CN112694225A - Novel treatment system and purification method for landfill leachate - Google Patents
Novel treatment system and purification method for landfill leachate Download PDFInfo
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- CN112694225A CN112694225A CN202110038281.XA CN202110038281A CN112694225A CN 112694225 A CN112694225 A CN 112694225A CN 202110038281 A CN202110038281 A CN 202110038281A CN 112694225 A CN112694225 A CN 112694225A
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- tank
- sludge
- precipitation
- struvite
- landfill leachate
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- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 130
- 238000000746 purification Methods 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 22
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 129
- 229910052567 struvite Inorganic materials 0.000 claims abstract description 119
- 238000004062 sedimentation Methods 0.000 claims abstract description 108
- 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 105
- 230000001112 coagulating effect Effects 0.000 claims abstract description 73
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 63
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 50
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 50
- 239000004571 lime Substances 0.000 claims abstract description 50
- 239000007787 solid Substances 0.000 claims abstract description 20
- 239000000706 filtrate Substances 0.000 claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 123
- 239000010802 sludge Substances 0.000 claims description 96
- 238000001556 precipitation Methods 0.000 claims description 88
- 238000005345 coagulation Methods 0.000 claims description 73
- 230000015271 coagulation Effects 0.000 claims description 73
- 239000000243 solution Substances 0.000 claims description 72
- 238000005086 pumping Methods 0.000 claims description 70
- 239000006228 supernatant Substances 0.000 claims description 69
- 239000013049 sediment Substances 0.000 claims description 68
- 238000006243 chemical reaction Methods 0.000 claims description 51
- 238000000926 separation method Methods 0.000 claims description 47
- 238000005868 electrolysis reaction Methods 0.000 claims description 38
- 238000003756 stirring Methods 0.000 claims description 37
- 230000009467 reduction Effects 0.000 claims description 32
- 229910019142 PO4 Inorganic materials 0.000 claims description 26
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 24
- 238000007872 degassing Methods 0.000 claims description 22
- 230000018044 dehydration Effects 0.000 claims description 22
- 238000006297 dehydration reaction Methods 0.000 claims description 22
- 239000010452 phosphate Substances 0.000 claims description 21
- 159000000003 magnesium salts Chemical class 0.000 claims description 19
- 239000000701 coagulant Substances 0.000 claims description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 238000007599 discharging Methods 0.000 claims description 14
- 230000005484 gravity Effects 0.000 claims description 14
- 239000012266 salt solution Substances 0.000 claims description 14
- 239000000126 substance Substances 0.000 claims description 13
- 239000010865 sewage Substances 0.000 claims description 12
- 239000002244 precipitate Substances 0.000 claims description 11
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 10
- 230000003750 conditioning effect Effects 0.000 claims description 10
- 230000009615 deamination Effects 0.000 claims description 10
- 238000006481 deamination reaction Methods 0.000 claims description 10
- 238000001035 drying Methods 0.000 claims description 9
- 238000004806 packaging method and process Methods 0.000 claims description 9
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 8
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 8
- -1 ceramsite Substances 0.000 claims description 7
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 6
- 230000014759 maintenance of location Effects 0.000 claims description 6
- 239000000843 powder Substances 0.000 claims description 6
- 239000000047 product Substances 0.000 claims description 6
- 239000003638 chemical reducing agent Substances 0.000 claims description 5
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 5
- 238000007790 scraping Methods 0.000 claims description 5
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 4
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 4
- 239000000945 filler Substances 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims 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 claims description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 3
- 239000004575 stone Substances 0.000 claims description 3
- BNIILDVGGAEEIG-UHFFFAOYSA-L disodium hydrogen phosphate Chemical compound [Na+].[Na+].OP([O-])([O-])=O BNIILDVGGAEEIG-UHFFFAOYSA-L 0.000 claims description 2
- 229910000397 disodium phosphate Inorganic materials 0.000 claims description 2
- 235000019800 disodium phosphate Nutrition 0.000 claims description 2
- 239000007791 liquid phase Substances 0.000 claims description 2
- 229960002337 magnesium chloride Drugs 0.000 claims description 2
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 2
- 229940050906 magnesium chloride hexahydrate Drugs 0.000 claims description 2
- DHRRIBDTHFBPNG-UHFFFAOYSA-L magnesium dichloride hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-] DHRRIBDTHFBPNG-UHFFFAOYSA-L 0.000 claims description 2
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 claims description 2
- 229940061634 magnesium sulfate heptahydrate Drugs 0.000 claims description 2
- 229910000403 monosodium phosphate Inorganic materials 0.000 claims description 2
- 235000019799 monosodium phosphate Nutrition 0.000 claims description 2
- 239000011435 rock Substances 0.000 claims description 2
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 claims description 2
- 239000001488 sodium phosphate Substances 0.000 claims description 2
- 229910000162 sodium phosphate Inorganic materials 0.000 claims description 2
- 235000011008 sodium phosphates Nutrition 0.000 claims description 2
- 239000007790 solid phase Substances 0.000 claims description 2
- RYFMWSXOAZQYPI-UHFFFAOYSA-K trisodium phosphate Chemical compound [Na+].[Na+].[Na+].[O-]P([O-])([O-])=O RYFMWSXOAZQYPI-UHFFFAOYSA-K 0.000 claims description 2
- ASTWEMOBIXQPPV-UHFFFAOYSA-K trisodium;phosphate;dodecahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[Na+].[O-]P([O-])([O-])=O ASTWEMOBIXQPPV-UHFFFAOYSA-K 0.000 claims description 2
- 238000005554 pickling Methods 0.000 claims 3
- 238000012856 packing Methods 0.000 claims 2
- 230000033228 biological regulation Effects 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 10
- 238000004064 recycling Methods 0.000 abstract description 2
- 230000003851 biochemical process Effects 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 94
- 229910052757 nitrogen Inorganic materials 0.000 description 47
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 44
- 229910052698 phosphorus Inorganic materials 0.000 description 44
- 239000011574 phosphorus Substances 0.000 description 44
- 239000003344 environmental pollutant Substances 0.000 description 25
- 231100000719 pollutant Toxicity 0.000 description 25
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 17
- 241000894006 Bacteria Species 0.000 description 12
- 239000011651 chromium Substances 0.000 description 12
- 229910001385 heavy metal Inorganic materials 0.000 description 12
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 12
- 150000002500 ions Chemical class 0.000 description 11
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 10
- 229910001425 magnesium ion Inorganic materials 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 8
- 230000001546 nitrifying effect Effects 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 7
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 7
- 229910052785 arsenic Inorganic materials 0.000 description 7
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 7
- 229910052793 cadmium Inorganic materials 0.000 description 7
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 7
- 229910052804 chromium Inorganic materials 0.000 description 7
- JOPOVCBBYLSVDA-UHFFFAOYSA-N chromium(6+) Chemical compound [Cr+6] JOPOVCBBYLSVDA-UHFFFAOYSA-N 0.000 description 7
- 239000012528 membrane Substances 0.000 description 7
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 7
- 229910052753 mercury Inorganic materials 0.000 description 7
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 6
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 6
- 229910021529 ammonia Inorganic materials 0.000 description 6
- 235000010265 sodium sulphite Nutrition 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 5
- 241001148470 aerobic bacillus Species 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000000460 chlorine Substances 0.000 description 5
- 229910052801 chlorine Inorganic materials 0.000 description 5
- 238000012554 master batch record Methods 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000000376 reactant Substances 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 5
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 5
- 230000009935 nitrosation Effects 0.000 description 4
- 238000007034 nitrosation reaction Methods 0.000 description 4
- 238000001223 reverse osmosis Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000005259 measurement Methods 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- 235000015097 nutrients Nutrition 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000003002 pH adjusting agent Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 230000001953 sensory effect Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002550 fecal effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 239000002515 guano Substances 0.000 description 1
- GVALZJMUIHGIMD-UHFFFAOYSA-H magnesium phosphate Chemical compound [Mg+2].[Mg+2].[Mg+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O GVALZJMUIHGIMD-UHFFFAOYSA-H 0.000 description 1
- 239000004137 magnesium phosphate Substances 0.000 description 1
- 229960002261 magnesium phosphate Drugs 0.000 description 1
- 229910000157 magnesium phosphate Inorganic materials 0.000 description 1
- 235000010994 magnesium phosphates Nutrition 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
Images
Classifications
-
- 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
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
-
- 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
- C02F1/48—Treatment of water, waste water, or sewage with magnetic or electric fields
- C02F1/488—Treatment of water, waste water, or sewage with magnetic or electric fields for separation of magnetic materials, e.g. magnetic flocculation
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/70—Treatment of water, waste water, or sewage by reduction
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/143—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances
- C02F11/145—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances using calcium compounds
-
- 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
- C02F2001/46119—Cleaning the electrodes
-
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention discloses a novel treatment system and a purification method of landfill leachate. The garbage percolate sequentially passes through a lime coagulating sedimentation device to remove a large amount of solid particulate matters (SS), partial COD and BOD5The filtrate after coagulating sedimentation is further subjected to a struvite sedimentation ammonia nitrogen removal device to remove 90-95% of ammonia nitrogen in the leachate, so that the ammonia nitrogen in the effluent is less than 120mg/L, the ammonia nitrogen is recovered, the leachate after removing the ammonia nitrogen is subjected to biochemical treatment, a large amount of COD and BOD5 are removed, and then the leachate is subjected to coagulating sedimentation and electrolytic purification; the invention has the advantages of removing and recycling ammonia nitrogen by struvite precipitationThe biochemical process and the electrolytic process are organically combined, so that indexes such as ammonia nitrogen, COD, SS, chromaticity and the like in the landfill leachate can be effectively reduced, and the effluent is discharged after reaching the standard.
Description
Technical Field
The invention relates to a novel system and a purification method for landfill leachate, in particular to a system and a purification method for treating the landfill leachate and recovering ammonia nitrogen, and belongs to the field of environmental protection.
Background
The landfill leachate is a liquid seeped from a landfill, is high-ammonia nitrogen high-concentration organic wastewater which is difficult to treat, and mainly comes from the following three aspects: 1. natural rainfall and runoff in the landfill; 2. the water content of the garbage itself; 3. water released by decomposition of microorganisms after landfill; with precipitation in the landfill being the major component. Typical values of the municipal landfill leachate pollutant content are shown in table 1.1.
TABLE 1.1 general landfill leachate principal Components (in mg/L apart from pH and sensory indices)
| Item | Range of concentration variation | Item | Range of concentration variation |
| Sensory index | Black/malodor | Chloride compound | 189～3262 |
| pH value | 4～9 | Fe | 50～600 |
| Total hardness | 3000～10000 | Cu | 0.1～1.43 |
| CODCr | 1200～60000 | |
200～300 |
| |
200～19000 | Pb | 0.1～2.0 |
| NH3-N | 20～7400 | Cr | 0.01～2.61 |
| Total phosphorus | 1～70 | Hg | 0～0.032 |
As can be seen from table 1.1, the quality of landfill leachate has the following basic characteristics: first, the concentration of contaminants is high, ammonia nitrogen, COD and BOD5Most of the industrial pollutants are dozens to hundreds of times of the national emission standard of the industrial pollutants. Secondly, there are both organic and inorganic polluting components and at the same timeAlso contains some trace heavy metal pollution components, and has obvious comprehensive pollution characteristics; and thirdly, the proportion of the microbial nutrient elements in the leachate is seriously imbalanced, the ammonia nitrogen concentration is very high, the C/N ratio is imbalanced, the nutrient proportion is far away from that required by the growth of microorganisms during the biological treatment, and certain difficulty is brought to the biological treatment.
The ammonia nitrogen content and the COD concentration of the landfill leachate are high, so that the ground water body is anoxic and the water quality is deteriorated; the nutrient substances such as nitrogen and phosphorus are the causes of water eutrophication, and can also seriously affect the drinking water source; generally, the COD, BOD, BOD/COD decreases with "age" of the landfill and the alkalinity content increases. In addition, with the increase of the stacking age, the fresh garbage is gradually changed into the stale garbage, the content of organic matters in the percolate is reduced to some extent, but the content of ammonia nitrogen is increased, and the biodegradability is reduced, so the treatment difficulty is very high.
The key point for treating the landfill leachate is the treatment of COD and ammonia nitrogen, in particular to the treatment of ammonia nitrogen. The existing mainstream technology comprises the steps of pretreatment, flocculation precipitation, biochemical treatment, chemical strong oxidation, MBR, ultrafiltration, nanofiltration, reverse osmosis and the like, and combines the means of physicochemical treatment and biological treatment. Similarly, the landfill leachate disclosed in CN1478737 is a combined treatment of physical and chemical treatment and biological treatment, in which the leachate after electrolytic oxidation treatment is subjected to reverse osmosis treatment by using ceramic membrane. The technology achieves certain effect on treating the landfill leachate, but has the following outstanding problems:
1. in China, except for the warm climate in coastal areas of southeast, low temperature exists in winter in most areas, when the water temperature is lower than 15 ℃, the activity of nitrifying bacteria in a garbage leachate treatment facility is greatly reduced, the nitrification effect is poor, the ammonia nitrogen concentration of biochemical effluent reaches 500-1000 mg/L, some ammonia nitrogen is even higher, and the ammonia nitrogen cannot be eliminated by subsequent membrane treatment, so the ammonia nitrogen of the effluent seriously exceeds the standard;
2. the existing garbage leachate treatment process combining biochemistry and membrane filtration technology has membrane treatment comprising MBR, ultrafiltration, nanofiltration and reverse osmosis, long treatment process, more investment, more operation posts and high operation cost, and particularly about 30 percent of concentrated solution can only be re-filled into a landfill site except for evaporation treatment, so that salt is continuously accumulated, and the salt content of leachate is higher and higher. If evaporation treatment is adopted, the operating cost of concentrated solution treatment is as high as 150-200 yuan/ton, and the concentrated solution is spread to reach more than 45 yuan/ton per ton of landfill leachate.
3. After the leachate of most landfill sites is treated, the subsequent membrane process treatment is disturbed by the high ammonia nitrogen in the MBR effluent, and meanwhile, the waste of ammonia nitrogen resources is caused.
In view of the above problems, a new treatment equipment and technology for the leachate of garbage is urgently needed to solve the outstanding problem of the treatment of the leachate of garbage, replace MBR, ultrafiltration, nanofiltration and reverse osmosis equipment and technology after biochemical treatment of the leachate of garbage, and solve the problems of excessive ammonia nitrogen in the discharged water and membrane concentrated solution.
Disclosure of Invention
The invention aims to overcome the defects of complex treatment process, large consumption of chemical agents, high cost, substandard discharge of the treated landfill leachate, difficult treatment of membrane concentrated solution and the like in the conventional landfill leachate treatment technology, and combines ammonia nitrogen recovery, electrolytic purification and coagulation purification by adopting a struvite method to make up for the deficiencies of the ammonia nitrogen recovery, thereby forming a novel treatment system and a novel purification method for the landfill leachate.
The invention is realized by the following technical scheme: the novel treatment system of the landfill leachate comprises a lime coagulating sedimentation device, a struvite precipitation deamination and denitrification device, a biochemical treatment device, a coagulating sedimentation device, an electrolysis purification device and a reduction device which are sequentially connected. The garbage percolate sequentially passes through a lime coagulating sedimentation device to remove a large amount of solid particulate matters (SS), partial COD and BOD5A large amount of heavy metal ions and chromaticity, the filtrate after coagulating sedimentation is further subjected to struvite sedimentation deamination and denitrification device to remove 90-95% of ammonia nitrogen in the percolate, so that the ammonia nitrogen of the effluent is less than 120mg/L and the ammonia nitrogen is recovered, and the percolate after removing the ammonia nitrogen is subjected to biochemical treatment again to remove a large amount of COD and BOD5Then coagulating sedimentation and electrolytic cleaningMelting; the invention has the advantages that the indexes of ammonia nitrogen, COD, SS, chromaticity and the like in the landfill leachate can be effectively reduced through the organic combination of the process of removing struvite sediment and recycling ammonia nitrogen and the biochemical and electrolytic processes, so that the effluent is discharged up to the standard.
The effluent indexes of the garbage leachate treated by the novel treatment system and the purification method of the garbage leachate are as follows: the chroma is less than 5, the COD is less than 100mg/L, BOD and less than 20mg/L, SS and less than 10mg/L, the total nitrogen is less than 30mg/L, the ammonia nitrogen is less than 20mg/L, the total phosphorus is less than 0.3mg/L, the faecal coliform group number is less than 3/L, the total mercury is 0.001mg/L, the total chromium is 0.01mg/L, the total cadmium is 0.1mg/L, the hexavalent chromium is 0.05mg/L, the total arsenic is 0.1mg/L, and the total lead is 0.1 mg/L.
Compared with the prior art, the invention has the following obvious advantages:
1. the purified effluent indexes all meet the requirements of table 2 of the domestic refuse landfill pollutant control standard (GB16889-2008), and the problem that the ammonia nitrogen of the effluent in winter exceeds the standard in the existing landfill leachate treatment technology is solved;
2. the purified effluent completely meets the index requirements of table 2 of the standard for controlling pollutants in domestic refuse landfill (GB16889-2008), and no concentrated solution exists, so that the treatment problem of 25-30% membrane concentrated solution in the existing landfill leachate treatment technology is solved;
3. the high-concentration ammonia nitrogen in the leachate is recovered by adopting a struvite precipitation method, so that the ammonia nitrogen treatment problem of the landfill leachate is solved, and the slow-release fertilizer struvite is obtained, so that the ammonia nitrogen resource is fully utilized, and the industrial policy of national waste resource utilization is met;
4. the 'MBR + UF + NF + RO' process after the biochemical treatment of the existing landfill leachate is removed, not only the process flow is greatly shortened, but also the investment is reduced to a certain extent;
5. the operating cost of landfill leachate treatment is greatly reduced, and the operation profit of landfill leachate treatment enterprises is improved. Taking a 100 ton/day landfill leachate treatment project as an example, the produced concentrated solution is about 30 ton/day, the concentrated solution can only be subjected to evaporation treatment, and the treatment cost is up to 4500 yuan/day.
Drawings
In order to more clearly illustrate the technical solution of the present invention, the drawings needed for the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
Fig. 1 is a schematic connection diagram of the novel landfill leachate treatment system of the present invention.
Fig. 2 is a process flow diagram of the novel landfill leachate treatment system of the present invention.
Fig. 3 is a schematic structural view of the lime coagulating sedimentation device of the invention.
Fig. 4 is a schematic structural diagram of a struvite precipitation deamination nitrogen device of the invention.
FIG. 5 is a schematic view showing the structure of the biochemical processing apparatus according to the present invention.
FIG. 6 is a schematic structural view of the coagulating sedimentation device of the present invention.
FIG. 7 is a schematic view showing the construction of the electrolytic cleaning device of the present invention.
FIG. 8 is a schematic view of the structure of the reduction apparatus of the present invention.
FIG. 9 is a schematic view of the structure of a sludge treatment apparatus of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments of the present invention without any inventive step, are within the scope of the present invention.
Referring to fig. 1, a novel treatment system for landfill leachate includes: lime coagulating sedimentation device (100), guano stone deposit deamination nitrogen device (200), biochemical treatment device (300), coagulating sedimentation device (400), electrolysis purifier (500), reduction device (600) and sludge treatment device (700), it specifically constitutes as follows:
lime coagulating sedimentation device (100)
Referring to the attached drawing 3, the lime coagulating sedimentation device (100) is composed of a garbage leachate collecting and adjusting tank (111), a dosing tank (112), a coagulating reaction tank (110), a settling tank (120) and a supernatant storage tank (130), a water inlet of the coagulating reaction tank (110) is connected with a water outlet of the garbage leachate collecting and adjusting tank (111), a water outlet of the coagulating reaction tank (110) is connected with a water inlet of the settling tank (120), a supernatant water outlet (122) of the settling tank (120) is connected with a water inlet of the supernatant storage tank (130), a sludge outlet of the settling tank is connected with an inlet of a sludge concentration tank, and a water outlet of the supernatant storage tank is connected with a struvite precipitation deamination nitrogen device.
Struvite precipitation deamination nitrogen device (200)
Referring to fig. 4, the struvite precipitation deamination nitrogen apparatus (200) is composed of a struvite precipitation reaction kettle (210), a magnesium salt solution storage tank (213), a phosphate solution storage tank (217), a precipitation separation tank (220), a supernatant storage tank (230), a struvite precipitation concentration tank (241), a struvite precipitation dehydrator (240), a solid dryer (250) and a packaging machine; the magnesium salt solution storage tank (213) and the phosphate solution storage tank (217) are respectively connected with the struvite precipitation reaction kettle (210) through metering pumps (214) and (218) and flow meters (215) and (219); a stirrer (216) is also arranged on the struvite precipitation reaction kettle (210); the water inlet of struvite precipitation reation kettle (210) is connected with the delivery port of lime coagulating sedimentation device (100) supernatant storage tank (130), delivery port (212) of struvite precipitation reation kettle is connected with water inlet (222) of precipitation knockout drum, the delivery port and the water inlet of supernatant basin (230) of precipitation knockout drum (220) are connected, the precipitation export (224) of precipitation knockout drum (220) are connected with struvite precipitation concentration jar (241), the precipitation export of struvite precipitation concentration jar (241) and the access connection of struvite precipitation hydroextractor (240), supernatant export (242) and the water inlet of supernatant basin (230) of struvite precipitation concentration jar (241) are connected, the solid phase of struvite precipitation hydroextractor (240) is connected with the feed inlet of solid drying machine (250), the liquid phase of struvite precipitation hydroextractor (240) is connected with supernatant basin (230), the discharge port of the solid dryer is connected with the packaging machine.
Biochemical treatment device (300)
Referring to the attached drawing 5, the biochemical treatment device comprises an anaerobic tank (310), an anoxic tank (320), an aerobic tank (330), a secondary sedimentation tank (340) and an intermediate tank body (350), wherein the anaerobic tank (310), the anoxic tank (320), the aerobic tank (330) and the secondary sedimentation tank (340) are sequentially connected, a water inlet of the anaerobic tank (310) is connected with a water outlet of a supernatant storage tank (230) of the struvite precipitation deamination and denitrification device, a water outlet of the secondary sedimentation tank (340) is connected with a water inlet of the intermediate tank body (350), and a sludge outlet of the aerobic tank is connected with an inlet of a sludge concentration tank.
Coagulating sedimentation device (400)
Referring to fig. 6, the coagulating sedimentation device (400) comprises a pH adjusting tank (410), a coagulating tank (420), a coagulation aiding tank (430), a sedimentation tank (440) and an intermediate water tank (450) which are connected in sequence, wherein a supernatant outlet (442) is arranged at the top of the sedimentation tank (440), the supernatant outlet is connected with a water inlet of the intermediate water tank (450), a sludge outlet (441) is arranged at the bottom of the sedimentation tank, and the sludge outlet is connected with a sludge pump (444);
electrolysis purifier (500)
Referring to the attached figure 7, the electrolytic purification device comprises an electrolytic machine (510), a direct current power supply (520), a degassing tank (530) and an electrode cleaning device (540), wherein a water inlet of the electrolytic machine (510) is connected with a water outlet of an intermediate water pool (450) of effluent of the coagulating sedimentation device (400), a water outlet of the electrolytic machine (510) is connected with a water inlet of the degassing tank (530), a water outlet of the degassing tank (530) is connected with a water inlet pipe of the reduction device (600), a water outlet pipe of the degassing tank (530) is further provided with a circulating water pump (535) to be connected with the water inlet pipe of the electrolytic machine (510), the electrode cleaning device (540) is composed of an acid cleaning solution storage tank (541) and an acid cleaning solution delivery pump (542), and the acid cleaning solution adopts 2% -3% hydrochloric acid solution or 4% -5% citric acid solution.
Reduction device (600)
Referring to fig. 8, the reduction device (600) comprises a reduction tank (613) and a reducing agent solution storage tank (610), the reducing agent solution storage tank (610) is connected with the reduction tank (613) through a valve (611) and a dosing pump (612), a stirrer is further installed on the reduction tank (613), a water inlet of the reduction tank is connected with water outlet of the electrolytic purification device (500), and a water outlet of the reduction tank is connected with a water drainage pipe network.
Sludge treatment equipment (700)
Referring to fig. 9, the sludge treatment apparatus (700) includes a sludge pump (714), a sludge concentration tank (710), a physicochemical conditioning tank (720) and a dewatering machine (730), an inlet of the sludge pump (714) is respectively communicated with sludge outlets of the lime coagulating sedimentation device, the biochemical treatment device and the coagulating sedimentation device, the sludge concentration tank is a gravity concentration tank, an outlet of the sludge pump is communicated with an inlet of the gravity concentration tank, a sludge outlet of the gravity concentration tank is communicated with an inlet of the physicochemical conditioning tank, and a sewage outlet of the gravity concentration tank is communicated with a water inlet of the biochemical treatment device; the outlet of the physical and chemical conditioning pool is communicated with the sludge inlet of the dehydrator, the sludge blocks of the dehydrator are collected in the sludge collecting terrace, and the sewage of the dehydrator is communicated with the water inlet of the biochemical treatment device.
The anaerobic tank, the anoxic tank and the aerobic tank of the biochemical treatment device can also be filled with a filler, and the filler is one of volcanic rock, crushed stone, furnace slag, ceramsite, plastic rings or plastic balls.
The coagulating sedimentation device is one of a high-efficiency sedimentation device, a magnetic coagulation device and a supermagnetic coagulating sedimentation device.
The pH adjusting tank (410) of the coagulating sedimentation device further comprises a dosing device of a pH adjusting agent and a stirrer, wherein a sodium hydroxide or sodium carbonate solution with the mass ratio of 5-20% is stored in the pH adjusting agent dosing device.
The coagulating tank of the coagulating sedimentation device also comprises a coagulant dosing device and a stirrer, wherein a ferric sulfate solution, a ferric trichloride solution or a polyaluminium chloride solution with the mass ratio of 2-20% is stored in the coagulant dosing device; the coagulant aid tank further comprises a coagulant aid dosing device and a stirrer, and a PAM solution with the mass ratio of 1-2 per mill is stored in the coagulant aid dosing device.
A water inlet (531) of a degassing tank of the electrolytic purification device is connected with a water distributor (532) positioned at the bottom of the degassing tank, a water outlet at the upper part of the degassing tank is connected with a water inlet pipe of a reduction device of the device for reducing and eliminating sodium hypochlorite, and the top of the degassing tank is also provided with a slag scraper and a bubble collecting tank.
The sludge treatment device is respectively connected with sludge outlets of the lime coagulating sedimentation device (100), the biochemical treatment device (300) and the coagulating sedimentation device (400), an outlet of the sludge pump (714) is communicated with an inlet of the gravity concentration tank (710), an upper layer area, a middle layer area and a lower layer area are arranged in the gravity concentration tank (710) from top to bottom, a water outlet of the upper layer area is used for communicating a water inlet of the biochemical treatment device (300), an outlet of the lower layer area is communicated with an inlet of the dewatering machine (730), and a stirrer is further arranged in the gravity concentration tank (710).
A novel treatment method of landfill leachate adopts the novel treatment system of the landfill leachate to treat the landfill leachate, and comprises the following steps:
(1) lime coagulating sedimentation: the lime coagulating sedimentation is that the landfill leachate is quantitatively pumped into a coagulating reaction tank (110) from a landfill leachate collecting and regulating tank (111), and a stirrer is started to perform coagulation according to the ratio of 5-20 Kg/m3Adding lime powder, stirring and reacting for 15-20 minutes, stopping stirring after the reaction is finished, pumping the garbage percolate after the reaction into a settling tank (120) for settling for 30-60 minutes, pumping supernatant of the settling tank (120) into a supernatant storage tank (130), pumping sludge at the bottom of the settling tank (120) into a sludge concentration tank, pumping the sludge in the sludge concentration tank into a dehydrator for dehydration, wherein sludge blocks generated by dehydration of the dehydrator are sludge, and sewage generated by dehydration of the dehydrator is pumped into a garbage percolate collecting and adjusting tank; the lime coagulating sedimentation is mainly used for removing a large amount of SS, COD and BOD in the landfill leachate5Total phosphorus and various heavy metal ions are removed by more than 95 percent of SS, COD and BOD after lime precipitation treatment5More than 40% of the total phosphorus is removed, more than 80% of the total phosphorus is removed, and more than 90% of various heavy metal ions are removed;
(2) removing ammonia nitrogen by struvite precipitation: ammonia removal by struvite precipitationPumping the landfill leachate containing ammonia nitrogen after the lime coagulation sedimentation treatment in the step (1) into a struvite sedimentation reaction kettle (210) from a supernatant storage tank (130) in the step (1), adding a magnesium salt solution with a theoretical calculation amount of 1.1 times under the condition of continuous stirring, then adding a phosphate solution with a calculation amount of 1.1 times, reacting at room temperature for 15-30 minutes under continuous stirring, fully reacting ammonia ions, magnesium ions and phosphate ions in effluent after the landfill leachate is subjected to lime coagulation sedimentation to generate magnesium ammonium phosphate sediment, pumping the reaction product into a sedimentation separation tank (220) for standing, performing solid-liquid separation, pumping clear liquor at the upper part of the sedimentation separation tank (220) into a supernatant storage tank (230) for storage, pumping the magnesium ammonium phosphate sediment at the lower part of the sedimentation separation tank (220) into a struvite sedimentation concentration tank (241), and then pumping the struvite sedimentation dehydrator (240) for dehydration to obtain solid struvite sediment containing 40-60% of water and filtrate, pumping the filtrate into a supernatant storage tank, placing the solid struvite precipitate into a solid dryer for further drying, metering and packaging to obtain a struvite product; the molar ratio of reactants for removing ammonia nitrogen in the struvite precipitation reaction is as follows: NH (NH)4 +：Mg2+：PO4 3-1: 1.1: 1.1, removing ammonia nitrogen by the struvite sediment, wherein the ammonia nitrogen in the landfill leachate is mainly removed, and the ammonia nitrogen in the effluent of the landfill leachate after removing the ammonia nitrogen by the struvite sediment is less than 120 mg/L;
(3) biochemical treatment: the biochemical treatment comprises anaerobic treatment, anoxic treatment and aerobic treatment, the biochemical treatment is to pump the garbage leachate after ammonia nitrogen removal of the struvite sediment in the step (2) into a biochemical treatment device (300) and sequentially treat the garbage leachate through an anaerobic tank (310), an anoxic tank (320) and an aerobic tank (330), the retention time of the biochemical treatment is 96-240 hours, organic matters in the garbage leachate are decomposed by using anaerobic bacteria and aerobic bacteria, and COD (chemical oxygen demand) and BOD (biochemical oxygen demand) in the garbage leachate are deeply removed5Simultaneously, the residual ammonia nitrogen in the percolate is converted into nitrate nitrogen or nitrite nitrogen by utilizing the nitrification of nitrifying bacteria and the nitrosation of nitrosating bacteria; the nitrate nitrogen or nitrite nitrogen in the percolate is reduced into nitrogen by using the denitrification of denitrifying bacteria, and the biochemical treatment is mainly used for removing the chroma, COD and BOD in the landfill percolate5Part of the ammoniaNitrogen and total nitrogen, wherein the chroma of the effluent of the landfill leachate after biochemical treatment is less than 100, the ammonia nitrogen is less than 40mg/L, the total nitrogen is less than 70mg/L, the COD is less than 700mg/L, and the BOD5 is less than 200 mg/L;
(4) coagulating sedimentation: the landfill leachate sequentially flows into a pH adjusting tank (410), a coagulation tank (420), a coagulation assisting tank (430) and a sedimentation tank (440) of a coagulation precipitation device after biochemical treatment in the step (3), 5-15% of sodium hydroxide or 5-20% of sodium carbonate solution is added into the pH adjusting tank (410) to adjust the pH to 9-9.5, then the landfill leachate flows into the coagulation tank (420), and 12-30 g/m of the landfill leachate is added into the coagulation tank through a coagulant adding device under the stirring condition3The 2-10% PAC solution is reacted for 5min completely and then enters a coagulation aiding tank (430), and 1-2 g/m is added into the coagulation aiding tank (430)3Stirring and reacting the PAM for 1-2 min, feeding the PAM into a sedimentation tank (440) for solid-liquid separation, pumping supernatant into an intermediate water tank (450), conveying precipitates (namely sludge) into a sludge concentration tank through a pump and a pipeline, wherein the coagulation sedimentation is mainly used for removing main pollutants such as residual COD, BOD, total phosphorus, SS and the like of the garbage percolate after biochemical treatment, and after coagulation treatment, the chroma of effluent is less than 100, the COD is less than 300mg/L, BOD and less than 100mg/L, the total phosphorus is less than 0.3mg/L, SS and less than 10mg/L, the ammonia nitrogen is less than 40mg/L and the total nitrogen is less than 70 mg/L;
(5) electrolytic purification: the coagulation effluent which is subjected to coagulation precipitation in the step (4) and stored in the middle water tank (450) is pumped into an electrolytic machine (510) for electrolytic purification, the working voltage of the electrolytic machine is 5-150V, the current is 10-10000A, the electrolyzed supernatant enters a degassing tank (530) for gas-liquid separation, bubbles at the upper part are scraped into a bubble collecting tank through a residue scraping machine, the lower part clear solution is pumped into the electrolytic machine again through a circulating water pump (535) for further electrolytic purification until ammonia nitrogen, total nitrogen, COD and BOD are qualified and then discharged into a drainage pipe network, the electrolysis is mainly used for removing main pollutants such as residual COD, BOD, total phosphorus, SS, ammonia nitrogen and total nitrogen in the landfill leachate after the front section treatment, and the landfill effluent after the electrolytic purification meets the following indexes: the chroma is less than 5, the COD is less than 100mg/L, BOD and less than 20mg/L, SS and less than 10mg/L, the total nitrogen is less than 30mg/L, the ammonia nitrogen is less than 20mg/L, the total phosphorus is less than 0.3mg/L, the number of faecal coliform bacteria is less than 3/L, the total mercury is 0.001mg/L, the total chromium is 0.01mg/L, the total cadmium is 0.1mg/L, the hexavalent chromium is 0.05mg/L, the total arsenic is 0.1mg/L and the total lead is 0.1mg/L, and the effluent comprehensively meets the pollutant control indexes in the table 2 of the domestic garbage landfill pollutant control standard (GB 16889-2008);
(6) reduction: and (3) discharging the effluent of the landfill leachate which reaches the discharge standard after the electrolysis in the step (5) into a reduction tank, measuring the concentration of the rest chlorine, adding 5-25% of sodium sulfite solution by metering, and discharging the effluent into a municipal drainage pipe network after removing excessive sodium hypochlorite by quantitatively adding the sodium sulfite solution.
(7) Sludge treatment: scum of lime coagulating sedimentation (100), biochemical treatment (300), coagulating sedimentation (400) and electrolytic purification (500) are respectively conveyed into a sludge concentration tank (710) for gravity concentration to form supernatant on the upper part and sludge on the bottom; conveying the supernatant liquid to a water inlet pipe of a biochemical treatment device (300), and conveying bottom sludge into a physicochemical conditioning tank (720); adding a physical and chemical conditioner into the physical and chemical conditioning pool (720), conveying the physical and chemical conditioner into a dehydrator (730), treating the physical and chemical conditioner into organic mud blocks, collecting the organic mud blocks, and burning the mud blocks, wherein the physical and chemical conditioner comprises lime, ferric trichloride and polyaluminium chloride.
The magnesium salt in the step (2) is one of magnesium sulfate heptahydrate, magnesium chloride or magnesium chloride hexahydrate, when in use, the magnesium salt is prepared into a 20-50% solution and stored in a magnesium salt solution storage tank (213) for later use, and the addition amount is as follows:
the addition amount of the magnesium salt solution is (the molecular weight of the magnesium salt is multiplied by the ammonia nitrogen concentration of the effluent of the landfill leachate) multiplied by 1.1/18,
the phosphate is one of sodium phosphate dodecahydrate, sodium hydrogen phosphate, sodium dihydrogen phosphate or anhydrous sodium phosphate, when in use, the phosphate is prepared into a 15-25% solution and stored in a phosphate solution storage tank (217) for later use, and the addition amount is as follows:
the adding amount of the phosphate solution is (the molecular weight of the phosphate is multiplied by the ammonia nitrogen concentration of the effluent of the landfill leachate) multiplied by 1.1/18.
The novel garbage leachate treatment system and the garbage leachate treated by the treatment method have the following effluent indexes: the chroma is less than 5, the COD is less than 100mg/L, BOD and less than 20mg/L, SS and less than 10mg/L, the total nitrogen is less than 30mg/L, the ammonia nitrogen is less than 20mg/L, the total phosphorus is less than 0.3mg/L, the faecal coliform group number is less than 3/L, the total mercury is 0.001mg/L, the total chromium is 0.01mg/L, the total cadmium is 0.1mg/L, the hexavalent chromium is 0.05mg/L, the total arsenic is 0.1mg/L, and the total lead is 0.1 mg/L.
Example 1
100 ton/day percolate treatment project for certain refuse landfill
The measured water quality of the raw landfill leachate is shown in table 2.
Table 2 water quality of landfill leachate raw water.
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 16800 | 5 | Ammonia nitrogen | mg/L | 2850 |
| 2 | SS | mg/L | 570 | 6 | Color intensity | Multiple times | 1200 |
| 3 | BOD5 | mg/L | 2866 | 7 | Total nitrogen | mg/L | 3219 |
| 4 | Total phosphorus | mg/L | 50 | 8 | pH value | - | 6.8 |
Step one, lime coagulating sedimentation
The lime coagulating sedimentation is that the landfill leachate is quantitatively pumped into a coagulating reaction tank (110) from a landfill leachate collecting and regulating tank (111), and a stirrer is started to perform coagulation according to 5Kg/m3Adding lime powder, stirring and reacting for 15-20 minutes, stopping stirring after the reaction is finished, pumping the garbage percolate after the reaction into a settling tank (120) for settling for 30-60 minutes, pumping the supernatant of the settling tank (120) into a supernatant storage tank (130), and pumping the bottom of the settling tank (120)Pumping partial sludge into a sludge concentration tank, pumping the sludge in the sludge concentration tank into a dehydrator for dehydration, wherein sludge blocks generated by dehydration of the dehydrator are sludge, and pumping the sewage generated by dehydration of the dehydrator into a garbage percolate collecting and adjusting tank; the lime coagulating sedimentation is mainly used for removing a large amount of SS, COD, BOD5, total phosphorus and various heavy metal ions in the landfill leachate, after the lime sedimentation treatment, the SS is removed by more than 95%, the COD and BOD5 are removed by more than 40%, the total phosphorus is removed by more than 80%, and the various heavy metal ions are removed by more than 90%;
step two, ammonia nitrogen removal by struvite precipitation: the ammonia nitrogen removal of the struvite sediment is implemented by pumping the garbage percolate containing ammonia nitrogen after the lime coagulation sedimentation treatment in the step (1) into a struvite sediment reaction kettle (210) from a supernatant storage tank (130) in the step (1), adding a magnesium salt solution with a theoretical calculation amount of 1.1 times under the condition of continuous stirring, then adding a phosphate solution with a calculation amount of 1.1 times, reacting at room temperature for 15-30 minutes under continuous stirring, fully reacting ammonia ions in the percolate with magnesium ions and phosphate ions to generate magnesium ammonium phosphate sediment, pumping the magnesium ammonium phosphate sediment at the lower part of the sediment separation tank (220) into a sediment separation tank (220) after the reaction is finished, standing, performing solid-liquid separation, pumping clear liquor at the upper part of the sediment separation tank (220) into a supernatant storage tank (230) for storage, pumping the magnesium ammonium phosphate sediment at the lower part of the sediment separation tank (220) into a struvite sediment concentration tank (241), then pumping the magnesium phosphate sediment dewatering machine (240) into a solid struvite sediment, pumping the filtrate into a supernatant storage tank, placing the solid struvite precipitate into a solid dryer for further drying, metering and packaging to obtain a struvite product; the molar ratio of reactants for removing ammonia nitrogen in the struvite precipitation reaction is as follows: NH (NH)4 +：Mg2+：PO4 3-1: 1.1: 1.1, removing ammonia nitrogen by the struvite sediment, wherein the ammonia nitrogen in the landfill leachate is mainly removed, and the ammonia nitrogen in the effluent of the landfill leachate after removing the ammonia nitrogen by the struvite sediment is less than 112 mg/L;
step three, biochemical treatment
The biochemical treatment comprises anaerobic treatment, anoxic treatment and aerobic treatment, wherein the biochemical treatment is to pump the garbage percolate obtained after ammonia nitrogen removal of the struvite sediment in the step (2) into a biochemical treatment deviceSequentially treated by an anaerobic tank (310), an anoxic tank (320) and an aerobic tank (330), the retention time of biochemical treatment is 96-240 hours, the organic matters in the landfill leachate are decomposed by using anaerobic bacteria and aerobic bacteria, and COD and BOD in the landfill leachate are deeply removed5Simultaneously, the nitrification of nitrifying bacteria and the nitrosation of nitrosating bacteria are utilized to convert ammonia nitrogen into nitrate nitrogen or nitrite nitrogen; the biochemical treatment is mainly used for removing chroma, COD and BOD in the landfill leachate5Part of ammonia nitrogen and total nitrogen, the chroma of the effluent of the landfill leachate after biochemical treatment is less than 90, the ammonia nitrogen is less than 35mg/L, the total nitrogen is less than 60mg/L, the COD is 650mg/L, BOD5Less than 182 mg/L;
step four, coagulating sedimentation
The landfill leachate sequentially flows into a pH adjusting tank (410), a coagulation tank (420), a coagulation tank (430) and a sedimentation tank (440) of a coagulation precipitation device after biochemical treatment in the step (3), 5% of sodium hydroxide solution is added into the pH adjusting tank (410) to adjust the pH to 9-9.5, then the landfill leachate flows into the coagulation tank (420), 2% of PAC solution is added through a coagulant adding device under the stirring condition to react for 5min, the landfill leachate completely enters the coagulation tank (430), and 1g/m of the landfill leachate is added into the coagulation tank3Stirring and reacting the PAM for 1-2 min, feeding the PAM into a sedimentation tank (440) for solid-liquid separation, pumping supernatant into an intermediate water tank (450), conveying precipitates (namely sludge) into a sludge concentration tank through a pump and a pipeline, wherein the coagulation sedimentation is mainly used for removing main pollutants such as residual COD, BOD, total phosphorus, SS and the like of the garbage percolate after biochemical treatment, and after coagulation treatment, the chroma of effluent is less than 80, the COD is less than 295mg/L, BOD and less than 79mg/L, the total phosphorus is 0.21mg/L, SS and less than 10mg/L, the ammonia nitrogen is 35mg/L and the total nitrogen is 61 mg/L;
step five, electrolytic purification
The coagulation effluent pump that is deposited and stored in middle pond (450) through step (4) is gone into electrolysis machine (510) and is electrolyzed and purified, the operating voltage of electrolysis machine is 5V, and electric current 10000A, and the supernatant after the electrolysis gets into degasification jar (530) and carries out gas-liquid separation, and the bubble of upper portion is scraped into the bubble collecting vat through the scum machine, and the lower part clear solution is pumped into the electrolysis machine again through circulating water pump (535) and is further electrolyzed and purified to ammonia nitrogen, total nitrogen, COD, BOD and arrange into the drainage pipe network after BOD is qualified, electrolysis mainly is used for getting rid of remaining main pollutants such as COD, BOD, total phosphorus, SS, ammonia nitrogen and total nitrogen in the landfill leachate after anterior segment treatment, and the landfill effluent after the electrolysis purification satisfies following index: the effluent water has the color of 2, the COD of 89mg/L, BOD of 11mg/L, SS of 8mg/L, the total nitrogen of 27mg/L, the ammonia nitrogen of 2mg/L, the total phosphorus of 0.2mg/L, the faecal coliform group number of 3/L, the total mercury of 0.001mg/L, the total chromium of 0.01mg/L, the total cadmium of 0.1mg/L, the hexavalent chromium of 0.05mg/L, the total arsenic of 0.1mg/L and the total lead of 0.1mg/L, and the effluent water comprehensively meets the pollutant control indexes in the table 2 of the municipal solid waste landfill pollutant control Standard (GB 16889-2008);
step six, reduction
And discharging the effluent of the landfill leachate which reaches the discharge standard after the electrolysis in the fifth step into a reduction tank, measuring the concentration of the rest chlorine, adding a calculated amount of sodium sulfite solution, and discharging the effluent into a municipal drainage pipe network after eliminating excessive sodium hypochlorite.
TABLE 3 effluent quality of the treated landfill leachate
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 89 | 5 | Ammonia nitrogen | mg/L | 2 |
| 2 | SS | mg/L | 8 | 6 | Color intensity | Multiple times | 2 |
| 3 | Total phosphorus | mg/L | 0.2 | 7 | pH value | - | 7.2 |
| 4 | BOD5 | mg/L | 11 | 8 | Total nitrogen | mg/L | 27 |
Example 2
300 ton/day percolate treatment project for certain refuse landfill
The raw water of landfill leachate has the measurement indexes shown in table 4.
Table 4 water quality of landfill leachate raw water.
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 89600 | 5 | Ammonia nitrogen | mg/L | 3660 |
| 2 | SS | mg/L | 802 | 6 | Total nitrogen | mg/L | 3841 |
| 3 | Total phosphorus | mg/L | 1 | 7 | Color intensity | Multiple times | 2500 |
| 4 | BOD5 | mg/L | 17900 | 8 | pH value | - | 8.5 |
Step one, lime coagulating sedimentation
The lime coagulating sedimentation is that the landfill leachate is quantitatively pumped into a coagulating reaction tank (110) from a landfill leachate collecting and regulating tank (111), and a stirrer is started to feed the landfill leachate into the coagulating reaction tank according to the proportion of 20Kg/m3Adding lime powder, stirring and reacting for 15-20 minutes, stopping stirring after the reaction is finished, pumping the garbage percolate after the reaction into a settling tank (120) for settling for 30-60 minutes, pumping supernatant of the settling tank (120) into a supernatant storage tank (130), pumping sludge at the bottom of the settling tank into a sludge concentration tank, pumping the sludge in the sludge concentration tank into a dehydrator for dehydration, wherein sludge blocks generated by dehydration of the dehydrator are sludge blocksPumping sewage generated by dehydration of the dehydrator into a garbage percolate collecting and adjusting tank; the lime coagulating sedimentation is mainly used for removing a large amount of SS, COD, BOD5, total phosphorus and various heavy metal ions in the landfill leachate, after the lime sedimentation treatment, the SS is removed by more than 95%, the COD and BOD5 are removed by more than 40%, the total phosphorus is removed by more than 80%, and the various heavy metal ions are removed by more than 90%;
step two, ammonia nitrogen removal by struvite precipitation: the ammonia nitrogen removal of the struvite sediment is implemented by pumping the garbage percolate containing ammonia nitrogen after the lime coagulation sedimentation treatment in the step (1) into a struvite sediment reaction kettle (210) from a supernatant storage tank (130) in the step (1), adding a magnesium salt solution with a theoretical calculation amount of 1.1 times under the condition of continuous stirring, then adding a phosphate solution with a calculation amount of 1.1 times, reacting at room temperature for 15-30 minutes under continuous stirring, fully reacting ammonia ions in the percolate with magnesium ions and phosphate ions to generate magnesium ammonium phosphate sediment, pumping the ammonium magnesium phosphate sediment in the lower part of the sediment separation tank into the sediment separation tank (220) for standing after the reaction is finished, performing solid-liquid separation, pumping clear liquor in the upper part of the sediment separation tank (220) into a supernatant storage tank (230) for storage, pumping the magnesium ammonium phosphate sediment in the lower part of the sediment separation tank into a struvite sediment concentration tank (241), then pumping the magnesium ammonium phosphate sediment dewatering machine (240) into a struvite sediment dehydrator (240, pumping the filtrate into a supernatant storage tank, placing the solid struvite precipitate into a solid dryer for further drying, metering and packaging to obtain a struvite product; the molar ratio of reactants for removing ammonia nitrogen in the struvite precipitation reaction is as follows: NH (NH)4+：Mg2+：PO4 3-1: 1.1: 1.1, removing ammonia nitrogen by the struvite sediment, wherein the ammonia nitrogen in the landfill leachate is mainly removed, and the ammonia nitrogen in the effluent of the landfill leachate after removing the ammonia nitrogen by the struvite sediment is less than 112 mg/L;
step three, biochemical treatment
The biochemical treatment comprises anaerobic treatment, anoxic treatment and aerobic treatment, the biochemical treatment is to pump the garbage percolate obtained after ammonia nitrogen removal by struvite precipitation in the step (2) into a biochemical treatment device, the garbage percolate sequentially passes through an anaerobic tank (310), an anoxic tank (320) and an aerobic tank (330) for treatment, the retention time of the biochemical treatment is 96-240 hours, and anaerobic bacteria and aerobic bacteria are utilized to decompose the garbage percolateDeeply removing COD and BOD in the landfill leachate by using organic matters in the landfill leachate5Simultaneously, the nitrification of nitrifying bacteria and the nitrosation of nitrosating bacteria are utilized to convert ammonia nitrogen into nitrate nitrogen or nitrite nitrogen; the biochemical treatment is mainly used for removing chroma, COD and BOD in the landfill leachate5Part of ammonia nitrogen and total nitrogen, the chroma of the effluent of the landfill leachate after biochemical treatment is less than 90, the ammonia nitrogen is less than 35mg/L, the total nitrogen is less than 70mg/L, the COD is 700mg/L, and BOD5Less than 230 mg/L;
step four, coagulating sedimentation
The landfill leachate sequentially flows into a pH adjusting tank (410), a coagulation tank (420), a coagulation tank (430) and a sedimentation tank (440) of a coagulation precipitation device after biochemical treatment in the step (3), 5% of sodium hydroxide solution is added into the pH adjusting tank (410) to adjust the pH to 9-9.5, then the landfill leachate flows into the coagulation tank (420), 2% of PAC solution is added through a coagulant adding device under the stirring condition to react for 5min, the landfill leachate completely enters the coagulation tank (430), and 1g/m of the landfill leachate is added into the coagulation tank3Stirring and reacting the PAM for 1-2 min, performing solid-liquid separation in a sedimentation tank, pumping supernatant into an intermediate water tank (450), conveying sediment (namely sludge) into a sludge concentration tank through a pump and a pipeline, wherein the coagulating sedimentation is mainly used for removing main pollutants such as residual COD, BOD, total phosphorus, SS and the like of the biochemical landfill leachate, and after coagulating treatment, the chroma of effluent is less than 80, the COD is less than 300mg/L, BOD and less than 129mg/L, the total phosphorus is 0.17mg/L, SS and less than 10mg/L, the ammonia nitrogen is 23mg/L and the total nitrogen is 70 mg/L;
step five, electrolytic purification
The coagulation effluent which is subjected to coagulation precipitation in the step (4) and stored in the middle water tank (450) is pumped into an electrolysis machine (510) for electrolysis and purification, the working voltage of the electrolysis machine is 45V, the current is 6000A, the electrolyzed supernatant enters a degassing tank (530) for gas-liquid separation, bubbles at the upper part are scraped into a bubble collecting tank through a residue scraping machine, and the lower part clear liquid is pumped into the electrolysis machine again through a circulating water pump (535) for further electrolysis and purification until ammonia nitrogen, total nitrogen, COD and BOD are obtained5Discharging the qualified waste water into a drainage pipe network, wherein the electrolysis is mainly used for removing residual COD, BOD, total phosphorus and the like in the landfill leachate after the front-stage treatment,Main pollutants such as SS, ammonia nitrogen and total nitrogen, and the like, and the effluent of the garbage after electrolytic purification meets the following indexes: the effluent water has the color of 2, the COD of 94mg/L, BOD of 17mg/L, SS of 6mg/L, the total nitrogen of 35mg/L, the ammonia nitrogen of 5mg/L, the total phosphorus of 0.11mg/L, the number of faecal coliform groups of 3/L, the total mercury of 0.001mg/L, the total chromium of 0.01mg/L, the total cadmium of 0.1mg/L, the hexavalent chromium of 0.05mg/L, the total arsenic of 0.1mg/L and the total lead of 0.1mg/L, and the effluent water comprehensively meets the pollutant control indexes in the table 2 of the municipal solid waste landfill pollutant control Standard (GB 16889-2008);
step six, reduction
And discharging the effluent of the landfill leachate which reaches the discharge standard after the electrolysis in the fifth step into a reduction tank, measuring the concentration of the rest chlorine, adding a calculated amount of sodium sulfite solution, and discharging the effluent into a municipal drainage pipe network after eliminating excessive sodium hypochlorite.
TABLE 5 effluent quality of landfill leachate after treatment
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 94 | 5 | Ammonia nitrogen | mg/L | ≤5 |
| 2 | SS | mg/L | 6 | 6 | Color intensity | Multiple times | 2 |
| 3 | Total phosphorus | mg/L | 0.11 | 7 | pH value | - | 7.2 |
| 4 | BOD5 | mg/L | 17 | 8 | Total nitrogen | mg/L | ≤35 |
Example 3
Leachate treatment project for certain refuse landfill with 50 tons/day
The raw water of landfill leachate has the measurement indexes shown in table 6.
Table 6 quality of raw landfill leachate.
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 20430 | 5 | Ammonia nitrogen | mg/L | 2510 |
| 2 | SS | mg/L | 1381 | 6 | Color intensity | Multiple times | 4500 |
| 3 | Total phosphorus | mg/L | 70 | 7 | pH value | - | 6.5 |
| 4 | BOD5 | mg/L | 42800 | 8 | Total nitrogen | mg/L | 2799 |
Step one, lime coagulating sedimentation
The lime coagulating sedimentation is that the landfill leachate is quantitatively pumped into a coagulating reaction tank (110) from a landfill leachate collecting and regulating tank (111), and a stirrer is started to be at 12Kg/m3Adding lime powder, carrying out stirring reaction for 15-20 minutes, stopping stirring after the reaction is finished, pumping the garbage percolate after the reaction into a settling tank (120) for settling for 30-60 minutes, pumping supernatant of the settling tank (120) into a supernatant storage tank (130), pumping sludge at the bottom of the settling tank into a sludge concentration tank, pumping the sludge in the sludge concentration tank into a dehydrator for dehydration, wherein sludge blocks generated by dehydration of the dehydrator are sludge, and sewage generated by dehydration of the dehydrator is pumped into a garbage percolate collecting and adjusting tank; the lime precipitation is mainly used for removing garbage infiltrationAfter lime precipitation treatment, a large amount of SS, COD, BOD5, total phosphorus and various heavy metal ions in the filtrate are removed by more than 95%, COD and BOD5 are removed by more than 40%, total phosphorus is removed by more than 80%, and various heavy metal ions are removed by more than 90%;
step two, ammonia nitrogen removal by struvite precipitation: the ammonia nitrogen removal of the struvite sediment is implemented by pumping the garbage percolate containing ammonia nitrogen after the lime coagulation sedimentation treatment in the step (1) into a struvite sediment reaction kettle (210) from a supernatant storage tank (130) in the step (1), adding a magnesium salt solution with a theoretical calculation amount of 1.1 times under the condition of continuous stirring, then adding a phosphate solution with a calculation amount of 1.1 times, reacting at room temperature for 15-30 minutes under continuous stirring, fully reacting ammonia ions in the percolate with magnesium ions and phosphate ions to generate magnesium ammonium phosphate sediment, pumping the ammonium magnesium phosphate sediment in the lower part of the sediment separation tank into the sediment separation tank (220) for standing after the reaction is finished, performing solid-liquid separation, pumping clear liquor in the upper part of the sediment separation tank (220) into a supernatant storage tank (230) for storage, pumping the magnesium ammonium phosphate sediment in the lower part of the sediment separation tank into a struvite sediment concentration tank (241), then pumping the magnesium ammonium phosphate sediment dewatering machine (240) into a struvite sediment dehydrator (240, pumping the filtrate into a supernatant storage tank, placing the solid struvite precipitate into a solid dryer for further drying, metering and packaging to obtain a struvite product; the molar ratio of reactants for removing ammonia nitrogen in the struvite precipitation reaction is as follows: NH (NH)4 +：Mg2+：PO4 3-1: 1.1: 1.1, removing ammonia nitrogen by the struvite sediment, wherein the ammonia nitrogen in the landfill leachate is mainly removed, and the ammonia nitrogen in the effluent of the landfill leachate after removing the ammonia nitrogen by the struvite sediment is less than 96 mg/L;
step three, biochemical treatment
The biochemical treatment comprises anaerobic treatment, anoxic treatment and aerobic treatment, the biochemical treatment is to pump the garbage percolate subjected to ammonia nitrogen removal by struvite precipitation in the step (2) into a biochemical treatment device, the garbage percolate sequentially passes through an anaerobic tank (310), an anoxic tank (320) and an aerobic tank (330) for treatment, the retention time of the biochemical treatment is 160 hours, organic matters in the garbage percolate are decomposed by using anaerobic bacteria and aerobic bacteria, and COD (chemical oxygen demand) and BOD (biochemical oxygen demand) in the garbage percolate are deeply removed5Simultaneously utilizes the nitrification of nitrifying bacteriaNitrite action of nitrifying bacteria enables ammonia nitrogen to be converted into nitrate nitrogen or nitrite nitrogen; the biochemical treatment is mainly used for removing chroma, COD and BOD in the landfill leachate5Part of ammonia nitrogen and total nitrogen, the chroma of the effluent of the landfill leachate after biochemical treatment is less than 86, the ammonia nitrogen is less than 32mg/L, the total nitrogen is less than 65mg/L, the COD is 580mg/L, BOD5Less than 210 mg/L;
step four, coagulating sedimentation
The garbage leachate is subjected to biochemical treatment in the step (3), then flows into a pH adjusting tank (410), a coagulation tank (420), a coagulation assisting tank (430) and a sedimentation tank (440) of a coagulation precipitation device in sequence, 15% of sodium carbonate solution is added into the pH adjusting tank (410) to adjust the pH to 9-9.5, then flows into the coagulation tank (420), 5% of ferric trichloride solution is added through a coagulant adding device under the stirring condition to react for 5min completely, then the mixture enters the coagulation assisting tank (430), 1g/m3 PAM is added into the coagulation assisting tank to stir for 1-2 min, then the mixture enters the sedimentation tank to perform solid-liquid separation, supernatant is pumped into an intermediate water tank (450), precipitates (namely sludge) are sent into a sludge concentration tank through a pump and a pipeline, the coagulation precipitation is mainly used for removing main pollutants such as residual COD, total phosphorus, SS and the like of the biochemical garbage leachate, and the like, and after the coagulation treatment, the chroma of effluent is less than 70, COD is less than 290mg/L, BOD and less than 99mg/L, total phosphorus is 0.13mg/L, SS and less than 10mg/L, ammonia nitrogen is 31.5mg/L, and total nitrogen is 65 mg/L;
step five, electrolytic purification
The coagulation effluent which is subjected to coagulation precipitation in the step (4) and stored in the middle water tank (450) is pumped into an electrolysis machine (510) for electrolysis and purification, the working voltage of the electrolysis machine is 150V, the current is 2000A, the electrolyzed supernatant enters a degassing tank (530) for gas-liquid separation, bubbles at the upper part are scraped into a bubble collecting tank through a residue scraping machine, the lower part clear solution is pumped into the electrolysis machine again through a circulating water pump (535) for further electrolysis and purification until ammonia nitrogen, total nitrogen, COD and BOD are qualified and then is discharged into a drainage pipe network, the electrolysis is mainly used for removing main pollutants such as residual COD, BOD, total phosphorus, SS, ammonia nitrogen and total nitrogen in the landfill leachate after front-stage treatment, and the landfill effluent after electrolysis and purification meets the following indexes: the color is 2, the COD is 87mg/L, BOD and is 13mg/L, SS and is 7mg/L, the total nitrogen is 29mg/L, the ammonia nitrogen is 6.5mg/L, the total phosphorus is 0.12mg/L, the number of faecal coliform groups is 3/L, the total mercury is 0.001mg/L, the total chromium is 0.01mg/L, the total cadmium is 0.1mg/L, the hexavalent chromium is 0.05mg/L, the total arsenic is 0.1mg/L and the total lead is 0.1mg/L, and the effluent comprehensively meets the pollutant control indexes in the table 2 of the municipal solid waste landfill pollutant control standard (GB 16889-2008);
step six, reduction
And D, discharging the effluent of the landfill leachate which reaches the discharge standard after the electrolytic purification in the fifth step into a reduction tank, measuring the concentration of the rest chlorine, adding a calculated amount of sodium sulfite solution, and discharging the effluent into a municipal drainage pipe network after eliminating excessive sodium hypochlorite.
TABLE 7 effluent quality of landfill leachate after treatment
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 87 | 5 | Ammonia nitrogen | mg/L | 6.5 |
| 2 | SS | mg/L | 7 | 6 | Color intensity | Multiple times | 2 |
| 3 | Total phosphorus | mg/L | 0.12 | 7 | pH value | - | 7.2 |
| 4 | BOD5 | mg/L | 13 | 8 | Total nitrogen | mg/L | 29 |
Example 4
Experiment for treating landfill leachate in certain laboratory
The raw water of landfill leachate has the measurement indexes shown in Table 8.
Table 8 water quality of landfill leachate raw water.
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 10230 | 5 | Ammonia nitrogen | mg/L | 1450 |
| 2 | SS | mg/L | 1381 | 6 | Color intensity | Multiple times | 900 |
| 3 | Total phosphorus | mg/L | 23 | 7 | pH value | - | 6.5 |
| 4 | BOD5 | mg/L | 2800 | 8 | Total nitrogen | mg/L | 1750 |
Step one, lime coagulating sedimentation
The lime coagulating sedimentation is that the landfill leachate is quantitatively pumped into a coagulating reaction tank (110) from a landfill leachate collecting and regulating tank (111), and a stirrer is started to carry out coagulation according to 8Kg/m3Adding lime powder, carrying out stirring reaction for 15-20 minutes, stopping stirring after the reaction is finished, pumping the garbage percolate after the reaction into a settling tank (120) for settling for 30-60 minutes, pumping supernatant of the settling tank (120) into a supernatant storage tank (130), pumping sludge at the bottom of the settling tank into a sludge concentration tank, pumping the sludge in the sludge concentration tank into a dehydrator for dehydration, wherein sludge blocks generated by dehydration of the dehydrator are sludge, and sewage generated by dehydration of the dehydrator is pumped into a garbage percolate collecting and adjusting tank; the lime precipitation is mainly used for removing a large amount of SS, COD and BOD in the landfill leachate5Total phosphorus and various heavy metal ions are removed by more than 95 percent of SS, COD and BOD after lime precipitation treatment5More than 40% of the total phosphorus is removed, more than 80% of the total phosphorus is removed, and more than 90% of various heavy metal ions are removed;
step two, ammonia nitrogen removal by struvite precipitation: the ammonia nitrogen removal of the struvite sediment is implemented by pumping the garbage percolate containing ammonia nitrogen after the lime coagulation sedimentation treatment in the step (1) into a struvite sediment reaction kettle (210) from a supernatant storage tank (130) in the step (1), adding a magnesium salt solution with a theoretical calculation amount of 1.1 times under the condition of continuous stirring, then adding a phosphate solution with a calculation amount of 1.1 times, reacting at room temperature for 15-30 minutes under continuous stirring, fully reacting ammonia ions in the percolate with magnesium ions and phosphate ions to generate magnesium ammonium phosphate sediment, pumping the ammonium magnesium phosphate sediment in the lower part of the sediment separation tank into the sediment separation tank (220) for standing after the reaction is finished, performing solid-liquid separation, pumping clear liquor in the upper part of the sediment separation tank (220) into a supernatant storage tank (230) for storage, pumping the magnesium ammonium phosphate sediment in the lower part of the sediment separation tank into a struvite sediment concentration tank (241), then pumping the magnesium ammonium phosphate sediment dewatering machine (240) into a struvite sediment dehydrator (240, pumping the filtrate into a supernatant storage tank, placing the solid struvite precipitate into a dryer for further drying, metering and packaging to obtain a struvite product; the molar ratio of reactants for removing ammonia nitrogen in the struvite precipitation reaction is as follows: NH (NH)4 +：Mg2+：PO4 3-1: 1.1: 1.1, removing ammonia nitrogen by the struvite sediment, wherein the ammonia nitrogen in the landfill leachate is mainly removed, and the ammonia nitrogen in the effluent of the landfill leachate after removing the ammonia nitrogen by the struvite sediment is less than 88.5 mg/L;
step three, biochemical treatment
The biochemical treatment comprises anaerobic treatment, anoxic treatment and aerobic treatment, wherein the biochemical treatment is to pump the garbage leachate obtained after ammonia nitrogen removal by struvite precipitation in the step (2) into a biochemical treatment device, sequentially pass through an anaerobic tank (310), an anoxic tank (320) and an aerobic tank (330) for treatment, the retention time of the biochemical treatment is 200 hours, organic matters in the garbage leachate are decomposed by using anaerobic bacteria and aerobic bacteria, COD (chemical oxygen demand) and BOD5 in the garbage leachate are deeply removed, and ammonia nitrogen is converted into nitrate nitrogen or nitrite nitrogen by using nitrification of nitrifying bacteria and nitrosation of the nitrifying bacteria; the biochemical treatment is mainly used for removing the chroma in the landfill leachate,COD, BOD5, partial ammonia nitrogen and total nitrogen, the chroma of the effluent of the landfill leachate after biochemical treatment is less than 70, the ammonia nitrogen is less than 22mg/L, the total nitrogen is less than 55mg/L, the COD is 600mg/L, and the BOD5Less than 185 mg/L;
step four, coagulating sedimentation
The landfill leachate sequentially flows into a pH adjusting tank (410), a coagulation tank (420), a coagulation tank (430) and a sedimentation tank (440) of a coagulation precipitation device after biochemical treatment in the step (3), 10% of sodium carbonate solution is added into the pH adjusting tank (410) to adjust the pH to 9-9.5, then the landfill leachate flows into the coagulation tank (420), 5% of ferric sulfate solution is added through a coagulant adding device under the stirring condition to react for 5min, and then the landfill leachate enters the coagulation tank (430), and 1g/m is added into the coagulation tank3Stirring and reacting the PAM for 1-2 min, performing solid-liquid separation in a sedimentation tank, pumping supernatant into an intermediate water tank (450), conveying sediment (namely sludge) into a sludge concentration tank through a pump and a pipeline, wherein the coagulating sedimentation is mainly used for removing main pollutants such as residual COD, BOD, total phosphorus, SS and the like in the garbage percolate after biochemical treatment, and after coagulating treatment, the chroma of effluent is less than 70, the COD is less than 289mg/L, BOD and less than 108mg/L, the total phosphorus is 0.12mg/L, SS and less than 8mg/L, the ammonia nitrogen is 26.2mg/L and the total nitrogen is 55 mg/L;
step five, electrolytic purification
The coagulation effluent which is subjected to coagulation precipitation in the step (4) and stored in the middle water tank (450) is pumped into an electrolysis machine (510) for electrolysis and purification, the working voltage of the electrolysis machine is 25V, the current is 10A, the electrolyzed supernatant enters a degassing tank (530) for gas-liquid separation, bubbles at the upper part are scraped into a bubble collecting tank through a residue scraping machine, and the lower part clear solution is pumped into the electrolysis machine again through a circulating water pump (535) for further electrolysis and purification until ammonia nitrogen, total nitrogen, COD and BOD are obtained5Discharging the qualified waste leachate into a drainage pipe network, wherein the electrolysis is mainly used for removing residual COD and BOD in the landfill leachate after the front-stage treatment5Main pollutants such as total phosphorus, SS, ammonia nitrogen and total nitrogen, and the waste effluent after electrolytic purification meets the following indexes: the chroma is 2, the COD is 81mg/L, BOD519mg/L, SS of 7mg/L, total nitrogen of 33mg/L, ammonia nitrogen of 2.5mg/L, total phosphorus of 0.11mg/L, fecal coliform number of 3/L, total mercury of 0.001mg/L and total chromium of 3/L0.01mg/L, 0.1mg/L of total cadmium, 0.05mg/L of hexavalent chromium, 0.1mg/L of total arsenic and 0.1mg/L of total lead, and the effluent comprehensively meets the pollutant control indexes in the table 2 of the Standard for controlling pollutants in municipal solid waste landfills (GB 16889-2008);
step six, reduction
And D, discharging the effluent of the landfill leachate which reaches the discharge standard after the electrolytic purification in the fifth step into a reduction tank, measuring the concentration of the rest chlorine, adding a calculated amount of sodium sulfite solution, and discharging the effluent into a municipal drainage pipe network after eliminating excessive sodium hypochlorite.
TABLE 9 effluent quality of landfill leachate after treatment
| Serial number | Item | Unit of | Measured value | Serial number | Item | Unit of | Measured value |
| 1 | CODCr | mg/L | 81 | 5 | Ammonia nitrogen | mg/L | 2.5 |
| 2 | SS | mg/L | 7 | 6 | Color intensity | Multiple times | 2 |
| 3 | Total phosphorus | mg/L | 0.11 | 7 | pH value | - | 7.2 |
| 4 | BOD5 | mg/L | 19 | 8 | Total nitrogen | mg/L | 33 |
While the foregoing description shows and describes the preferred embodiments of the present invention, it is to be understood that the invention is not limited to the forms disclosed herein, but is not to be construed as excluding other embodiments and is capable of use in various other combinations, modifications, and environments and is capable of changes within the scope of the inventive concept as described herein, commensurate with the above teachings, or the skill or knowledge of the relevant art. And that modifications and variations may be effected by those skilled in the art without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. A novel treatment system for landfill leachate is characterized by comprising a lime coagulating sedimentation device, a struvite precipitation deamination and denitrification device, a biochemical treatment device, a coagulating sedimentation device, an electrolysis purification device and a reduction device which are connected in sequence,
the lime coagulating sedimentation device consists of a garbage leachate collecting and adjusting tank, a dosing tank, a coagulating reaction tank, a sedimentation tank and a supernatant storage tank, wherein a water inlet of the coagulating reaction tank is connected with a water outlet of the garbage leachate collecting and adjusting tank, a water outlet of the coagulating reaction tank is connected with a water inlet of the sedimentation tank, a supernatant water outlet of the sedimentation tank is connected with a water inlet of the supernatant storage tank, a sludge outlet of the sedimentation tank is connected with an inlet of a sludge concentration tank, and a water outlet of the supernatant storage tank is connected with a struvite precipitation ammonia nitrogen removal device;
the struvite precipitation deamination and denitrification device consists of a struvite precipitation reaction kettle, a magnesium salt solution storage tank, a phosphate solution storage tank, a precipitation separation tank, a supernatant storage tank, a struvite precipitation concentration tank, a struvite precipitation dehydrator, a solid dryer and a packaging machine; the magnesium salt solution storage tank and the phosphate solution storage tank are respectively connected with the struvite precipitation reaction kettle; the device comprises a struvite precipitation reaction kettle, a supernatant storage tank, a precipitation separation tank, a struvite precipitation dehydration machine, a solid phase drying machine, a solid drying machine, a liquid phase storage tank, a liquid outlet tank, a packing machine and a packing machine, wherein the water inlet of the struvite precipitation reaction kettle is connected with the water outlet of the supernatant storage tank, the water outlet of the struvite precipitation reaction kettle is connected with the water inlet of the precipitation separation tank, the water outlet of the precipitation separation tank is connected with the water inlet of the supernatant storage tank, the precipitation outlet of the precipitation separation tank is connected with the struvite precipitation concentration tank, the precipitation outlet of the precipitation separation tank is connected with the inlet of the struvite precipitation dehydration machine, the precipitation outlet of the struvite precipitation concentration tank is connected with the inlet of the struvite;
the biochemical treatment device comprises an anaerobic tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank and an intermediate tank body which are connected in sequence, wherein a water inlet of the anaerobic tank is connected with a water outlet of the supernatant storage tank, a water outlet of the secondary sedimentation tank is connected with a water inlet of the intermediate tank body, and a sludge outlet of the aerobic tank is connected with an inlet of a sludge concentration tank;
the coagulating sedimentation device comprises a pH adjusting tank, a coagulating tank, a coagulation assisting tank, a sedimentation tank and an intermediate water tank which are connected in sequence, wherein a supernatant water outlet is formed in the top of the sedimentation tank and is connected with a water inlet of the intermediate water tank, a sludge outlet is formed in the bottom of the sedimentation tank and is connected with a sludge pump;
the electrolytic purification device comprises an electrolytic machine, a direct current power supply and a degassing tank, wherein a water inlet of the electrolytic machine is connected with a water outlet of the intermediate water tank, a water outlet of the electrolytic machine is connected with a water inlet of the degassing tank, a water outlet of the degassing tank is connected with a water inlet pipe of the reduction device, a water outlet pipe of the degassing tank is also provided with a circulating water pump, and the circulating water pump is connected with a water inlet pipe of the electrolytic machine;
the reduction device comprises a reduction tank and a reducing agent solution storage tank, the reducing agent solution storage tank is connected with the reduction tank through a metering dosing pump, a water inlet of the reduction tank is connected with water outlet of the electrolytic purification device, and a water outlet of the reduction tank is connected with a water drainage pipe network.
2. The novel treatment system for landfill leachate according to claim 1, further comprising a sludge treatment device, wherein the sludge treatment device comprises a sludge pump, a sludge concentration tank, a physicochemical conditioning tank and a dehydrator, wherein an inlet of the sludge pump is respectively communicated with sludge outlets of the lime coagulation sedimentation device, the biochemical treatment device and the coagulation sedimentation device, the sludge concentration tank is a gravity concentration tank, an outlet of the sludge pump is communicated with an inlet of the gravity concentration tank, a sludge outlet of the gravity concentration tank is communicated with an inlet of the physicochemical conditioning tank, and a sewage outlet of the gravity concentration tank is communicated with a water inlet of the biochemical treatment device; the outlet of the physical and chemical conditioning pool is communicated with the sludge inlet of the dehydrator, and the sewage of the dehydrator is communicated with the water inlet of the biochemical treatment device.
3. The novel landfill leachate treatment system according to any one of claims 1 or 2, wherein the electrolytic purification device further comprises an electrode cleaning device, the electrode cleaning device is composed of a pickling solution storage tank and a pickling solution delivery pump, and the pickling solution is 2-3% hydrochloric acid solution or 4-5% citric acid solution.
4. The novel landfill leachate treatment system according to claim 1, wherein a filler is further placed in the anaerobic tank, the anoxic tank and the aerobic tank, and the filler is one of volcanic rock, crushed stone, slag, ceramsite, plastic ring or plastic ball.
5. The novel landfill leachate treatment system according to claim 1, wherein the coagulating sedimentation device is one of a high efficiency sedimentation device, a magnetic coagulation device and a super magnetic coagulating sedimentation device.
6. The novel landfill leachate treatment system according to claim 1, wherein the coagulation tank of the coagulation sedimentation device further comprises a coagulant dosing device and a mixer, wherein a ferric sulfate, trichloro iron or polyaluminium chloride solution with a mass ratio of 2-20% is stored in the coagulant dosing device; the coagulant aid tank further comprises a coagulant aid dosing device and a stirrer, and a PAM solution with the mass ratio of 1-2 per mill is stored in the coagulant aid dosing device.
7. The novel landfill leachate treatment system according to claim 1, wherein the water inlet of the degassing tank is connected to a water distributor located at the bottom of the degassing tank, the water outlet of the upper part of the degassing tank is connected to the water inlet pipe of the reduction device, and the top of the degassing tank is further provided with a slag scraper and a bubble collecting tank.
8. A method for purifying landfill leachate, which is characterized in that the novel treatment system for landfill leachate according to claims 1 to 7 is used for treating the landfill leachate, and comprises the following steps:
(1) lime coagulating sedimentation
Quantitatively pumping the landfill leachate from a landfill leachate collection and regulation tank into a coagulation reaction tank, starting a stirrer, and stirring according to 5-20 Kg/m3Adding lime powder, stirring and reacting for 15-20 minutes, stopping stirring after the reaction is finished, pumping the garbage percolate after the reaction into a settling tank for settling for 30-60 minutes, pumping supernatant of the settling tank into a supernatant storage tank, pumping sludge at the bottom of the settling tank into a sludge concentration tank, pumping sludge in a sludge concentration tank into a dehydrator for dehydration, and pumping sewage generated by dehydration of the dehydrator into a garbage percolate collecting and adjusting tank;
(2) removing ammonia nitrogen by struvite precipitation
Pumping sewage of the supernatant storage tank in the step (1) into a struvite precipitation reaction kettle, adding a magnesium salt solution with a theoretical calculation amount of 1.1 times under the condition of continuous stirring, then adding a phosphate solution with a calculation amount of 1.1 times, reacting at room temperature for 15-30 minutes under the condition of continuous stirring, pumping into a precipitation separation tank for standing after the reaction is finished, carrying out solid-liquid separation, pumping clear liquid at the upper part of the precipitation separation tank into a supernatant storage tank for storage, pumping precipitate at the lower part of the precipitation separation tank into a struvite precipitation concentration tank, pumping into a struvite precipitation dehydrator for dehydration to obtain solid struvite precipitate and filtrate, pumping the filtrate into a supernatant storage tank, drying the solid struvite precipitate and packaging to obtain a struvite finished product;
(3) biochemical treatment
Pumping the garbage percolate obtained after removing ammonia nitrogen by the struvite sediment in the step (2) into a biochemical treatment device, sequentially treating the garbage percolate by an anaerobic tank, an anoxic tank and an aerobic tank, wherein the retention time of the biochemical treatment is 96-240 hours,
(4) coagulating sedimentation
The sewage after the biochemical treatment in the step (3) flows into a pH adjusting tank, a coagulation tank and an assistant of a coagulation and precipitation device in sequenceAdding 5-15% of sodium hydroxide or 5-20% of sodium carbonate solution into a pH adjusting tank to adjust the pH to 9-9.5, then flowing into a coagulation tank, adding 12-30 g/m through a coagulant dosing device under the stirring condition3The 2-10% PAC solution is reacted for 5min completely and then enters a coagulation aiding tank, and 1-2 g/m is added into the coagulation aiding tank3Stirring and reacting the PAM for 1-2 min, then, allowing the PAM to enter a sedimentation tank for solid-liquid separation, pumping supernatant of the sedimentation tank into an intermediate water tank, and conveying sediment into a sludge concentration tank;
(5) electrolytic purification
Pumping the coagulated water which is subjected to coagulation precipitation in the step (4) and stored in the intermediate water tank into an electrolysis machine for electrolysis and purification, wherein the working voltage of the electrolysis machine is 5-150V, the current is 10-10000A, the electrolyzed supernatant enters a degassing tank for gas-liquid separation, bubbles at the upper part are scraped into a bubble collecting tank through a residue scraping machine, and the lower part clear liquid is pumped into the electrolysis machine again for electrolysis through a circulating water pump;
(6) reduction of
And (4) discharging the effluent of the landfill leachate electrolyzed in the step (5) into a reduction tank, reacting excessive sodium hypochlorite in the effluent with a reducing agent, and discharging the effluent into a municipal drainage pipe network after eliminating the excessive sodium hypochlorite.
9. The novel landfill leachate treatment system according to claim 8, further comprising a sludge treatment step, wherein the scum obtained by lime coagulation sedimentation, biochemical treatment, coagulation sedimentation and electrolytic purification is respectively conveyed to a sludge concentration tank for gravity concentration to form an upper supernatant and a bottom sludge; and (2) conveying the supernatant to a water inlet pipe of a biochemical treatment device, performing gravity concentration on sludge in a sludge concentration tank, then feeding the sludge into a treatment and conditioning tank, adding a physicochemical conditioner in the physicochemical conditioning tank, and then conveying the sludge to a dehydrator for dehydration, wherein the physicochemical conditioner comprises lime, ferric trichloride and polyaluminium chloride.
10. The novel landfill leachate treatment system according to claim 8, wherein the magnesium salt in step (2) is one of magnesium sulfate heptahydrate, magnesium chloride or magnesium chloride hexahydrate, which is prepared into a 20-50% solution and stored in a magnesium salt solution storage tank for later use, and the addition amount thereof is:
the addition amount of the magnesium salt solution is (the molecular weight of the magnesium salt is multiplied by the ammonia nitrogen concentration of the effluent of the landfill leachate) multiplied by 1.1/18,
the phosphate is one of sodium phosphate dodecahydrate, sodium hydrogen phosphate, sodium dihydrogen phosphate or anhydrous sodium phosphate, when in use, the phosphate is prepared into a 15-25% solution and stored in a phosphate solution storage tank for later use, and the addition amount of the phosphate is as follows:
the adding amount of the phosphate solution is (the molecular weight of the phosphate is multiplied by the ammonia nitrogen concentration of the effluent of the landfill leachate) multiplied by 1.1/18.
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