, analyzing and detecting the flue gas solution to determine the content of heavy metals contained in the flue gas sample, and if the content of the heavy metals is higher than a preset threshold value, returning the flue gas solution to a water washing treatment step, or adding absorption liquid, and carrying out physical adsorption and chemical digestion on the absorption liquid and heavy metal particles in the flue gas to purify the flue gas.
According to GB5085.3-2007Z 'hazardous waste identification Standard Leaching toxicity identification' standard, the glassy state slag is subjected to a heavy metal toxicity exudation test, and the toxicity is lower than a standard limit value.
In this embodiment, the fly ash slurry is sequentially subjected to water washing treatment and filtration treatment to obtain soluble salt waste liquid and filter residue, so that the fly ash can be subjected to reduction treatment before plasma melting treatment; soluble salt water in the fly ash is washed away by water, acid-base balance treatment is not needed to be carried out on filter residues in the plasma melting treatment process, the plasma melting treatment process is optimized, equipment cannot be corroded, and the treatment cost is reduced; evaporating the soluble salt waste liquid to obtain industrial salt, thereby realizing the recycling of the soluble salt waste liquid; sequentially carrying out dehydration treatment and plasma melting treatment on the filter residue to remove toxic substances contained in the filter residue so as to obtain glassy-state slag with leaching toxicity reaching the standard; the harmful substances such as particulate matters, volatile heavy metals, acid gases and dioxin in the flue gas are subjected to flue gas treatment and then discharged after reaching the standard, so that the leaching toxicity of the product meets the standard, the treatment cost is low, and the stable operation can be realized.
It should be noted that, in this document, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrases "comprising a component of' 8230; \8230;" does not exclude the presence of another like element in a process, method, article, or apparatus that comprises the element.
The above-mentioned serial numbers of the embodiments of the present application are merely for description and do not represent the merits of the embodiments.
Through the above description of the embodiments, those skilled in the art will clearly understand that the method of the above embodiments can be implemented by software plus a necessary general hardware platform, and certainly can also be implemented by hardware, but in many cases, the former is a better implementation manner. Based on such understanding, the technical solutions of the present application may be embodied in the form of a software product, which is stored in a storage medium (e.g., ROM/RAM, magnetic disk, optical disk) and includes instructions for enabling a terminal device (e.g., a mobile phone, a computer, a server, a device, or a network device) to execute the method according to the embodiments of the present application.
The above description is only a preferred embodiment of the present application, and not intended to limit the scope of the present application, and all modifications of equivalent structures and equivalent processes, which are made by the contents of the specification and the drawings of the present application, or which are directly or indirectly applied to other related technical fields, are included in the scope of the present application.
Claims (10)
1. A method for treating fly ash generated by waste incineration is characterized by comprising the following steps:
carrying out water washing pretreatment on fly ash generated by burning garbage to obtain fly ash slurry;
washing and filtering the fly ash slurry in sequence to obtain soluble salt waste liquid and filter residue;
evaporating the soluble salt waste liquid to obtain industrial salt;
and (3) sequentially carrying out dehydration treatment and plasma melting treatment on the filter residue to obtain the glassy state slag with the leaching toxicity reaching the standard.
2. The method according to claim 1, wherein the water washing treatment process is a multi-stage counter-current water washing process, and the number of water washing stages of the multi-stage counter-current water washing process is determined based on the chlorine content in the fly ash slurry.
3. The method according to claim 2, wherein the water quality purification treatment and the chemical precipitation treatment are sequentially performed on the soluble salt waste liquid obtained from the previous stage of water washing before the last stage of water washing in the multistage countercurrent water washing process to remove mineral ions and heavy metal ions in the soluble salt waste liquid.
4. The method according to claim 1, wherein the amount of waste salt in the dehydrated filter residue is 2 to 5%.
5. The method according to claim 1, wherein the step of evaporating the soluble salt waste liquid to obtain industrial salt comprises:
flashing the soluble salt waste liquid to a saturated state to obtain concentrated soluble salt waste liquid;
sequentially cooling, crystallizing and centrifugally dewatering the concentrated soluble salt waste liquid to obtain solid crystal salt;
the solid crystalline salt is used as industrial salt.
6. The method according to claim 1, wherein before the step of evaporating the soluble salt waste liquid to obtain industrial salt, the method further comprises:
and carrying out chemical conditioning treatment and ultrafiltration treatment on the soluble salt waste liquid to ensure that the hardness of the soluble salt waste liquid is less than 50mg/L and the turbidity is less than 5NTU.
7. The method for treating fly ash generated by burning garbage according to claim 1, wherein the plasma melting treatment process comprises controlling the residence time of the filter residue in a reduction zone of a plasma melting furnace so as to reduce heavy metals in the filter residue.
8. The method according to claim 7, wherein the residence time of the filter residue in the plasma melting furnace is 60 to 150 minutes.
9. The method for treating fly ash generated by burning garbage according to claim 1, wherein the flue gas generated in the plasma melting treatment process is treated by flue gas to reach the emission standard.
10. The method according to claim 1, wherein the plasma melting temperature is 1200 to 1400 ℃.
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