CN116984343B - System and process for recycling waste incineration fly ash - Google Patents
System and process for recycling waste incineration fly ash Download PDFInfo
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- CN116984343B CN116984343B CN202311235579.5A CN202311235579A CN116984343B CN 116984343 B CN116984343 B CN 116984343B CN 202311235579 A CN202311235579 A CN 202311235579A CN 116984343 B CN116984343 B CN 116984343B
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- 239000010881 fly ash Substances 0.000 title claims abstract description 71
- 238000000034 method Methods 0.000 title claims abstract description 37
- 238000004064 recycling Methods 0.000 title claims abstract description 34
- 238000004056 waste incineration Methods 0.000 title claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 107
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims abstract description 74
- 238000005406 washing Methods 0.000 claims abstract description 66
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 58
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 48
- 238000000197 pyrolysis Methods 0.000 claims abstract description 30
- 238000003825 pressing Methods 0.000 claims abstract description 29
- 238000011084 recovery Methods 0.000 claims abstract description 29
- 239000002956 ash Substances 0.000 claims abstract description 17
- 239000004566 building material Substances 0.000 claims abstract description 7
- 150000003841 chloride salts Chemical class 0.000 claims abstract description 6
- 239000002002 slurry Substances 0.000 claims description 70
- 238000002156 mixing Methods 0.000 claims description 69
- 239000007788 liquid Substances 0.000 claims description 49
- 238000000746 purification Methods 0.000 claims description 39
- 239000012528 membrane Substances 0.000 claims description 37
- 239000001103 potassium chloride Substances 0.000 claims description 36
- 235000011164 potassium chloride Nutrition 0.000 claims description 34
- 239000000706 filtrate Substances 0.000 claims description 32
- 239000011780 sodium chloride Substances 0.000 claims description 27
- 239000012452 mother liquor Substances 0.000 claims description 20
- 239000002562 thickening agent Substances 0.000 claims description 20
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 18
- 239000012065 filter cake Substances 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 239000003546 flue gas Substances 0.000 claims description 12
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims description 11
- 239000007800 oxidant agent Substances 0.000 claims description 10
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 9
- 230000001699 photocatalysis Effects 0.000 claims description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 9
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 9
- 235000011152 sodium sulphate Nutrition 0.000 claims description 9
- 238000000108 ultra-filtration Methods 0.000 claims description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 8
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 8
- 150000003839 salts Chemical class 0.000 claims description 7
- 229910052979 sodium sulfide Inorganic materials 0.000 claims description 7
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 239000003344 environmental pollutant Substances 0.000 claims description 6
- 231100000719 pollutant Toxicity 0.000 claims description 6
- 239000002244 precipitate Substances 0.000 claims description 6
- 229910052802 copper Inorganic materials 0.000 claims description 5
- 239000002893 slag Substances 0.000 claims description 5
- 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 claims description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- PQLVXDKIJBQVDF-UHFFFAOYSA-N acetic acid;hydrate Chemical compound O.CC(O)=O PQLVXDKIJBQVDF-UHFFFAOYSA-N 0.000 claims description 3
- 230000000536 complexating effect Effects 0.000 claims description 3
- 229910052745 lead Inorganic materials 0.000 claims description 3
- 239000011268 mixed slurry Substances 0.000 claims description 3
- 238000001728 nano-filtration Methods 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 238000001223 reverse osmosis Methods 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 230000001502 supplementing effect Effects 0.000 claims description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 2
- 235000010755 mineral Nutrition 0.000 claims description 2
- 239000011707 mineral Substances 0.000 claims description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract description 3
- XLYOFNOQVPJJNP-ZSJDYOACSA-N Heavy water Chemical compound [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 239000012466 permeate Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 239000010802 sludge Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- WIKSRXFQIZQFEH-UHFFFAOYSA-N [Cu].[Pb] Chemical compound [Cu].[Pb] WIKSRXFQIZQFEH-UHFFFAOYSA-N 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 238000005111 flow chemistry technique Methods 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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
-
- 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
- B09B3/32—Compressing or compacting
-
- 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
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B2101/00—Type of solid waste
- B09B2101/30—Incineration ashes
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to the technical field of waste incineration fly ash treatment, in particular to a waste incineration fly ash recycling system and process. The system for recycling the waste incineration fly ash can recycle and recycle heavy metals, naCl and KCl in the fly ash, and can convert Ca in the fly ash into CaCO 3 And CaSO 4 And carrying out resource utilization. Because heavy metals in the ash are removed, the weather resistance of the ash when being used for building materials can be greatly improved. The process of the invention carries out water washing, heavy metal recovery, chloride salt recovery and low-temperature pyrolysis nearly synchronously, thus greatly reducing the treatment period; the recovery rate of chloride is improved by adopting three-stage water washing; the plate-frame filter pressing mode is adopted to improve the period of heavy metal recovery.
Description
Technical Field
The invention relates to the technical field of waste incineration fly ash treatment, in particular to a waste incineration fly ash recycling system and a waste incineration fly ash recycling process.
Background
The waste incineration fly ash (namely the fly ash captured by a flue gas purification system in a waste incineration line) contains Ca, na, K, cl and heavy metals such as Cu, pb and the like, and has resource utilization value.
At present, common fly ash recycling treatment modes comprise water washing, cement kiln cooperation, high-temperature sintering, high-temperature melting (resistance type and plasma type) and the like, and the scheme has advantages and application limitations and cannot maximally realize resource utilization.
CN114988626a discloses a process for treating waste water from waste incineration fly ash washing, which comprises the following steps: delivering the wastewater to a raw water regulating tank; delivering the wastewater of the raw water regulating tank to a heavy metal removing system for removing heavy metal, and performing solid-liquid separation on the generated mud-water mixture to generate heavy water and heavy metal removing sludge; delivering the heavy water to a first softening system for removing calcium, and performing solid-liquid separation on the produced mud-water mixture to produce softened water and calcium sulfate sludge; delivering softened water to a mud-water mixture generated by a second softening system for solid-liquid separation to generate deeply softened water and calcium carbonate sludge; delivering the deeply softened water to an ultrafiltration membrane system to generate ultrafiltration concentrated solution and ultrafiltration permeate, and delivering the ultrafiltration concentrated solution to a raw water regulating tank; delivering the ultrafiltration permeate to a membrane separation system to generate separation membrane concentrated solution and separation membrane permeate; the separation membrane concentrate is conveyed to a first softening system; regulating the pH value of the separation membrane permeate to generate reclaimed water; and (5) evaporating, crystallizing and separating salt from the reclaimed water.
The patent application adopts a treatment method of fly ash washing liquid, and relates to heavy metal removal (dosing, coagulation, flocculation and precipitation), heavy metal removal (adding sodium sulfate and sodium carbonate), COD and SS removal (ultrafiltration membrane) and salt separation (separation membrane). However, this technique still has some drawbacks, such as: (1) the total period of single flow processing is long; (2) the precipitation process of heavy metal removal is time consuming; (3) the effect of salt separation by a membrane system is general.
Therefore, developing a system or process for treating waste incineration fly ash, which can maximize the utilization of resources, is one of the technical problems that need to be solved in the art.
Disclosure of Invention
The invention aims to solve the technical problem of providing a system and a process for recycling waste incineration fly ash, which are realized in a mode of water washing, membrane treatment, precipitation, mechanical evaporation and low-temperature pyrolysisThe recovery of heavy metals such as Cu, pb, and the like, the recovery of NaCl and KCl, and CaCO 3 And CaSO 4 Is used for recycling ash and slag.
In order to solve the technical problems, the application provides the following technical scheme:
a waste incineration fly ash recycling system comprises a fly ash pretreatment subsystem, a three-stage countercurrent water washing subsystem, a low-temperature pyrolysis subsystem, a heavy metal recovery subsystem, and NaCl and KCl recovery subsystem.
Wherein the fly ash pretreatment subsystem comprises a fly ash bin, and the fly ash bin is connected with the wet ball mill through a quantitative feeding device.
Wherein the dosing device is a rotary feeder or a screw conveyor.
The three-stage countercurrent washing subsystem comprises a primary pulp mixing tank, an outlet of the wet ball mill is connected with the primary pulp mixing tank, the primary pulp mixing tank is connected with a primary washing filter press, a mud outlet of the primary washing filter press is connected with a secondary pulp mixing tank, and a clear water outlet of the primary washing filter press is connected with a primary filtrate tank;
the secondary slurry mixing tank is connected with the secondary water washing filter press, a slurry outlet of the secondary water washing filter press is connected with the tertiary slurry mixing tank, a clear water outlet of the secondary water washing filter press is connected with the secondary filtrate tank, and an outlet of the secondary filtrate tank is connected with an inlet of the secondary slurry mixing tank;
the three-stage slurry mixing tank is connected with the three-stage water washing filter press, a slurry outlet of the three-stage water washing filter press is connected with the desiccator, a clear water outlet of the three-stage water washing filter press is connected with the three-stage filtrate tank, and an outlet of the three-stage filtrate tank is connected with an inlet of the three-stage slurry mixing tank.
Wherein, the three-stage size mixing tank is provided with a water supplementing port for external water.
The low-temperature pyrolysis subsystem comprises a desiccator, an outlet of the desiccator is connected with a low-temperature pyrolysis furnace, and an outlet of the low-temperature pyrolysis furnace discharges ash; and the desiccator and the low-temperature pyrolysis furnace are both provided with a flue gas pollutant discharge port connected with a flue gas purification system.
The heavy metal recovery subsystem comprises a membrane treatment system, an outlet of the primary filtrate tank is connected with the membrane treatment system, a concentrated liquid outlet of the membrane treatment system is connected with the concentrated water tank, an outlet of the concentrated water tank is connected with a plate-and-frame filter press, and a clear liquid outlet of the plate-and-frame filter press is respectively connected with the concentrated water tank, the primary pulp mixing tank and the wet ball mill.
The NaCl and KCl recycling subsystem comprises a purification reaction tank, a purification filter press, a purification liquid buffer tank, a steam condensate preheater, a heater, a photocatalytic oxidizer, a separator, a sodium chloride thickener, a sodium chloride mother liquor tank, a flash evaporator, a potassium chloride thickener and a potassium chloride mother liquor tank which are connected in sequence, and a clear liquid outlet of the membrane treatment system is connected with the purification reaction tank; and a clear liquid outlet of the potassium chloride mother liquor tank is connected with an inlet of the purifying liquid buffer tank.
Wherein, the purification reaction tank is provided with a sodium carbonate/sodium sulfate inlet.
The invention relates to a waste incineration fly ash recycling process, which comprises the following steps:
(1) The method comprises the steps of (1) storing raw fly ash in a fly ash bin, adding the fly ash into a wet ball mill through a quantitative feeding device, simultaneously adding water and ethylenediamine tetraacetic acid into the wet ball mill, fully stirring and mixing, complexing water-insoluble heavy metals in the fly ash by ethylenediamine tetraacetic acid, dissolving the heavy metals in the water, and enabling the mixed slurry to enter a primary slurry mixing tank;
(2) The slurry of the primary slurry mixing tank enters a primary washing filter press, the slurry after filter pressing enters a secondary slurry mixing tank, and the clear water after filter pressing enters a primary filter liquid tank; the slurry of the secondary slurry mixing tank enters a secondary washing filter press, the slurry after filter pressing enters a tertiary slurry mixing tank, the clear water after filter pressing enters a secondary filtrate tank, and the clear water of the secondary filtrate tank enters a secondary slurry mixing tank; the slurry of the three-stage slurry mixing tank enters a three-stage washing filter press, the slurry after filter pressing enters a desiccator, the clear water after filter pressing enters a three-stage filtrate tank, the clear water of the three-stage filtrate tank enters a three-stage slurry mixing tank, and meanwhile, the three-stage slurry mixing tank is added with external water to carry out washing water replenishing; separating the soluble and insoluble parts in the fly ash slurry by three-stage countercurrent water washing;
(3) The desiccator evaporates the slurry conveyed by the three-stage washing filter press by using saturated steam to obtain a solid filter cake, the filter cake is crushed and then enters a low-temperature pyrolysis furnace, and dioxin in the filter cake is removed under the conditions of 350-450 ℃ and nitrogen charging state and pyrolysis time of 1-2 hours to obtain ash slag for building material industry; the flue gas pollutants generated in the drying and pyrolysis process are discharged after being removed in a flue gas purification system;
(4) The first-stage filtrate tank enters a membrane treatment system, heavy metal-enriched concentrated solution is obtained through nanofiltration membrane, ultrafiltration membrane and reverse osmosis method, sodium sulfide is added into the concentrated solution tank, the sodium sulfide reacts with heavy metal to generate heavy metal precipitate, and then the heavy metal precipitate is separated through a plate-and-frame filter press to obtain Cu and Pb mineral salt filter cakes which can be used for subsequent separation and purification, and finally heavy metal is obtained; the clear liquid after filter pressing is divided into three paths, wherein the first path returns to the concentrated water tank for circulating filter pressing, the second path enters the primary pulp mixing tank, and the third path enters the wet ball mill;
(5) The clear liquid after membrane treatment enters a purification reaction tank, sodium carbonate and sodium sulfate are added into the tank for reaction, and then the clear liquid enters a purification filter press to obtain calcium carbonate and calcium sulfate filter cakes, and after the clear liquid after filter pressing enters a purification buffer tank, naCl and KCl are recovered, namely the clear liquid sequentially passes through a steam condensate water preheater, a heater, a photocatalytic oxidizer, a separator, a sodium chloride thickener, a sodium chloride mother liquor tank, a flash evaporator, a potassium chloride thickener and a potassium chloride mother liquor tank; the photocatalytic oxidizer completely decomposes a small amount of EDTA remained in the clear liquid, so that the quality of the obtained chloride salt can be ensured; the clear liquid passes through a sodium chloride thickener to obtain NaCl salt, and passes through a potassium chloride thickener to obtain KCl salt, wherein the clear liquid in a potassium chloride mother liquor tank enters a purifying liquid buffer tank for recycling.
Compared with the prior art, the system and the process for recycling the waste incineration fly ash have the following beneficial effects:
the system for recycling the waste incineration fly ash can recycle and recycle heavy metals, naCl and KCl in the fly ash, and can convert Ca in the fly ash into CaCO 3 And CaSO 4 To make recycling beneficialThe harmless product ash is comprehensively recycled (heavy metal recovery, calcium recovery, chloride recovery and ash high-value application). Because heavy metals in the ash are removed, the weather resistance of the ash when being used for building materials can be greatly improved.
The process of the invention carries out water washing, heavy metal recovery, chloride salt recovery and low-temperature pyrolysis nearly synchronously, thus greatly reducing the treatment period; the recovery rate of chloride is improved by adopting three-stage water washing; the plate-frame filter pressing mode is adopted to improve the period of heavy metal recovery; and the defects in CN114988626A are overcome by low temperature pyrolysis.
The garbage incineration fly ash recycling system and the process are further described below with reference to the accompanying drawings.
Drawings
FIG. 1 is a schematic diagram of the system for recycling waste incineration fly ash.
Wherein, the system comprises a 100-fly ash pretreatment subsystem, a 200-three-stage countercurrent washing subsystem, a 300-low-temperature pyrolysis subsystem, a 400-heavy metal recovery subsystem, a 500-NaCl and a KCl recovery subsystem;
101-ash flying bin, 102-wet ball mill;
201-primary pulp mixing tank, 202-primary washing filter press, 203-secondary pulp mixing tank, 204-secondary washing filter press, 205-tertiary pulp mixing tank, 206-tertiary washing filter press, 207-primary filtrate tank, 208-secondary filtrate tank and 209-tertiary filtrate tank;
301-a desiccator, 302-a low-temperature pyrolysis furnace and 303-a flue gas purification system;
401-a membrane treatment system, 402-a concentrated water tank and 403-a plate-and-frame filter press;
501-purification reaction tank, 502-purification filter press, 503-purification buffer tank, 504-steam condensate preheater, 505-heater, 506-photocatalytic oxidizer, 507-separator, 508-sodium chloride thickener, 509-sodium chloride mother liquor tank, 510-flash evaporator, 511-potassium chloride thickener and 512-potassium chloride mother liquor tank.
Detailed Description
As shown in fig. 1, a system for recycling waste incineration fly ash comprises a fly ash pretreatment subsystem 100, a three-stage countercurrent water washing subsystem 200, a low-temperature pyrolysis subsystem 300, a heavy metal recovery subsystem 400, and a NaCl and KCl recovery subsystem 500.
The fly ash pretreatment subsystem 100 comprises a fly ash silo 101, said fly ash silo 101 being connected to a wet ball mill 102 by means of a dosing device. The quantitative feeding device is a rotary feeder or a screw conveyor, and the conveying quantity is calculated through a weightless scale.
The three-stage countercurrent washing subsystem 200 comprises a primary pulp mixing tank 201, wherein an outlet of the wet ball mill 102 is connected with the primary pulp mixing tank 201, the primary pulp mixing tank 201 is connected with a primary washing filter press 202, a mud outlet of the primary washing filter press 202 is connected with a secondary pulp mixing tank 203, and a clear water outlet of the primary washing filter press 202 is connected with a primary filter liquor tank 207;
the secondary pulp mixing tank 203 is connected with the secondary washing filter press 204, a slurry outlet of the secondary washing filter press 204 is connected with the tertiary pulp mixing tank 205, a clear water outlet of the secondary washing filter press 204 is connected with the secondary filtrate tank 208, and an outlet of the secondary filtrate tank 208 is connected with an inlet of the secondary pulp mixing tank 203;
the three-stage slurry mixing tank 205 is connected with the three-stage water washing filter press 206, a slurry outlet of the three-stage water washing filter press 206 is connected with the desiccator 301, a clear water outlet of the three-stage water washing filter press 206 is connected with the three-stage filtrate tank 209, and an outlet of the three-stage filtrate tank 209 is connected with an inlet of the three-stage slurry mixing tank 205. The three-stage size mixing tank 205 is provided with a water supplementing port for external water.
The low-temperature pyrolysis subsystem 300 comprises a desiccator 301 (a Holsley dryer is selected, and model TST-1030 is selected), wherein the outlet of the desiccator 301 is connected with a low-temperature pyrolysis furnace 302 (a manufacturer selected: hitachi shipbuilding or Shanghai le), and the outlet of the low-temperature pyrolysis furnace 302 discharges ash; the desiccator 301 and the low-temperature pyrolysis furnace 302 are both provided with a flue gas pollutant discharge port connected with a flue gas purification system 303.
The heavy metal recovery subsystem 400 comprises a membrane treatment system 401, wherein an outlet of the primary filtrate tank 207 is connected with the membrane treatment system 401, a concentrated solution outlet of the membrane treatment system 401 is connected with a concentrated water tank 402, an outlet of the concentrated water tank 402 is connected with a plate-and-frame filter press 403, and a clear solution outlet of the plate-and-frame filter press 403 is respectively connected with the concentrated water tank 402, the primary pulp mixing tank 201 and the wet ball mill 102.
The NaCl and KCl recovery subsystem 500 comprises a purification reaction tank 501, a purification filter press 502, a purification liquid buffer tank 503, a steam condensate preheater 504, a heater 505, a photocatalytic oxidizer 506, a separator 507, a sodium chloride thickener 508, a sodium chloride mother liquor tank 509, a flash evaporator 510, a potassium chloride thickener 511 and a potassium chloride mother liquor tank 512 which are sequentially connected, wherein a clear liquid outlet of the membrane treatment system 401 is connected with the purification reaction tank 501; the clear liquid outlet of the potassium chloride mother liquor tank 512 is connected to the inlet of the purified liquid buffer tank 503. The NaCl and KCl recovery subsystem is a mature matched system, and suppliers can select Chinese and national lubrication or Anhui conch.
The purification reaction tank 501 is provided with a sodium carbonate/sodium sulfate inlet.
The waste incineration fly ash resource utilization process adopting the system comprises the following steps:
(1) The raw fly ash enters a fly ash bin for storage, the fly ash is added into a wet ball mill through a quantitative feeding device, the conveying amount is calculated through a weightless scale by the quantitative feeding device, and the feeding amount is 10-50t/d.
Adding water and ethylenediamine tetraacetic acid (EDTA) into a wet ball mill simultaneously, stirring and mixing thoroughly, wherein the ratio of fly ash to water is 1:1-3:2, the addition amount of EDTA is 5% -10% of the water washing amount, and the stirring time is 15-30min. Complexing water-insoluble heavy metals in fly ash by ethylenediamine tetraacetic acid to make the heavy metals dissolved in water, and enabling the mixed slurry to enter a primary slurry mixing tank;
(2) The slurry of the primary slurry mixing tank enters a primary washing filter press, the slurry after filter pressing enters a secondary slurry mixing tank, and the clear water after filter pressing enters a primary filter liquid tank; the slurry of the secondary slurry mixing tank enters a secondary washing filter press, the slurry after filter pressing enters a tertiary slurry mixing tank, the clear water after filter pressing enters a secondary filtrate tank, and the clear water of the secondary filtrate tank enters a secondary slurry mixing tank; the slurry of the three-stage slurry mixing tank enters a three-stage washing filter press, the slurry after filter pressing enters a desiccator, the clear water after filter pressing enters a three-stage filtrate tank, the clear water of the three-stage filtrate tank enters a three-stage slurry mixing tank, and meanwhile, the three-stage slurry mixing tank is added with external water to carry out washing water replenishing; separating the soluble and insoluble parts in the fly ash slurry by three-stage countercurrent water washing;
the water-to-ash ratio (the ratio of the total mass of the treated fly ash to the total mass of the consumed water) is 2:1-6:1; the water washing time of each stage is 10-30min; the water content of the filter cake generated by each stage of filter press is lower than 30 percent.
(3) The drying machine evaporates the slurry conveyed by the three-stage washing filter press by using saturated steam to obtain a solid filter cake, the filter cake is crushed and then enters a low-temperature pyrolysis furnace, dioxin in the filter cake is removed under the conditions of 350-450 ℃ and nitrogen charging state and pyrolysis time of 1-2 hours, ash slag used in the building material industry is obtained, and the ash slag is cooled (the temperature is not more than 60 ℃) and then is applied to building materials; and (5) removing the smoke pollutants generated in the drying and pyrolysis process in a smoke purification system and discharging.
(4) The first-stage filtrate tank enters a membrane treatment system, and heavy metal-enriched concentrated solution is obtained through nanofiltration membrane, ultrafiltration membrane and reverse osmosis method, and the membrane rejection rate of the membrane treatment system is 60-90%.
The concentrated solution enters a concentrated water tank, sodium sulfide is added into the tank, and the adding amount of the sodium sulfide is 0.5-1% of that of the concentrated water; the sodium sulfide reacts with heavy metals to generate heavy metal precipitates, and then the heavy metal precipitates are separated by a plate-and-frame filter press to obtain Cu and Pb ore salt filter cakes (the water content of the copper-lead ore filter cakes is not higher than 20 percent), so that the copper-lead ore filter cakes can be used for subsequent separation and purification, and finally heavy metals are obtained; the clear liquid after filter pressing is divided into three paths, wherein the first path returns to the concentrated water tank for circulating filter pressing, the second path enters the primary pulp mixing tank, and the third path enters the wet ball mill;
(5) Adding clear liquid subjected to membrane treatment into a purification reaction tank, adding sodium carbonate and sodium sulfate into the tank for reaction (the mass ratio of sodium carbonate to sodium sulfate is 2:1-1:1, the content of sodium carbonate and sodium sulfate is 15-35 percent of that of clear water), then, adding the clear liquid into a purification filter press to obtain calcium carbonate and calcium sulfate filter cakes, and after the clear liquid subjected to filter pressing enters a purification liquid buffer tank, recycling NaCl and KCl, namely, sequentially passing through a steam condensate water preheater, a heater, a photocatalytic oxidizer, a separator, a sodium chloride thickener, a sodium chloride mother liquor tank, a flash evaporator, a potassium chloride thickener and a potassium chloride mother liquor tank; the photocatalytic oxidizer completely decomposes a small amount of EDTA remained in the clear liquid, so that the quality of the obtained chloride salt can be ensured; the clear liquid passes through a sodium chloride thickener to obtain NaCl salt, and passes through a potassium chloride thickener to obtain KCl salt, wherein the clear liquid in a potassium chloride mother liquor tank enters a purifying liquid buffer tank for recycling.
In summary, the fly ash treatment system in the prior art only comprises a three-stage countercurrent water washing and evaporation powder salt (chloride salt recovery) process link, compared with the process link, the system provided by the invention is added with heavy metal recovery, calcium salt recovery and low-temperature pyrolysis of dioxin, and heavy metals in the fly ash are efficiently separated, so that the system can be used for recycling after purification; meanwhile, after the heavy metal is removed from the fly ash, the weather resistance of the material is greatly improved in the subsequent building material application. The system and the process have more thorough resource utilization of the fly ash and higher ash product value.
The above examples are only illustrative of the preferred embodiments of the present invention and are not intended to limit the scope of the present invention, and various modifications and improvements made by those skilled in the art to the technical solution of the present invention should fall within the scope of protection defined by the claims of the present invention without departing from the spirit of the present invention.
Claims (9)
1. The waste incineration fly ash recycling utilization process is characterized in that the waste incineration fly ash recycling utilization system comprises a fly ash pretreatment subsystem (100), a three-stage countercurrent water washing subsystem (200), a low-temperature pyrolysis subsystem (300), a heavy metal recovery subsystem (400), and a NaCl and KCl recovery subsystem (500);
the method specifically comprises the following steps:
(1) The method comprises the steps of (1) storing raw fly ash in a fly ash bin, adding the fly ash into a wet ball mill through a quantitative feeding device, simultaneously adding water and ethylenediamine tetraacetic acid into the wet ball mill, fully stirring and mixing, complexing water-insoluble heavy metals in the fly ash by ethylenediamine tetraacetic acid, dissolving the heavy metals in the water, and enabling the mixed slurry to enter a primary slurry mixing tank;
(2) The slurry of the primary slurry mixing tank enters a primary washing filter press, the slurry after filter pressing enters a secondary slurry mixing tank, and the clear water after filter pressing enters a primary filter liquid tank; the slurry of the secondary slurry mixing tank enters a secondary washing filter press, the slurry after filter pressing enters a tertiary slurry mixing tank, clear water after filter pressing enters a secondary filtrate tank, and clear water of the secondary filtrate tank enters the secondary slurry mixing tank; the slurry of the three-stage slurry mixing tank enters a three-stage washing filter press, the slurry after filter pressing enters a desiccator, clear water after filter pressing enters a three-stage filtrate tank, clear water of the three-stage filtrate tank enters the three-stage slurry mixing tank, and external water is added into the three-stage slurry mixing tank to carry out washing water replenishing; separating the soluble and insoluble parts in the fly ash slurry by three-stage countercurrent water washing;
(3) The desiccator evaporates the slurry conveyed by the three-stage washing filter press by using saturated steam to obtain a solid filter cake, the filter cake is crushed and then enters a low-temperature pyrolysis furnace, and dioxin in the filter cake is removed under the conditions of 350-450 ℃ and nitrogen charging state and pyrolysis time of 1-2 hours to obtain ash slag for building material industry; the flue gas pollutants generated in the drying and pyrolysis process are discharged after being removed in a flue gas purification system;
(4) The first-stage filtrate tank enters a membrane treatment system, heavy metal-enriched concentrated solution is obtained through nanofiltration membrane, ultrafiltration membrane and reverse osmosis method, sodium sulfide is added into the concentrated solution tank, the sodium sulfide reacts with heavy metal to generate heavy metal precipitate, and then the heavy metal precipitate is separated through a plate-and-frame filter press to obtain Cu and Pb mineral salt filter cakes which can be used for subsequent separation and purification, and finally heavy metal is obtained; the clear liquid after filter pressing is divided into three paths, wherein the first path returns to the concentrated water tank for circulating filter pressing, the second path enters the primary pulp mixing tank, and the third path enters the wet ball mill;
(5) The clear liquid after membrane treatment enters a purification reaction tank, sodium carbonate and sodium sulfate are added into the tank for reaction, and then the clear liquid enters a purification filter press to obtain calcium carbonate and calcium sulfate filter cakes, and after the clear liquid after filter pressing enters a purification buffer tank, naCl and KCl are recovered, namely the clear liquid sequentially passes through a steam condensate water preheater, a heater, a photocatalytic oxidizer, a separator, a sodium chloride thickener, a sodium chloride mother liquor tank, a flash evaporator, a potassium chloride thickener and a potassium chloride mother liquor tank; the photocatalytic oxidizer completely decomposes a small amount of residual ethylenediamine tetraacetic acid in the clear liquid, so that the quality of the obtained chloride salt can be ensured; the clear liquid passes through a sodium chloride thickener to obtain NaCl salt, and passes through a potassium chloride thickener to obtain KCl salt, wherein the clear liquid in a potassium chloride mother liquor tank enters a purifying liquid buffer tank for recycling.
2. The waste incineration fly ash recycling process according to claim 1, which is characterized in that: the fly ash pretreatment subsystem (100) comprises a fly ash bin (101), and the fly ash bin (101) is connected with a wet ball mill (102) through a dosing device.
3. The waste incineration fly ash recycling process according to claim 2, which is characterized in that: the dosing device is a rotary feeder or a screw conveyor.
4. The waste incineration fly ash recycling process according to claim 2, which is characterized in that: the three-stage countercurrent washing subsystem (200) comprises a primary pulp mixing tank (201), wherein an outlet of the wet ball mill (102) is connected with the primary pulp mixing tank (201), the primary pulp mixing tank (201) is connected with a primary washing filter press (202), a slurry outlet of the primary washing filter press (202) is connected with a secondary pulp mixing tank (203), and a clear water outlet of the primary washing filter press (202) is connected with a primary filter liquor tank (207);
the secondary slurry mixing tank (203) is connected with the secondary water washing filter press (204), a slurry outlet of the secondary water washing filter press (204) is connected with the tertiary slurry mixing tank (205), a clear water outlet of the secondary water washing filter press (204) is connected with the secondary filter liquid tank (208), and an outlet of the secondary filter liquid tank (208) is connected with an inlet of the secondary slurry mixing tank (203);
the three-stage slurry mixing tank (205) is connected with the three-stage water washing filter press (206), a slurry outlet of the three-stage water washing filter press (206) is connected with the desiccator (301), a clear water outlet of the three-stage water washing filter press (206) is connected with the three-stage filtrate tank (209), and an outlet of the three-stage filtrate tank (209) is connected with an inlet of the three-stage slurry mixing tank (205).
5. The waste incineration fly ash recycling process according to claim 4, which is characterized in that: and the three-stage size mixing tank (205) is provided with a water supplementing port for external water.
6. The waste incineration fly ash recycling process according to claim 4, which is characterized in that: the low-temperature pyrolysis subsystem (300) comprises a desiccator (301), wherein an outlet of the desiccator (301) is connected with a low-temperature pyrolysis furnace (302), and ash residues are discharged from an outlet of the low-temperature pyrolysis furnace (302); the drier (301) and the low-temperature pyrolysis furnace (302) are both provided with a flue gas pollutant discharge port connected with a flue gas purification system (303).
7. The waste incineration fly ash recycling process according to claim 6, which is characterized in that: the heavy metal recovery subsystem (400) comprises a membrane treatment system (401), an outlet of the primary filtrate tank (207) is connected with the membrane treatment system (401), a concentrated solution outlet of the membrane treatment system (401) is connected with a concentrated water tank (402), an outlet of the concentrated water tank (402) is connected with a plate-and-frame filter press (403), and a clear solution outlet of the plate-and-frame filter press (403) is respectively connected with the concentrated water tank (402), the primary pulp mixing tank (201) and the wet ball mill (102).
8. The waste incineration fly ash recycling process according to claim 7, which is characterized in that: the NaCl and KCl recycling subsystem (500) comprises a purification reaction tank (501), a purification filter press (502), a purification liquid buffer tank (503), a steam condensate preheater (504), a heater (505), a photocatalytic oxidizer (506), a separator (507), a sodium chloride thickener (508), a sodium chloride mother liquor tank (509), a flash evaporator (510), a potassium chloride thickener (511) and a potassium chloride mother liquor tank (512) which are sequentially connected, and a clear liquor outlet of the membrane treatment system (401) is connected with the purification reaction tank (501); the clear liquid outlet of the potassium chloride mother liquor tank (512) is connected with the inlet of the purifying liquid buffer tank (503).
9. The waste incineration fly ash recycling process according to claim 8, which is characterized in that: the purification reaction tank (501) is provided with a sodium carbonate/sodium sulfate inlet.
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| CN117960761B (en) * | 2024-03-28 | 2024-07-19 | 北京中科润宇环保科技股份有限公司 | Harmless near-zero emission system for waste incineration fly ash and working method |
| CN118180110A (en) * | 2024-03-28 | 2024-06-14 | 北京中科润宇环保科技股份有限公司 | System for cooperatively removing dioxin and heavy metals in waste incineration fly ash and working method |
| CN118417216A (en) * | 2024-07-05 | 2024-08-02 | 滁州明华包装有限公司 | Surface cleaning device for paperboard before printing |
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