CN110902979B - NMP wastewater biological treatment method and device - Google Patents
NMP wastewater biological treatment method and device Download PDFInfo
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- CN110902979B CN110902979B CN201911377494.4A CN201911377494A CN110902979B CN 110902979 B CN110902979 B CN 110902979B CN 201911377494 A CN201911377494 A CN 201911377494A CN 110902979 B CN110902979 B CN 110902979B
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- 238000000034 method Methods 0.000 title claims abstract description 66
- 239000002351 wastewater Substances 0.000 title claims abstract description 62
- 238000004062 sedimentation Methods 0.000 claims abstract description 143
- 230000008569 process Effects 0.000 claims abstract description 41
- 238000001556 precipitation Methods 0.000 claims abstract description 27
- 239000000701 coagulant Substances 0.000 claims abstract description 11
- 238000005189 flocculation Methods 0.000 claims abstract description 11
- 230000016615 flocculation Effects 0.000 claims abstract description 11
- 238000009388 chemical precipitation Methods 0.000 claims abstract description 10
- 238000002156 mixing Methods 0.000 claims abstract description 4
- 239000010802 sludge Substances 0.000 claims description 119
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 43
- 238000010992 reflux Methods 0.000 claims description 41
- 238000005273 aeration Methods 0.000 claims description 29
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 15
- 229910052760 oxygen Inorganic materials 0.000 claims description 15
- 239000001301 oxygen Substances 0.000 claims description 15
- 230000014759 maintenance of location Effects 0.000 claims description 12
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 claims description 8
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 229910052744 lithium Inorganic materials 0.000 claims description 5
- 239000002244 precipitate Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 40
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 20
- 239000010865 sewage Substances 0.000 abstract description 5
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 4
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 4
- 239000011574 phosphorus Substances 0.000 abstract description 4
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 47
- 238000003825 pressing Methods 0.000 description 16
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 14
- 239000000126 substance Substances 0.000 description 12
- 230000001546 nitrifying effect Effects 0.000 description 8
- 238000007599 discharging Methods 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 230000009286 beneficial effect Effects 0.000 description 5
- 239000011259 mixed solution Substances 0.000 description 5
- 239000013049 sediment Substances 0.000 description 5
- 239000002910 solid waste Substances 0.000 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 description 4
- 239000003153 chemical reaction reagent Substances 0.000 description 4
- 239000008103 glucose Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000004537 pulping Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 239000001632 sodium acetate Substances 0.000 description 3
- 235000017281 sodium acetate Nutrition 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000011085 pressure filtration Methods 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 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 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F2101/34—Organic compounds containing oxygen
-
- 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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- 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
Abstract
The invention provides an NMP wastewater biological treatment method and device, which belong to the technical field of sewage treatment, wherein the treatment method comprises the following steps: 1) Sequentially carrying out anaerobic treatment and anaerobic precipitation treatment on NMP wastewater to obtain first precipitation effluent; 2) Carrying out primary anoxic treatment, primary aerobic treatment, primary sedimentation treatment, secondary anoxic treatment, secondary aerobic treatment and secondary sedimentation treatment on the first sedimentation effluent to obtain secondary sedimentation effluent; 3) And mixing the secondary precipitation effluent with PAC flocculant and PAM coagulant for flocculation treatment, and performing physical and chemical precipitation to obtain final effluent. The method and the device can synchronously perform denitrification and dephosphorization, remove COD and reduce chromaticity, effectively solve the problems of difficult treatment of nitrogen and phosphorus in NMP wastewater, and the effluent can reach the emission standard; the whole process has small mud yield, effectively reduces the investment and the operation cost of the mud treatment, and has the advantages of low operation cost, simple operation management and the like.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to an NMP wastewater biological treatment method and device.
Background
In the lithium battery production process, a small amount of waste water is discharged, particularly in the positive and negative electrode pulping process in the lithium battery production process, raw materials such as methyl pyrrolidone NMP, graphite powder, carbon powder and the like are used in the pulping process; therefore, the cleaning wastewater discharged from the cleaning pulping tank after pulping is finished must contain pollutants such as NMP, SS (carbon powder, graphite powder) and the like, and substances such as SS (graphite powder, carbon powder) and the like in the wastewater can be effectively removed by utilizing a traditional coagulating sedimentation chemical method, but organic matters (CODcr) are difficult to reach standards.
Disclosure of Invention
In view of the above, the invention aims to provide a NMP wastewater biological treatment method and a NMP wastewater biological treatment device which have low running cost and are simple and convenient to operate; the treatment method can synchronously perform denitrification and dephosphorization, reduce COD value, has good treatment effect, and can reach the discharge standard after NMP wastewater is treated by the method and the device.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides an NMP wastewater biological treatment method, which comprises the following steps:
1) Sequentially performing anaerobic treatment and anaerobic precipitation treatment on NMP wastewater to obtain first precipitation effluent and a precipitate, and refluxing part of sludge to the anaerobic treatment process;
2) Carrying out primary anoxic treatment, primary aerobic treatment, primary sedimentation treatment, secondary anoxic treatment, secondary aerobic treatment and secondary sedimentation treatment on the first sedimentation effluent to obtain secondary sedimentation effluent;
3) Mixing the secondary precipitation effluent with PAC flocculant and PAM coagulant for flocculation treatment, and performing physical and chemical precipitation to obtain final effluent;
preferably, the anaerobic treatment temperature is 35-37 ℃, the pH value is 7.0-8.0, the hydraulic retention time is 0.5 days, and the sludge sedimentation ratio is 80-90%;
preferably, the carbon-nitrogen ratio of the primary anoxic treatment is 5:1, the hydraulic retention time of the primary anoxic treatment is 0.5 day, and the sludge sedimentation ratio is 80% -90%;
preferably, in the process of the secondary anoxic-secondary aerobic treatment, the dissolved oxygen in the anoxic treatment stage is less than or equal to 0.2mg/L, and the aeration rate is 0.5 to 1.0m 3 /(m 2 H); the dissolved oxygen in the aerobic treatment stage is 3-5 mg/L, and the aeration rate is 5-6 m 3 /(m 2 ·h)；
Preferably, the pH value of the primary aerobic treatment is 7.5-8.5; the sludge sedimentation ratio of the primary aerobic treatment is 70-80%;
preferably, the NMP wastewater is in a stepThe anaerobic treatment in step 1) is preceded by aeration pretreatment; the aeration quantity of the aeration pretreatment is 2-4 m 3 /(m 2 H), the aeration time is 6-8 h.
Preferably, the muddy water mixed solution in the anaerobic precipitation treatment in the step 1) flows back to the anaerobic treatment process according to the reflux ratio of 150-300%.
Preferably, the carbon-nitrogen ratio of the primary anoxic treatment is controlled by adding a carbon source.
Preferably, the nitrifying liquid generated by the primary aerobic treatment flows back to the primary anoxic treatment process according to the reflux ratio of 350-400%.
Preferably, the precipitated sludge in the primary precipitation treatment is refluxed to the primary anoxic treatment process according to a reflux ratio of 150-300%.
Preferably, the nitrifying liquid generated by the secondary aerobic treatment flows back to the secondary anoxic treatment process according to the reflux ratio of 350-400%; and the precipitated sludge in the secondary precipitation treatment is refluxed to the secondary anoxic treatment process according to the reflux ratio of 150-300%.
Preferably, the addition amount of the PAC flocculant in the step 3) is 0.5-1.0 kg per cubic meter of the third effluent, and the addition amount of the PAM coagulant is 0.005-0.010 kg.
The invention provides an NMP wastewater biological treatment device, which comprises an anaerobic tank, an anaerobic sedimentation tank, a primary anoxic tank, a primary aerobic tank, a primary sedimentation tank, a secondary anoxic tank, a secondary aerobic tank, a secondary sedimentation tank, a reaction tank and a materialized sedimentation tank which are sequentially communicated through pipelines;
a muddy water mixed liquid reflux device is arranged between the anaerobic sedimentation tank and the anaerobic tank, a nitrifying liquid reflux device is arranged between the primary aerobic tank and the primary anoxic tank, and a nitrifying liquid reflux device is arranged between the secondary aerobic tank and the secondary anoxic tank; the sludge reflux device is arranged between the primary sedimentation tank and the primary anoxic tank, the sludge reflux device is arranged between the secondary sedimentation tank and the secondary anoxic tank, and the primary sedimentation tank and the secondary sedimentation tank are communicated with the sludge concentration tank.
Preferably, the mud discharging port of the materialized sedimentation tank is communicated with the mud inlet of the mud concentrating tank.
The invention has the beneficial effects that: the NMP wastewater biological treatment method provided by the invention adopts a biological denitrification treatment process with the core of anaerobic treatment, anaerobic precipitation, two-stage anoxic-aerobic integrated treatment and precipitation treatment which are serially connected, and performs stepwise biological treatment on NMP wastewater by serially connecting two sections of anoxic and aerobic treatment to form a two-stage A/O process, so that denitrification and dephosphorization can be synchronously performed, COD (chemical oxygen demand) can be removed, chromaticity can be reduced, the problems of difficult treatment of nitrogen and phosphorus in NMP wastewater and the like can be effectively solved, and effluent can reach the discharge standard (COD is less than or equal to 500mg/L, ammonia nitrogen is less than or equal to 25mg/L and total nitrogen is less than or equal to 40mg/L in the wastewater quality standard of sewage discharge into cities (CJ 343-2010)); the whole process has small sludge yield, can digest most of sludge in the system, effectively reduces the investment and the operation cost of sludge treatment, and has the advantages of low operation cost, simple operation management and the like.
The invention provides an NMP wastewater biological treatment device, which is designed according to the treatment method provided by the invention, and comprises an anaerobic tank, an anaerobic sedimentation tank, a primary anoxic tank, a primary aerobic tank, a primary sedimentation tank, a secondary anoxic tank, a secondary aerobic tank, a secondary sedimentation tank, a reaction tank and a materialized sedimentation tank which are sequentially communicated through pipelines; the device provided by the invention has the advantages that the arrangement of each treatment tank is reasonable, the gradual biological treatment of NMP wastewater can be realized, the problems of difficult treatment of nitrogen and phosphorus in NMP wastewater and the like are effectively solved, the operation cost is low, the operation management is simple, and the like.
Drawings
FIG. 1 is a schematic diagram of a biological NMP wastewater treatment device according to the present invention, which comprises an adjusting tank (distribution tank), an anaerobic tank, an anaerobic sedimentation tank, a primary anoxic tank, a primary aerobic tank, a primary sedimentation tank, a secondary anoxic tank, a secondary aerobic tank, a secondary sedimentation tank, a reaction tank, a materialized sedimentation tank and a sludge tank.
Detailed Description
The invention provides an NMP wastewater biological treatment method, which comprises the following steps:
1) Sequentially performing anaerobic treatment and anaerobic precipitation treatment on NMP wastewater to obtain first precipitation effluent and a precipitate, and refluxing part of sludge to the anaerobic treatment process;
2) Carrying out primary anoxic treatment, primary aerobic treatment, primary sedimentation treatment, secondary anoxic treatment, secondary aerobic treatment and secondary sedimentation treatment on the first sedimentation effluent to obtain secondary sedimentation effluent;
3) Mixing the secondary precipitation effluent with PAC flocculant and PAM coagulant for flocculation treatment, and performing physical and chemical precipitation to obtain final effluent;
in the invention, NMP wastewater is subjected to anaerobic treatment and anaerobic precipitation treatment in sequence to obtain first precipitated effluent. And carrying out primary anoxic treatment, primary aerobic treatment, primary sedimentation treatment, secondary anoxic treatment, secondary aerobic treatment and secondary sedimentation treatment on the first sedimentation effluent to obtain secondary sedimentation effluent.
In the invention, the anaerobic treatment temperature is 35-37 ℃, the pH value is 7.0-8.0, the hydraulic retention time is 0.5 days, and the sludge sedimentation ratio is 80-90%; the carbon nitrogen ratio of the primary anoxic treatment is 5:1, the dissolved oxygen of the primary anoxic treatment is less than or equal to 0.2mg/L, the hydraulic retention time is 0.5 day, and the sludge sedimentation ratio is 80% -90%; the pH value of the primary aerobic treatment is 7.5-8.5; the dissolved oxygen of the primary aerobic treatment is 3-5 mg/L, and the sludge sedimentation ratio of the primary aerobic treatment is 70-80%; the aeration rate of the primary aerobic treatment is 5-6 m 3 /(m 2 H), the aeration rate of the primary anoxic treatment is 0.5-1.0 m 3 /(m 2 ·h)。
The type or source of the NMP wastewater is not particularly limited, and any NMP wastewater to be treated can be used. In the implementation process of the invention, the NMP wastewater is preferably NMP wastewater of a certain lithium battery production plant, the Chemical Oxygen Demand (COD) of the NMP wastewater is less than or equal to 8000mg/L, the ammonia nitrogen concentration (NH 3-N) is less than or equal to 100mg/L, the total nitrogen concentration (TN) is less than or equal to 700mg/L, the total phosphorus concentration (TP) is 5-10 mg/L, and most of suspended matters in the wastewater are carbon powder, graphite powder and the like.
In the invention, the NMP wastewater further comprises aeration pretreatment before the anaerobic treatment; the aeration quantity of the aeration pretreatment is preferably 2-4 m 3 /(m 2 H), more preferably 2.5 to 3.5m 3 /(m 2 H), the aeration time is 6-8 h. In the present invention, the aeration pretreatment is preferably carried out with stirring, and the rotation speed and the mode of stirring are not particularly limited, and stirring rotation speed and mode conventional in the art are adopted; the aeration pretreatment aims to remove a small part of organic matters through aerobic action in advance while sufficiently homogenizing water quality through aeration.
In the present invention, the anaerobic treatment is preferably carried out at 36℃and at a pH of 7.2 to 7.8, the hydraulic retention time of the anaerobic treatment is preferably 0.4 to 0.6d, more preferably 0.5d, and the sludge sedimentation ratio of the anaerobic treatment is preferably 80 to 90%, more preferably 82 to 88%, and most preferably 85%. The invention preferably controls the sludge sedimentation ratio of anaerobic treatment to be in the range of 80% -90%, and simultaneously cooperates with the limitation of the sludge sedimentation ratio in the subsequent primary anoxic-primary aerobic treatment process and the secondary anoxic-secondary aerobic treatment process, thereby being beneficial to ensuring the full removal of ammonia nitrogen and total nitrogen in NMP wastewater, and if the sludge sedimentation ratio of anaerobic treatment is too low, the ammonia nitrogen and/or total nitrogen in final effluent is easy to be not up to standard.
After the anaerobic treatment is finished, the NMP wastewater is subjected to anaerobic precipitation treatment, and first precipitated effluent is obtained. In the present invention, after the anaerobic precipitation treatment, the muddy water mixture is preferably refluxed to the anaerobic treatment process.
After the first precipitated effluent is obtained in the invention, the first-stage anoxic treatment is carried out to obtain a second effluent and muddy water mixed solution. In the present invention, the Dissolved Oxygen (DO) of the primary anoxic treatment is preferably not more than 0.2mg/L, more preferably 0.05 to 0.15mg/L; the primary anoxic treatment carbon nitrogen ratio (abbreviated as C/N, specifically the mass ratio of COD to ammonia nitrogen) is preferably (4-6): 1, more preferably 5:1. according to the invention, the carbon-nitrogen ratio of the system is controlled, so that the requirement of denitrifying bacteria on a carbon source under an anoxic condition can be met, and the denitrification efficiency is improved. The carbon to nitrogen ratio is preferably met by the present invention by adding a carbon source, which in the present invention preferably comprises glucose or sodium acetate. In the present invention, for example, 0.6 to 1kg of glucose or 0.8 to 1.2kg of sodium acetate, more preferably 0.8kg of glucose or 1.0kg of sodium acetate, is preferably added per cubic meter of NMP wastewater. In the present invention, the hydraulic retention time of the primary anoxic treatment is preferably 9 to 20 hours, more preferably 12 hours. In the invention, the sludge sedimentation ratio of the primary anoxic treatment is preferably 80-90%, more preferably 82-88%, and most preferably 85%; the invention preferably controls the sludge sedimentation ratio of the anoxic treatment within the range, and simultaneously combines the limitation of the sludge sedimentation ratio in the anaerobic treatment and the subsequent secondary anoxic treatment-secondary aerobic treatment process, thereby being beneficial to ensuring that ammonia nitrogen and total nitrogen in NMP wastewater are fully removed, and if the sludge sedimentation ratio of the anoxic treatment is too low, the ammonia nitrogen and/or total nitrogen in final effluent is easy to not reach the standard.
The invention preferably returns the muddy water mixed solution of the anaerobic sedimentation tank to the anaerobic treatment process according to the proportion of 150-300% of the reflux ratio. The invention preferably controls the reflux ratio of the muddy water mixed solution within the range, thereby being beneficial to reducing the operation load of the subsequent primary anoxic treatment-primary aerobic treatment and secondary anoxic treatment-secondary aerobic treatment, and further influencing the nitrification in the middle aerobic treatment stage of the secondary anoxic treatment-secondary aerobic treatment.
In the invention, the anaerobic treatment and anoxic treatment conditions can enable heterotrophic bacteria cultured by the anaerobic treatment and anoxic treatment to fully hydrolyze suspended matters and soluble organic matters in NMP wastewater into organic acids, and macromolecular organic matters are decomposed into micromolecular organic matters, and insoluble organic matters are converted into soluble organic matters, so that the subsequent primary anoxic treatment-primary aerobic treatment-secondary anoxic treatment-secondary aerobic treatment can be conveniently carried out.
After the first anoxic treatment, the invention carries out primary aerobic treatment on the obtained second effluent to obtain third effluent and nitrified liquid. In the invention, the pH value of the primary aerobic treatment is 7.5-8.5, preferably 7.8-8.2; the dissolved oxygen of the primary aerobic treatment is preferably 3-5 mg/L, more preferably 4mg/L; the aeration amount of the primary aerobic treatment is preferably 5-6 m 3 /(m 2 H), more preferably 5.2 to 5.8m 3 /(m 2 H); the primary aerobicThe sedimentation ratio of the treated sludge is preferably 70% to 80%, more preferably 72% to 78%, and most preferably 75%. In the present invention, the pH is preferably achieved by adding an alkaline reagent, and the type of the alkaline reagent is not particularly limited, so that the pH of the primary aerobic treatment can be ensured to be within a desired range, and in the specific implementation process of the present invention, a NaOH solution with a mass concentration of 20% is preferred. The limitation of the pH value is favorable for meeting the requirement of autotrophic bacteria nitrification under aerobic conditions on alkalinity.
The invention carries out the primary sedimentation treatment after the primary aerobic treatment is finished, in the invention, the surface load of the primary sedimentation treatment is preferably 0.6-0.8 m 3 /m 2 H, more preferably 0.7m 3 /m 2 H, the settling time is preferably 3 to 5h, more preferably 4h. After the primary sedimentation treatment, the sediment sludge obtained by the primary sedimentation treatment is preferably refluxed to the primary anoxic treatment process according to the reflux ratio of 150-300 percent; preferably, the surplus precipitated sludge is discharged into a sludge concentration tank, and is subjected to filter pressing concentration treatment by adopting a plate-and-frame filter press until the water content of the obtained concentrated sludge is about 70%, and then is transported out for disposal as general solid waste.
The invention carries out secondary anoxic treatment and secondary aerobic treatment after the primary sedimentation treatment. The dissolved oxygen of the secondary anoxic treatment is preferably less than or equal to 0.2mg/L, more preferably 0.05 to 0.15mg/L, and the aeration amount of the secondary anoxic treatment is preferably 0.5 to 1.0m 3 /(m 2 H), more preferably 0.6 to 0.9m 3 /(m 2 H); the dissolved oxygen of the secondary aerobic treatment is preferably 3-5 mg/L, more preferably 4mg/L; the aeration amount of the secondary aerobic treatment is preferably 5-6 m 3 /(m 2 H), more preferably 5.5m 3 /(m 2 H). In the present invention, the total hydraulic retention time of the secondary anoxic treatment and the secondary aerobic treatment is preferably 2.5d, and the hydraulic retention time of the secondary anoxic treatment and the secondary aerobic treatment is preferably equal. In the present invention, the sludge sedimentation ratio (SV 30) of the secondary anoxic treatment and the secondary aerobic treatment is preferably 70% to 80%,more preferably 72% to 78%; the invention preferably controls the sludge sedimentation ratio of the secondary anoxic treatment and the secondary aerobic treatment within the range, and simultaneously combines the limitation of the sludge sedimentation ratio in the anaerobic treatment and the primary anoxic treatment-primary aerobic treatment process, thereby being beneficial to ensuring the full removal of ammonia nitrogen and total nitrogen in NMP wastewater, and if the sludge sedimentation ratio of the secondary anoxic-aerobic comprehensive treatment is too low, ammonia nitrogen and/or total nitrogen in final effluent is easy to be not up to standard.
After the secondary aerobic treatment, the effluent from the secondary aerobic treatment is subjected to secondary sedimentation treatment. In the present invention, the secondary precipitation treatment surface load is preferably 0.6 to 0.8m 3 /m 2 H, more preferably 0.7m 3 /m 2 H, the settling time is preferably 2 to 4h, more preferably 3h. After the secondary sedimentation treatment, the sediment sludge obtained by the secondary sedimentation treatment is preferably refluxed into the secondary anoxic treatment process according to the reflux ratio of 150-300 percent; preferably, the surplus precipitated sludge is discharged into a sludge concentration tank, and is subjected to filter pressing concentration treatment by adopting a plate-and-frame filter press until the water content of the obtained concentrated sludge is about 70%, and then is transported out for disposal as general solid waste.
After the secondary sedimentation treatment, the secondary sedimentation effluent is mixed with PAC flocculant and PAM coagulant for flocculation treatment, and then physical and chemical sedimentation is carried out to obtain final effluent. In the present invention, al in the PAC flocculant 2 O 3 The content is preferably 24%, and the molecular weight of the PAM coagulant is preferably 1200 ten thousand. In the present invention, the PAC flocculant is preferably added in an amount of 0.5 to 1.0kg, more preferably 0.6 to 0.9kg, per cubic meter of the third effluent; the addition amount of the PAM coagulant is preferably 0.005 to 0.010kg, more preferably 0.006 to 0.009kg. The flocculation treatment time in the present invention is preferably 10 to 20 minutes, more preferably 15 minutes. The invention removes Suspended Substances (SS) of the third effluent and reduces the chromaticity by flocculation treatment, so that the chromaticity of the treated sewage is 80 times or less.
After the flocculation treatment, the invention carries out physical and chemical precipitation to obtain the final effluent. The materialized precipitation treatment in the invention mainly further realizes mud-water separation, so that the effluent is clearer, and the sludge loss is avoided. The specific operation conditions of the physical and chemical precipitation treatment are not particularly limited, and those well known to those skilled in the art may be employed. In the invention, after physical and chemical precipitation treatment, the obtained effluent can reach the discharge standard and can be directly discharged. In the invention, the materialized and precipitated sludge is also obtained after materialized and precipitated treatment, and the materialized and precipitated sludge is preferably subjected to filter pressing concentration treatment; the present invention is not particularly limited to the above-mentioned pressure filtration concentration treatment, and may be carried out by referring to the above-mentioned method for pressure filtration concentration treatment of the precipitated sludge. In the invention, after the materialized and precipitated sludge is subjected to filter pressing concentration treatment, the water content of the obtained concentrated sludge is about 70 percent, and the obtained concentrated sludge can be further treated as common solid waste. In the invention, the final effluent preferably overflows to a clean water tank and is discharged through a discharge port of the clean water tank.
In the invention, in order to ensure that the sludge of anaerobic treatment, primary anoxic-primary aerobic treatment and secondary anoxic-secondary aerobic treatment preferably adopts the activated sludge of a sludge concentration tank of an urban sewage treatment plant when a system is started, the sludge in the starting period reaches the sludge concentration requirement; the specific manner of operation of the relevant steps is not limited and may be in any manner known to those skilled in the art.
In the invention, part of the precipitated sludge is returned to anaerobic treatment, and the residual precipitated sludge is subjected to filter pressing concentration treatment in the process of primary anoxic treatment, secondary anoxic treatment and secondary aerobic treatment. In the invention, the reflux process is concretely as follows, in the anaerobic treatment process, the sludge in the anaerobic sedimentation tank is refluxed to the anaerobic treatment process; the sludge in the first-stage sedimentation tank flows back to the first-stage anoxic treatment process, and the sludge in the second-stage sedimentation tank flows back to the second-stage anoxic treatment process. The invention preferably adopts the treatment, is favorable for greatly reducing the residual sludge and is convenient for the subsequent filter pressing concentration treatment. In the invention, after the precipitation treatment, the residual sludge is preferably 2 to 5 percent of the total amount of the obtained precipitation sludge and is subjected to subsequent filter pressing concentration treatment. (after each 1000 tons of NMP wastewater is treated, the produced materialized precipitated sludge is subjected to filter pressing concentration treatment, about 0.5 ton of concentrated sludge is obtained, and the investment and the operation cost of sludge treatment are effectively reduced)
The invention provides an NMP wastewater biological treatment device, which comprises an anaerobic tank, an anaerobic sedimentation tank, a primary anoxic tank, a primary aerobic tank, a primary sedimentation tank, a secondary anoxic tank, a secondary aerobic tank, a secondary sedimentation tank, a reaction tank and a materialized sedimentation tank which are sequentially communicated through pipelines;
in the invention, a muddy water mixed liquid reflux device is arranged between the anaerobic sedimentation tank and the anaerobic tank, a nitrifying liquid reflux device is arranged between the primary aerobic tank and the primary anoxic tank, and a nitrifying liquid reflux device is arranged between the secondary aerobic tank and the secondary anoxic tank; the sludge reflux device is arranged between the primary sedimentation tank and the primary anoxic tank, the sludge reflux device is arranged between the secondary sedimentation tank and the secondary anoxic tank, and the primary sedimentation tank and the secondary sedimentation tank are communicated with the sludge concentration tank. The mud discharging port of the materialized sedimentation tank is preferably communicated with the mud inlet of the mud concentration tank.
In the invention, the device also comprises an adjusting tank, and an anaerobic lifting pump is arranged between the adjusting tank and the anaerobic tank and used for pumping the effluent of the adjusting tank into the anaerobic tank; the anaerobic lift pump is preferably a stainless steel transfer pump.
In the invention, a sludge reflux device is arranged between the anaerobic sedimentation tank and the anaerobic tank, the primary anoxic-aerobic treatment and the secondary anoxic-aerobic treatment, so that the sedimentation sludge generated in the anaerobic sedimentation tank is refluxed to the anaerobic tank, the residual sludge in the primary sedimentation tank is refluxed to the primary anoxic tank, and the residual sludge in the secondary sedimentation tank is refluxed to the secondary anoxic tank. As an embodiment of the invention, a sludge outlet and a sludge reflux pump can be arranged at the bottoms of the 3 sedimentation tanks, so that the sedimentation sludge can be respectively refluxed into the anaerobic tank, the primary anoxic tank and the secondary anoxic tank through pipelines.
In the invention, the primary sedimentation tank and the secondary sedimentation tank are communicated with a sludge concentration tank, and particularly, the sludge outlets of the primary sedimentation tank and the secondary sedimentation tank are communicated with the sludge inlet of the sludge concentration tank; the sludge concentration tank is used for carrying out filter pressing concentration treatment on sludge so as to realize sludge reduction and facilitate outward transportation and disposal.
In the invention, the NMP wastewater biological treatment device comprises a reaction tank and a materialized sedimentation tank, in particular, a water inlet of the reaction tank is communicated with a water outlet of the secondary sedimentation tank, and a water outlet of the reaction tank is communicated with a water inlet of the materialized sedimentation tank; the reaction tank and the materialized sedimentation tank are used for carrying out flocculation-sedimentation treatment on the effluent of the secondary sedimentation tank.
As one embodiment of the invention, the sludge discharge port of the materialized and precipitated tank is communicated with the sludge inlet of the sludge concentration tank so as to realize the filter pressing concentration treatment of materialized and precipitated sludge generated in the materialized and precipitated tank.
As an embodiment of the invention, the NMP wastewater biological treatment device further comprises a clean water tank, wherein a water inlet of the clean water tank is communicated with a water outlet of the materialized sedimentation tank, and is used for containing standard-reaching effluent discharged by the materialized sedimentation tank and further discharging the standard-reaching effluent.
The shape, the size and the like of each treatment tank in the NMP wastewater biological treatment device are not particularly limited, and the corresponding treatment process can be ensured to be smoothly carried out according to the water treatment amount.
FIG. 1 is a schematic diagram of the biological treatment device for NMP wastewater. The following describes a method for treating NMP wastewater by using the NMP wastewater biological treatment device provided by the invention with reference to fig. 1:
firstly, collecting wastewater to be treated, then automatically flowing into an adjusting tank for aeration pretreatment, and lifting the effluent of the adjusting tank into an anaerobic tank for anaerobic treatment by an anaerobic lifting pump; the effluent of the anaerobic tank flows into an anaerobic sedimentation tank, and the muddy water mixed solution generated by the anaerobic sedimentation tank is controlled to flow back into the anaerobic tank according to the reflux ratio of 150-300%;
the effluent (first effluent) of the anaerobic sedimentation tank automatically flows into a secondary anoxic-secondary aerobic comprehensive treatment tank (comprising an anoxic tank 1, an aerobic tank 1, a primary sedimentation tank, an anoxic tank 2, an aerobic tank 2 and a secondary sedimentation tank which are communicated with each other).
The effluent (second effluent) of the anoxic tank 1 in the comprehensive treatment tank flows into the aerobic tank 2 automatically, an alkaline reagent is added at the water inlet of the aerobic tank 1 to control the pH value of the system to 7.5-8.5, and simultaneously, nitrifying liquid generated by the aerobic tank flows back into the anoxic tank 1 according to the reflux ratio of 350-400%;
automatically flowing the effluent (third effluent) of the primary aerobic tank to a primary sedimentation tank for sedimentation treatment, wherein the obtained sediment sludge is refluxed to the primary anoxic tank according to a reflux ratio of 150% -300%; discharging the residual precipitated sludge into a sludge concentration tank for filter pressing concentration treatment;
and (3) automatically flowing the effluent (fourth effluent) of the primary sedimentation tank to a secondary anoxic tank for anoxic treatment.
The effluent (fifth effluent) of the secondary anoxic tank automatically flows into the secondary aerobic tank, and nitrified liquid generated by the aerobic tank flows back into the secondary anoxic tank according to the reflux ratio of 350-400%;
automatically flowing the effluent (sixth effluent) of the secondary aerobic tank into a secondary sedimentation tank for sedimentation treatment, wherein the obtained sedimentation sludge is refluxed to the secondary anoxic tank according to a reflux ratio of 150% -300%; discharging the residual precipitated sludge into a sludge concentration tank for filter pressing concentration treatment;
the effluent of the secondary sedimentation tank automatically flows into a reaction tank, and a flocculating agent and a coagulant are added at a water inlet of the reaction tank for flocculation treatment;
the effluent of the reaction tank automatically flows into a materialized sedimentation tank for materialized sedimentation treatment to obtain materialized sedimentation sludge and effluent reaching the standard; the materialized and precipitated sludge is discharged into a sludge concentration tank for filter pressing concentration treatment; and the effluent reaching the standard overflows to a clean water tank and is discharged through a discharge port of the clean water tank.
The technical solutions provided by the present invention are described in detail below with reference to examples, but they should not be construed as limiting the scope of the present invention.
Example 1
NMP waste water from a lithium battery production plant is used as NMP waste water to be treated for treatment, and the Chemical Oxygen Demand (COD) of the NMP waste water from the plant is 8000mg/L, and ammonia nitrogenConcentration (NH) 3 -N) is 100mg/L, total nitrogen concentration (TN) is 700mg/L, and suspended matters in the wastewater are mostly graphite powder, carbon powder impurities and the like.
S1: after the wastewater is collected, the wastewater automatically flows into a regulating tank to regulate the water quality and the water quantity, an aeration stirring device is arranged in the regulating tank, and the aeration intensity is controlled to be 3m 3 /(m 2 H), performing aeration pretreatment;
s2: lifting the effluent of the regulating tank into an anaerobic tank through an anaerobic lifting pump (specifically a stainless steel conveying pump) for anaerobic treatment; wherein the temperature of anaerobic treatment is controlled at 36 ℃, the pH value is controlled at 7.8, the hydraulic retention time is 0.5 day, and the sludge sedimentation ratio (SV 30) is 85%;
s3: automatically flowing the effluent of the anaerobic tank into an anaerobic sedimentation tank, controlling the mud-water mixed liquor of the sedimentation tank to be in a reflux ratio of 150-300%, and refluxing the mud-water mixed liquor to the anaerobic treatment process;
s4: the method comprises the steps that effluent (first effluent) of an anaerobic sedimentation tank flows into an anoxic 1 process in a secondary anoxic-aerobic system (comprising an anoxic tank 1, an aerobic tank 1, a primary sedimentation tank, an anoxic tank 2, an aerobic tank 2 and a secondary sedimentation tank which are communicated), glucose is added to a water inlet of the anoxic tank 1, so that the carbon nitrogen ratio of the system in the anoxic tank 1 is 5:1, performing anoxic treatment; wherein, the dissolved oxygen in the anoxic treatment is less than or equal to 0.2mg/L, the hydraulic retention time is 0.5 day, and the sludge sedimentation ratio (SV 30) is 85%;
s5: automatically flowing the effluent (second effluent) of the anoxic tank 1 into an aerobic tank 1, adding an alkaline reagent (NaOH solution with the mass concentration of 20%) into a water inlet of the aerobic tank 1, controlling the pH value of the system to be 7.5-8.5, and carrying out aerobic treatment; the dissolved oxygen in the aerobic treatment stage is 4mg/L, and the aeration rate is 5.5m 3 /(m 2 H) a sludge sedimentation ratio (SV 30) of 75%; simultaneously, the nitrifying liquid generated by the aerobic tank 1 is refluxed into the anoxic tank 1 according to the reflux ratio of 380 percent;
s6: automatically flowing the effluent (third effluent) of the aerobic tank 1 into a first-stage sedimentation tank for sedimentation treatment, wherein the obtained sediment sludge is refluxed into the anoxic tank 1 according to a reflux ratio of 200%; discharging the residual precipitated sludge into a sludge concentration tank, performing filter pressing concentration treatment on the residual precipitated sludge by adopting a plate-and-frame filter press until the water content of the obtained concentrated sludge is about 70%, and then carrying out outward treatment to treat the residual precipitated sludge as general solid waste;
s7: the effluent (fourth effluent) of the first-stage sedimentation tank automatically flows to an anoxic tank 2 for anoxic treatment; the effluent (fifth effluent) of the anoxic tank 2 automatically flows into the aerobic tank 2, and nitrified liquid generated in the aerobic tank flows back into the anoxic tank according to the reflux ratio of 350-400%;
s8: automatically flowing the effluent (sixth effluent) of the aerobic tank 2 into a secondary sedimentation tank for sedimentation treatment, wherein the obtained sedimentation sludge is refluxed to the anoxic tank 2 according to a reflux ratio of 200%; discharging the residual precipitated sludge into a sludge concentration tank for filter pressing concentration treatment;
s9: automatically flowing the effluent (seventh effluent) of the secondary sedimentation tank to a reaction tank, and adding PAC flocculant (Al) at the water inlet of the reaction tank 2 O 3 24% of the content) and PAM coagulant (molecular weight is 1200 ten thousand), and performing flocculation treatment; wherein, the dosage of the PAC flocculant is 0.7kg and the dosage of the PAM coagulant is 0.007kg based on the third water outlet per cubic meter;
s10: the effluent of the reaction tank automatically flows into a materialized sedimentation tank for materialized sedimentation treatment to obtain materialized sediment sludge and final effluent; the materialized and precipitated sludge is discharged into a sludge concentration tank, is subjected to filter pressing by adopting a plate-and-frame filter press until the water content of the obtained concentrated sludge is about 70%, and is then transported to be treated as general solid waste; the final effluent overflows to a clean water tank and is discharged through a discharge port of the clean water tank;
in the embodiment, the COD of the NMP wastewater treated by the secondary anoxic-aerobic comprehensive treatment tank is less than 600mg/L; ammonia nitrogen concentration is less than 25mg/L; the total nitrogen concentration is less than 55mg/L;
after flocculation treatment, suspended Substances (SS) in NMP wastewater are removed, the chromaticity is reduced, COD in the final effluent obtained after physical and chemical precipitation treatment is less than 500mg/L, ammonia nitrogen concentration is less than 25mg/L, total nitrogen concentration is less than 40mg/L, and the effluent reaches the discharge standard (COD is less than or equal to 500mg/L, ammonia nitrogen is less than or equal to 25mg/L, and total nitrogen is less than or equal to 40 mg/L) in the wastewater quality standard (CJ 343-2010) of urban sewer, and can be directly discharged.
Comparative example 1
The procedure of example 1 was repeated except that the anaerobic treatment was performed at a sludge sedimentation ratio of 55%, the primary anoxic-aerobic treatment was performed at a sludge sedimentation ratio of 55%, and the secondary anoxic-aerobic treatment was performed at a sludge sedimentation ratio of 55%. The ammonia nitrogen in the effluent water after physical and chemical precipitation treatment can still be reduced to below 25mg/L, but the total nitrogen is about 31-60 mg/L, and the total nitrogen is not up to the standard at the moment.
Comparative example 2
The procedure of example 1 was repeated except that the anaerobic treatment was performed at a sludge sedimentation ratio of 35%, the primary anoxic-aerobic treatment was performed at a sludge sedimentation ratio of 35%, and the secondary anoxic-aerobic treatment was performed at a sludge sedimentation ratio of 35%. The ammonia nitrogen in the effluent water of the physical and chemical precipitation treatment is about 21-30 mg/L, and the total nitrogen is about 61-90 mg/L, at this time, the ammonia nitrogen and the total nitrogen do not reach the standard.
The foregoing is merely a preferred embodiment of the present invention and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present invention, which are intended to be comprehended within the scope of the present invention.
Claims (7)
1. A method for biologically treating NMP wastewater, comprising the steps of:
1) Sequentially performing anaerobic treatment and anaerobic precipitation treatment on NMP wastewater to obtain first precipitation effluent and a precipitate, and refluxing part of sludge to the anaerobic treatment process;
2) Carrying out primary anoxic treatment, primary aerobic treatment, primary sedimentation treatment, secondary anoxic treatment, secondary aerobic treatment and secondary sedimentation treatment on the first sedimentation effluent to obtain secondary sedimentation effluent;
3) Mixing the secondary precipitation effluent with PAC flocculant and PAM coagulant for flocculation treatment, and performing physical and chemical precipitation to obtain final effluent;
the anaerobic treatment temperature is 35-37 ℃, the pH value is 7.0-8.0, the hydraulic retention time is 0.5 days, and the sludge sedimentation ratio is 80% -90%;
the carbon-nitrogen ratio of the primary anoxic treatment is 5:1, the hydraulic retention time of the primary anoxic treatment is 0.5 day, and the sludge sedimentation ratio is 80% -90%;
in the process of the secondary anoxic-secondary aerobic treatment, the dissolved oxygen in the anoxic treatment stage is less than or equal to 0.2mg/L, and the aeration rate is 0.5-1.0 m 3 /(m 2 H); the dissolved oxygen in the aerobic treatment stage is 3-5 mg/L, and the aeration rate is 5-6 m 3 /(m 2 ·h)；
The pH value of the primary aerobic treatment is 7.5-8.5; the sludge sedimentation ratio of the primary aerobic treatment is 70-80%;
the NMP wastewater is NMP wastewater of lithium battery factories.
2. The process according to claim 1, wherein said NMP wastewater further comprises an aeration pretreatment prior to said anaerobic treatment of step 1); the aeration quantity of the aeration pretreatment is 2-4 m 3 /(m 2 H), and the aeration time is 6-8 h.
3. The treatment method according to claim 1, wherein the slurry-water mixture in the anaerobic precipitation treatment in step 1) is refluxed to the anaerobic treatment process at a reflux ratio of 150-300%.
4. The method according to claim 1, wherein the carbon-nitrogen ratio of the primary anoxic treatment is controlled by adding a carbon source.
5. The treatment method according to claim 1, wherein the nitrified liquid produced by the primary aerobic treatment is returned to the primary anoxic treatment process at a reflux ratio of 350-400%.
6. The treatment method according to claim 1, wherein the precipitated sludge in the primary precipitation treatment is returned to the primary anoxic treatment process at a reflux ratio of 150% -300%.
7. The treatment method according to claim 1, wherein the nitrified liquid generated by the secondary aerobic treatment is refluxed to the secondary anoxic treatment process according to a reflux ratio of 350-400%; and the precipitated sludge in the secondary precipitation treatment is refluxed to the secondary anoxic treatment process according to the reflux ratio of 150% -300%.
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