CN110436630A - Toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor - Google Patents
Toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor Download PDFInfo
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- CN110436630A CN110436630A CN201910822254.4A CN201910822254A CN110436630A CN 110436630 A CN110436630 A CN 110436630A CN 201910822254 A CN201910822254 A CN 201910822254A CN 110436630 A CN110436630 A CN 110436630A
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- pond
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- tank
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- 239000010865 sewage Substances 0.000 title claims abstract description 99
- 238000011282 treatment Methods 0.000 title claims abstract description 44
- 238000003889 chemical engineering Methods 0.000 title claims abstract description 32
- 230000002588 toxic effect Effects 0.000 title claims abstract description 31
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 231100000331 toxic Toxicity 0.000 title claims abstract description 30
- 239000010802 sludge Substances 0.000 claims abstract description 132
- 239000012528 membrane Substances 0.000 claims abstract description 114
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 81
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 72
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 71
- 230000000694 effects Effects 0.000 claims abstract description 68
- 238000007667 floating Methods 0.000 claims abstract description 64
- 230000003647 oxidation Effects 0.000 claims abstract description 63
- 238000000034 method Methods 0.000 claims abstract description 53
- 238000010992 reflux Methods 0.000 claims abstract description 47
- 206010021143 Hypoxia Diseases 0.000 claims abstract description 45
- 230000007954 hypoxia Effects 0.000 claims abstract description 45
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 36
- 230000008569 process Effects 0.000 claims abstract description 32
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000012545 processing Methods 0.000 claims abstract description 27
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 42
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 40
- 229910052799 carbon Inorganic materials 0.000 claims description 40
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 25
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 24
- 229910052760 oxygen Inorganic materials 0.000 claims description 24
- 239000001301 oxygen Substances 0.000 claims description 24
- 239000000725 suspension Substances 0.000 claims description 24
- 238000000108 ultra-filtration Methods 0.000 claims description 24
- 230000015556 catabolic process Effects 0.000 claims description 23
- 238000006731 degradation reaction Methods 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 20
- 239000000945 filler Substances 0.000 claims description 16
- 244000005700 microbiome Species 0.000 claims description 15
- 241000894006 Bacteria Species 0.000 claims description 14
- 239000005416 organic matter Substances 0.000 claims description 14
- 238000005276 aerator Methods 0.000 claims description 13
- 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 claims description 12
- 230000007062 hydrolysis Effects 0.000 claims description 10
- 238000006460 hydrolysis reaction Methods 0.000 claims description 10
- 230000009189 diving Effects 0.000 claims description 9
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 claims description 8
- 230000020477 pH reduction Effects 0.000 claims description 8
- 239000001632 sodium acetate Substances 0.000 claims description 8
- 235000017281 sodium acetate Nutrition 0.000 claims description 8
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- 239000003814 drug Substances 0.000 claims description 5
- 238000002513 implantation Methods 0.000 claims description 5
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 4
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 claims description 4
- 239000008103 glucose Substances 0.000 claims description 4
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- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 230000009286 beneficial effect Effects 0.000 claims description 3
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- 239000010959 steel Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 239000003054 catalyst Substances 0.000 abstract description 4
- 239000007800 oxidant agent Substances 0.000 abstract description 4
- 238000010276 construction Methods 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 abstract description 3
- 230000001590 oxidative effect Effects 0.000 abstract description 3
- 230000035939 shock Effects 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract 1
- 239000002351 wastewater Substances 0.000 description 22
- 239000000126 substance Substances 0.000 description 20
- 238000006243 chemical reaction Methods 0.000 description 17
- 239000003344 environmental pollutant Substances 0.000 description 14
- 231100000719 pollutant Toxicity 0.000 description 14
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 13
- 241000108664 Nitrobacteria Species 0.000 description 13
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 10
- 238000006396 nitration reaction Methods 0.000 description 10
- 231100000419 toxicity Toxicity 0.000 description 10
- 230000001988 toxicity Effects 0.000 description 10
- 230000008901 benefit Effects 0.000 description 9
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 8
- 238000004939 coking Methods 0.000 description 8
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 8
- 238000005273 aeration Methods 0.000 description 7
- 230000008859 change Effects 0.000 description 7
- 230000008878 coupling Effects 0.000 description 7
- 238000010168 coupling process Methods 0.000 description 7
- 238000005859 coupling reaction Methods 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 150000003222 pyridines Chemical class 0.000 description 7
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 description 6
- 229920002972 Acrylic fiber Polymers 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 6
- 230000000813 microbial effect Effects 0.000 description 6
- 230000000050 nutritive effect Effects 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 239000003440 toxic substance Substances 0.000 description 6
- 238000009303 advanced oxidation process reaction Methods 0.000 description 5
- 238000004176 ammonification Methods 0.000 description 5
- 238000002306 biochemical method Methods 0.000 description 5
- 238000009395 breeding Methods 0.000 description 5
- 230000001488 breeding effect Effects 0.000 description 5
- 238000011049 filling Methods 0.000 description 5
- 230000005484 gravity Effects 0.000 description 5
- 230000005764 inhibitory process Effects 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 230000001546 nitrifying effect Effects 0.000 description 5
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 5
- 231100000167 toxic agent Toxicity 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 4
- 101150049074 SALR gene Proteins 0.000 description 4
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- -1 acrylic nitrile Chemical class 0.000 description 4
- 230000001651 autotrophic effect Effects 0.000 description 4
- 238000011109 contamination Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 230000005611 electricity Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000004907 flux Effects 0.000 description 4
- 239000012510 hollow fiber Substances 0.000 description 4
- 230000002401 inhibitory effect Effects 0.000 description 4
- 238000011081 inoculation Methods 0.000 description 4
- 230000013011 mating Effects 0.000 description 4
- CUXQLKLUPGTTKL-UHFFFAOYSA-M microcosmic salt Chemical compound [NH4+].[Na+].OP([O-])([O-])=O CUXQLKLUPGTTKL-UHFFFAOYSA-M 0.000 description 4
- 125000001477 organic nitrogen group Chemical group 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- 231100000614 poison Toxicity 0.000 description 4
- 230000033458 reproduction Effects 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 230000001360 synchronised effect Effects 0.000 description 4
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- 240000002853 Nelumbo nucifera Species 0.000 description 3
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 3
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- 238000007380 fibre production Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 235000016709 nutrition Nutrition 0.000 description 3
- NRADCUWKNUKPHY-UHFFFAOYSA-N oxalonitrile;phenol Chemical compound N#CC#N.OC1=CC=CC=C1 NRADCUWKNUKPHY-UHFFFAOYSA-N 0.000 description 3
- 238000006385 ozonation reaction Methods 0.000 description 3
- 239000002574 poison Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002689 soil Substances 0.000 description 3
- 231100001234 toxic pollutant Toxicity 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 208000036142 Viral infection Diseases 0.000 description 2
- HGINCPLSRVDWNT-UHFFFAOYSA-N acrylaldehyde Natural products C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 235000019441 ethanol Nutrition 0.000 description 2
- 231100000086 high toxicity Toxicity 0.000 description 2
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000002166 wet spinning Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 239000005906 Imidacloprid Substances 0.000 description 1
- 108090000913 Nitrate Reductases Proteins 0.000 description 1
- 244000131316 Panax pseudoginseng Species 0.000 description 1
- 235000005035 Panax pseudoginseng ssp. pseudoginseng Nutrition 0.000 description 1
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 208000005374 Poisoning Diseases 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 208000005735 Water intoxication Diseases 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007900 aqueous suspension Substances 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000004567 concrete Substances 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
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- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000007255 decyanation reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
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- 235000013399 edible fruits Nutrition 0.000 description 1
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- 235000008434 ginseng Nutrition 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- YWTYJOPNNQFBPC-UHFFFAOYSA-N imidacloprid Chemical compound [O-][N+](=O)\N=C1/NCCN1CC1=CC=C(Cl)N=C1 YWTYJOPNNQFBPC-UHFFFAOYSA-N 0.000 description 1
- 229940056881 imidacloprid Drugs 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
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- 239000011259 mixed solution Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 150000002825 nitriles Chemical class 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000003359 percent control normalization Methods 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 238000009428 plumbing Methods 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000035755 proliferation Effects 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 231100000241 scar Toxicity 0.000 description 1
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 description 1
- VGTPCRGMBIAPIM-UHFFFAOYSA-M sodium thiocyanate Chemical compound [Na+].[S-]C#N VGTPCRGMBIAPIM-UHFFFAOYSA-M 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 231100000816 toxic dose Toxicity 0.000 description 1
- 231100000563 toxic property Toxicity 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000003403 water pollutant Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/004—Apparatus and plants for the biological treatment of water, waste water or sewage comprising a selector reactor for promoting floc-forming or other bacteria
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/11—Turbidity
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/22—O2
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention relates to a kind of toxic, high nitrogenous chemical engineering sewage coupled film biological treatment and reactors, by using a kind of coupled film biological treatment and reactor, sewage successively after the processing of bioselection pond, floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and membrane cisterna, obtains the water outlet for meeting discharge standard.Technique and reactor of the invention has removal efficiency high, and strong shock resistance, being discharged COD, ammonia nitrogen and total nitrogen can stably reaching standard；Without using oxidant and catalyst, operating cost is low, without secondary pollution；Reactor is integrated, energy consumption needed for saving land occupation and reducing mixed liquor and sludge reflux, and construction investment is low；The features such as process flow is simple, convenient operating maintenance, can be used in the industrial production of toxic, high nitrogenous chemical engineering sewage.
Description
Technical field
The invention belongs to sewage treatment fields, and in particular at a kind of toxic, high nitrogenous chemical engineering sewage coupled film biology
Manage reactor.
Background technique
With " petro chemical industry pollutant emission standard " GB 31571-2015, " coking chemistry emission of industrial pollutants
Standard " professional standards such as GB16171-2012 publication, stringent ammonia nitrogen and total nitrogen control limit are proposed to chemical engineering sewage discharge
Value.Nitrogen is the one of the chief elements in industrial chemicals or product, containing the nitrogen of different shape, institute in most chemical engineering sewages
It is all suffered from chemical company and sewage treatment facility is carried out to propose mark transformation, improve the removal rate of ammonia nitrogen, increased total nitrogen processing and set
It applies.Proposing mark transformation is to increase the secondary biochemical treatment with denitrification denitrogenation function behind existing biochemical treatment facility mostly
Facility.First round transformation is basically completed, due to BOD in sewage5It is very low, even if adding carbon source, it is numerous still to there is microorganism
It grows slowly, the very low problem for the treatment of effeciency, it is still problem that enterprise faces that total nitrogen is exceeded.Some Enterprises have contemplated that the second wheel changes
It makes, needs treatment effeciency height, stable new technology；Newly-built chemical company also needs new technology.
And in most of chemical engineering sewages, containing to the virose pollutant of microorganism, as acrylonitrile, cyanide, acetonitrile,
Phenols and pyridine etc..These pollutants itself are bio-degradables, but when use Biochemical method, these toxicants can press down
The growth and breeding of microorganism processed, or even can not survive." the used water difficult to degradate that Wu Xikang writes, China Light Industry Press publishes
Treatment process " in can look into, acrylonitrile, phenol and pyridine etc. to aerobic degradation microorganism generate toxicity concentration be respectively 53mg/
L, 64mg/L and 340mg/L.In the nitration denitrification processing system of nitrogenous organic sewage, autotrophic type nitrobacteria is to these poison
Property substance it is more sensitive, inhibiting effect is just generated at lower concentrations, and with the increase of toxicant concentration, rate of nitrification
It can decline rapidly.Such as: delivering that " phenol is to wastewater biological nitrifying process Li Juanying in March, 2007 at " Shanghai Aquatic Products Univ. 9CN)'s journal "
Inhibition ", experiment obtains: as phenol concentration increases to 4.72mg/L from 0, phenol utilizes the inhibition of rate to high specific matrix
Rate increases to 65% from 0." 2-vhloro-5-chloromethylpyridine inhibits biological nitration to the doctoral thesis of Wang Hanyu in imidacloprid wastewater
Research " in obtain, with the increase of 2-vhloro-5-chloromethylpyridine (CCMP) concentration, to the inhibition strength of nitrification also with
Increasing, when CCMP concentration increases to 25.0mg/L by 2.0mg/L, the most fast degradation rate of ammonia nitrogen is by 7.90mg/ (gMLSS
H) it is reduced to 0.02mg/ (gMLSSh), Nitrifying inhibition rate rises to 99.38%.In industrial application, due to sewage discharge by
The influence of produce load adjustment and device operating condition, variation water quality range is very big, the poison that biological treatment system can actually be born
Property material concentration is low more than the numerical value that experimental study obtains.So for there is the difficult point of toxic, high nitrogenous chemical industry sewage treatment
First is that how to release the toxicity of sewage.The prior art generally uses advanced oxidation processes to be pre-processed, and reduces toxic pollutant
After concentration, then carry out Biochemical method.Such as:
Chinese patent CN201511005767 discloses a kind of " electrocatalysis oxidation reaction dress for handling toxicity organic wastewater
Set ", virose organic wastewater is handled using electrocatalysis oxidation reaction device, solves traditional electrode consersion unit treatment effeciency
Low, poor processing effect problem, reduces power consumption, reduces processing cost (20kWh/m3Sewage).
Chinese patent CN201510010373 discloses " a kind of acrylic fiber wastewater processing system ", the process flow of use are as follows:
It is heavy that conditioning tank-waste water strengthens flotation tank-ozone catalytic sedimentation basin-deflector type anoxic anaerobic reation pool-aerobic contact oxidation pond-two
Pond-sand filter, wherein using ozone catalytic sedimentation basin as toxic substances such as acrylonitrile, acetonitrile and cyanides in reduction acrylic fiber wastewater
Then matter concentration uses anaerobic-aerobic Biochemical method.
Chinese patent CN201410743068 discloses " a kind of processing method of acrylonitrile and two step wet spinning acrylic fiber waste water ",
Wet acrylic fiber production wastewater is divided into acrylic nitrile waste water, polymeric wastewater, filature wastewater, acid waste water and other waste water, is used
Fenton oxidation technique pre-processes polymeric wastewater and acrylic nitrile waste water, reduces acrylonitrile and cyanogen root concentration, then uses
Anaerobic-aerobic or Anoxybiotic-aerobic biologic processing.
Chinese patent CN201110031791 discloses " a kind of high-purity pyridine class waste water treatment process and equipment ", processing
Process is that electrocatalytic oxidation-light electrolysis-coagulating sedimentation-anaerobic hydrolysis-is pressed into contact oxidation, electrocatalytic oxidation-therein
Weak electrolysis mechanism for reducing pyridine substance in sewage toxicity.
Hydroxyl radical free radical (OH) oxidability that advanced oxidation system generates is very strong, can make many difficult for biological degradation and one
As chemical oxidization method be difficult to the oxidation operation aoxidized decomposition, it is preferable to toxic, hardly degraded organic substance removal effect.But it
(1) is had the disadvantage in that due to the no selectivity of removal of the advanced oxidation to organic matter, when as pretreatment measure, in waste water
The organic matter of a large amount of easily biological-degradables is decomposed simultaneously, need to consume a large amount of oxidants, catalyst or electric energy, therefore operating cost is very
It is high；(2) advanced oxidation reaction need to generally control the pH value of sewage in acid range, as Fenton oxidation reaction appropriate pH is 2~
4, electrocatalysis oxidation reaction appropriate pH is 3~5.Sewage needs first acid adding to be adjusted to acidity before entering pretreatment facility, pre-processes
Add alkali neutralization to 7.0~8.1, again afterwards to meet the requirement of subsequent biochemical processing.Soda acid medicament is added in addition to generating additional expense
With, it is big to the corrosivity of equipment and pipeline, it needs using expensive material, investment and maintenance cost are high；(3) advanced oxidation reaction
The catalyst added will generate a large amount of sludge, belong to hazardous waste, increase the environmental burden of enterprise；(4) advanced oxidation reaction pair
Condition responsive controls more demanding.
Have that capital cost is low, processing cost is low, simple operation and other advantages using Biochemical method organic sewage, but also deposits
In limitation.Be using the difficult point of Biochemical method for toxic, high nitrogenous chemical engineering sewage: how (one) reduces the poison of sewage
Property, enable biological treatment system stable operation；(2) how denitrification percent is improved, makes the ammonia nitrogen of water outlet and total nitrogen can be up to standard.
In order to solve the problems, such as to improve denitrification percent, need from the principle of analysis biological denitrificaion.The principle of bioanalysis denitrogenation is: organic
Nitrogen generates ammonia nitrogen by ammonification first；Under aerobic condition, autotrophic type nitrobacteria is carbon source using inorganic carbon, makes ammonia nitrogen that nitre occur
Change reaction, generates nitrate nitrogen；Then under anoxic conditions, heterotroph denitrifying bacterium is supplied using the organic matter in sewage as electronics
Body, by nitrate-nitrogen reduction at nitrogen, finally realizes sewage water denitrification using nitrate nitrogen as electron acceptor.In order to realize efficient denitrification,
Other than control temperature, nutrition influence the common factor of nitrification and denitrification process than, toxicant concentration and sludge age etc., it is necessary to
Condition needed for recognizing nitrification and denitrification reaction is different: (1) nitration reaction requires the dissolved oxygen (DO) for having sufficient, DO
Higher Nitrification rate is higher, and general control is in 2mg/L or more.And DO has inhibiting effect to denitrification, is primarily due to oxygen meeting and nitre
Hydrochlorate competes electron donor, and molecular oxygen can also inhibit the synthesis and its activity of nitrate reductase.So DO is lower, anti-nitre
Rate is higher；When dissolved oxygen is 0, if carbon source is sufficient, theoretically nitrate nitrogen removal rate is up to 100%.Due to sludge wadding body
Anoxic or anaerobic state can be still presented in inside, and the DO that anoxic pond is controlled in industrial application is less than 0.5mg/L.(2) nitrifying process benefit
It uses inorganic carbon as carbon source, needs to react under weak basic condition, suitable pH is 7.5~8.5；And denitrification process is releasable
A small amount of basicity, suitable pH are 7.0~7.5；(3) nitrobacteria ratio present in aerobic reaction system depends in sewage
The ratio of carbonaceous material and kjeldahl nitrogen.Carbon-nitrogen ratio is higher, and the activity of heterotroph oxidation bacteria is larger, and mass propagation consumes dissolved oxygen rate
Fastly, make nitrobacteria can not struggle for existence；, whereas if carbon-nitrogen ratio is lower, be then conducive to the proliferation of nitrobacteria.The Summer Solstice it is red
It is recorded in Master's thesis " influence research of the carbon-nitrogen ratio to nitrifying sludge extracellular polymeric and sludge characteristics ", carbon-nitrogen ratio (C/N) is right
The growth of activated sludge has a significant impact, and in carbon source abundance situation, heterotrophic microorganism mass propagation generates competing with nitrobacteria
It strives, it will Mud up-floating, sludge bulking etc. is caused to endanger.When carbon source deficiency, Autotrophic nitrification bacterium will be turned out, it is active at this time
Sludge slow growth.In carbon source abundance system, the obvious shadow by high C/N of the Nitrification of nitrifying sludge and mud-water separation effect
It rings, even if reducing water inlet C/N, it is also difficult to restore.When C/N reaches 10, there is sticky inflation caused by Nonaqueous reaction in sludge,
Reactor is deteriorated for the removal effect of ammonia nitrogen.According to another information, if BOD in system5It, will be to nitrification greater than 20mg/l
Bacterium generates inhibition.So needing first to remove organic matter when influent COD is higher, so that COD is in reduced levels, continue to expose
Gas gives the enough growth times of nitrobacteria and dissolved oxygen.(4) denitrification process needs sufficient carbon source and could complete,
But and not all COD can be used as denitrifying carbon source.In the July, 1996 such as Zhang Feijuan delivers " carbon source pair in " industrial plumbing "
The influence of biological denitrification " proposes: carbon source kind has larger impact to denitrification effect, has with the dissolubility being readily biodegradable
Machine object, such as denitrification rate is most fast when methanol, ethyl alcohol, glucose are as carbon source；Made with the gas chromatography in combined sewage
When for carbon source, incipient stage carbon source is sufficient, and denitrification rate is very fast, and the later period gradually decreases；Carbon source property is also to influence denitrification
One key factor of effect, COD/NH3- N cannot function as measure carbon-nitrogen ratio whether Chong Zu unique foundation.Therefore, in order to reach
To higher denitrification percent, nitrification and denitrification process should be completed in two different reactors.
The biological denitrification process of early stage mainly has A/O, multistage A/O, SBR and oxidation ditch etc., develops short distance nitre in recent years
Change the techniques such as denitrification and synchronous nitration and denitrification, plays an important role in sewage treatment.But these technologies have for handling
When toxicity, nitrogenous organic sewage, there are microbial reproductions to be inhibited by higher concentration toxicant, and treatment effeciency is low；Nitrify anti-nitre
Change reaction not to carry out at optimum conditions, denitrogenation is not thorough, be discharged total nitrogen can not be up to standard；Antipollution object impact capacity is poor, system
The problems such as fluctuation of service.
Chinese patent CN201310436432 discloses a kind of high toxicity coking wastewater containing phenol and cyanide treatment for reuse system and waste water
Treatment for reuse method.The process flow used is dissolved air flotation-AHCR anaerobic hydrolysis reactor-DNCR denitrification reactor-one
Grade OHCR aerobic reactor-second level OHCR aerobic reactor-secondary settling tank-efficient sedimentation tank-advanced oxidation reaction device, second level OHCR
The suspension of aerobic reactor is back to DNCR denitrification reactor, can be by sulfur-bearing 400mg/L or so, total nitrogen 700mg/L or so
Coking phenol cyanogen high toxicity wastewater treatment after reuse, aqueous suspension 59mg/L, COD65mg/L, ammonia nitrogen 2.7mg/L are not provided out
It is discharged total nitrogen concentration.The invention the problem is that: (1) high wastewater containing phenol and cyanide passes through mechanical stirring in air bearing Reaction Separation device
Part volatile phenol and hydrogen cyanide stripping are achieved the purpose that reduce sewage toxicity to atmosphere with air aeration.Stripping belongs to pollution
Object transfer, phenol cyanogen enter gas phase and are more difficult to be removed, and discharge exhaust gas will be caused exceeded.(2) stripping has preferably high-concentration waste water
Removal rate, is generally used for material recycle in production process, and air bearing can not be such that phenol cyanogen concentration is down to below Ecotoxicology value.
(3) present invention is merely with level-one Prepositive denitrification as the facility for removing nitrate nitrogen in whole flow process.The advantages of Prepositive denitrification
It is to reduce additional carbon using the carbon source in water inlet, reduces operating cost.The disadvantage is that being discharged from aerobic biochemical pool, it is discharged total nitrogen
It can not be up to standard.Because nitrate is identical with the suspension for being back to DNCR denitrification reactor in water outlet.In order to mention
High denitrification percent reduces nitrate nitrogen content in water outlet, needs to improve the reflux ratio of mixed liquor.And the reflux ratio of mixed liquor is improved, one
Aspect causes energy consumption to increase, and on the other hand causes the DO of anoxic pond to increase, influences denitrification rate.So using level-one anoxic/
Aerobic total denitrification percent highest 75% or so.
Chinese patent CN201310003283 discloses a kind of biochemical processing method of sewage containing pyridines, mixed using water inlet
It closes area, synchronous nitration and denitrification pond, anoxic pond and membrane biological reaction pond and handles sewage containing pyridines.In the invention, high concentration
Sewage containing pyridines is mixed in water inlet mixed zone with the muddy water mixed solution that synchronous nitration-denitrification pond end returns, and makes mixed zone
The pyridines concentration of water outlet is less than or equal to 200 mg/litres.Water inlet is carried out using the phegma Jing Guo biochemical treatment dilute
It releases, achievees the effect that reduce pyridine toxicity, compared with being pre-processed using advanced oxidation processes or being diluted using industry water, substantially reduce
Processing cost.But the invention using synchronous nitration and denitrification pond as pyridines itrogenous organic substance difficult to degrade ammonification with
Nitrification measure, DO are controlled in 0.3~0.5 mg/litre.Advantage is reduction of energy consumption and additional carbon, the disadvantage is that DO is unsatisfactory for nitre
Change the optimum condition of reaction, rate of nitrification is low, and total denitrification percent is also low.In addition, pyridine belongs to hardly degraded organic substance, low DO is unfavorable
In its degradation.
Summary of the invention
Problem to be solved by this invention is: 1) existing processing technique needs to add big using advanced oxidation as pretreatment
Chemical agent and catalyst are measured, operating cost is high and generates a large amount of sludge；2) in existing biologic treating technique microbial reproduction by
Higher concentration toxicant inhibits, and treatment effeciency is low；Nitration denitrification reaction does not carry out at optimum conditions, denitrogenation is not thorough,
Being discharged total nitrogen can not be up to standard；The problems such as antipollution object impact capacity is poor, system fluctuation of service.The present invention is toxic, Gao Han
Nitrogen chemical engineering sewage provides the biological treatment and reactor of a kind of coupling, has removal efficiency high, water outlet COD, ammonia nitrogen and total
Nitrogen can be up to standard；Integral structure is saved and is taken up an area, and low energy consumption needed for mixed liquor and sludge reflux；Without using oxidant and catalysis
The features such as agent, operating cost is low.
In order to solve the above technical problems, The technical solution adopted by the invention is as follows: a kind of toxic, high nitrogenous chemical engineering sewage
Coupled film biological treatment and reactor, including what is be sequentially connected in series:
Bioselection pond, for carrying out adaptability screening to microorganism in sewage and carrying out primary treatment to sewage；
Floating stuffing oxidation pond makes beneficial microbe implantation and breeds, and degradation is special in sewage after the processing of bioselection pond
Levy pollutant；
Aerobic activated sludge pond makes after the processing of floating stuffing oxidation pond the nitrification of organic matter degradation and ammonia nitrogen in sewage；
Hypoxia activity sludge-tank makes denitrifying bacteria quickly convert N2 evolution for nitrate nitrogen；
Membrane cisterna sludge and water is discharged respectively, and play degradation denitrification residue carbon source for separating sludge and water
Effect；
The bioselection pond is connected to floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank, described
Bioselection pond couples being integrally formed with floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and membrane cisterna
Membrane bioreactor (Combination of Carrier and Membrane Bio-Reactor, abridge CCMBR) is toxic
Property, high nitrogenous chemical engineering sewage after the processing of above-mentioned coupling membrane bioreactor (CCMBR), obtain meeting discharge standard out
Water.
Preferably, toxic, the high nitrogenous chemical engineering sewage initially enters the bioselection pond, and described
Aerobic activated sludge pond or the reflux of hypoxia activity sludge-tank end suspension and the medicament that adds as needed it is sufficiently mixed
It closes；Wherein, sewage and suspension reflux ratio are 2~10, make toxic concentration, pH value and the nutritional ingredient satisfaction life of sewage after mixing
The requirement of object processing.
Preferably, bioselection pond water outlet enters floating stuffing oxidation pond, fills Large ratio surface in pond
Product floating stuffing, filler surface are conducive to implantation and the breeding of the superior microorganism of degradation characteristic contamination；Bottom of pond installs mesoporous
Aerator, control dissolved oxygen content (DO) are greater than 4mg/L, make filler that fluidized state be presented, and provide abundance for the breeding of microorganism
Oxygen, so that easily biodegradable organics is degraded in a short time, and make organic nitrogen ammonification, avoid striving in subsequent aerobic tank with nitration reaction
Take oxygen by force.Setting filler is exported in floating stuffing oxidation pond and intercepts aperture plate, and the gap size of aperture plate should be less than the minimum ruler of filler
It is very little.
Preferably, the floating stuffing oxidation pond effluent enters aerobic activated sludge pond, returns with from membrane cisterna
The activated sludge of stream mixes, and reflux ratio desirable 50%~100% controls the sludge concentration of aerobic activated sludge pond in 5~8g/L
Between；The dominant bacteria of nitrobacteria and degradable characteristic contamination rich in period length in returned sludge, can accelerate difficult to degrade
The degradation of organic matter and the nitrification of ammonia nitrogen；Bottom of pond installs micro-hole aerator, and control DO is 2~3mg/L, and ammonia nitrogen is made to obtain abundant nitre
Change.
Preferably, the nitre state liquid of the aerobic activated sludge pond end enters hypoxia activity sludge-tank, according to
4 times of total nitrogen concentration add carbon source in nitre state liquid, and carbon source uses the methanol or sodium acetate or glucose etc. of easy biochemical degradation；Control
DO is less than 0.5mg/L；Diving mixer is installed in pond, accelerates the mixing of nitre state liquid and carbon source, and prevents sludge settling, makes anti-nitre
Change bacterium and quickly converts N for nitrate nitrogen2Evolution.
Preferably, the hypoxia activity sludge-tank effluent enters membrane cisterna, installs immersion ultrafiltration in membrane cisterna
Membrane module, membrane cisterna bottom and membrane module bottom are equipped with aerator, and aeration air prevents film blocking outer in addition to washing away film surface,
Also act as the effect of degradation denitrification residue carbon source；Processed water outlet is extracted out by water outlet pump from the water outlet of membrane module, water outlet
Meet the requirement of discharge standard.Activated sludge is trapped in membrane cisterna completely, and the aerobic work is flowed back by sludge reflux pump
Property sludge-tank and/or floating stuffing oxidation pond, some residual sludge discharge system.
Preferably, the integrated film bioreactor (CCMBR) can be the armored concrete water built jointly
Pond or steel water tank.
Preferably, the bioselection pond can be used as preaeration tank or hydrolysis acidification pool；As preaeration tank
When, flow back suspension from the aerobic activated sludge pond end, reflux unit can be used airlift, submersible water impeller or
Sewage pump；When as hydrolysis acidification pool, from the hypoxia activity sludge-tank end reflux suspension, reflux unit can be used latent
Water impeller or sewage pump.
Preferably, hollow membrane or plate membrane can be used in the hyperfiltration membrane assembly.
Refer to " petro chemical industry pollutant emission mark using the discharge standard reached is discharged after method processing of the invention
It is quasi- " the discharge limit in general area in GB31571-2015 or " coking chemistry emission of industrial pollutants standard " GB16171-2012
Value.If user has higher requirement, ammonia nitrogen and total nitrogen can pass through the ginseng of control aerobic activated sludge pond and hypoxia activity sludge-tank
Meet ammonia nitrogen after number less than 5mg/L, total nitrogen is less than 15mg/L；It in addition can be by increasing ozone catalytic after reactor of the invention
Facility is aoxidized, the COD of not bio-degradable is removed partially, makes to be discharged COD less than 50mg/L, since ultrafiltration membrane delivery turbidity is less than
5NTU not will increase additional ozone consumption.
In the method for the present invention, toxic, high nitrogenous chemical engineering sewage initially enters bioselection pond, with aerobic activated sludge pond
Or the hypoxia activity sludge-tank end suspension to flow back and the medicament added as needed mix, and adapt to microorganism
Property screening；The oxygen activity dirt because the bioselection pond that toxic sewage passes through in the method for the present invention, floating stuffing oxidation pond are become reconciled
After mud sump processing, toxic pollutant has been removed substantially, so suspension reflux can dilute water inlet Poisoning material concentration, is reduced
To the inhibiting effect of heterotrophic microorganism and autotrophic type nitrobacteria in subsequent biological treatment system；Suspension regurgitant volume depends on dirt
The concentration of water intoxication contact scar object, reflux ratio take 2~10 dilution requirements that can substantially meet chemical engineering sewage；It is main to add medicament
It is nutritional ingredient needed for adjusting pH value and supplement microbial reproduction, such as P, Fe, Ca, the specific sewage property that regards determines.Biology
It selects pond water outlet to enter floating stuffing oxidation pond, bigger serface floating stuffing is filled in pond, the packing ratio of floating stuffing is desirable
20~60%, specific surface area is 200~1200m2/m3, true specific gravity is 0.95~1.0g/cm3, filler surface is conducive to degradable
The implantation of the superior microorganism of characteristic contamination and breeding；Bottom of pond installs mesoporous aerator, and control DO is greater than 4mg/L, makes filler
Fluidized state is presented, biomembrane can homoepitaxial；It is to be convenient for demoulding to wash away filler, prevent filler stifled using hollow aerator
Plug；Sufficient oxygen makes the organic matter of easily biological-degradable in sewage degrade in a short time, so that organic nitrogen is completed ammonification, avoids
Subsequent aerobic tank and nitration reaction fight for oxygen；Setting filler, which is exported, in floating stuffing oxidation pond intercepts aperture plate, the gap of aperture plate
It should be less than the size of filler.Floating stuffing oxidation pond effluent enters aerobic activated sludge pond, mixes with the sludge to flow back from membrane cisterna
It closes, reflux ratio takes 50%~100%, controls the sludge concentration of aerobic activated sludge pond between 5~8g/L；It is rich in returned sludge
Hardly degraded organic substance and ammonia nitrogen can be improved in the dominant bacteria of long nitrobacteria and degradation Recalcitrant chemicals containing the generation cycle
Removal rate and removal rate；Bottom of pond installs micro-hole aerator, and control DO is 2~3mg/L, nitrifies ammonia nitrogen sufficiently；It is small
Bubble can extend the residence time in oxidation pond, improve the utilization rate of oxygen.The nitre state liquid of aerobic activated sludge pond end enters
Hypoxia activity sludge-tank adds carbon source according to 4 times of total nitrogen concentration in nitre state liquid；In order to make denitrification process carry out more thorough
Bottom, while COD concentration in hypoxia activity sludge-tank effluent is controlled, carbon source is using the methanol or sodium acetate being readily biodegradable；
It controls anoxic pond DO and is less than 0.5mg/L；In order to mix nitre state liquid with carbon source Quick uniform, and sludge settling is prevented, pacified in pond
Fill diving mixer；Under the conditions ofs having sufficient and high-quality carbon source, suitable DO and pH etc., nitrate nitrogen can be turned by thorough denitrification
Become N2Evolution.Hypoxia activity sludge-tank effluent enters membrane cisterna, installs submerged ultrafiltration component in membrane cisterna, the aperture of film is
0.08~0.5 μm, active pollution index and microorganism can be effectively intercepted, so that the difficult drop of nitrobacteria and degradation that the generation cycle is long
The dominant bacteria of solution pollutant is preserved in biological treatment system；Membrane cisterna bottom and membrane module bottom are equipped with aerator,
Aeration air is prevented film from blocking, also provides enough DO for the microorganism in membrane cisterna in addition to washing away film surface, anti-with fast degradation
Remaining carbon source is nitrified, since additional carbon is methanol or sodium acetate, remaining carbon source is easy to degradable；It is treated go out
Water is extracted out by water outlet pump from the water outlet of membrane module, and water outlet reaches " petro chemical industry pollutant emission standard " GB31571-
The requirement of the emission limit in general area in 2015 or " coking chemistry emission of industrial pollutants standard " GB16171-2012；If with
There is higher requirement at family, and ammonia nitrogen and total nitrogen can be by meeting after the parameter of control aerobic activated sludge pond and hypoxia activity sludge-tank
Ammonia nitrogen is less than 5mg/L, and total nitrogen is less than 15mg/L.
In addition part not bio-degradable can be removed by increasing catalytic ozonation facility after reactor of the invention
COD (i.e. hard COD), water outlet COD can reach less than 50mg/L, since ultrafiltration membrane delivery turbidity is less than 5NTU, not will increase
Additional ozone consumption；The activated sludge being trapped flows back into aerobic activated sludge pond front end by sludge reflux pump, and part is surplus
Remaining sludge discharge system.By bioselection pond, floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and film
The integrated film bioreactor (CCMBR) that pond is coupled into, can be according to factors such as actual size, place, investment and construction periods
It determines and uses reinforced concrete water pond or steel water tank.According to dirty water pollutant biochemical degradation characteristic, bioselection Chi Kezuo
For preaeration tank or hydrolysis acidification pool；When as preaeration tank, from aerobic activated sludge pond end reflux suspension, it can be recycled outstanding
Airlift, submersible water impeller or sewage pump can be used in DO in supernatant liquid, reflux unit；When as hydrolysis acidification pool, from lack
Flow back suspension for oxygen activity sludge-tank end, it is easy to just form hydrolysis environment, airlift does not can be used in reflux unit, can
Using submersible water impeller or sewage pump；The form of suspension reflux unit should be according to treatment scale and reflux ratio, to needed for promotion
Energy consumption and equipment investment be compared after determine.Hollow membrane or plate membrane can be used in hyperfiltration membrane assembly, can play same effect
Fruit.
In the method for the present invention, intake using aerobic activated sludge pond or the dilution of the suspension of hypoxia activity sludge-tank end,
Achieve the purpose that reduce sewage toxicity.In order to reach the purpose, it is only necessary to which consumption promotes required energy, has benefited from the present invention one
The reactor of body, hoisting depth and distance be it is the smallest, energy consumption is also the smallest.Conventional method otherwise use advanced oxidation processes
It pre-processes or is diluted using industry water or sewage of low concentration.That there are operating costs is very high for advanced oxidation processes pretreatment, to equipment
It is big with corrosion of pipe, generate secondary pollution the disadvantages of；It does not meet national energy-saving using industry water or sewage of low concentration dilution and subtracts
Row's policy, and the load for the treatment of facility is improved, increase operation energy consumption.It is compared with the traditional method, reduces sewage in the present invention
The method of toxicity has many advantages, such as that process is simple, equipment investment is low, operating cost is low, easy to operate.
In the method for the present invention, connected with aerobic activated sludge pond as aerobe reaction using floating stuffing oxidation pond
Pond.Floating stuffing oxidation pond combines the advantages of activated sludge process and biofilm, has both possessed microbial population in biofilm
Abundant, dominant bacteria enrichment, the features such as impact resistance ability is strong, at the same possess in activated sludge process microbial profile uniformly, pool capacity
The advantages that utilization rate is high, processing load adjustment is flexible, can also rejuvenate quickly under excess load or toxic pollutant impact, make
Treatment effect is stablized.In the method for the present invention, floating stuffing oxidation pond controls DO and is greater than 4mg/L, remove big portion as high load capacity section
Divide organic matter and make organic nitrogen ammonification, avoids fighting for oxygen in aerobic activated sludge pond and nitration reaction；Most of toxicity is organic
Object is also degraded, and the inhibiting effect to nitrobacteria is mitigated；Aerobic activated sludge pond as underload section, control DO be 2~
3mg/L, the dominant bacteria of nitrobacteria and degradation Recalcitrant chemicals rich in generation cycle length from the sludge that membrane cisterna flows back,
It can accelerate the degradation of hardly degraded organic substance and the nitrification of ammonia nitrogen, and keep reaction more thorough.With traditional aerobe reaction pond
Or short-cut nitrification and denitrification pond is compared, the method for the present invention has that reaction rate is fast, removal efficiency is high, strong shock resistance etc. is excellent
Point.
In the method for the present invention, nitrate nitrogen is removed using the hypoxia activity sludge-tank of postposition, nitre state liquid is discharged before reactor entirely
Portion is handled by denitrification.According to information and pilot plant test, there are the conditions such as sufficient and good carbon source, suitable DO and pH
Under, theoretically Denitrification rate is up to 100%, and the total nitrogen removal efficiency of reactor is up to 90% or more；Denitrification rate may be up to
1.0kgNO3- N/kgMLSS.d is the several times or even dozens of times of Prepositive denitrification, greatly reduces the residence time of anoxic pond,
Save occupied area.Traditional front establishment method is that aerobic biochemical pool end, the nitre state liquid without denitrification denitrogenation is straight
Run in secondary settling tank, is discharged after mud-water separation, nitrate is very high in water outlet.In order to improve denitrification percent, nitre in water outlet is reduced
State nitrogen content needs to improve the reflux ratio of nitre state liquid；And the reflux ratio of nitre state liquid is improved, and on the one hand energy consumption is caused to increase, it is another
Aspect causes the DO of anoxic pond to increase, and influences denitrification rate.So using level-one anoxic/aerobic total denitrification percent up to
75% or so.It is up to standard in order to be discharged total nitrogen, it needs using multi-stage anaerobic/aerobic process series connection, process is very long, increases engineering throwing
Money and place space.Compared with traditional Prepositive denitrification or short-cut nitrification and denitrification technique, hypoxia activity is dirty in the method for the present invention
Mud sump has many advantages, such as that nitric efficiency is high, process is simple, land occupation is few.Although carbon source needed for denitrification all relies on external carbon
Source, expense are lower compared with advanced oxidation processes or second level anoxic/aerobic.
High-quality water outlet not only can be obtained using ultrafiltration membrane pool component in reactor end, and it is dense can also to improve sludge in reactor
Degree extends sludge sludge age (SRT), keeps sludge loading lower, is conducive to the breeding enrichment of dominant bacteria, improves reaction rate.
There is toxic, high nitrogenous chemical engineering sewage using coupled film biological treatment and reactor for treatment of the invention, tool
There is removal efficiency high, strong shock resistance, being discharged COD, ammonia nitrogen and total nitrogen can stably reaching standard；Without using oxidant and catalysis
Agent, operating cost is low, without secondary pollution；Reactor is integrated, and saves land occupation and reduces mixed liquor and sludge reflux
Required energy consumption, construction investment are low；The advantages that process flow is simple, convenient operating maintenance, has good practical value, obtains
Preferable technical effect.
Detailed description of the invention
Fig. 1 is the structure and processing flow schematic diagram of present system；
A, toxic, the nitrogenous chemical engineering sewage of height: B, nutritive salt in figure；C, carbon source；D, treated water；E, excess sludge；
1, sludge reflux pump；2, aperture plate；3, suspension reflux unit；4, diving mixer；5, supermembrane component；6, water outlet pump.
Specific embodiment
Biological coupling membrane bioreactor (CCMBR) structure includes being sequentially connected in series as shown in Figure 1: in the present invention:
Bioselection pond 7, for carrying out adaptability screening to toxic, high nitrogenous chemical engineering sewage A treatment process microorganism
And primary treatment is carried out to toxic, high nitrogenous chemical engineering sewage A；
Floating stuffing oxidation pond 8 makes beneficial microbe implantation and breeds, and degradation is after bioselection pond 7 is handled in sewage
Characteristic contamination；
Aerobic activated sludge pond 9 makes after the processing of floating stuffing oxidation pond 8 nitre of organic matter degradation and ammonia nitrogen in sewage
Change；
Hypoxia activity sludge-tank 10, makes denitrifying bacteria quickly convert N for nitrate nitrogen2Evolution；
Suspension reflux unit is mounted in heretofore described aerobic activated sludge pond 9 and hypoxia activity sludge-tank 10
3。
Membrane cisterna 11 sludge and water is discharged respectively, and play degradation denitrification residue carbon source for separating sludge and water
Effect；
Bioselection pond 7 is connected to floating stuffing oxidation pond 8, aerobic activated sludge pond 9, hypoxia activity sludge-tank 10, institute
Bioselection pond 7 is stated to be coupled into floating stuffing oxidation pond 8, aerobic activated sludge pond 9, hypoxia activity sludge-tank 10 and membrane cisterna 11
For integrated membrane bioreactor.
The sewage that bioselection pond 7 is handled enters floating stuffing oxidation pond 8: the big ratio of filling in the floating stuffing oxidation pond 8
The floating stuffing of surface area, 8 bottom of pond of floating stuffing oxidation pond install mesoporous aerator, and control dissolved oxygen content is greater than 4mg/L, suspends
Setting filler in the outlet of filler oxidation pond 8 intercepts aperture plate 2.The sewage that floating stuffing oxidation pond 8 flows out and the work to flow back from membrane cisterna 11
Property sludge press than (0.5~1): 1 mixes in the aerobic activated sludge pond 9 for being equipped with micro-hole aerator, and the aerobic activity is dirty
The sludge concentration of mud sump 9 is 5~8g/L, and dissolved oxygen content is 2~3mg/L.
The nitre state liquid that aerobic activated sludge pond 9 is discharged, which enters, to be equipped in the hypoxia activity sludge-tank 10 of diving mixer 4,
Methanol or sodium acetate or glucose are added as carbon source C according to 4 times of concentration of total nitrogen concentration in nitre state liquid, and control dissolved oxygen content
Less than 0.5mg/L.
10 effluent of hypoxia activity sludge-tank enters membrane cisterna 11, installs submerged ultrafiltration component 5, ultrafiltration membrane in membrane cisterna 11
Component 5 is hollow membrane or plate membrane.Membrane cisterna bottom and membrane module bottom are mounted on aerator；After being handled using water outlet pump 6
Water D extracted out from the water outlet of membrane module, the activated sludge in membrane cisterna 11 is flowed back into the aerobic activity by sludge reflux pump 1
Sludge-tank 9 and/or floating stuffing oxidation pond 8, some residual sludge E are discharged at toxic, high nitrogenous chemical engineering sewage coupled film biology
Manage reactor.
In the present invention, nutritive salt B can be added into bioselection pond 7 to meet microbial reproduction institute according to the actual situation
The microelement needed.
Embodiment 1
Certain wet spinning acrylic fiber production waste, processing capacity 150m3/ h, after neutralizing and coagulation air-float removes oil removal
Water quality: COD:1000mg/L, total nitrogen: 115mg/L, ammonia nitrogen: 15mg/L, acrylonitrile: 80mg/L, sodium sulfocyanate: 100mg/L.
Treatment process and structure of reactor as shown in Figure 1, the coupling membrane bioreactor (CCMBR) used for reinforced concrete
Soil structure.
Floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and membrane cisterna carry out dirt in 2~4 weeks respectively
After mud inoculation and domestication, acrylon sewage sequentially enters bioselection pond, floating stuffing oxidation pond, aerobic activated sludge pond, anoxic
Activated sludge tank and membrane cisterna, final outflow water are extracted out from the hyperfiltration membrane assembly of membrane cisterna.
Bioselection pond is as mixing preaeration tank, the suspension of acrylic fiber production process sewage and the reflux of aerobic activated sludge pond end
Liquid mixing realizes using airlift and flows back, reflux ratio is taken 5, is stirred using compressed air；It is added by C:P for 200:1
Microcosmic salt, adding the pH value of lye control aerobic activated sludge pond is 7.5~8.1.
The water outlet of bioselection pond enters floating stuffing oxidation pond, and floating stuffing filling rate is 35% in pond, and filler surface has
Machine load (SALR) is 15g/m2D, floating stuffing specific surface area 500m2/m3, DO control is in 4~5mg/L；Floating stuffing oxidation pond
End mixed liquor enters aerobic activated sludge pond by the flowing hole of partition wall, and aperture plate intercepting padding material is arranged on flowing hole.
Mixed liquor mixes after entering aerobic activated sludge pond with the sludge to flow back from membrane cisterna, and control reflux ratio is 75%, dirty
Mud concentration about 5gMLSS/L, end DO about 2mg/L, design organic matter removal load are 0.18kgCOD/kgMLSS.d, and nitrification is negative
Lotus is 0.04kgNH3-N/kgMLSS.d。
The nitre state liquid of aerobic activated sludge pond end enters hypoxia activity sludge-tank, and denitrification load takes 0.50kgTN/
m3.d, methanol about 300mg/L is added according to 4 times of water inlet total nitrogen concentration, controls DO in 0.5mg/L hereinafter, installing diving in pond
Blender.
The effluent gravity stream of hypoxia activity sludge-tank enters membrane cisterna, installs immersion hollow fiber ultrafiltration membrane module in membrane cisterna.
The hydraulic detention time (HRT) of membrane cisterna is 2.5h, and ultrafiltration membrane flux is~17L/m2.h, the MBR ultrafiltration membrane gross area is needed to be
8823m2, by the MBR module membrane area 1500m of standard2/ group needs 6 groups of MBR modules altogether, is divided into 3 column, 2 groups of MBR modules of each column, often
Arranging a mating water yield is 75m3The frequency conversion suction pump of/h.Ultrafiltration membrane effluent quality are as follows: COD≤80mg/L, TN≤25mg/L,
NH3- N≤5mg/L, other indexs are also all satisfied " petro chemical industry pollutant emission standard " GB 31571-2015 discharge and want
It asks.2 150m are set3/ h sludge reflux pump, frequency control.Some residual sludge is from sludge pump outlet header's discharge system.
Water outlet COD substantially belongs to the COD of not bio-degradable, if it is desired to which COD≤60mg/L, can add after the reactor
Catalytic ozonation pond.
The operating cost statistics of this example 1 is as follows:
About 0.1 yuan/m of nutritive salt and lye expense3；Methanol dosage about 300mg/L, unit price is based on 1800 yuan/ton, methanol
Expense is 0.54 yuan/m3；The power consumption of Aeration fan, blender and pump about 2kW/m3Sewage, based on 0.7 yuan/kWh, the electricity charge are unit price
1.4 yuan/m3；MBR film presses 5 year replacement cycle, about 0.52 yuan/m of renewal cost3:
Total directly operating cost=0.1+0.54+1.4+0.52=2.56 member/m3。
Embodiment 2
Certain acrylonitrile installation production waste, processing capacity 50m3/ h, influent quality COD:
3500mg/L, total nitrogen: 280mg/L, ammonia nitrogen: 80mg/L, NO3 -- N:12mg/l, acrylonitrile: 100mg/L, pyridines:
600mg/L。
Treatment process and structure of reactor as shown in Figure 1, the coupling membrane bioreactor (CCMBR) used for reinforced concrete
Soil structure.
Floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and membrane cisterna carry out dirt in 2~4 weeks respectively
After mud inoculation and domestication, acrylonitrile sewage sequentially enters bioselection pond, floating stuffing oxidation pond, aerobic activated sludge pond, lacks
Oxygen activity sludge-tank and membrane cisterna, final outflow water are extracted out from the hyperfiltration membrane assembly of membrane cisterna.
Bioselection pond is mixed as the suspension that hydrolysis acidification pool, acrylonitrile sewage and hypoxia activity sludge-tank end are flowed back
It closes, is realized and flowed back using submersible water impeller, reflux ratio takes 3, HRT 8h；It is that 200:1 adds microcosmic salt by C:P, lye is added to control
The pH value of oxygen activity sludge-tank is 7.5~8.1.
Floating stuffing filling rate is 50% in floating stuffing oxidation pond, and the SALR of filler is 15g/m2.d, floating stuffing ratio
Surface area 500m2/m3, DO control is in 5~6mg/L；Floating stuffing oxidation pond end mixed liquor is entered by the flowing hole of partition wall
Oxygen activity sludge-tank, setting filler intercepts aperture plate on flowing hole.
Mixed liquor mixes after entering aerobic activated sludge pond with the sludge to flow back from membrane cisterna, reflux ratio 100%；Control pond
Interior sludge concentration about 6gMLSS/L, end DO about 2mg/L, organic matter removal load take 0.20kgCOD/kgMLVSS.d, and nitrification is negative
Lotus takes 0.04kgNH3-N/kgMLVSS.d。
The nitre state liquid of aerobic activated sludge pond end enters hypoxia activity sludge-tank, and denitrification rate takes 0.85kgTN/
m3.d, methanol is added according to 4 times of water inlet total nitrogen concentration, dosage about 800mg/L, DO should control 0.5mg/L hereinafter, pacifying in pond
Fill diving mixer.
The effluent gravity stream of hypoxia activity sludge-tank enters membrane cisterna, installs immersion hollow fiber ultrafiltration membrane module in membrane cisterna.
The design HRT of membrane cisterna is 4h, and ultrafiltration membrane flux is~15L/m2.h, needing the MBR ultrafiltration membrane gross area is 3333m2, by standard
MBR module membrane area 1500m2/ group needs 3 groups of MBR modules altogether, is divided into 3 column, 1 group of MBR module of each column, the mating water outlet of each column
Amount is 25m3The suction pump of the frequency control of/h.Ultrafiltration membrane effluent quality are as follows: COD≤100mg/L, TN≤40mg/L, NH3-N≤
8mg/L, other indexs are also all satisfied the requirement of " petro chemical industry pollutant emission standard " GB 31571-2015.Setting 2
50m3/ h sludge reflux pump, frequency control.Some residual sludge is from sludge pump outlet header's discharge system.
Contain the COD of higher not bio-degradable in acrylonitrile sewage, if it is desired to COD≤60mg/L, it can be in the reactor
After add catalytic ozonation pond.
2 operating cost of this example statistics is as follows:
About 0.25 yuan/m of nutritive salt and lye expense3；Methanol dosage about 800mg/L, unit price is based on 1800 yuan/ton, first
Alcohol expense is 1.44 yuan/m3；The power consumption of Aeration fan, blender and pump about 3.8kW/m3Sewage, unit price is based on 0.7 yuan/kWh, electricity
Take for 2.66 yuan/m3；MBR film presses 5 year replacement cycle, about 0.54 yuan/m of renewal cost3:
Total directly operating cost=0.25+1.44+2.66+0.54=4.89 member/m3。
Embodiment 3
Certain coking wastewater, processing capacity 100m3/ h recycles sodium phenolate, liquefied ammonia and cyanogen by dephenolize, ammonia still process, decyanation in advance
After compound, sewage quality COD:3000mg/L, ammonia nitrogen: 300mg/L, phenol: 300mg/L, cyanogen root: less than 20mg/L.
Treatment process and structure of reactor as shown in Figure 1, the coupling membrane bioreactor (CCMBR) used for reinforced concrete
Soil structure.
Floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and membrane cisterna carry out dirt in 2~4 weeks respectively
After mud inoculation and domestication, acrylon sewage sequentially enters bioselection pond, floating stuffing oxidation pond, aerobic activated sludge pond, anoxic
Activated sludge tank and membrane cisterna, final outflow water are extracted out from the hyperfiltration membrane assembly of membrane cisterna.
Bioselection pond is mixed as the suspension that hydrolysis acidification pool, coking wastewater and hypoxia activity sludge-tank end are flowed back
It closes, is realized and flowed back using sewage pump, reflux ratio takes 4, HRT 6h；It is that 200:1 adds microcosmic salt by C:P, lye is added to control aerobic work
Property sludge-tank pH value be 7.5~8.1.
The water outlet of bioselection pond enters floating stuffing oxidation pond, and the filling rate of floating stuffing is that 55%, SALR is in pond
25g/m2.d, specific surface area 800m2/m3, DO control is in 4~5mg/L；Floating stuffing oxidation pond end mixed liquor passes through partition wall
Flowing hole enter aerobic activated sludge pond, aperture plate intercepting padding material is set on flowing hole.
Mixed liquor mixes after entering aerobic activated sludge pond with the sludge to flow back from membrane cisterna, and control reflux ratio is 100%, dirty
Mud concentration about 6.5gMLSS/L, end DO about 2mg/L, design organic matter removal load are 0.17kgCOD/kgMLSS.d, nitrification
Load is 0.05kgNH3-N/kgMLSS.d。
The nitre state liquid of aerobic activated sludge pond end enters hypoxia activity sludge-tank, and denitrification load takes 0.70kgTN/
m3.d, methanol about 800mg/L is added according to 4 times of water inlet total nitrogen concentration, controls DO in 0.5mg/L hereinafter, installing diving in pond
Blender.
The effluent gravity stream of hypoxia activity sludge-tank enters membrane cisterna, installs immersion hollow fiber ultrafiltration membrane module in membrane cisterna.
The hydraulic detention time (HRT) of membrane cisterna is 4h, and ultrafiltration membrane flux is~17L/m2.h, the MBR ultrafiltration membrane gross area is needed to be
5882m2, by the MBR module membrane area 750m of standard2/ group needs 8 groups of MBR modules altogether, is divided into 4 column, 2 groups of MBR modules of each column, often
Arranging a mating water yield is 35m3The frequency conversion suction pump of/h.Ultrafiltration membrane effluent quality are as follows: COD≤80mg/L, TN≤20mg/L,
NH3-N≤10mg/L meets " coking chemistry emission of industrial pollutants standard " GB16171-2012 emission request.Setting 2
100m3/ h sludge reflux pump, frequency control.Some residual sludge is from sludge pump outlet header's discharge system.
The operating cost statistics of this example 3 is as follows:
About 0.2 yuan/m of nutritive salt and lye expense3；Methanol dosage about 800mg/L, unit price is based on 1800 yuan/ton, methanol
Expense is 1.44 yuan/m3；The power consumption of Aeration fan, blender and pump about 3.5kW/m3Sewage, unit price is based on 0.7 yuan/kWh, the electricity charge
For 2.45 yuan/m3；MBR film presses 5 year replacement cycle, about 0.53 yuan/m of renewal cost3, total directly operating cost=0.2+1.44+
2.45+0.53=4.62 member/m3。
Embodiment 4
Certain coal chemical industrial waste water, processing capacity 400m3/ h, by coagulation air-float or coagulating sedimentation removal petroleum-type and suspension
The sewage quality of object be COD:1500mg/L, ammonia nitrogen: 120mg/L, total nitrogen: 150mg/L, phenols: 100mg/L, cyanogen root: less than
10mg/L。
The coupling membrane bioreactor (CCMBR) used is reinforced concrete structure.
Floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and membrane cisterna carry out dirt in 2~4 weeks respectively
After mud inoculation and domestication, sewage sequentially enters bioselection pond, floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity
Sludge-tank and membrane cisterna, final outflow water are extracted out from the hyperfiltration membrane assembly of membrane cisterna.
Bioselection pond is mixed as mixing preaeration tank, sewage with the suspension that aerobic activated sludge pond end is flowed back,
It is realized and is flowed back using diving mixer, reflux ratio is taken 10, is stirred using compressed air；It is that 200:1 adds microcosmic salt by C:P,
The pH value for adding lye control aerobic activated sludge pond is 7.5~8.1.
The water outlet of bioselection pond enters floating stuffing oxidation pond, and the filling rate of floating stuffing is that 40%, SALR is in pond
20g/m2.d, specific surface area 800m2/m3, DO control is in 4~5mg/L；Floating stuffing oxidation pond end mixed liquor passes through partition wall
Flowing hole enter aerobic activated sludge pond, aperture plate intercepting padding material is set on flowing hole.
Mixed liquor mixes after entering aerobic activated sludge pond with the sludge to flow back from membrane cisterna, and control reflux ratio is 50%, dirty
Mud concentration about 5gMLSS/L, end DO about 2mg/L, design organic matter removal load are 0.16kgCOD/kgMLSS.d, and nitrification is negative
Lotus is 0.04kgNH3-N/kgMLSS.d。
The nitre state liquid of aerobic activated sludge pond end enters hypoxia activity sludge-tank, and denitrification load takes 0.55kgTN/
m3.d, sodium acetate about 900mg/L is added according to 4 times of water inlet total nitrogen concentration, controls DO in 0.5mg/L hereinafter, installing in pond latent
Water mixer.
The effluent gravity stream of hypoxia activity sludge-tank enters membrane cisterna, installs immersion hollow fiber ultrafiltration membrane module in membrane cisterna.
The hydraulic detention time (HRT) of membrane cisterna is 4.5h, and ultrafiltration membrane flux is~17L/m2.h, the MBR ultrafiltration membrane gross area is needed to be
23530m2, by the MBR module membrane area 1500m of standard2/ group needs 16 groups of MBR modules altogether, is divided into 4 column, 4 groups of MBR modules of each column,
The mating water yield of each column is 135m3The frequency conversion suction pump of/h.Ultrafiltration membrane effluent quality are as follows: COD≤60mg/L, TN≤
30mg/L, NH3-N≤5mg/L meet " petro chemical industry pollutant emission standard " GB31571-2015 emission request.Setting
2 400m3/ h sludge reflux pump, frequency control.Some residual sludge is from sludge pump outlet header's discharge system.
The operating cost statistics of this example 4 is as follows:
About 0.16 yuan/m of nutritive salt and lye expense3；Sodium acetate dosage about 900mg/L, it is monovalent based on 2500 yuan/ton,
Sodium acetate expense is 2.25 yuan/m3；The power consumption of Aeration fan, blender and pump about 1.8kW/m3Sewage, unit price press 0.7 yuan/kWh
Meter, the electricity charge are 1.26 yuan/m3；MBR film presses 5 year replacement cycle, about 0.52 yuan/m of renewal cost3, total directly operating cost=0.16
+ 2.25+1.26+0.52=4.19 member/m3。
The above is merely preferred embodiments of the present invention, practical range not for the purpose of limiting the invention, i.e. Fan Yiben
Equivalent changes and modifications made by the content of patent application the scope of the patents all should be technology scope of the invention.
Claims (10)
1. a kind of toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor, which is characterized in that including being sequentially connected in series
:
Bioselection pond carries out adaptability screening for the microorganism to sewage disposal process and carries out primary treatment to sewage；
Floating stuffing oxidation pond makes beneficial microbe implantation and breeds, and feature is dirty in sewage after the processing of bioselection pond for degradation
Contaminate object；
Aerobic activated sludge pond makes after the processing of floating stuffing oxidation pond the nitrification of organic matter degradation and ammonia nitrogen in sewage；
Hypoxia activity sludge-tank, makes denitrifying bacteria quickly convert N for nitrate nitrogen2Evolution；
Membrane cisterna sludge and water is discharged respectively, and play the work of degradation denitrification residue carbon source for separating sludge and water
With；
The bioselection pond is connected to floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank, the biology
It is raw that selection pond couples being integrally formed film with floating stuffing oxidation pond, aerobic activated sludge pond, hypoxia activity sludge-tank and membrane cisterna
Object reactor.
2. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as described in claim 1, which is characterized in that
Toxic, the high nitrogenous chemical engineering sewage initially enters the bioselection pond, and the aerobic activated sludge pond or lacks
The suspension of oxygen activity sludge-tank end reflux and the medicament added as needed are sufficiently mixed；Wherein, sewage and suspension
Reflux ratio is 2~10.
3. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as described in claim 1, which is characterized in that
The sewage handled through bioselection pond enters floating stuffing oxidation pond: Large ratio surface is filled in the floating stuffing oxidation pond
Long-pending floating stuffing, floating stuffing oxidation pond bottom of pond install mesoporous aerator, and control dissolved oxygen content is greater than 4mg/L, floating stuffing
Setting filler in oxidation pond outlet intercepts aperture plate.
4. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as described in claim 1, which is characterized in that
The sewage of the described floating stuffing oxidation pond outflow is pressed with the activated sludge to flow back from membrane cisterna than (0.5~1): 1 be equipped with it is micro-
It is mixed in the aerobic activated sludge pond of hole aerator, the sludge concentration of the aerobic activated sludge pond is 5~8g/L, dissolved oxygen content
For 2~3mg/L.
5. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as described in claim 1, which is characterized in that
The nitre state liquid of the aerobic activated sludge pond discharge, which enters, to be equipped in the hypoxia activity sludge-tank of diving mixer, according to nitre
4 times of concentration of total nitrogen concentration add methanol or sodium acetate or glucose as carbon source in state liquid, and control dissolved oxygen content and be less than
0.5mg/L。
6. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as described in claim 1, which is characterized in that
The hypoxia activity sludge-tank effluent enters membrane cisterna, installs immersion hollow membrane or flat membrane ultrafiltration membrane module in membrane cisterna,
Membrane cisterna bottom and membrane module bottom are mounted on aerator；Treated water is taken out from the water outlet of membrane module using water outlet pump
Out, the activated sludge in membrane cisterna is flowed back into the aerobic activated sludge pond and/or floating stuffing oxidation pond by sludge reflux pump,
Toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor is discharged in some residual sludge.
7. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as described in claim 1, which is characterized in that
The integrated film bioreactor is reinforced concrete water pond or steel water tank.
8. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as described in claim 1, which is characterized in that
The bioselection pond is preaeration tank or hydrolysis acidification pool.
9. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as claimed in claim 8, which is characterized in that
The bioselection pond is preaeration tank, and from the aerobic activated sludge pond end reflux suspension, reflux unit be can be used
Airlift, submersible water impeller or sewage pump.
10. toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor as claimed in claim 8, which is characterized in that
When the bioselection pond is hydrolysis acidification pool, from the hypoxia activity sludge-tank end reflux suspension, reflux unit is adopted
With submersible water impeller or sewage pump.
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| CN111732275A (en) * | 2020-06-25 | 2020-10-02 | 长春黄金研究院有限公司 | Advanced treatment method for high-hardness cyanide-containing wastewater |
| CN113354203A (en) * | 2021-06-15 | 2021-09-07 | 广东新大禹环境科技股份有限公司 | Biological treatment method for electroplating comprehensive wastewater |
| CN113603304A (en) * | 2021-08-19 | 2021-11-05 | 华南理工大学 | Three-sludge aerobic-hydrolysis-aerobic-membrane bioreactor and method |
| CN114105292A (en) * | 2020-08-27 | 2022-03-01 | 中国石油化工股份有限公司 | Wastewater denitrification device and process and application |
| CN114436473A (en) * | 2022-01-26 | 2022-05-06 | 北京铭泽源环境工程有限公司 | Full-flow nylon 66 salt production wastewater treatment method |
| CN116535001A (en) * | 2023-04-08 | 2023-08-04 | 山东源广环保科技有限公司 | Multiple synchronous nitrification and denitrification sewage treatment process |
| CN119643816A (en) * | 2025-02-18 | 2025-03-18 | 中国环境科学研究院 | Evaluation method for organic wastewater as sewage treatment carbon source |
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| CN113603304A (en) * | 2021-08-19 | 2021-11-05 | 华南理工大学 | Three-sludge aerobic-hydrolysis-aerobic-membrane bioreactor and method |
| CN114436473A (en) * | 2022-01-26 | 2022-05-06 | 北京铭泽源环境工程有限公司 | Full-flow nylon 66 salt production wastewater treatment method |
| CN116535001A (en) * | 2023-04-08 | 2023-08-04 | 山东源广环保科技有限公司 | Multiple synchronous nitrification and denitrification sewage treatment process |
| CN119643816A (en) * | 2025-02-18 | 2025-03-18 | 中国环境科学研究院 | Evaluation method for organic wastewater as sewage treatment carbon source |
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