CN111847797A - Zero-emission treatment system and method for leachate of waste incineration plant - Google Patents
Zero-emission treatment system and method for leachate of waste incineration plant Download PDFInfo
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- CN111847797A CN111847797A CN202010758292.0A CN202010758292A CN111847797A CN 111847797 A CN111847797 A CN 111847797A CN 202010758292 A CN202010758292 A CN 202010758292A CN 111847797 A CN111847797 A CN 111847797A
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- 238000004056 waste incineration Methods 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 95
- 239000012528 membrane Substances 0.000 claims abstract description 86
- 238000006243 chemical reaction Methods 0.000 claims abstract description 43
- 238000004821 distillation Methods 0.000 claims abstract description 36
- 238000010894 electron beam technology Methods 0.000 claims abstract description 23
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 claims abstract description 22
- 229910052567 struvite Inorganic materials 0.000 claims abstract description 22
- 238000005345 coagulation Methods 0.000 claims abstract description 19
- 230000015271 coagulation Effects 0.000 claims abstract description 19
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims abstract description 18
- 230000007062 hydrolysis Effects 0.000 claims abstract description 16
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 16
- 230000020477 pH reduction Effects 0.000 claims abstract description 16
- 238000004062 sedimentation Methods 0.000 claims abstract description 14
- 239000010802 sludge Substances 0.000 claims description 18
- 239000011777 magnesium Substances 0.000 claims description 12
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052698 phosphorus Inorganic materials 0.000 claims description 10
- 239000011574 phosphorus Substances 0.000 claims description 10
- 238000005188 flotation Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 7
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 6
- 229910052749 magnesium Inorganic materials 0.000 claims description 6
- 239000012510 hollow fiber Substances 0.000 claims description 4
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 14
- 239000010813 municipal solid waste Substances 0.000 description 10
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 230000004907 flux Effects 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000000149 chemical water pollutant Substances 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 230000001174 ascending effect Effects 0.000 description 4
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 4
- 229910001629 magnesium chloride Inorganic materials 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 229910000403 monosodium phosphate Inorganic materials 0.000 description 4
- 235000019799 monosodium phosphate Nutrition 0.000 description 4
- 229920002401 polyacrylamide Polymers 0.000 description 4
- -1 polypropylene Polymers 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 230000009615 deamination Effects 0.000 description 3
- 238000006481 deamination reaction Methods 0.000 description 3
- 208000028659 discharge Diseases 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 239000002033 PVDF binder Substances 0.000 description 2
- 239000004743 Polypropylene Substances 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000000701 coagulant Substances 0.000 description 2
- 230000001112 coagulating effect Effects 0.000 description 2
- 239000010791 domestic waste Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000001728 nano-filtration Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 229920001155 polypropylene Polymers 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- BNIILDVGGAEEIG-UHFFFAOYSA-L disodium hydrogen phosphate Chemical compound [Na+].[Na+].OP([O-])([O-])=O BNIILDVGGAEEIG-UHFFFAOYSA-L 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000002515 guano Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000009285 membrane fouling Methods 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/45—Phosphates containing plural metal, or metal and ammonium
- C01B25/451—Phosphates containing plural metal, or metal and ammonium containing metal and ammonium
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05B—PHOSPHATIC FERTILISERS
- C05B7/00—Fertilisers based essentially on alkali or ammonium orthophosphates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/305—Treatment of water, waste water, or sewage by irradiation with electrons
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5254—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using magnesium compounds and phosphoric acid for removing ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Inorganic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention relates to the technical field of sewage treatment, in particular to a zero-emission treatment system and method for leachate of a waste incineration plant. The treatment system comprises an adjusting tank, a hydrolysis acidification tank, a UASB anaerobic reaction tank, an air floatation tank, a struvite reaction tank, a sedimentation tank, an A/O reaction tank, an MBR membrane tank, electron beam irradiation equipment, a coagulation tank, a security filter and negative pressure membrane distillation equipment which are sequentially connected along the water flow direction. The zero-emission treatment system for the percolate generated by the refuse incineration plant can ensure that the quality of the treated percolate reaches the emission limit standard of the domestic refuse landfill control standard (GB16889 + 2008), has the advantages of good treatment effect, low cost and stable operation, can realize zero emission of the percolate after treatment, has better application and popularization prospects, and can realize stable production, cost reduction, efficiency improvement, driving protection and navigation protection of the refuse incineration plant.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a zero-emission treatment system and method for leachate of a waste incineration plant.
Background
The waste incineration power generation technology has the remarkable advantages of small occupied area, high mechanization degree, realization of reduction, harmlessness, resource treatment and the like of the waste, and is gradually replacing sanitary landfill to become the mainstream technology of urban domestic waste treatment in China. However, because the water content of domestic garbage in China is high at present, in order to improve the combustion heat value of the garbage, the garbage needs to be fermented before being incinerated, so that the garbage is cured and the water is drained, and a large amount of garbage leachate is generated in the process. Landfill leachate is organic polluted wastewater which is complex in water quality and high in pollutant concentration and difficult to treat, and if the organic polluted wastewater is directly discharged without treatment, soil and water can be seriously polluted, so that the health of urban residents is harmed. The zero-emission treatment of the landfill leachate is one of the hotspots in the industry at present, the requirements of the incineration process are fully considered aiming at the output characteristics and the pollutant characteristics of the landfill leachate, the stable production, cost reduction and efficiency improvement of the incineration plant and the high-efficiency treatment of the leachate are organically combined, the development is economical and reasonable, the technology is feasible, and the stable-running zero-emission treatment process of the leachate is imperative.
Chinese patent CN110510794A discloses a zero-discharge treatment device and method for landfill leachate. The method mainly uses a membrane treatment system to remove most of COD, ammonia nitrogen and total hardness in water, and converts the ammonia nitrogen into ammonium salt for resource utilization. The concentrated solution generated by the membrane treatment is subjected to low-temperature evaporation and solidification treatment to achieve the effect of zero emission. The disadvantages of this method are: firstly, leachate directly enters a nanofiltration unit without pretreatment, organic matters and suspended matters in water are easy to cause membrane fouling and blocking, and membranes are frequently cleaned/replaced, so that the stable operation of the whole process is influenced; secondly, the concentration of the ammonium sulfate solution generated by the membrane deamination unit is low, and further concentration is needed, so that additional energy consumption is generated. And a large amount of alkali is added to adjust the pH in the deamination process, so that the treatment cost is obviously increased. Thirdly, after the concentrated water enters the evaporation system, high-concentration organic matters in the concentrated water easily form an azeotrope, so that the evaporated condensed water contains a large amount of organic pollutants. The condensed water returns to the nanofiltration unit, and the organic matters in the condensed water aggravate the pollution and blockage of the unit.
Chinese patent CN110255728A discloses a novel combined process method and system for landfill leachate treatment. The method comprises pretreatment, ammonia nitrogen membrane separation, MBR, iron-carbon micro-electrolysis-Fenton, RO and evaporation units, can ensure that the effluent conductivity reaches the standard, and has the advantages of high recovery rate, stable water quality, near zero emission and the like. The method also faces the problem that the concentration of the ammonium salt solution generated by the membrane deamination unit can not reach the industrial use standard, and the resource utilization of ammonia is not really realized. Meanwhile, the iron raw material and the carbon raw material are separately used in the iron-carbon micro-electrolysis unit, so that the raw material is easily hardened and is difficult to clean and replace, and the treatment effect is also remarkably reduced.
Disclosure of Invention
The invention provides a zero-emission treatment system and a zero-emission treatment method for leachate of a waste incineration plant, which provide a new solution for the problems of difficulty in treatment of concentrated phase liquid after membrane, high operating cost and the like in the membrane method treatment process of the leachate of the waste at the present stage, the treated water quality can reach the emission limit standard of the control standard of a domestic waste landfill (GB16889 + 2008), and the zero-emission treatment system has a good application and popularization prospect, and can be used for stable production, cost reduction, efficiency improvement and driving protection of the waste incineration plant.
In order to achieve the purpose, the invention adopts the following technical scheme:
the utility model provides a zero release processing system of waste incineration factory filtration liquid, includes equalizing basin, hydrolysis-acidification pool, UASB anaerobic reaction jar, air supporting pond, guano stone reaction tank, sedimentation tank, AO reaction tank, MBR membrane tank, electron beam irradiation equipment, coagulating basin, cartridge filter and negative pressure membrane distillation plant that connect gradually along the rivers direction.
Preferably, among the zero release processing system of above-mentioned waste incineration plant leachate, still include sludge dewatering device, the sludge outlet of UASB anaerobic reaction tank, the dross export of air supporting pond, the sludge outlet of A/O reaction tank, the sludge outlet of MBR membrane cisterna, the sludge outlet of coagulating basin all with sludge dewatering device connects.
Preferably, in the zero-emission treatment system for leachate of a waste incineration plant, the MBR membrane tank is an external MBR membrane tank.
Preferably, in the zero-emission treatment system for leachate in a waste incineration plant, the external MBR membrane tank is internally provided with a curtain-type MBR membrane module.
Preferably, in the zero-discharge treatment system for leachate from a waste incineration plant, the membrane module in the negative pressure membrane distillation apparatus is a hollow fiber membrane module.
Preferably, among the zero release processing system of above-mentioned waste incineration plant leachate, negative pressure membrane distillation plant includes former water pitcher, be equipped with the heating steam coil pipe in the former water pitcher, the heating steam coil pipe is connected with the waste heat steam supply pipeline of waste incineration plant. The negative pressure membrane distillation equipment heats raw water by using waste heat steam.
Preferably, in the zero-discharge treatment system for leachate in a waste incineration plant, the concentrated water outlet of the negative pressure membrane distillation equipment is communicated with the hearth of the incinerator of the waste incineration plant through a spray head. And the concentrated water generated by the negative pressure membrane distillation equipment is sprayed back to the hearth of the incinerator of the garbage incineration plant.
The invention also provides a method for treating the percolate by adopting the zero-emission treatment system of the percolate of the waste incineration plant, which sequentially comprises the following steps of:
(1) the percolate enters a regulating tank to regulate the water quantity and the water quality;
(2) the effluent of the leachate enters a hydrolysis acidification tank for hydrolysis acidification treatment, and macromolecular organic matters are decomposed into micromolecular organic matters;
(3) the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank for anaerobic treatment;
(4) the effluent of the UASB anaerobic reaction tank enters an air floatation tank for air floatation treatment to remove part of suspended matters and surfactants;
(5) the effluent of the air flotation tank enters a struvite reaction tank;
(6) the effluent of the struvite reaction tank enters a sedimentation tank, and the formed struvite sediment is discharged;
(7) the effluent of the sedimentation tank enters an A/O reaction tank for biochemical treatment;
(8) the effluent of the A/O reaction tank enters an MBR membrane tank for treatment;
(9) the effluent of the MBR membrane tank enters electron beam irradiation equipment for electron beam irradiation treatment;
(10) the effluent of the electron beam irradiation equipment enters a coagulation tank for coagulation treatment;
(11) the effluent of the coagulation tank enters a security filter to remove suspended matters;
(12) and the effluent of the cartridge filter enters negative pressure membrane distillation equipment for concentration treatment to obtain membrane distillation produced water and membrane distillation concentrated water.
The membrane distillation produced water can be recycled to the production process, and the membrane distillation concentrated water is sprayed back to the hearth of the incinerator for treatment.
Preferably, in the method, in the step (6), the pH of the solution in the struvite reaction tank is adjusted to 8.0-9.0, and a magnesium source and a phosphorus source are added to adjust the content of Mg: n: the molar ratio of P is (0.8-1.4): 1: (0.8 to 1.5).
Preferably, in the above method, in the step (10), in the electron beam irradiation device, the energy of electrons accelerated by an accelerator is 0.5 to 5.0MeV, and the irradiation dose is 2 to 15 kGy.
Preferably, in the method, in the step (12), the raw water side temperature of the negative pressure membrane distillation equipment is 50-60 ℃, and the water generating side pressure is 40-50 kPa (absolute pressure).
The invention has the following beneficial effects:
(1) the treatment system and the method provided by the invention are utilized to treat the percolate of the waste incineration plant, the concentrated phase liquid after the membrane is deeply concentrated and can be directly sprayed back to the hearth of the incinerator, no additional treatment equipment is required to be built, no relevant treatment cost is generated, and the treatment system and the treatment method have the advantages of stable operation, guaranteed water quality of produced water and controllable cost;
(2) the invention utilizes the action of electron beams and water molecules to generate strong oxidant, destroys and removes refractory organics of the percolate, improves the deep treatment efficiency, and has the advantages of no secondary pollution and high treatment speed;
(3) the invention utilizes low-temperature low-pressure steam generated by an incineration plant as a heat source of the membrane distillation unit, thereby reducing the treatment energy consumption and cost of the percolate;
(4) the struvite sediment can be further processed to obtain struvite, and the struvite can be used as a high-quality fertilizer, so that economic benefits can be generated, and the recovery and resource utilization of ammonia nitrogen can be realized.
Drawings
Figure 1 shows a schematic view of a zero emission treatment system of percolate from a waste incineration plant according to the invention.
Detailed Description
In order to facilitate understanding of the present invention, the system and method for zero-emission treatment of leachate from a waste incineration plant according to the present invention will be further described with reference to the accompanying drawings and examples, which are not intended to limit the scope of the present invention.
Fig. 1 shows a schematic view of a zero-emission treatment system of percolate from waste incineration plants according to the present invention, comprising, connected in series:
(1) a regulating pool: the leachate enters an adjusting tank to adjust the water quantity and the water quality, so that the fluctuation of the production quantity and the water quality of the leachate caused by seasonal changes is reduced, and the balance and the stability of the water quantity and the water quality of a leachate treatment facility are ensured;
(2) a hydrolysis acidification pool: the effluent of the regulating reservoir enters a hydrolysis acidification pool, and the long-chain high molecular polymer in the water is destroyed and degraded in the hydrolysis acidification pool, so that the B/C ratio in the water is improved. After hydrolysis and acidification, the pH value of water is reduced to about 5.2, and the pH value is adjusted to 6.7-7.1 by using sodium carbonate so as to meet the condition of methanation in the UASB anaerobic reaction tank;
(3) UASB anaerobic reaction jar: the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank to remove most organic matters in the water;
(4) an air floatation tank: and (3) enabling the effluent of the UASB anaerobic reaction tank to enter an air floatation tank, removing a surfactant, floating oil and part of suspended matters which may exist in the effluent, and simultaneously realizing foam separation. The gas-water ratio is controlled to be 10: 1-30: 1, and the ascending flow rate is controlled to be 1.2-3 m/h;
(5) a struvite reaction tank: and (2) enabling the effluent of the air flotation tank to enter a struvite reaction tank, adding sodium hydroxide to adjust the pH of the water to be 8.0-9.0, using one or more of magnesium chloride, magnesium sulfate and magnesium oxide as a magnesium source, using sodium dihydrogen phosphate or sodium monohydrogen phosphate as a phosphorus source, and adjusting the ratio of Mg: n: the molar ratio of P is (0.8-1.4): 1: (0.8-1.5), the ammonia nitrogen concentration in the water is rapidly reduced;
(6) a sedimentation tank: the effluent of the struvite reaction tank enters a sedimentation tank for solid-liquid separation, and precipitates are collected at the bottom of the sedimentation tank and separated to obtain struvite precipitates;
(7) A/O + MBR biochemical treatment unit: and the effluent of the sedimentation tank enters an A/O + MBR biochemical treatment unit. The sludge concentration in the A/O reaction tank is 4-6 g/L, the anoxic zone mainly carries out denitrification on nitrate in water, the dissolved oxygen in the anoxic zone is controlled to be 0.2-0.5 mg/L, the aerobic zone removes organic matters in the water and carries out nitration reaction, and the dissolved oxygen in the aerobic zone is controlled to be 3-5 mg/L. The MBR membrane tank is externally arranged, a curtain type MBR ultrafiltration membrane is arranged in the membrane tank, and the membrane flux is 0.1-0.2 m3/(m2·d)；
(8) An electron beam irradiation unit: and (3) enabling effluent of the AO + MBR biochemical treatment unit to enter an electron beam irradiation device, and performing electron beam irradiation treatment to generate a large amount of strong oxidants such as hydroxyl free radicals, so as to remove part of COD, most of chroma and peculiar smell in water and destroy/modify part of macromolecular organic matters. Selecting an intermediate energy section (0.5-5.0 MeV) by an irradiation source accelerator of the electron beam irradiation equipment, wherein the irradiation dose is 2-15 kGy;
(9) a coagulation tank: and (3) enabling the effluent of the electron beam irradiation equipment to enter a coagulation tank, and adding a certain amount of coagulant to realize solid-liquid separation in the coagulation tank so as to remove suspended matters and partial COD in water. The coagulant is one or more of polymeric ferric sulfate, polymeric aluminum chloride and polyacrylamide, and the adding amount is 0.1-2 g/L;
(10) a cartridge filter: enabling the effluent of the coagulation tank to enter a cartridge filter to further remove suspended matters in the water, wherein the pore diameter range of the cartridge filter is 0.5-1 mu m;
(11) negative pressure membrane distillation equipment: and the effluent of the cartridge filter enters a negative pressure membrane distillation device for advanced treatment and concentration. The membrane component used by the negative pressure membrane distillation equipment is a hollow fiber type component, the membrane material is hydrophobic polyvinylidene fluoride, polypropylene or polytetrafluoroethylene, and the operation mode is an immersion type. The negative pressure membrane distillation equipment heats raw water by using waste heat steam, a heating steam coil of a raw water tank is communicated with a waste heat steam supply pipeline of a waste incineration plant, the steam temperature is 100-120 ℃, and the pressure is 0.2-0.4 MPa. Under the negative pressure condition, the negative pressure membrane distillation equipment can realize a better treatment effect at a lower temperature, and particularly, the temperature of the raw water side is maintained at 50-60 ℃, and the pressure of the produced water side is controlled at 40-50 kPa. The water molecules penetrating through the separation membrane are collected into produced water, the produced water has good quality and can be recycled, the volume of concentrated water is greatly reduced after concentration, and the concentrated water can be sprayed back to the hearth of the incinerator for treatment.
Further, sludge and scum produced by the UASB anaerobic tank, the AO + MBR unit, the coagulation tank and the air flotation tank are collected and dehydrated to reach the water content of below 60 percent, and then are put into an incinerator of a garbage incineration plant for incineration treatment.
Example 1
The basic water quality of the percolate of a certain garbage incineration plant in Hebei is as follows: the pH value is 6.7-6.8; the COD concentration is 58000-77000 mg/L; the ammonia nitrogen concentration is 680-800 mg/L; the total nitrogen concentration is about 1100-1240 mg/L. The leachate treatment system is utilized to treat leachate, and the specific method comprises the following steps:
1. the percolate enters a regulating tank to regulate the water quantity and the water quality;
2. the effluent of the regulating tank enters a hydrolysis acidification tank, after hydrolysis acidification, the pH value of the water is reduced to 5.3, and the pH value is regulated to 6.8-7.2 by using sodium carbonate so as to meet the condition of methanation produced in the UASB anaerobic reaction tank;
3. the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank to remove most organic matters in the water. The pH value of the effluent is 7.8-8.0, the COD concentration is 8300-11000 mg/L, the ammonia nitrogen concentration is 2200-2400 mg/L, and the SS is 9-12 g/L;
4. the effluent of the UASB anaerobic reaction tank enters an air floatation tank, the air-water ratio is controlled at 16:1, and the ascending flow rate is controlled at 2.0 m/h;
5. and (3) enabling the effluent of the air flotation tank to enter a struvite reaction tank, adding sodium hydroxide alkali liquor, adjusting the pH of water to be 8.9, using magnesium chloride as a magnesium source, using sodium dihydrogen phosphate as a phosphorus source, and adjusting the Mg content in the water: n: the molar ratio of P is 1.2: 1: 0.9, after treatment, the ammonia nitrogen concentration in the water is reduced to about 600 mg/L;
6. the effluent of the struvite reaction tank enters a sedimentation tank, and precipitates are collected at the bottom of the sedimentation tank and separated to obtain struvite precipitates;
7. and the effluent of the sedimentation tank enters an A/O + MBR biochemical treatment unit. The sludge concentration in the A/O reaction tank is 4.8g/L, the dissolved oxygen in the anoxic zone is controlled to be 0.3-0.4 mg/L, and the dissolved oxygen in the aerobic zone is controlled to be 4.0-4.5 mg/L. The membrane flux of the MBR membrane tank is 0.2m3/(m2D), effluent COD is 500-600 mg/L, ammonia nitrogen concentration is 30-42 mg/L, total nitrogen concentration is 55-73 mg/L, total phosphorus is 0.5-1.2 mg/L, and pH is 6.8-7.0;
8. and the effluent of the A/O + MBR biochemical unit enters electron beam irradiation equipment. An irradiation source accelerator of the electron beam irradiation equipment is an intermediate energy section (0.5-5.0 MeV), and the irradiation dose is controlled to be 9 kGy;
9. feeding the effluent of the electron beam irradiation equipment into a coagulation tank, and sequentially adding polymeric ferric sulfate and polyacrylamide in the amount of 1.2g/L and 1.0mg/L respectively;
10. the supernatant of the coagulation tank enters a cartridge filter to further remove suspended matters in water;
11. the outlet water of the cartridge filter enters negative pressure membrane distillation equipment. The membrane component used by the negative pressure membrane distillation equipment is a hollow fiber type component, the membrane material is hydrophobic polyvinylidene fluoride, the operation mode is an immersion type, the heating heat source is low-temperature steam generated by a waste incineration power plant, the steam temperature is 100-120 ℃, and the pressure is 0.2-0.4 MPa. The raw water side temperature of the negative pressure membrane distillation equipment is maintained at 55 ℃, the water production side pressure is controlled at 46kPa, and the average membrane flux is 25L/(m)2H) the salt rejection was about 99.7%. The concentrated water is sprayed back to the hearth of the incinerator.
The main indexes of the final effluent quality are as follows: the pH value is about 7, the COD concentration is 40-50 mg/L, the BOD concentration is 6-10 mg/L, the ammonia nitrogen concentration is 3-6 mg/L, the total nitrogen concentration is 12-15 mg/L, the total phosphorus concentration is 0.3-0.7 mg/L, the SS concentration is 10-20 mg/L, the chromaticity is 14-24, the conductivity is 40-55 us/cm, and the emission limit value standards in the table 3 of the household garbage landfill control standard (GB16889-2008) are all met.
In addition, sludge and scum produced by the UASB anaerobic tank, the AO + MBR unit, the coagulation tank and the air flotation tank are collected and dehydrated to reach the water content of below 60 percent, and then are put into an incinerator for incineration treatment.
Example 2
The basic water quality of percolate from a certain waste incineration plant in Jiangsu is as follows: the pH value is 6.4-6.8; the COD concentration is 45000-65000 mg/L; the ammonia nitrogen concentration is 520-690 mg/L; the total nitrogen concentration is about 820-1080 mg/L.
The leachate was treated as in example 1, with the difference that:
the pH value of the effluent of the adjusting tank is reduced to 5.3, and the pH value is adjusted to 6.9-7.0 by using sodium carbonate;
the air-water ratio of the air floatation tank is controlled at 20:1, and the ascending flow rate is controlled at 2.8 m/h;
adjusting the pH value of water in the struvite reaction tank to be 9.0, using magnesium chloride as a magnesium source, using sodium dihydrogen phosphate as a phosphorus source, and adjusting the ratio of Mg: n: the molar ratio of P is 1.1: 1: 1;
the sludge concentration in the A/O system is 4.5g/L, the dissolved oxygen in the anoxic zone is controlled to be 0.35-0.4 mg/L, and the dissolved oxygen in the aerobic zone is controlled to be 3.6-4.2 mg/L; the membrane flux of the MBR membrane tank is 0.18m3/(m2·d)；
The irradiation dose of the electron beam is controlled to be 9.6 kGy;
adding polymeric ferric sulfate and polyacrylamide into the coagulation tank, wherein the adding amount is 1.5g/L and 1.2mg/L respectively;
the negative pressure membrane distillation unit uses a membrane material of polypropylene, a heating heat source is low-temperature steam generated by a waste incineration power plant, the temperature of the steam is 110-120 ℃, and the pressure is 0.3-0.4 MPa. The raw water side temperature is maintained at 60 ℃, the water production side pressure is controlled at 50kPa, and the average membrane flux is 20L/(m)2·h)。
After the leachate is treated, the final effluent quality has the following main indexes: the pH value is about 6.9, the COD concentration is 44-49 mg/L, the BOD concentration is 6.4-13.2 mg/L, the ammonia nitrogen concentration is 3.7-6.6 mg/L, the total nitrogen concentration is 11-17 mg/L, the total phosphorus concentration is 0.2-0.7 mg/L, the SS concentration is 9-15 mg/L, the chroma is 10-20, and the conductivity is 50-66 us/cm, and all meet the emission limit value standard in table 3 of the control standard of domestic refuse landfill (GB 16889-.
Example 3
The basic water quality of the percolate of a certain waste incineration plant in Anhui province is as follows: the pH value is 6.5-6.7; the COD concentration is 60000-75000 mg/L; the ammonia nitrogen concentration is 800-920 mg/L; the total nitrogen concentration is about 1100-1200 mg/L.
The leachate was treated as in example 1, with the difference that:
the pH value of the effluent of the adjusting tank is reduced to 5.4, and the pH value is adjusted to 6.8-7.0 by using sodium carbonate;
the air-water ratio of the air floatation tank is controlled at 22:1, and the ascending flow rate is controlled at 3 m/h;
adjusting the pH value of water in the struvite reaction tank to be 9.0, using magnesium chloride as a magnesium source, using sodium dihydrogen phosphate as a phosphorus source, and adjusting the ratio of Mg: n: the molar ratio of P is 1.2: 1: 1;
the sludge concentration in the A/O system is 4.9g/L, the dissolved oxygen in the anoxic zone is controlled to be 0.3-0.4 mg/L, and the dissolved oxygen in the aerobic zone is controlled to be 3.8-4.4 mg/L; the membrane flux of the MBR membrane tank is 0.2m3/(m2·d)；
The irradiation dose of the electron beam is controlled to be 8.8 kGy;
adding polymeric ferric sulfate and polyacrylamide into the coagulation tank, wherein the adding amount is 1.8g/L and 1.6mg/L respectively;
the negative pressure membrane distillation unit uses polytetrafluoroethylene as a membrane material, a heating heat source is low-temperature steam generated by a waste incineration power plant, the temperature of the steam is 100-110 ℃, and the pressure is 0.2-0.3 MPa. The raw water side temperature is maintained at 48 ℃, the water production side pressure is controlled at 40kPa, and the average membrane flux is 18.6L/(m)2·h)。
After the leachate is treated, the final effluent quality has the following main indexes: the pH value is about 6.9, the COD concentration is 48-54 mg/L, the BOD concentration is 7.1-11.4 mg/L, the ammonia nitrogen concentration is 4-6 mg/L, the total nitrogen concentration is 12-15 mg/L, the total phosphorus concentration is 0.3-0.9 mg/L, the SS concentration is 11-20 mg/L, the chroma is 15-21, and the conductivity is 55-60 us/cm, which all meet the emission limit standard in table 3 of the municipal solid waste landfill control Standard (GB16889 + 2008).
Comparative example 1
Compared with example 1, the difference is only that: the water discharged by the electron beam irradiation equipment directly enters a negative pressure membrane distillation unit. Because a certain amount of suspended matters exist in water, the water yield of the negative pressure membrane distillation unit is reduced after the negative pressure membrane distillation unit operates for a period of time, the water quality of the produced water is deteriorated, and the membrane distillation unit needs to be cleaned in an acid cleaning and alkali cleaning mode to recover the treatment capacity of the membrane distillation unit.
Although the invention has been described in detail hereinabove by way of general description, specific embodiments and experiments, it will be apparent to those skilled in the art that many modifications and improvements can be made thereto based on the invention. Accordingly, such modifications and improvements are intended to be within the scope of the invention as claimed.
Claims (10)
1. The zero-emission treatment system for the leachate of the waste incineration plant is characterized by comprising an adjusting tank, a hydrolysis acidification tank, a UASB anaerobic reaction tank, an air flotation tank, a struvite reaction tank, a sedimentation tank, an A/O reaction tank, an MBR membrane tank, electron beam irradiation equipment, a coagulation tank, a security filter and negative pressure membrane distillation equipment which are sequentially connected along the water flow direction.
2. The zero-emission treatment system for leachate of waste incineration plant of claim 1, further comprising a sludge dewatering device, wherein the sludge outlet of the UASB anaerobic reaction tank, the scum outlet of the air flotation tank, the sludge outlet of the A/O reaction tank, the sludge outlet of the MBR membrane tank and the sludge outlet of the coagulation tank are connected with the sludge dewatering device.
3. The zero emission treatment system for leachate of a waste incineration plant of claim 1, wherein the MBR membrane tank is an external MBR membrane tank.
4. The zero emission treatment system for leachate of a waste incineration plant of claim 3, wherein a curtain MBR membrane module is arranged in the external MBR membrane tank.
5. The zero emission treatment system for leachate of waste incineration plant of claim 1, wherein the membrane module in the negative pressure membrane distillation apparatus is a hollow fiber membrane module.
6. The zero-emission treatment system for leachate of waste incineration plant of claim 1, wherein the negative pressure membrane distillation apparatus comprises a raw water tank, and a heating steam coil is disposed in the raw water tank and connected to a residual heat steam supply pipeline of the waste incineration plant.
7. The zero emission treatment system for leachate of waste incineration plant of claim 1, wherein the concentrated water outlet of the negative pressure membrane distillation apparatus is in communication with the incinerator furnace of the waste incineration plant through a spray nozzle.
8. A method for leachate treatment with the zero-emission treatment system for leachate of waste incineration plants according to any of claims 1 to 7, characterized in that it comprises the following steps in sequence:
(1) the percolate enters a regulating tank to regulate the water quantity and the water quality;
(2) the effluent of the leachate enters a hydrolysis acidification tank for hydrolysis acidification treatment, and macromolecular organic matters are decomposed into micromolecular organic matters;
(3) the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank for anaerobic treatment;
(4) the effluent of the UASB anaerobic reaction tank enters an air floatation tank for air floatation treatment to remove part of suspended matters and surfactants;
(5) the effluent of the air flotation tank enters a struvite reaction tank;
(6) the effluent of the struvite reaction tank enters a sedimentation tank, and the formed struvite sediment is discharged;
(7) the effluent of the sedimentation tank enters an A/O reaction tank for biochemical treatment;
(8) the effluent of the A/O reaction tank enters an MBR membrane tank for treatment;
(9) the effluent of the MBR membrane tank enters electron beam irradiation equipment for electron beam irradiation treatment;
(10) the effluent of the electron beam irradiation equipment enters a coagulation tank for coagulation treatment;
(11) the effluent of the coagulation tank enters a security filter to remove suspended matters;
(12) and the effluent of the cartridge filter enters negative pressure membrane distillation equipment for concentration treatment to obtain membrane distillation produced water and membrane distillation concentrated water.
9. The method according to claim 8, wherein in the step (6), the pH of the solution in the struvite reaction tank is adjusted to be 8.0-9.0, and the magnesium source and the phosphorus source are added to adjust the ratio of Mg: n: the molar ratio of P is (0.8-1.4): 1: (0.8 to 1.5).
10. The method according to claim 8 or 9, wherein in the step (10), in the electron beam irradiation apparatus, the energy of the electrons accelerated by the accelerator is 0.5 to 5.0MeV, and the irradiation dose is 2 to 15 kGy.
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