CN116730544A - Efficient treatment system and process for dye intermediate wastewater - Google Patents
Efficient treatment system and process for dye intermediate wastewater Download PDFInfo
- Publication number
- CN116730544A CN116730544A CN202310813192.7A CN202310813192A CN116730544A CN 116730544 A CN116730544 A CN 116730544A CN 202310813192 A CN202310813192 A CN 202310813192A CN 116730544 A CN116730544 A CN 116730544A
- Authority
- CN
- China
- Prior art keywords
- tank
- wastewater
- anoxic
- sludge
- aerobic
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 146
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000007062 hydrolysis Effects 0.000 claims abstract description 48
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 48
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 8
- 231100000719 pollutant Toxicity 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 87
- 230000001105 regulatory effect Effects 0.000 claims description 79
- 239000010802 sludge Substances 0.000 claims description 69
- 238000004062 sedimentation Methods 0.000 claims description 62
- 239000007788 liquid Substances 0.000 claims description 40
- 238000006386 neutralization reaction Methods 0.000 claims description 35
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 27
- 229910052799 carbon Inorganic materials 0.000 claims description 27
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 23
- 238000010992 reflux Methods 0.000 claims description 23
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims description 20
- 230000020477 pH reduction Effects 0.000 claims description 17
- 230000001546 nitrifying effect Effects 0.000 claims description 15
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 239000011780 sodium chloride Substances 0.000 claims description 12
- 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 11
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 11
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 11
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 11
- 235000019270 ammonium chloride Nutrition 0.000 claims description 10
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 claims description 9
- 238000005273 aeration Methods 0.000 claims description 9
- 239000003814 drug Substances 0.000 claims description 9
- 238000006396 nitration reaction Methods 0.000 claims description 9
- 238000003825 pressing Methods 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 9
- 238000005276 aerator Methods 0.000 claims description 8
- 239000000945 filler Substances 0.000 claims description 8
- 244000005700 microbiome Species 0.000 claims description 7
- 238000004065 wastewater treatment Methods 0.000 claims description 7
- 235000012255 calcium oxide Nutrition 0.000 claims description 6
- 239000000292 calcium oxide Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000000463 material Substances 0.000 abstract description 2
- 239000000543 intermediate Substances 0.000 description 22
- 235000002639 sodium chloride Nutrition 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000010865 sewage Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 150000002826 nitrites Chemical class 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 230000001112 coagulating effect Effects 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 230000000593 degrading effect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- 150000007522 mineralic acids Chemical class 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 150000001448 anilines Chemical class 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000010919 dye waste Substances 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 150000002391 heterocyclic compounds Chemical class 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000010977 unit operation 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/308—Dyes; Colorants; Fluorescent agents
-
- 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
- C02F3/02—Aerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/286—Anaerobic digestion processes including two or more steps
-
- 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
-
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
Landscapes
- Life Sciences & Earth Sciences (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)
Abstract
The invention provides a dye intermediate wastewater high-efficiency treatment system and a process, wherein the system comprises a high-index low-salt wastewater pretreatment system, a mixed hydrolysis pretreatment system, a multistage reinforced AO system and the like. The high-efficiency treatment system for the waste water of the material intermediate can adapt to the condition of large fluctuation of the quality and quantity of the waste water of the dye intermediate, can effectively remove pollutants, and has low operation cost.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a dye intermediate wastewater efficient treatment system and a process.
Background
The dye waste water mainly comes from dye, printing and dyeing and dye intermediate production industries, and consists of waste mother liquor of various products and intermediate crystallization, materials lost in various working procedures in the production process and sewage for flushing the ground.
The dye production is often carried out from raw materials, intermediates to products through various unit operations, and the production technology and the production process are complex, the production flow is long, the side reactions are more, and the conversion rate and the yield of the products are low due to certain reasons. During the production process, about 10-30% of the organic raw material and 90% of the inorganic raw material are transferred into the waste water of the dye production, resulting in the presence of a large amount of organic compounds in the waste water. In the production process of the dye, a large amount of inorganic acid, alkali and inorganic salt are consumed, about 90% of the inorganic acid, alkali and inorganic salt are transferred into the wastewater, so that the pH value of the wastewater is greatly changed, the common salt content is very high, the dye mainly contains ammonium sulfate and sodium chloride, and anilines and heterocyclic compounds are also stored in the wastewater and are difficult to degrade by microorganisms. On the other hand, the dye production has the characteristics of small batch and multiple varieties, most of the dye production is intermittently operated, the wastewater discharge is intermittent, and the water quantity and the water quality have great fluctuation and change, so that a lot of difficulties are added to the engineering design and operation management of wastewater treatment.
Therefore, the treatment of dye wastewater is still an important and difficult task for the industry environment protection, and one of the most difficult wastewater treatment with dye and intermediate wastewater is urgent to need new technologies, new processes to reform or replace the traditional processes, and new treatment technologies are sought in the aspect of wastewater treatment.
The traditional dye intermediate wastewater treatment method is generally neutralization, coagulating sedimentation and biochemical treatment, or neutralization, iron-carbon micro-electrolysis and sedimentation, or catalytic oxidation, resin adsorption and other processes, and the treatment methods do not achieve ideal effects from the main pollution index removal rate to the running cost.
Therefore, it is necessary to develop a dye intermediate wastewater efficient treatment system and process that is effective in treatment and low in operating cost.
Disclosure of Invention
In order to solve the defects in the prior art, the invention provides a high-efficiency treatment system and a technology for dye intermediate wastewater, which can realize the purposes of standard removal of main pollutants of the dye intermediate wastewater and low operation cost, and the specific technical scheme is as follows:
the invention firstly provides a dye intermediate wastewater high-efficiency treatment system which comprises a No. 1 pre-acidification tank, a Fenton reactor, a neutralization tank, a filter press, a No. 1 wastewater regulating tank, a comprehensive regulating tank, a mixed hydrolysis tank, a No. 1 anoxic tank, a No. 1 aerobic tank, a No. 2 anoxic tank, a No. 2 aerobic tank, a secondary sedimentation tank, an air floatation tank and a clean water tank which are sequentially communicated through pipelines;
the water outlet of the 2# wastewater regulating tank is communicated with the water inlet of the comprehensive regulating tank through a pipeline;
the mixed hydrolysis tank is also communicated with a No. 2 anoxic tank through a pipeline;
the 2# aerobic tank is communicated with the 1# anoxic tank through a return pipeline or the 2# aerobic tank is communicated with the 2# anoxic tank through a return pipeline, and the 1# aerobic tank is communicated with the 1# anoxic tank through a return pipeline;
the secondary sedimentation tank is communicated with the No. 1 anoxic tank and the No. 2 anoxic tank through a sludge return pipeline;
the secondary sedimentation tank is also communicated with the neutralization tank through a return pipeline;
the air floatation tank is communicated with the neutralization tank through a return pipeline.
In some embodiments of the invention, the secondary sedimentation tank is also in communication with the mixing hydrolysis tank via a sludge return line.
In some embodiments of the invention, a strain incubator is arranged in a sludge return pipeline connected with the 1# anoxic tank, the 2# anoxic tank and the mixed hydrolysis tank.
In some specific embodiments of the invention, the water inlet of the pre-acidification tank is high-index low-salt wastewater (COD is more than or equal to 15000 mg/L); the water inlet of the wastewater regulating tank 2 is MVR condensate; the water inlet of the comprehensive regulating tank also comprises low-index wastewater (COD is less than or equal to 1000 mg/L).
In some embodiments of the present invention, the wastewater regulating tank 2 is in communication with an ammonium sulfate MVR system, an ammonium chloride MVR system, and a sodium chloride MVR system, and the MVR condensate is one or more of an ammonium sulfate MVR system, an ammonium chloride MVR system, and a sodium chloride MVR system condensate.
In some embodiments of the invention, secondary sedimentation tank sludge reflux liquid is refluxed to the mixed hydrolysis tank to maintain the mixed hydrolysis tank sludge concentration.
In some embodiments of the invention, the aeration devices of the No. 1 aerobic tank and the No. 2 aerobic tank are lifting aerators.
The invention also provides a high-efficiency treatment process for the dye intermediate wastewater, which comprises the following steps: the high-index low-salt wastewater (COD is more than or equal to 15000 mg/L) enters a pre-acidification tank, a stirring device completely mixes inlet water with sludge, acidizing and hydrolyzing refractory organic matters, and then outlet water enters a Fenton reactor through a pipeline; adding a medicament into the Fenton reactor, further degrading refractory organic matters by using high-index low-salt wastewater, and then enabling effluent to enter a neutralization tank through a pipeline; meanwhile, the neutralization tank also receives residual sludge from the secondary sedimentation tank and the air floatation device in a backflow way, quicklime is added into the neutralization tank to adjust the pH value to 8.5-9, and then the discharged water is subjected to filter pressing through a filter press, and filter pressing liquid enters the wastewater adjusting tank 1; MVR condensate enters a wastewater regulating tank 2, wastewater in the wastewater regulating tank 2 and wastewater in the wastewater regulating tank 1 enter a comprehensive regulating tank according to a proportion, so that COD (chemical oxygen demand) of the comprehensive regulating tank is less than or equal to 2500mg/L, low-index wastewater (COD is less than or equal to 1000 mg/L) directly enters the comprehensive regulating tank at the same time, and the low-index wastewater and inflow water from the wastewater regulating tanks 1 and 2 are completely mixed in the comprehensive regulating tank; the effluent of the comprehensive regulating tank enters a mixed hydrolysis tank through a pipeline, the pH of the wastewater in the mixed hydrolysis tank is controlled to be between 6.8 and 8, DO is controlled to be within 0.5mg/L, the sludge concentration is maintained through the self-propagation of microorganisms, the sludge can be supplemented through the backflow of sludge in a secondary sedimentation tank when necessary, and the mixed hydrolysis tank further converts refractory organic matters in the wastewater into easily degradable organic matters, so that the biodegradability is improved; mixing the water discharged from the hydrolysis tank according to the proportion of 5:1-3:1 respectively enter a 1# anoxic tank and a 2# anoxic tank, the 1# anoxic tank is stirred, and a denitrification reaction is carried out by using a raw water carbon source, a reflux nitrified liquid of an aerobic tank and nitrite nitrogen and nitrate nitrogen in a sludge reflux liquid from a secondary sedimentation tank, and then the raw water carbon source, the reflux nitrified liquid and the nitrate nitrogen enter the 1# aerobic tank; the wastewater is aerated and stirred in a No. 1 aerobic tank 1 Hour, control DO is 2-4mg/L, and a combined biological filler is arranged in the pool, so that organic matters are converted into inorganic matters through nitration reaction; the effluent of the No. 1 aerobic tank enters a No. 2 anoxic tank, is mixed and stirred with the inlet water from the mixed hydrolysis tank, and is subjected to denitrification reaction by utilizing a raw water carbon source, nitrite nitrogen and nitrate nitrogen in the effluent of the No. 1 aerobic tank and the sludge reflux liquid from the secondary sedimentation tank, and then enters the No. 2 aerobic tank; the wastewater is aerated and stirred in a No. 2 aerobic tank 2 The DO is controlled to be 2-4mg/L in an hour, and a combined biological filler is arranged in the pool, so that organic matters are converted into inorganic matters through nitration reaction; refluxing the nitrifying liquid of the No. 2 aerobic tank to the No. 1 anoxic tank or the No. 1 anoxic tank; returning the nitrifying liquid of the aerobic tank 1 to the anoxic tank 1 and returning the nitrifying liquid of the aerobic tank 2 to the anoxic tank 2; the effluent of the No. 2 aerobic tank enters a secondary sedimentation tank to realize mud-water separation; the secondary sedimentation tank sludge flows back to the 1# anoxic tank, the 2# anoxic tank and the neutralization tank through a sludge backflow pipeline, wherein a strain incubator is arranged in the sludge backflow pipeline of the 1# anoxic tank and the 2# anoxic tank, and carbon sources are periodically added into the strain incubator to optimize strain quality; enabling the effluent of the secondary sedimentation tank to enter an air floatation tank, and adding a medicament to further remove pollutants so as to enable the effluent to reach the standard; and the water discharged from the air floatation tank enters a clean water tank.
In some embodiments of the present invention, the 35.ltoreq.t 1 ≤40；15≤t 2 ≤20。
In some embodiments of the invention, the secondary sedimentation tank sludge reflux liquid is refluxed to the mixed hydrolysis tank to maintain the mixed hydrolysis tank sludge concentration.
The invention relates to a dye intermediate wastewater high-efficiency treatment system and a working process and principle thereof, wherein the working process and principle comprise the following steps:
(1) The high-index low-salt wastewater enters a pre-acidification tank
The purpose of the pre-acidification tank is mainly to optimize the carbon source in the high-index low-salt wastewater, and the refractory substances in the raw water are pre-acidified to convert macromolecular organic matters into micromolecular organic matters, so that the degradation of microorganisms is facilitated, and the carbon source is provided for the subsequent denitrification.
(2) The effluent of the pre-acidification tank enters a Fenton reactor
And adding a medicament into the Fenton reactor to further degrade refractory organic matters in the high-index low-salt-content wastewater. Compared with the traditional Fenton process, the Fenton reactor is provided with the pre-acidification tank, and the dosage of the Fenton reactor can be reduced through the treatment of the pre-acidification tank, so that the operation cost is saved.
(3) The effluent of the Fenton reactor enters a neutralization tank
The neutralization pond not only has the inflow water from Fenton reactor effluent, but also receives the residual sludge from the secondary sedimentation pond and the air floatation device for backflow, and quick lime is added into the neutralization pond to adjust the pH value, and sulfate ions in the wastewater are used for generating calcium sulfate precipitation when the pH value is adjusted. In addition, the pH value of the returned sludge from the secondary sedimentation tank and the air floatation tank is 7-8.5, and the returned sludge flows back to the neutralization tank to partially neutralize the pH value of the high-index low-salt wastewater, so that the dosage and the sludge yield of quicklime are reduced.
(4) The effluent of the Fenton reactor enters a filter press
After the filter press is used for press filtration, the mud cake can be transported outwards, and press filtration liquid enters the wastewater regulating tank 1.
(5) The filtrate enters a wastewater regulating tank 1, and MVR condensate enters a wastewater regulating tank 2
The filter-pressing liquid of the filter press enters a waste water regulating tank 1; after the wastewater of ammonium sulfate, ammonium chloride and sodium chloride is treated by an ammonium sulfate MVR system, an ammonium chloride MVR system and a sodium chloride MVR system respectively, the crystal salt can be used for other purposes, can be sold, and the mixed salt is used for dangerous waste treatment, and condensed water enters a wastewater regulating tank 2.
(6) Waste water enters into the comprehensive regulating tank
The low index waste water directly enters the regulating tank, the waste water in the waste water regulating tank 1 and the waste water in the waste water regulating tank 2 enter the comprehensive regulating tank according to a certain proportion, and the inflow water is completely mixed by stirring, so that the condition that the fluctuation of the water quality of the comprehensive regulating tank is large and the subsequent multistage reinforced AO system is prevented from being impacted.
(7) The effluent of the comprehensive regulating tank enters a mixed hydrolysis tank
After the effluent of the comprehensive regulating tank enters the mixed hydrolysis tank, the pH of the wastewater in the mixed hydrolysis tank is controlled to be in a range of 6.8-8, DO is controlled to be in a range of 0.5mg/L, the sludge concentration is maintained through microorganism self-propagation, the sludge can be supplemented through secondary sedimentation tank sludge reflux when necessary, and the mixed hydrolysis tank further converts refractory organic matters in the wastewater into easily degradable organic matters, so that the biodegradability is improved.
(8) Mixed hydrolysis tank effluent enters a multistage reinforced AO system
The effluent of the mixed hydrolysis tank enters a 1# anoxic tank and a 2# anoxic tank in proportion, a stirring device is arranged in the 1# anoxic tank, and the carbon source of raw water, nitrites nitrogen in nitrites liquid reflux liquid and nitrites nitrogen in sludge reflux liquid of the secondary sedimentation tank are utilized for denitrification reaction; then the wastewater enters a No. 1 aerobic tank, aeration stirring is carried out on the wastewater in the No. 1 aerobic tank, and organic matters are converted into inorganic matters through nitration reaction; the effluent of the No. 1 aerobic tank and the split raw water of the mixed hydrolysis tank are mixed and enter a No. 2 anoxic tank, a stirring device is arranged in the No. 2 anoxic tank, a carbon source of raw water, nitrite nitrogen in the effluent of the No. 1 aerobic tank and nitrate nitrogen in sludge reflux liquid of the secondary sedimentation tank are utilized to carry out denitrification reaction, then the mixture enters the No. 2 aerobic tank, the wastewater is subjected to aeration stirring in the No. 2 aerobic tank, and organic matters are converted into inorganic matters through nitrification reaction.
Under normal conditions, the nitrifying liquid flows back from the 2# aerobic tank to the 1# anoxic tank, and the denitrification effect is enhanced by adopting cross backflow and through the front denitrification and the rear denitrification. When water inflow COD: ammonia nitrogen > 20:1, a nitrifying liquid single-stage reflux mode can be adopted, namely nitrifying liquid in a No. 2 aerobic tank is refluxed to a No. 2 anoxic tank, nitrifying liquid in a No. 1 aerobic tank is refluxed to a No. 1 anoxic tank, so that matching and effective degradation of carbon and nitrogen are ensured.
The multistage enhanced AO system of the invention is characterized in that:
(1) the effluent of the mixed hydrolysis tank is distributed to a No. 1 anoxic tank and a No. 2 anoxic tank according to different proportions to form a multistage reinforced AO system;
(2) the multi-stage reinforced AO system is adopted to replace the traditional AO system, the carbon source is reasonably distributed, the carbon source adding amount of the system is reduced, carbon and nitrogen are simultaneously subjected to balanced degradation, and the carbon source is fully degraded and removed on the premise of not wasting the carbon source;
(3) the lifting aerator is adopted in the 1# aerobic tank and the 2# aerobic tank, and the aeration quantity is controlled by controlling the valve on each branch pipe, so that compared with the traditional microporous aerator, the precise aeration is realized, and the aeration energy consumption is saved;
(4) compared with the traditional microporous aerator, the lifting aerator can be replaced when the system is operated, and the maintenance and overhaul of the later-stage system are facilitated.
(9) The effluent of the No. 2 aerobic tank enters a secondary sedimentation tank
And the effluent of the No. 2 aerobic tank enters a secondary sedimentation tank to realize mud-water separation, and sludge in the secondary sedimentation tank flows back to the No. 1 anoxic tank, the No. 2 anoxic tank and the neutralization tank through a sludge backflow pipeline, wherein a strain incubator is arranged in the sludge backflow pipeline of the No. 1 anoxic tank and the No. 2 anoxic tank, and carbon sources are periodically added into the strain incubator to optimize strain quality.
(10) The effluent of the secondary sedimentation tank enters an air floatation tank
The effluent of the secondary sedimentation tank enters an air floatation tank, and the reagent is added to further remove pollutants so as to enable the effluent to reach the standard, and the effluent of the air floatation tank enters a clean water tank.
Air floatation replaces the traditional coagulating sedimentation process, thereby saving the occupied area and the dosage of medicaments.
The beneficial effects of the invention are as follows: the high-efficiency treatment system and the process for the dye intermediate wastewater are designed according to the characteristics of the dye intermediate wastewater, and the main pollutants of the dye intermediate wastewater can be removed in a high-efficiency and deep manner through the designs of a high-index low-salt wastewater pretreatment system, a mixed hydrolysis pretreatment system, a multi-stage reinforced AO system and the like; furthermore, the synergistic effect among the sewage treatment units can reduce the overall operation cost while improving the sewage treatment effect, and is beneficial to the commercial operation of the technical scheme of the invention.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a dye intermediate wastewater efficient treatment system provided by the invention;
fig. 2 is a schematic diagram of a dye intermediate wastewater efficient treatment system provided by the invention.
Detailed Description
The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it should be apparent that the described embodiments are only some of the embodiments of the present invention and should not be used to limit the protection scope of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, are intended to fall within the scope of the present invention.
Example 1: efficient treatment system for dye intermediate wastewater
A No. 1 pre-acidification tank, a Fenton reactor, a neutralization tank, a filter press, a No. 1 wastewater regulating tank, a comprehensive regulating tank, a mixed hydrolysis tank, a No. 1 anoxic tank, a No. 1 aerobic tank, a No. 2 anoxic tank, a No. 2 aerobic tank, a secondary sedimentation tank, an air floatation tank and a clean water tank which are sequentially communicated through pipelines; the water outlet of the 2# wastewater regulating tank is communicated with the water inlet of the comprehensive regulating tank through a pipeline; the mixed hydrolysis tank is also communicated with a No. 2 anoxic tank through a pipeline; the No. 2 aerobic tank is communicated with the No. 1 anoxic tank through a return pipeline; the secondary sedimentation tank is communicated with the 1# anoxic tank and the 2# anoxic tank through a sludge return pipeline, and a strain incubator is arranged on the sludge return pipeline of the secondary sedimentation tank; the secondary sedimentation tank is also communicated with the neutralization tank through a return pipeline; the air floatation tank is communicated with the neutralization tank through a return pipeline; the water inlet of the pre-acidification tank is high-index low-salt wastewater; the wastewater regulating tank 2 is communicated with an ammonium sulfate MVR system, an ammonium chloride MVR system and a sodium chloride MVR system, condensate water of the ammonium sulfate MVR system, the ammonium chloride MVR system and the sodium chloride MVR system enters the wastewater regulating tank 2 through pipelines, and water entering the wastewater regulating tank 2 is MVR condensate; the water inlet of the comprehensive regulating tank also comprises low-index wastewater; the aeration devices of the No. 1 aerobic tank and the No. 2 aerobic tank are lifting aerators.
Example 2: efficient treatment system for dye intermediate wastewater
A No. 1 pre-acidification tank, a Fenton reactor, a neutralization tank, a filter press, a No. 1 wastewater regulating tank, a comprehensive regulating tank, a mixed hydrolysis tank, a No. 1 anoxic tank, a No. 1 aerobic tank, a No. 2 anoxic tank, a No. 2 aerobic tank, a secondary sedimentation tank, an air floatation tank and a clean water tank which are sequentially communicated through pipelines; the water outlet of the 2# wastewater regulating tank is communicated with the water inlet of the comprehensive regulating tank through a pipeline; the mixed hydrolysis tank is also communicated with a No. 2 anoxic tank through a pipeline; the 2# aerobic tank is communicated with the 2# anoxic tank through a return pipeline, and the 1# aerobic tank is communicated with the 1# anoxic tank through a return pipeline; the secondary sedimentation tank is communicated with the 1# anoxic tank and the 2# anoxic tank through a sludge return pipeline, and a strain incubator is arranged on the sludge return pipeline of the secondary sedimentation tank; the secondary sedimentation tank is also communicated with the neutralization tank through a return pipeline; the air floatation tank is communicated with the neutralization tank through a return pipeline; the water inlet of the pre-acidification tank is high-index low-salt wastewater; the wastewater regulating tank 2 is communicated with an ammonium sulfate MVR system, an ammonium chloride MVR system and a sodium chloride MVR system, condensate water of the ammonium sulfate MVR system, the ammonium chloride MVR system and the sodium chloride MVR system enters the wastewater regulating tank 2 through pipelines, and water entering the wastewater regulating tank 2 is MVR condensate; the water inlet of the comprehensive regulating tank also comprises low-index wastewater; the aeration devices of the No. 1 aerobic tank and the No. 2 aerobic tank are lifting aerators.
Example 3: sewage treatment process of dye intermediate wastewater high-efficiency treatment system based on embodiment 1
The high-index low-salt wastewater enters a pre-acidification tank, a stirring device completely mixes inlet water with sludge, acidizes and hydrolyzes refractory organic matters, and then outlet water enters a Fenton reactor through a pipeline; fenton reactor molar concentration Fe 2+ ：H 2 O 2 =1: 3, adding ferrous iron and hydrogen peroxide to further degrade refractory organic matters in the high-index low-salt wastewater, removing 60% of COD in the wastewater after Fenton treatment, and then enabling the effluent to enter a neutralization tank through a pipeline; meanwhile, the neutralization tank also receives residual sludge from the secondary sedimentation tank and the air floatation device in a backflow way, quicklime is added into the neutralization tank to adjust the pH value to 8.5-9, and then the discharged water is subjected to filter pressing through a filter press, and filter pressing liquid enters the wastewater adjusting tank 1; MVR condensate enters a wastewater regulating tank 2, wastewater in the wastewater regulating tank 2 and wastewater in the wastewater regulating tank 1 enter a comprehensive regulating tank according to a proportion,the COD of the comprehensive regulating tank is less than or equal to 2500mg/L, the low-index wastewater directly enters the comprehensive regulating tank at the same time, and the low-index wastewater and the inflow water from the wastewater regulating tanks 1 and 2 are completely mixed in the comprehensive regulating tank; the effluent of the comprehensive regulating tank enters a mixed hydrolysis tank through a pipeline, the pH of the wastewater in the mixed hydrolysis tank is controlled to be between 6.8 and 8, DO is controlled to be within 0.5mg/L, the sludge concentration is maintained through the self-propagation of microorganisms, the sludge can be supplemented through the backflow of sludge in a secondary sedimentation tank when necessary, and the mixed hydrolysis tank further converts refractory organic matters in the wastewater into easily degradable organic matters, so that the biodegradability is improved; mixing the water discharged from the hydrolysis tank according to the weight ratio of 5:1-3: the ratio of 1 is respectively fed into a No. 1 anoxic tank and a No. 2 anoxic tank, the No. 1 anoxic tank is stirred, raw water carbon source is utilized to carry out denitrification reaction with nitrite nitrogen and nitrate nitrogen in reflux nitrified liquid from a No. 2 aerobic tank and sludge reflux liquid from a secondary sedimentation tank, and then the raw water carbon source is fed into the No. 1 aerobic tank; the wastewater is aerated and stirred for 35 hours in an aerobic tank of a No. 1 aerobic tank, DO is controlled to be 2-4mg/L, a combined biological filler is arranged in the tank, and organic matters are converted into inorganic matters through nitration reaction; the effluent of the No. 1 aerobic tank enters a No. 2 anoxic tank, is mixed and stirred with the inlet water from the mixed hydrolysis tank, and is subjected to denitrification reaction by utilizing a raw water carbon source, nitrite nitrogen and nitrate nitrogen in the effluent of the No. 1 aerobic tank and the sludge reflux liquid from the secondary sedimentation tank, and then enters the No. 2 aerobic tank; the wastewater is aerated and stirred for 15 hours in an aerobic tank of a No. 2 aerobic tank, DO is controlled to be 2-4mg/L, and a combined biological filler is arranged in the tank, so that organic matters are converted into inorganic matters through nitration reaction; returning the nitrifying liquid of the No. 2 aerobic tank to the No. 1 anoxic tank; the effluent of the No. 2 aerobic tank enters a secondary sedimentation tank to realize mud-water separation; the secondary sedimentation tank sludge flows back to the 1# anoxic tank, the 2# anoxic tank and the neutralization tank through a sludge backflow pipeline, wherein a strain incubator is arranged in the sludge backflow pipeline of the 1# anoxic tank and the 2# anoxic tank, and the strain incubator is periodically fed with an efficient composite carbon source to optimize strain quality; enabling the effluent of the secondary sedimentation tank to enter an air floatation tank, and adding a medicament to further remove pollutants so as to enable the effluent to reach the standard; and the water discharged from the air floatation tank enters a clean water tank.
Example 4: sewage treatment process of dye intermediate wastewater high-efficiency treatment system based on embodiment 2
The high-index low-salt wastewater enters a pre-acidification tank, a stirring device completely mixes inlet water with sludge, acidizes and hydrolyzes refractory organic matters, and then outlet water enters a Fenton reactor through a pipeline; adding a medicament into the Fenton reactor, further degrading refractory organic matters by using high-index low-salt wastewater, and then enabling effluent to enter a neutralization tank through a pipeline; meanwhile, the neutralization tank also receives residual sludge from the secondary sedimentation tank and the air floatation device in a backflow way, quicklime is added into the neutralization tank to adjust the pH value to 8.5-9, and then the discharged water is subjected to filter pressing through a filter press, and filter pressing liquid enters the wastewater adjusting tank 1; MVR condensate enters a wastewater regulating tank 2, wastewater in the wastewater regulating tank 2 and wastewater in the wastewater regulating tank 1 enter a comprehensive regulating tank according to a proportion, so that COD (chemical oxygen demand) in the comprehensive regulating tank is less than or equal to 2500mg/L, low-index wastewater directly enters the comprehensive regulating tank at the same time, and the low-index wastewater and inflow water from the wastewater regulating tanks 1 and 2 are completely mixed in the comprehensive regulating tank; the effluent of the comprehensive regulating tank enters a mixed hydrolysis tank through a pipeline, the pH of the wastewater in the mixed hydrolysis tank is controlled to be between 6.8 and 8, DO is controlled to be within 0.5mg/L, the sludge concentration is maintained through the self-propagation of microorganisms, the sludge can be supplemented through the backflow of sludge in a secondary sedimentation tank when necessary, and the mixed hydrolysis tank further converts refractory organic matters in the wastewater into easily degradable organic matters, so that the biodegradability is improved; the effluent of the mixed hydrolysis tank is respectively fed into a No. 1 anoxic tank and a No. 2 anoxic tank according to a proportion, the No. 1 anoxic tank is stirred, raw water carbon sources are utilized to carry out denitrification reaction with nitrite nitrogen and nitrate nitrogen in reflux liquid of sludge from a No. 1 aerobic tank and from a secondary sedimentation tank, and then the raw water carbon sources are fed into the No. 1 aerobic tank; the wastewater is aerated and stirred for 35 hours in an aerobic tank of a No. 1 aerobic tank, DO is controlled to be 2-4mg/L, a combined biological filler is arranged in the tank, and organic matters are converted into inorganic matters through nitration reaction; the nitrifying liquid of the No. 1 aerobic tank flows back to the No. 1 anoxic tank, the effluent of the No. 1 aerobic tank enters the No. 2 anoxic tank, and is mixed and stirred with the inflow water from the mixed hydrolysis tank, and the carbon source of the raw water is utilized to carry out denitrification reaction with nitrite nitrogen and nitrate nitrogen in the effluent of the No. 1 aerobic tank, the nitrifying liquid of the No. 2 aerobic tank and the sludge nitrifying liquid from the secondary sedimentation tank, and then enters the No. 2 aerobic tank; the wastewater is aerated and stirred for 15 hours in an aerobic tank of a No. 2 aerobic tank, DO is controlled to be 2-4mg/L, and a combined biological filler is arranged in the tank, so that organic matters are converted into inorganic matters through nitration reaction; returning nitrifying liquid of the No. 2 aerobic tank to the No. 2 anoxic tank, and enabling effluent of the No. 2 aerobic tank to enter a secondary sedimentation tank to realize mud-water separation; the secondary sedimentation tank sludge flows back to the 1# anoxic tank, the 2# anoxic tank and the neutralization tank through a sludge backflow pipeline, wherein a strain incubator is arranged in the sludge backflow pipeline of the 1# anoxic tank and the 2# anoxic tank, and carbon sources are periodically added into the strain incubator to optimize strain quality; enabling the effluent of the secondary sedimentation tank to enter an air floatation tank, and adding a medicament to further remove pollutants so as to enable the effluent to reach the standard; and the water discharged from the air floatation tank enters a clean water tank.
The foregoing embodiments are merely examples of the present invention, and the scope of the present invention includes, but is not limited to, the forms and styles of the foregoing embodiments, and any suitable changes or modifications made by those skilled in the art, which are consistent with the claims of the present invention, shall fall within the scope of the present invention.
Claims (9)
1. A dye intermediate wastewater high-efficiency treatment system is characterized in that: the device comprises a No. 1 pre-acidification tank, a Fenton reactor, a neutralization tank, a filter press, a No. 1 wastewater regulating tank, a comprehensive regulating tank, a mixed hydrolysis tank, a No. 1 anoxic tank, a No. 1 aerobic tank, a No. 2 anoxic tank, a No. 2 aerobic tank, a secondary sedimentation tank, an air floatation tank and a clean water tank which are sequentially communicated through pipelines;
the water outlet of the 2# wastewater regulating tank is communicated with the water inlet of the comprehensive regulating tank through a pipeline;
the mixed hydrolysis tank is also communicated with a No. 2 anoxic tank through a pipeline;
the 2# aerobic tank is communicated with the 1# anoxic tank through a return pipeline or the 2# aerobic tank is communicated with the 2# anoxic tank through a return pipeline, and the 1# aerobic tank is communicated with the 1# anoxic tank through a return pipeline;
the secondary sedimentation tank is communicated with the No. 1 anoxic tank and the No. 2 anoxic tank through a sludge return pipeline;
the secondary sedimentation tank is also communicated with the neutralization tank through a return pipeline;
the air floatation tank is communicated with the neutralization tank through a return pipeline.
2. The dye intermediate wastewater treatment system of claim 1, wherein:
the secondary sedimentation tank is also communicated with the mixed hydrolysis tank through a sludge return pipeline.
3. The dye intermediate wastewater efficient treatment system as claimed in claim 2, wherein:
and a strain incubator is arranged on a sludge reflux pipeline connected with the secondary sedimentation tank, the No. 1 anoxic tank, the No. 2 anoxic tank and the mixed hydrolysis tank.
4. The dye intermediate wastewater treatment system of claim 1, wherein:
the water inlet of the pre-acidification tank is high-index low-salt wastewater; the water inlet of the wastewater regulating tank 2 is MVR condensate; the water inlet of the comprehensive regulating tank also comprises low-index wastewater.
5. The dye intermediate wastewater efficient treatment system as claimed in claim 4, wherein:
the wastewater regulating tank 2 is communicated with an ammonium sulfate MVR system, an ammonium chloride MVR system and a sodium chloride MVR system, and the MVR condensate is one or more of the ammonium sulfate MVR system, the ammonium chloride MVR system and the sodium chloride MVR system condensate.
6. A dye intermediate wastewater treatment system as claimed in any one of claims 1 to 5, wherein:
the aeration devices of the No. 1 aerobic tank and the No. 2 aerobic tank are lifting aerators.
7. A high-efficiency treatment process for dye intermediate wastewater is characterized by comprising the following steps of:
the high-index low-salt wastewater enters a pre-acidification tank, a stirring device completely mixes inlet water with sludge, acidizes and hydrolyzes refractory organic matters, and then outlet water enters a Fenton reactor through a pipeline; the Fenton reactor is added with a medicament to further degrade refractory organic matters in the high-index low-salt wastewater, and then the effluent enters a neutralization tank through a pipelineThe method comprises the steps of carrying out a first treatment on the surface of the Meanwhile, the neutralization tank also receives residual sludge from the secondary sedimentation tank and the air floatation device in a backflow way, quicklime is added into the neutralization tank to adjust the pH value to 8.5-9, and then the discharged water is subjected to filter pressing through a filter press, and filter pressing liquid enters the wastewater adjusting tank 1; MVR condensate enters a wastewater regulating tank 2, wastewater in the wastewater regulating tank 2 and wastewater in the wastewater regulating tank 1 enter a comprehensive regulating tank according to a proportion, so that COD (chemical oxygen demand) in the comprehensive regulating tank is less than or equal to 2500mg/L, low-index wastewater directly enters the comprehensive regulating tank at the same time, and the low-index wastewater and inflow water from the wastewater regulating tanks 1 and 2 are completely mixed in the comprehensive regulating tank; the effluent of the comprehensive regulating tank enters a mixed hydrolysis tank through a pipeline, the pH of the wastewater in the mixed hydrolysis tank is controlled to be between 6.8 and 8, DO is controlled to be within 0.5mg/L, the sludge concentration is maintained through the self-propagation of microorganisms, the sludge can be supplemented through the backflow of sludge in a secondary sedimentation tank when necessary, and the mixed hydrolysis tank further converts refractory organic matters in the wastewater into easily degradable organic matters, so that the biodegradability is improved; mixing the water discharged from the hydrolysis tank according to the proportion of 5:1-3:1 respectively enter a 1# anoxic tank and a 2# anoxic tank, the 1# anoxic tank is stirred, and a denitrification reaction is carried out by using a raw water carbon source, a reflux nitrified liquid of an aerobic tank and nitrite nitrogen and nitrate nitrogen in a sludge reflux liquid from a secondary sedimentation tank, and then the raw water carbon source, the reflux nitrified liquid and the nitrate nitrogen enter the 1# aerobic tank; the wastewater is aerated and stirred in a No. 1 aerobic tank 1 The DO is controlled to be 2-4mg/L in an hour, and a combined biological filler is arranged in the pool, so that organic matters are converted into inorganic matters through nitration reaction; the effluent of the No. 1 aerobic tank enters a No. 2 anoxic tank, is mixed and stirred with the inlet water from the mixed hydrolysis tank, and is subjected to denitrification reaction by utilizing a raw water carbon source, nitrite nitrogen and nitrate nitrogen in the effluent of the No. 1 aerobic tank and the sludge reflux liquid from the secondary sedimentation tank, and then enters the No. 2 aerobic tank; the wastewater is aerated and stirred in a No. 2 aerobic tank 2 The DO is controlled to be 2-4mg/L in an hour, and a combined biological filler is arranged in the pool, so that organic matters are converted into inorganic matters through nitration reaction; refluxing the nitrifying liquid of the No. 2 aerobic tank to the No. 1 anoxic tank or the No. 1 anoxic tank; returning the nitrifying liquid of the aerobic tank 1 to the anoxic tank 1 and returning the nitrifying liquid of the aerobic tank 2 to the anoxic tank 2; the effluent of the No. 2 aerobic tank enters a secondary sedimentation tank to realize mud-water separation; the secondary sedimentation tank sludge flows back to the 1# anoxic tank, the 2# anoxic tank and the neutralization tank through a sludge return pipeline, wherein the secondary sedimentation tank sludge flows back to the 1# anoxic tank and the 2# anoxic tankA strain incubator is arranged in the sludge return pipeline, and carbon sources are periodically added into the strain incubator to optimize strain quality; enabling the effluent of the secondary sedimentation tank to enter an air floatation tank, and adding a medicament to further remove pollutants so as to enable the effluent to reach the standard; and the water discharged from the air floatation tank enters a clean water tank.
8. The efficient treatment process for dye intermediate wastewater according to claim 7, wherein: the t is more than or equal to 35 1 ≤40；15≤t 2 ≤20。
9. The efficient treatment process for dye intermediate wastewater according to claim 7, wherein: and the secondary sedimentation tank sludge reflux liquid flows back to the mixed hydrolysis tank to maintain the sludge concentration of the mixed hydrolysis tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310813192.7A CN116730544A (en) | 2023-07-04 | 2023-07-04 | Efficient treatment system and process for dye intermediate wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310813192.7A CN116730544A (en) | 2023-07-04 | 2023-07-04 | Efficient treatment system and process for dye intermediate wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116730544A true CN116730544A (en) | 2023-09-12 |
Family
ID=87913282
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310813192.7A Pending CN116730544A (en) | 2023-07-04 | 2023-07-04 | Efficient treatment system and process for dye intermediate wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116730544A (en) |
-
2023
- 2023-07-04 CN CN202310813192.7A patent/CN116730544A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108483655B (en) | Method for deep denitrification by coupling shortcut nitrification and denitrification with anaerobic ammonia oxidation and sulfur autotrophic denitrification | |
| CN110902978B (en) | Method and device for treating high-salt-content high-organic chemical wastewater | |
| CN110436704B (en) | Urban sewage treatment upgrading and reforming process based on anaerobic ammonia oxidation | |
| CN106966498B (en) | Shortcut nitrification and denitrification coupled anaerobic ammonia oxidation denitrification process and control method | |
| CN111573991B (en) | Chemical plating comprehensive wastewater treatment method | |
| WO2012155790A1 (en) | Method for treating total nitrogen in wastewater in coal chemical industry by using microbes | |
| US20100200496A1 (en) | Method and installation for biologically treating waste water | |
| CN109205954A (en) | Light electrolysis catalysis oxidation, biochemical treatment high-concentration waste hydraulic art | |
| CN109368782B (en) | Sewage shortcut nitrification method and system based on side-stream SBR (sequencing batch reactor) enhanced continuous flow process | |
| CN212982734U (en) | Treatment system for coal chemical industry wastewater | |
| CN102336483A (en) | Method and device for treating landfill leachate thick water | |
| CN108101310B (en) | Device and method for treating desulfurization and denitrification wastewater of thermal power plant | |
| CN111196663A (en) | Biological treatment method and device for printing and dyeing wastewater | |
| CN105800873A (en) | Method for treating high-concentration ammonia nitrogen wastewater by autotrophic denitrification process | |
| CN107010794B (en) | Dye wastewater treatment device and method | |
| CN211595368U (en) | Biological treatment device for printing and dyeing wastewater | |
| CN105984991B (en) | A kind of sewerage advanced treatment process | |
| CN206680346U (en) | A kind of waste water advanced removal of carbon and nitrogen processing unit | |
| CN215712067U (en) | Sewage deep denitrification treatment device | |
| CN213357071U (en) | System for realizing short-cut nitrification-anaerobic ammonia oxidation denitrification stable operation of low-ammonia-nitrogen wastewater | |
| CN211595362U (en) | High-salt-content high-organic-matter chemical wastewater treatment device | |
| CN116730544A (en) | Efficient treatment system and process for dye intermediate wastewater | |
| CN114085012A (en) | Organic wastewater treatment system and organic wastewater treatment method | |
| CN211226792U (en) | Waste water denitrification device | |
| CN113443714A (en) | Sewage deep denitrification treatment device and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |