CN113511779A - Organic nitrogen wastewater treatment system and process - Google Patents
Organic nitrogen wastewater treatment system and process Download PDFInfo
- Publication number
- CN113511779A CN113511779A CN202110727236.5A CN202110727236A CN113511779A CN 113511779 A CN113511779 A CN 113511779A CN 202110727236 A CN202110727236 A CN 202110727236A CN 113511779 A CN113511779 A CN 113511779A
- Authority
- CN
- China
- Prior art keywords
- tank
- pipe
- sludge
- section
- water
- 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
- 125000001477 organic nitrogen group Chemical group 0.000 title claims abstract description 67
- 238000000034 method Methods 0.000 title claims abstract description 31
- 230000008569 process Effects 0.000 title claims abstract description 26
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 22
- 239000010802 sludge Substances 0.000 claims abstract description 121
- 239000002351 wastewater Substances 0.000 claims abstract description 79
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 73
- 238000004062 sedimentation Methods 0.000 claims abstract description 44
- 238000002156 mixing Methods 0.000 claims abstract description 42
- 238000001179 sorption measurement Methods 0.000 claims abstract description 40
- 230000007062 hydrolysis Effects 0.000 claims abstract description 27
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 27
- 230000020477 pH reduction Effects 0.000 claims abstract description 26
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 11
- 238000004064 recycling Methods 0.000 claims abstract description 7
- 239000010865 sewage Substances 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 140
- 230000001276 controlling effect Effects 0.000 claims description 45
- 230000014759 maintenance of location Effects 0.000 claims description 35
- 238000005189 flocculation Methods 0.000 claims description 27
- 230000016615 flocculation Effects 0.000 claims description 26
- 238000011001 backwashing Methods 0.000 claims description 24
- 230000001105 regulatory effect Effects 0.000 claims description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 19
- 239000000463 material Substances 0.000 claims description 19
- 239000001301 oxygen Substances 0.000 claims description 19
- 229910052760 oxygen Inorganic materials 0.000 claims description 19
- 238000010992 reflux Methods 0.000 claims description 18
- 239000000945 filler Substances 0.000 claims description 17
- 238000005273 aeration Methods 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- 239000002245 particle Substances 0.000 claims description 11
- 238000009826 distribution Methods 0.000 claims description 10
- 239000003344 environmental pollutant Substances 0.000 claims description 9
- 238000005192 partition Methods 0.000 claims description 9
- 231100000719 pollutant Toxicity 0.000 claims description 9
- 229920002401 polyacrylamide Polymers 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 8
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 8
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 8
- 239000012528 membrane Substances 0.000 claims description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 238000005345 coagulation Methods 0.000 claims description 5
- 230000015271 coagulation Effects 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 5
- 238000005070 sampling Methods 0.000 claims description 5
- 230000008719 thickening Effects 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 238000012856 packing Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 claims description 3
- 229910052740 iodine Inorganic materials 0.000 claims description 3
- 239000011630 iodine Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 238000010926 purge Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims 1
- 230000000630 rising effect Effects 0.000 claims 1
- 231100000419 toxicity Toxicity 0.000 abstract description 10
- 230000001988 toxicity Effects 0.000 abstract description 10
- 230000009467 reduction Effects 0.000 abstract description 7
- 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 abstract description 3
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 3
- 238000011010 flushing procedure Methods 0.000 description 14
- 241000894006 Bacteria Species 0.000 description 9
- 230000007059 acute toxicity Effects 0.000 description 8
- 231100000403 acute toxicity Toxicity 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 238000000855 fermentation Methods 0.000 description 7
- 230000004151 fermentation Effects 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 5
- RCTYPNKXASFOBE-UHFFFAOYSA-M chloromercury Chemical compound [Hg]Cl RCTYPNKXASFOBE-UHFFFAOYSA-M 0.000 description 5
- 239000000575 pesticide Substances 0.000 description 5
- 239000000725 suspension Substances 0.000 description 5
- 239000003403 water pollutant Substances 0.000 description 5
- 239000010842 industrial wastewater Substances 0.000 description 4
- 230000001174 ascending effect Effects 0.000 description 3
- 238000010170 biological method Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000008235 industrial water Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000004753 textile Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 241000252212 Danio rerio Species 0.000 description 1
- 241001494246 Daphnia magna Species 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 241000607568 Photobacterium Species 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 231100000584 environmental toxicity Toxicity 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 230000007102 metabolic function Effects 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F2101/38—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
- 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
- C02F3/30—Aerobic and anaerobic processes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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)
- Water Treatment By Sorption (AREA)
- Activated Sludge Processes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses an organic nitrogen wastewater treatment system and process, belonging to the technical field of sewage treatment. The process comprises the following steps: after pretreatment, the organic nitrogen wastewater enters a micro-aerobic hydrolysis acidification pool to strengthen the ammoniation of organic nitrogen and improve the biodegradability of wastewater; the effluent of the micro-aerobic hydrolysis acidification tank enters a two-stage A/O sludge film mixing tank for biological denitrification; and the effluent of the two-stage A/O sludge film mixing tank sequentially enters a high-efficiency sedimentation tank, a denitrification filter tank and an active carbon adsorption tank to carry out advanced treatment on organic pollutants such as nitrate nitrogen, organic nitrogen and the like. The method has the advantages of high denitrification efficiency, high reduction rate of wastewater toxicity, stable operation and the like, and is suitable for advanced treatment and recycling of organic nitrogen wastewater under high standards.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to an organic nitrogen wastewater treatment system and process.
Background
The organic nitrogen wastewater refers to wastewater and waste liquid generated in the industrial production processes of pharmacy, textile and the like, and contains nitrogen-containing organic pollutants such as intermediate products and by-products generated in the production process, industrial raw materials and products which run off along with water, so that the organic nitrogen component accounts for a high proportion and becomes the main characteristic of the organic nitrogen wastewater. At present, the organic nitrogen wastewater is mainly treated by traditional biological methods such as an anaerobic method and an aerobic method, the method firstly decomposes difficultly-degradable pollutants by using an anaerobic section to improve the biodegradability of the pollutants, then removes most of the pollutants and nutrients by using an aerobic section, and finally realizes the reduction and discharge of part of the pollutants. However, due to the factors of multiple organic nitrogen components, poor bioavailability and the like, the traditional biological method has limited capability of removing organic nitrogen molecules in organic nitrogen wastewater, the COD of effluent is generally 150mg/L-300mg/L, and the total nitrogen is generally 50mg/L-60mg/L, so that the water pollutant discharge requirement of corresponding industries cannot be met, and the industrial water standard for utilizing reclaimed water cannot be met. Therefore, the removal of organic nitrogen becomes one of the important factors for restricting the standard discharge and reuse of the organic nitrogen wastewater.
In addition, due to the existence of a large amount of high-polarity and high-unsaturation-degree soluble organic nitrogen molecules, the organic nitrogen wastewater has high biotoxicity, the reduction capacity of the existing biological treatment process on the soluble organic nitrogen molecules is limited, and the organic nitrogen wastewater discharge still has high ecological risk. Recently, with the improvement of health and living consciousness, the control of wastewater ecotoxicity has become the key point of the current pollutant control policy, and the comprehensive toxicity control of organic nitrogen wastewater is also gradually concerned. For example, in the national standard of discharge Standard of Water pollutants for pharmaceutical industry of fermentation (GB21903-2008), acute toxicity of wastewater is used as a control item for the first time, and acute toxicity (HgCl) of luminescent bacteria is specified2Toxicity equivalent) limit of 0.07 mg/L. In 2019, acute toxicity control items of daphnia magna and luminescent bacteria are added into the emission standard (draft of comments) of water pollutants in textile industry. In 2021, the latest release of electronic industry Water pollutant discharge Standard (GB 3970322020) by the department of ecological Environment stipulates that after 2024, acute toxicity index of zebra fish roe needs to be monitored by all electronic industry sewage centralized treatment facilities. Therefore, under the current high discharge standard and recycling requirement, the development of a novel treatment process of organic nitrogen wastewater is urgently needed, the organic nitrogen treatment and toxicity reduction efficiency of the wastewater treatment process is improved, and the promotion is promotedAnd (3) resource utilization process of organic nitrogen wastewater.
In recent years, many scholars at home and abroad research the development and optimization of organic nitrogen wastewater treatment processes, and a series of novel processes and technologies are developed and applied. The Chinese patent application No. 201811147297.9 discloses a high concentration organic nitrogen wastewater treatment process, which comprises the steps of decomposing macromolecular organic matters into micromolecular organic matters through anaerobic reaction, converting organic nitrogen into ammonia nitrogen, enabling effluent to enter a first sedimentation tank, removing suspended matters, enabling supernatant to enter an anoxic tank, enabling supernatant of nitrification reaction in an aerobic tank to flow back to the anoxic tank, and not only can denitrifying to utilize carbon sources and reduce COD load of subsequent nitrification reaction, but also can utilize nitrate nitrogen generated by the nitrification reaction. However, the process only enhances the biological denitrification effect, but has no obvious synergy on a large amount of organic nitrogen components which are difficult to biodegrade, and cannot realize toxicity reduction and resource utilization of the organic nitrogen wastewater.
Disclosure of Invention
1. Problems to be solved
Aiming at the problems that the existing organic nitrogen wastewater treatment process cannot meet the requirements of toxicity reduction, standard wastewater discharge and reuse and the like, the invention provides an organic nitrogen wastewater treatment system and process, which meet the requirements of high-standard organic nitrogen wastewater discharge and reuse.
2. Technical scheme
The technical scheme of the invention is as follows: an organic nitrogen wastewater treatment system comprises a micro-aerobic hydrolysis acidification tank, a two-stage A/O sludge membrane mixing tank, a high-efficiency sedimentation tank, a denitrification filter tank and an active carbon adsorption tank which are connected in series in sequence,
the bottom of the micro-aerobic hydrolysis acidification tank is provided with an aeration device and a porous water and mud distribution system, the top of the micro-aerobic hydrolysis acidification tank is provided with a water collection tank with a triangular weir and an exhaust pipe, the water collection tank is provided with a first flow guide pipe connected to the two-stage A/O mud film mixing tank,
the two-stage A/O sludge film mixing tank is formed by jointly building an A1 section, an O1 section, an A2 section and an O2 section, each section is divided into two lattices, the lattices and the sections are separated by partition walls, one side of each partition wall is provided with a water outlet hole as a flow guide channel, both sides of the tank walls of the A1 section and the A2 section are provided with stirrers, the upper part of the tank wall of the A1 section is provided with a first water inlet pipe connected with a first flow guide pipe, the bottom of the tank wall is provided with a sludge return pipe, the bottoms of the O1 section and the O2 section are provided with aeration pipelines with microporous aeration disks, a suspension filler is added into the O2 section, the upper part of the tank wall is provided with an inner return pipe connected to the A1 section and a second flow guide pipe connected to a secondary sedimentation tank, and the inner sides of the second flow guide pipes are provided with filter screen covers,
the high-efficiency sedimentation tank consists of a mixing zone, a flocculation zone and a sedimentation zone, wherein the upper part of the mixing zone is provided with a polymeric ferric sulfate dosing pipe and a water inlet connected with a water outlet of a secondary sedimentation tank, the middle part of the mixing zone is provided with a stirrer, the bottom of the mixing zone is provided with a flow guide channel connected with the flocculation zone, the upper part of the flocculation zone is provided with a polyacrylamide dosing pipe, the middle part of the flocculation zone is provided with a flow guide cylinder with the stirrer, the flow guide cylinder is connected with the coagulation zone through a flow guide pipe, the bottom of the flocculation zone is provided with a sludge return pipe, the upper part of the sedimentation zone is provided with an inclined pipe assembly, a triangular weir and a water collecting tank with a flow guide pipe III, the bottom of the sedimentation zone is provided with a sludge scraper and a sludge concentration tank, and the concentration tank is internally provided with a sludge return pipe and a sludge discharge pipe connected with the flocculation zone,
a back-flushing drainage tank with a triangular weir and a water outlet tank with a triangular weir are arranged in parallel at the top of the denitrification filter tank, a back-flushing drainage pipe is arranged at the bottom of the back-flushing drainage tank, a diversion pipe four connected with the activated carbon adsorption tank is arranged at the bottom of the water outlet tank, a filter material layer, a supporting layer and a filter plate with a long-handle filter head are sequentially arranged at the middle part from top to bottom, a water inlet channel is arranged at the bottom, a back-flushing air inlet pipe, a water inlet pipe II, a back-flushing water inlet pipe and an emptying pipe are arranged at two sides of the water inlet channel,
the top of the activated carbon adsorption tank is provided with a manhole and a third water inlet pipe connected with the flow guide pipe, the third water inlet pipe is connected with a porous water distributor, the middle part of the activated carbon adsorption tank is provided with an adsorption layer and a filter plate with a short-handle filter head, the side surface of the tank body is provided with a sampling hole and a carbon discharge pipe, and the bottom of the tank body is provided with a water discharge pipe.
Furthermore, the volume of the section A1 is 43% -90% of that of the section O1, the volume of the section A2 is 30% -56% of that of the section O2, and the sections A2 and O2 account for 49% -64% of the total volume.
Description of the drawings: the method is designed according to the characteristics of high organic nitrogen concentration, poor biodegradability and the like of the organic nitrogen industrial wastewater. The retention time of the wastewater in different stages is reasonably distributed according to the volume ratio, so that the treatment effect of each stage of two-stage AO and the synergistic removal effect on organic nitrogen molecules are ensured.
Furthermore, the suspension filler is a three-layer hollow cylinder with a corrugated shape, the concentric circles are supported by blades at intervals to ensure that the cross section of the filler is in a trapezoidal oblique wave shape, and the specific surface area is 500m2/m3-1000 m2/m3The diameter of the outer ring cylinder is 20mm-30mm, and the filling rate is 30% -50%.
Description of the drawings: the specific surface area and the content of the suspended filler are set to ensure the sufficient contact of the activated sludge and the biological membrane and the enrichment effect of the nitrifying bacteria group so as to realize the O2The section synchronous nitrification-denitrification biological denitrification process is smoothly developed.
Furthermore, the diameter of the inclined tube component is 50mm-100mm, the inclination angle of the inclined tube is 60 degrees, and the inclined length of the inclined tube is 600-1500mm, so that the full precipitation of the flocculating agent can be ensured.
Furthermore, the filter material layer is a ceramsite filter material with the particle size of 3mm-5mm and the specific surface area of 4 multiplied by 104cm2/g-6×104cm2The porosity is more than or equal to 40 percent, the packing height is 2.5m to 4m, the supporting layer 48 is gravel, and the density is 2.5g/cm3-2.7g/cm3The thickness is less than or equal to 300 mm.
Description of the drawings: the stipulation of the filter material mainly ensures that the surface of the ceramsite has sufficient microorganism attachment sites and ensures the enrichment effect of denitrifying bacteria. The supporting layer mainly plays the roles of water and gas distribution and filter material loss prevention.
Furthermore, the particle size of the active carbon used in the adsorption layer is 0.8mm-2mm, and the specific surface area is 1000m2/g-1500m2The iodine value is 800-.
Description of the drawings: the design mainly aims at the proportion of activated carbon micropores and the capability of removing small molecular organic matters. Since small molecular organic nitrogen in organic nitrogen industrial wastewater is difficult to remove in the front-end process, activated carbon adsorption is mainly used for treating the substances. The specific surface area and iodine value of the activated carbon are specified, namely the micropore occupation ratio of the activated carbon and the removal capacity of the activated carbon to micromolecular organic matters are determined, and the removal capacity of the activated carbon to micromolecular organic nitrogen is ensured. Therefore, the design mainly aims at the proportion of activated carbon micropores and the capability of removing small molecular organic matters.
The invention also discloses a process for treating organic nitrogen wastewater by applying the system, which comprises the following steps:
step S1: carrying out primary pretreatment on the organic nitrogen wastewater, wherein the water quality of the pretreated organic nitrogen wastewater is characterized by COD (chemical oxygen demand) being 300-3000 mg/L, total nitrogen being 100-500 mg/L and organic nitrogen concentration being 50-300 mg/L; then the sewage enters a micro-aerobic hydrolysis acidification tank through a porous water distribution and sludge discharge system, the pH value in the micro-aerobic hydrolysis acidification tank is controlled to be 5.0-9.0, the sludge concentration is 4.0-8.0 g/L, when the non-soluble COD is more than 60%, the hydraulic retention time is 2-6 h, when the non-soluble COD is less than 60%, the hydraulic retention time is 4-12 h, the dissolved oxygen concentration is 0.2-0.4 mg/L, and the wastewater ascending flow rate is 0.5-2 m/h; the wastewater flows through a sludge bed (13) to contact with activated sludge to degrade pollutants and retain suspended particles by pushing of water power and air bubbles, and the treated wastewater enters a water collection tank through a triangular weir to be collected and then flows out through a first flow guide pipe; and entrapping suspended particles, and allowing the treated wastewater to enter a water collection tank through a triangular weir and to flow out through a first flow guide pipe;
step S2: waste water flowing out of the draft tube enters an A1 section of the two-stage A/O sludge film mixing pool through a water inlet pipe, the sludge concentration in the two-stage A/O sludge film mixing pool is regulated to be 3.5g/L-4.5g/L, the sludge retention time is regulated to be 15d-20d, the hydraulic retention time of the A1 section and the A2 section is regulated to be 6h-9h, and the dissolved oxygen concentration is 0.2mg/L-0.5 mg/L; regulating the hydraulic retention time of the O1 section to be 10-14 h and the concentration of dissolved oxygen to be 2.5-4.0 mg/L; regulating and controlling the hydraulic retention time of the O2 section to be 16-20 h and the dissolved oxygen concentration to be 3.0-6.0 mg/L, and simultaneously refluxing the O2 section sludge-water mixed liquid to the A1 section through an internal reflux pipe, wherein the internal reflux ratio is 200-400%; the treated wastewater enters a secondary sedimentation tank from a second diversion pipe at the upper part of the O2 section for mud-water separation, a part of sludge after sedimentation flows back to the A1 section through a sludge return pipe, the sludge return ratio is 60-100%, and the other part of the sludge is discharged through a sludge discharge pipe;
step S3: the effluent of the secondary sedimentation tank enters a high-efficiency sedimentation tank through a water inlet, the hydraulic retention time of a mixing zone is controlled to be 2.0-3.5 min, the speed gradient of a stirrer is 300-500L/s, and the concentration of polymeric ferric sulfate is 50-120 mg/L; controlling the hydraulic retention time of the flocculation area to be 7min-10min, controlling the flow velocity in the guide cylinder barrel to be 0.4m/s-1.2m/s, and controlling the barrelThe external flow rate is 0.1m/s-0.3m/s, the speed gradient of the stirrer is 75L/s-250L/s, and the concentration of polyacrylamide is 0.6mg/L-2.0 mg/L; controlling the sludge concentration time of the settling zone to be 5-10 h and the surface load of the inclined tube component to be 12m3/(m2·h)-25m3/(m2H), simultaneously returning the sludge in the concentration tank to a flocculation area through a sludge return pipe, wherein the return ratio is 2-10%, and the wastewater enters a water collecting tank after being subjected to shallow sedimentation by an inclined pipe assembly and finally flows out through a flow guide pipe III;
step S4: the effluent of the diversion pipe III enters the water inlet channel of the denitrification filter through the water inlet pipe II, and the volume load of the denitrification filter is controlled to be 0.5 kg/(m)3·d)-3.0kg/(m3D), the hydraulic retention time is 15min to 20min, the filtering speed is 10m/h to 15m/h, the wastewater enters a backwashing drainage tank after being biodegraded and filtered by a filter material layer, a part of effluent enters an inlet channel through a backwashing drainage pipe for backwashing, the backwashing period is controlled to be 24h to 48h, and the water washing intensity is 15m3/(m2·h)-25m3/(m2H) air purge strength of 90m3/(m2·h)-150m3/(m2H), the backwashing lasts for 10min to 20min, and the other part of effluent enters the effluent trough and is discharged through the flow guide pipe IV;
step S5: and leading the effluent of the flow guide pipe IV into an active carbon adsorption tank through a water inlet pipe III, controlling the filtration speed in the active carbon adsorption tank to be 5-10 m/h and the operating pressure to be 0.1-0.3 MPa, and finally discharging or recycling the wastewater through a drain pipe after the wastewater is adsorbed and filtered by an adsorption layer.
3. Advantageous effects
Compared with the prior art, the invention has the beneficial effects that:
(1) the organic nitrogen wastewater treatment system and the process provided by the invention can efficiently remove organic nitrogen molecules in the organic nitrogen wastewater, reduce the toxicity of the wastewater, and solve the problems that the conventional treatment process lacks toxicity reduction capability, and the wastewater cannot be discharged and recycled up to the standard.
(2) The invention adopts a micro-aerobic hydrolysis acidification tank, and an aeration device is added in the traditional hydrolysis acidification tank, so that the hydrolysis acidification environment is in a micro-aerobic state (the dissolved oxygen concentration is 0.2mg/L-0.4 mg/L). The early experimental research proves that the micro-aerobic condition can strengthen the metabolic function of bacteria in the hydrolysis acidification tank, promote the production of extracellular enzyme, further enhance the ammoniation capability of the bacteria on organic nitrogen molecules in organic nitrogen wastewater and improve the biodegradability of the organic nitrogen wastewater. In addition, the introduction of oxygen can also improve water conservancy conditions, so that the organic nitrogen wastewater is fully mixed with the activated sludge in the sludge bed, and the hydrolysis and adsorption effects of the sludge on organic nitrogen molecules are enhanced.
(3) The invention adopts the two-stage A/O sludge film mixing tank, the treatment efficiency is high, the denitrification performance is good, the operation is stable, and the anti-load capacity is strong; in addition, the sludge film mixing process is formed by adding the suspended filler into the section O2, so that the biomass and the microorganism species in the reaction tank are obviously improved, the nitrifying bacteria are enriched on the surface of the filler, and the biodegradation and denitrification functions are further enhanced.
(4) The invention sets a series of combined treatment processes such as a high-efficiency sedimentation tank, a denitrification filter tank, an activated carbon adsorption tank and the like in the advanced treatment section, carries out advanced treatment on organic pollutants such as nitrate nitrogen, organic nitrogen and the like, and realizes the aims of reducing the toxicity of organic nitrogen wastewater, and reaching the discharge standard and recycling.
Drawings
FIG. 1 is a block diagram of a process flow of the present invention;
FIG. 2 is a schematic cross-sectional view of the micro-aerobic hydrolysis acidification pool of the present invention;
FIG. 3 is a schematic plan view of a two-stage A/O sludge film mixing tank according to the present invention;
FIG. 4 is a schematic sectional view of the high efficiency settling tank of the present invention;
FIG. 5 is a schematic structural view of the cross section of the denitrification filter tank of the invention;
fig. 6 is a schematic sectional structure of an activated carbon adsorption tank of the present invention.
Wherein, 1-micro-aerobic hydrolysis acidification tank, 11-aeration device, 12-porous water distribution sludge discharge system, 13-sludge bed, 14-triangular weir, 15-water collection tank, 16-exhaust pipe, 17-draft tube I, 2-two-stage A/O sludge membrane mixing tank, 21-A1 section, 22-O1 section, 23-A2 section, 24-O2 section, 25-partition wall, 26-water outlet, 27-stirrer, 28-water inlet tube I, 29-sludge reflux pipe, 210-microporous aeration disc, 211-aeration pipeline, 212-suspension filler, 213-internal reflux pipe, 214-draft tube II, 3-high efficiency sedimentation tank, 31-mixing zone, 32-flocculation zone, 33-sedimentation zone, 34-polymeric ferric sulfate dosing pipe, 35 water inlet, 36-stirrer, 37-guide channel, 38-polyacrylamide dosing pipe, 39-guide cylinder, 310-guide pipe, 311-sludge return pipe, 312-inclined pipe assembly, 314-guide pipe III, 315-water collecting tank, 316-mud scraper, 317-sludge concentration tank, 318-sludge return pipe, 319-sludge discharge pipe, 4-denitrification filter tank, 42-backwashing drainage tank, 44-water outlet tank, 45-backwashing drainage pipe, 46-guide pipe IV, 47-filter material layer, 48-bearing layer, 49-long handle filter head, 410-filter plate, 411-water inlet channel, 412-backwashing air inlet pipe, 413-water inlet pipe II, 414-backwashing water inlet pipe, 415-emptying pipe, 5-activated carbon adsorption tank, 51-a water inlet pipe III, 52-a sieve pipe water distributor, 53-an adsorption layer, 54-a short-handle filter head, 55-a filter plate, 56-a sampling hole, 57-a carbon discharge pipe and 58-a water discharge pipe.
Detailed Description
The invention is further described with reference to specific examples. The scope of the invention is not limited thereto.
Example 1
The embodiment adopts the actual treatment device of a certain pesticide chemical industry park wastewater treatment plant, and the treatment capacity is 20000m3The water quality is characterized in that: average COD value of 329mg/L, average total nitrogen value of 121mg/L, average organic nitrogen concentration of 56mg/L, and acute toxicity of photobacteria (HgCl)2Toxicity equivalent) of 0.16mg/L, and high-toxicity wastewater is obtained according to the toxicity classification standard.
The structure of the wastewater treatment system is shown in figure 1, and comprises a micro-aerobic hydrolysis acidification tank 1, a two-stage A/O sludge membrane mixing tank 2, a high-efficiency sedimentation tank 3, a denitrification filter tank 4 and an activated carbon adsorption tank 5 which are sequentially connected in series.
As shown in figure 2, the bottom of the micro-aerobic hydrolysis acidification tank 1 is provided with an aeration device 11 and a porous water distribution and sludge discharge system 12, the middle part is filled with sludge to form a sludge bed 13, the top part is provided with a water collection tank 15 with a triangular weir 14 and an exhaust pipe 16, and the water collection tank 15 is provided with a first draft tube 17 connected to the two-stage A/O sludge film mixing tank 2.
As shown in fig. 3, two-stage a/O mudThe membrane mixing tank 2 is built by an A1 section 21, an O1 section 22, an A2 section 23 and an O2 section 24, each section is divided into two lattices, the lattices and the sections are separated by partition walls 25, one side of each partition wall is provided with a water outlet 26 as a flow guide channel, both sides of the tank wall of the A1 section 21 and the A2 section 22 are provided with stirrers 27, the upper part of the tank wall of the A1 section 21 is provided with a first water inlet pipe 28 connected with a first flow guide pipe 17, the bottom of the tank wall is provided with a sludge return pipe 29, the bottoms of the O1 section 23 and the O2 section 24 are provided with aeration pipelines 211 with microporous aeration disks 210 in a paving mode, a suspended filler 212 is added into the O2 section, the middle part of each membrane mixing tank is provided with an inner return pipe 213 connected to the A1 section 21 and a second flow guide pipe 214 connected to a second sedimentation tank, and the inner sides of the second flow guide pipe 214 are provided with filter screen covers 215; the suspended filler 212 is a three-layer hollow cylinder with a corrugated shape, the concentric circles are supported by blades at intervals to make the cross section of the filler in a trapezoidal oblique wave shape, and the specific surface area is 560m2/m3The diameter of the outer ring cylinder is 20mm, the filling rate is 30%, and K3 suspension filler in the prior art is adopted.
As shown in fig. 4, the high-efficiency sedimentation tank 3 is composed of a mixing zone 31, a flocculation zone 32 and a sedimentation zone 33, wherein the upper part of the mixing zone 31 is provided with a polymeric ferric sulfate dosing pipe 34 and a water inlet 35 connected with the water outlet of the secondary sedimentation tank, the middle part is provided with a stirrer 36, and the bottom part is provided with a flow guide channel 37 connected with the flocculation zone 32; the upper part of the flocculation area 32 is provided with a polyacrylamide dosing pipe 38, the middle part is provided with a guide cylinder 39 with a stirrer, the guide cylinder 39 is connected with the coagulation area 31 through a guide pipe 310, and the bottom part is provided with a sludge return pipe 311; an inclined pipe assembly 312, a triangular weir 14 and a water collecting tank 315 with a flow guide pipe III 314 are arranged at the upper part of the settling zone 33, the diameter of an inclined pipe of the inclined pipe assembly 312 is 50mm, the inclined angle of the inclined pipe is 60 degrees, and the inclined length of the inclined pipe is 600 mm; the bottom of the settling zone is provided with a mud scraper 316 and a sludge thickening tank 317, and a sludge return pipe 318 and a sludge discharge pipe 319 which are connected to the flocculation zone 32 are arranged in the sludge thickening tank 317.
As shown in FIG. 5, a back-flushing drainage tank 42 with a triangular weir 14 and an effluent tank 44 with a triangular weir 14 are arranged in parallel at the top of the denitrification filter tank 4, a back-flushing drainage pipe 45 is arranged at the bottom of the back-flushing drainage tank 42, a draft tube four 46 connected with the activated carbon adsorption tank 5 is arranged at the bottom of the effluent tank 44, and a filter material layer 47, a supporting layer 48 and a filter head with a long handle are arranged in sequence from top to bottom at the middle of the denitrification filter tank 449 of the filter plate 410, the filter material layer 47 is a ceramsite filter material with the particle size of 3mm-5mm and the specific surface area of 5.4 multiplied by 104cm2(ii)/g, porosity of 62%, packing height of 2.5m, supporting layer 48 of gravel, density of 2.5g/cm3The thickness is 150 mm; an inlet channel 411 is arranged at the bottom of the denitrification filter tank 4, and a back-washing air inlet pipe 412, a second water inlet pipe 413, a back-washing water inlet pipe 414 and an emptying pipe 415 are arranged on two sides of the inlet channel 411.
As shown in fig. 6, the top of the activated carbon adsorption tank 5 is provided with a third water inlet pipe 51 connected with a fourth draft tube 46, the third water inlet pipe 51 is connected with a sieve pipe water distributor 52, the middle part is provided with an adsorption layer 53 and a filter plate 55 with a short handle filter head 54, the side of the tank body is provided with a sampling hole 56 and a carbon discharge pipe 57, and the bottom is provided with a water discharge pipe 58.
The process for treating the pesticide chemical wastewater by using the system comprises the following steps:
step S1: carrying out primary pretreatment on pesticide chemical wastewater in a coagulation tank sedimentation mode, enabling the pretreated pesticide chemical wastewater to enter a micro-aerobic hydrolysis acidification tank 1 from a porous water distribution sludge discharge system 12, controlling the pH value in the micro-aerobic hydrolysis acidification tank 1 to be 9.0, controlling the sludge concentration to be 4.0-6.0 g/L, controlling the hydraulic retention time to be 5h (non-soluble COD is 65%), controlling the dissolved oxygen concentration to be 0.2-0.3 mg/L, and controlling the wastewater ascending flow rate to be 2 m/h; wastewater flows through a sludge bed 13 to contact with activated sludge to degrade pollutants and intercept suspended particles by being pushed by water power and air bubbles, and the treated wastewater enters a water collection tank 15 through a triangular weir 14 to be collected and then flows out through a first flow guide pipe 17;
step S2: enabling the wastewater flowing out of the first flow guide pipe 17 to enter an A1 section 21 of the two-stage A/O sludge film mixing tank 2 through a first water inlet pipe 28, regulating and controlling the sludge concentration in the two-stage A/O sludge film mixing tank 2 to be 3.5g/L-4.5g/L, the sludge retention time to be 20d, regulating and controlling the hydraulic retention time of the section 21 of A1 and the section 23 of A2 to be 9h and 6h, and regulating and controlling the dissolved oxygen concentration to be 0.3mg/L-0.5 mg/L; regulating the hydraulic retention time of the O1 section 22 to be 10h, wherein the concentration of dissolved oxygen is 2.5mg/L-4.0 mg/L; regulating and controlling the hydraulic retention time of 24 sections of O2 to be 20h and the concentration of dissolved oxygen to be 3.0mg/L-5.0mg/L, and simultaneously refluxing 24 sludge-water mixed liquor of the O2 section to 21 sections of A1 through an internal reflux pipe 211, wherein the internal reflux ratio is 200%; the treated wastewater enters a secondary sedimentation tank from the second flow guide pipe 212 at the upper part of the O2 section 24 for mud-water separation, a part of sludge after sedimentation returns to the section 21A 1 through a sludge return pipe 28, the sludge return ratio is 60 percent, and the other part of sludge is discharged through a sludge discharge pipe;
step S3: the effluent of the secondary sedimentation tank enters a high-efficiency sedimentation tank 3 through a water inlet 35, the hydraulic retention time of a mixing zone 31 is controlled to be 2.0min, the speed gradient of a stirrer 36 is 300L/s, and the concentration of polymeric ferric sulfate is 50 mg/L; controlling the hydraulic retention time of the flocculation area 32 to be 7min, controlling the flow velocity in the guide cylinder 39 to be 0.4m/s, the flow velocity outside the guide cylinder 39 to be 0.1m/s, controlling the speed gradient of the stirrer to be 75L/s and controlling the concentration of polyacrylamide to be 0.6 mg/L; controlling the sludge concentration time of the settling zone 33 to be 5h, and controlling the surface load of the inclined pipe component 312 to be 12m3/(m2H), simultaneously, the sludge in the concentration tank 317 flows back to the flocculation area 32 through sludge return pipes 311 and 318, the reflux ratio is 2%, the wastewater enters a water collection tank after being deposited in a shallow layer through the inclined pipe assembly 312, and finally flows out through a flow guide pipe III 314;
step S4: the effluent of the draft tube III 314 enters the water inlet channel 411 of the denitrification filter tank 4 through the water inlet tube II 413, and the volume load of the denitrification filter tank 4 is controlled to be 0.5 kg/(m)3D), the hydraulic retention time is 15min, the filtering speed is 15m/h, the wastewater enters the backwashing drainage tank 42 after being biologically degraded and filtered by the filter material layer 47, a part of the effluent enters the water inlet channel 411 through the backwashing drainage pipe 45 for backwashing, the backwashing period is controlled to be 48h, and the water washing intensity is 15m3/(m2H) air purge strength of 90m3/(m2H), the backwashing duration is 10min, and the other part of effluent enters the effluent groove 44 and is discharged through the four flow guide pipes 46;
step S5: and leading the effluent of the draft tube four 46 into the activated carbon adsorption tank 5 through a water inlet tube three 51, controlling the filtering speed in the activated carbon adsorption tank 5 to be 10m/h and the operating pressure to be 0.3MPa, and finally discharging or recycling the wastewater through a drain pipe 58 after the wastewater is adsorbed and filtered by an adsorption layer 53.
After the treatment of the steps, the COD of the effluent of the wastewater of the pesticide chemical industry park is less than 60mg/L, the total nitrogen is less than 20mg/L, the concentration of the organic nitrogen is less than 5mg/L, and other indexes meet the relevant requirements on industrial water (SL 368-plus 2006) in the reclaimed water quality standard. In addition, acute toxicity of photobacterium (HgCl)2Toxicity equivalent) of less than 0.07mg/L, classified by toxicityThe standard is low-toxicity or non-toxic wastewater.
Example 2
In this embodiment, a set of actual treatment apparatus of a wastewater treatment plant of a certain fermentation pharmaceutical company is adopted, and the treatment capacity is 3000m3The water quality is characterized in that: average COD value of 2950mg/L, average total nitrogen value of 281mg/L, average organic nitrogen concentration of 74mg/L, and acute toxicity of luminescent bacteria (HgCl)2Toxicity equivalent) of 0.29mg/L, and the wastewater is highly toxic according to the toxicity classification standard.
The structure of the wastewater treatment system is shown in figure 1, and comprises a micro-aerobic hydrolysis acidification tank 1, a two-stage A/O sludge membrane mixing tank 2, a high-efficiency sedimentation tank 3, a denitrification filter tank 4 and an activated carbon adsorption tank 5 which are sequentially connected in series.
As shown in figure 2, the bottom of the micro-aerobic hydrolysis acidification tank 1 is provided with an aeration device 11 and a porous water distribution and sludge discharge system 12, the middle part is filled with sludge to form a sludge bed 13, the top part is provided with a water collection tank 15 with a triangular weir 14 and an exhaust pipe 16, and the water collection tank 15 is provided with a first draft tube 17 connected to the two-stage A/O sludge film mixing tank 2.
As shown in fig. 3, the two-stage a/O sludge film mixing tank 2 is built by combining a1 section 21, an O1 section 22, a2 section 23 and an O2 section 24, each section is divided into two cells, the cells and the cells are separated by partition walls 25, one side of each partition wall is provided with a water outlet 26 as a flow guide channel, both sides of the tank walls of the a1 section 21 and the a2 section 22 are provided with stirrers 27, the upper part of the tank wall of the a1 section 21 is provided with a first water inlet pipe 28 connected with a first flow guide pipe 17, the bottom of the tank wall is provided with a sludge return pipe 29, the bottoms of the O1 section 23 and the O2 section 24 are provided with an aeration pipeline 211 with a microporous aeration disc 210, a suspension filler 212 is added into the O2 section 24, the middle part of the inner return pipe 213 connected to the a1 section 21 and a second flow guide pipe 214 connected to a secondary sedimentation tank, and the inner side of the second flow guide pipe 214 is provided with a filter screen cover 215; the suspended filler 212 is a three-layer hollow cylinder with corrugated shape, and the cross section of the filler is trapezoidal oblique wave with specific surface area of 982m and supported by blades at intervals between concentric circles2/m3The diameter of the outer ring cylinder is 30mm, and the filling rate is 50%.
As shown in fig. 4, the high-efficiency sedimentation tank 3 is composed of a mixing zone 31, a flocculation zone 32 and a sedimentation zone 33, wherein the upper part of the mixing zone 31 is provided with a polymeric ferric sulfate dosing pipe 34 and a water inlet 35 connected with the water outlet of the secondary sedimentation tank, the middle part is provided with a stirrer 36, and the bottom part is provided with a flow guide channel 37 connected with the flocculation zone 32; the upper part of the flocculation area 32 is provided with a polyacrylamide dosing pipe 38, the middle part is provided with a guide cylinder 39 with a stirrer, the guide cylinder 39 is connected with the coagulation area 31 through a guide pipe 310, and the bottom part is provided with a sludge return pipe 311; an inclined pipe assembly 312, a triangular weir 14 and a water collecting tank 315 with a flow guide pipe III 314 are arranged at the upper part of the settling zone 33, the diameter of an inclined pipe of the inclined pipe assembly 312 is 100mm, the inclined angle of the inclined pipe is 60 degrees, and the inclined length of the inclined pipe is 1500 mm; the bottom of the settling zone is provided with a mud scraper 316 and a sludge thickening tank 317, and a sludge return pipe 318 and a sludge discharge pipe 319 which are connected to the flocculation zone 32 are arranged in the sludge thickening tank 317.
As shown in figure 5, a back flush water drainage tank 42 with a triangular weir 14 and a water outlet tank 44 with a triangular weir 14 are arranged in parallel at the top of the denitrification filter tank 4, a back flush water drainage pipe 45 is arranged at the bottom of the back flush water drainage tank 42, a flow guide pipe four 46 connected with the activated carbon adsorption tank 5 is arranged at the bottom of the water outlet tank 44, a filter material layer 47, a supporting layer 48 and a filter plate 410 with a long handle filter head 49 are sequentially arranged at the middle part of the denitrification filter tank 4 from top to bottom, the filter material layer 47 is a ceramsite filter material, the particle size is 3mm-5mm, and the specific surface area is 4.2 multiplied by 104cm2A porosity of 52%, a packing height of 4m, a supporting layer 48 of gravel, a density of 2.7g/cm3280mm in thickness; an inlet channel 411 is arranged at the bottom of the denitrification filter tank 4, and a back-washing air inlet pipe 412, a second water inlet pipe 413, a back-washing water inlet pipe 414 and an emptying pipe 415 are arranged on two sides of the inlet channel 411.
As shown in fig. 6, the top of the activated carbon adsorption tank 5 is provided with a third water inlet pipe 51 connected with a fourth draft tube 46, the third water inlet pipe 51 is connected with a sieve pipe water distributor 52, the middle part is provided with an adsorption layer 53 and a filter plate 55 with a short handle filter head 54, the side of the tank body is provided with a sampling hole 56 and a carbon discharge pipe 57, and the bottom is provided with a water discharge pipe 58.
The process for treating the wastewater of the fermentation pharmaceutical industry by applying the system comprises the following steps:
step S1: carrying out primary pretreatment on the fermentation pharmaceutical industrial wastewater through a fine grid and an air flotation tank, feeding the pretreated fermentation pharmaceutical industrial wastewater into a micro-aerobic hydrolysis acidification tank 1 from a porous water distribution sludge discharge system 12, controlling the pH value in the micro-aerobic hydrolysis acidification tank 1 to be 5.0, controlling the sludge concentration to be 6.0-8.0 g/L, controlling the hydraulic retention time to be 12d (the non-soluble COD is 42%), controlling the dissolved oxygen concentration to be 0.3-0.4 mg/L, and controlling the wastewater ascending flow rate to be 0.5 m/h; wastewater flows through a sludge bed 13 to contact with activated sludge to degrade pollutants and intercept suspended particles by being pushed by water power and air bubbles, and the treated wastewater enters a water collection tank 15 through a triangular weir 14 to be collected and then flows out through a first flow guide pipe 17;
step S2: enabling the wastewater flowing out of the draft tube I17 to enter an A1 section 21 of the two-stage A/O sludge film mixing tank 2 through a water inlet pipe 28, regulating and controlling the sludge concentration in the two-stage A/O sludge film mixing tank 2 to be 3.5g/L-4.5g/L, the sludge retention time to be 15d, regulating and controlling the hydraulic retention time of the section 21 of A1 and the section 23 of A2 to be 6h and 9h respectively, and regulating and controlling the dissolved oxygen concentration to be 0.2mg/L-0.4 mg/L; regulating the hydraulic retention time of the O1 section 22 to be 14h, wherein the concentration of dissolved oxygen is 2.5mg/L-4.0 mg/L; regulating and controlling the hydraulic retention time of 24 sections of O2 to be 16h and the concentration of dissolved oxygen to be 4.0mg/L-6.0mg/L, and simultaneously refluxing 24 sludge-water mixed liquor of the O2 section to 21 sections of A1 through an internal reflux pipe, wherein the internal reflux ratio is 400%; the treated wastewater enters a secondary sedimentation tank from a second diversion pipe at the upper part of the O2 section 24 for mud-water separation, a part of sludge after sedimentation returns to the A1 section 21 through a sludge return pipe, the sludge return ratio is 100 percent, and the other part of sludge is discharged through a sludge discharge pipe;
step S3: the effluent of the secondary sedimentation tank enters a high-efficiency sedimentation tank 3 through a water inlet, the hydraulic retention time of a mixing zone 31 is controlled to be 3.5min, the speed gradient of a stirrer 36 is 500L/s, and the concentration of polymeric ferric sulfate is 120 mg/L; controlling the hydraulic retention time of the flocculation area 32 to be 10min, controlling the flow velocity in the guide cylinder 39 to be 1.2m/s, the flow velocity outside the guide cylinder to be 0.3m/s, controlling the speed gradient of the stirrer to be 250L/s and controlling the concentration of polyacrylamide to be 2.0 mg/L; controlling the sludge concentration time of the settling zone 33 to be 10h, and controlling the surface load of the inclined tube component 312 to be 25m3/(m2H), simultaneously returning the sludge in the concentration tank to the flocculation area through sludge return pipes 311 and 318, wherein the return ratio is 10%, and the wastewater enters a water collecting tank 315 after being subjected to shallow sedimentation through an inclined pipe assembly 312 and finally flows out through a flow guide pipe III 314;
step S4: the effluent of the draft tube III 314 enters the water inlet channel 411 of the denitrification filter tank 4 through the water inlet tube II 413, and the volume load of the denitrification filter tank 4 is controlled to be 3.0 kg/(m)3D) hydraulic retention time of 20min and filtration rate of 10m/h, the wastewater enters a back-flushing drainage tank 42 after being biologically degraded and filtered by a filter material layer 47, a part of the effluent enters an inlet channel 411 through a back-flushing drainage pipe 45 for back flushing, the back-flushing period is controlled to be 24h, and the water flushing intensity is controlled to be 25m3/(m2H) air flushing intensity of 150m3/(m2H), the backwashing duration is 20min, and the other part of effluent enters the effluent groove 44 and is discharged through the four flow guide pipes 46;
step S5: and leading the effluent of the flow guide pipe four 46 into the activated carbon adsorption tank 5 through a water inlet pipe three 51, controlling the filtering speed in the activated carbon adsorption tank 5 to be 5m/h and the operating pressure to be 0.1MPa, and finally discharging or recycling the wastewater through a drain pipe 58 after the wastewater is adsorbed and filtered by an adsorption layer 53.
After the treatment of the steps, the COD of the effluent of the fermentation pharmaceutical wastewater is less than 100mg/L, the total nitrogen is less than 50mg/L, the concentration of organic nitrogen is less than 10mg/L, and the acute toxicity (HgCl) of the luminescent bacteria of the effluent is2Toxicity equivalent) is less than 0.07mg/L, and all indexes meet the relevant requirements of the discharge standard of water pollutants for fermentation pharmaceutical industry (GB 21903-2008).
Claims (7)
1. An organic nitrogen wastewater treatment system is characterized by comprising a micro-aerobic hydrolysis acidification tank (1), a two-stage A/O sludge membrane mixing tank (2), a high-efficiency sedimentation tank (3), a denitrification filter tank (4) and an activated carbon adsorption tank (5) which are sequentially connected in series,
an aeration device (11) and a porous water distribution and sludge discharge system (12) are arranged at the bottom of the micro-aerobic hydrolysis acidification tank (1), a sludge bed (13) is formed by filling sludge in the middle, a water collection tank (15) with a triangular weir (14) and an exhaust pipe (16) are arranged at the top of the micro-aerobic hydrolysis acidification tank, a first guide pipe (17) connected to the two-stage A/O sludge film mixing tank (2) is arranged on the water collection tank (15),
the two-stage A/O sludge film mixing tank (2) is built by combining an A1 section (21), an O1 section (22), an A2 section (23) and an O2 section (24), each section is divided into two grids, the grids and the sections are separated by partition walls (25), one side of each partition wall is provided with a water outlet (26) as a flow guide channel, both sides of the tank walls of the A1 section (21) and the A2 section (22) are respectively provided with a stirrer (27), the upper part of the tank wall of the A1 section (21) is provided with a first water inlet pipe (28) connected with a first flow guide pipe (17), the bottom of the tank wall is provided with a sludge return pipe (29), the bottoms of the O1 section (23) and the O2 section (24) are respectively provided with a stirrer (211) with a microporous aeration disc (210), a suspended filler (212) is added into the O2), the middle part of the O1 section (24) is provided with an inner return pipe (213) connected with the A1 section (21) and a second flow guide pipe (214) connected with a second sedimentation tank, and the inner side of the guide pipe (214) is provided with a screen cover (215),
high-efficient sedimentation tank (3) comprises mixing district (31), flocculation district (32) and settling zone (33), mixing district (31) upper portion is equipped with polyferric sulfate dosing pipe (34) and water inlet (35) of being connected with two heavy pond delivery ports, and the centre is equipped with mixer (36), and the bottom is equipped with diversion channel (37) of being connected with flocculation district (32), flocculation district (32) upper portion is equipped with polyacrylamide dosing pipe (38), and the middle part is equipped with draft tube (39) of taking the mixer, and draft tube (39) are connected with coagulation district (31) through draft tube (310), and the bottom is equipped with mud reflux pipe (311), settling zone (33) upper portion is equipped with pipe chute subassembly (312), triangle weir (14) and has catchment groove (315) of three draft tubes (314), and the bottom is equipped with mud scraper (316) and sludge concentration groove (317), be equipped with mud reflux pipe (318) and the mud discharge pipe (319) that are connected to flocculation district (32) in sludge concentration groove (317) ,
the top of the denitrification filter tank (4) is provided with a back flush water drainage tank (42) with a triangular weir (14) and a water outlet tank (44) with a triangular weir (14) in parallel, the bottom of the back flush water drainage tank (42) is provided with a back flush water drainage pipe (45), the bottom of the water outlet tank (44) is provided with a four diversion pipe (46) connected with the activated carbon adsorption tank (5), the middle part of the denitrification filter tank (4) is sequentially provided with a filter material layer (47), a supporting layer (48) and a filter plate (410) with a long handle filter head (49) from top to bottom, the bottom is provided with a water inlet channel (411), two sides of the water inlet channel (411) are provided with a back flush air inlet pipe (412), a second water inlet pipe (413), a back flush water inlet pipe (414) and an emptying pipe (415),
the top of the activated carbon adsorption tank (5) is provided with a third water inlet pipe (51) connected with a fourth draft tube (46), the third water inlet pipe (51) is connected with a sieve tube water distributor (52), the middle part of the activated carbon adsorption tank is provided with an adsorption layer (53) and a filter plate (55) with a short-handle filter head (54), the side surface of the tank body is provided with a sampling hole (56) and a carbon discharge pipe (57), and the bottom of the activated carbon adsorption tank is provided with a water discharge pipe (58).
2. The organic nitrogen wastewater treatment system of claim 1, wherein the volume of the section A1 (21) is 43% -90% of that of the section O1 (22), the volume of the section A2 (23) is 30% -56% of that of the section O2 (24), and the sections A2+ O2 account for 49% -64% of the total volume.
3. The organic wastewater treatment system according to claim 1, wherein the suspended filler (212) is a three-layer hollow cylinder with a corrugated shape, and the cross section of the filler is trapezoidal and inclined waves with a specific surface area of 500m and is supported by blades at intervals between concentric circles2/m3-1000m2/m3The diameter of the outer ring cylinder is 20mm-30mm, and the filling rate is 30% -50%.
4. The organic nitrogen wastewater treatment system as claimed in claim 1, wherein the inclined tube assembly (312) has an inclined tube diameter of 50mm-100mm, an inclined tube inclination angle of 60 ° and an inclined tube inclination length of 600-1500 mm.
5. The organic nitrogen wastewater treatment system of claim 1, wherein the filter material layer (47) is a ceramsite filter material with a particle size of 3mm-5mm and a specific surface area of 4 x 104cm2/g-6×104cm2The porosity is more than or equal to 40 percent, the packing height is 2.5m to 4m, the bearing layer (48) is gravel, and the density is 2.5g/cm3-2.7g/cm3The thickness is less than or equal to 300 mm.
6. The organic nitrogen wastewater treatment system of claim 1, wherein the activated carbon used in the adsorption layer (53) has a particle size of 0.8mm-2mm and a specific surface area of 1000m2/g-1500m2The iodine value is 800-.
7. The process for organic nitrogen wastewater treatment using the system of any one of claims 1 to 6, characterized by comprising the steps of:
step S1: carrying out primary pretreatment on the organic nitrogen wastewater, wherein the water quality of the organic nitrogen wastewater after the primary pretreatment is characterized in that: 300mg/L-3000mg/L of COD, 100mg/L-500mg/L of total nitrogen and 50mg/L-300mg/L of organic nitrogen; then the sewage enters a micro-aerobic hydrolysis acidification pool (1) through a porous water distribution and sludge discharge system (12), the pH value in the micro-aerobic hydrolysis acidification pool (1) is controlled to be 5.0-9.0, the sludge concentration is 4.0-8.0 g/L, when the non-soluble COD is more than 60%, the hydraulic retention time is 2-6 h, when the non-soluble COD is less than 60%, the hydraulic retention time is 4-12 h, the dissolved oxygen concentration is 0.2-0.4 mg/L, and the wastewater rising flow rate is 0.5-2 m/h; the wastewater flows through a sludge bed (13) to contact with activated sludge to degrade pollutants and retain suspended particles by pushing of water power and air bubbles, and the treated wastewater enters a water collection tank (15) through a triangular weir (14) to be collected and then flows out through a first flow guide pipe (17);
step S2: wastewater flowing out of a flow guide pipe (17) enters an A1 section (21) of a two-stage A/O sludge film mixing pool (2) through a first water inlet pipe (28), the sludge concentration in the two-stage A/O sludge film mixing pool (2) is regulated to be 3.5g/L-4.5g/L, the sludge retention time is regulated to be 15d-20d, the hydraulic retention time of the A1 section (21) and the A2 section (23) is regulated to be 6h-9h, and the dissolved oxygen concentration is 0.2mg/L-0.5 mg/L; regulating the hydraulic retention time of the O1 section (23) to be 10-14 h and the dissolved oxygen concentration to be 2.5-4.0 mg/L; regulating and controlling the hydraulic retention time of the O2 section (24) to be 16-20 h and the dissolved oxygen concentration to be 3.0-6.0 mg/L, and simultaneously refluxing the O2 section (24) sludge-water mixed liquid to the A1 section (21) through an internal reflux pipe (211), wherein the internal reflux ratio is 200-400%; the treated wastewater enters a secondary sedimentation tank from a second diversion pipe (212) at the upper part of the O2 section (24) for mud-water separation, a part of sludge after sedimentation returns to the A1 section (21) through a sludge return pipe (28), the sludge return ratio is 60-100%, and the other part of sludge is discharged through a sludge discharge pipe;
step S3: the effluent of the secondary sedimentation tank enters a high-efficiency sedimentation tank (3) through a water inlet (35), the hydraulic retention time of a mixing zone (31) is controlled to be 2.0min-3.5min, the speed gradient of a stirrer (36) is 300L/s-500L/s, and the concentration of polymeric ferric sulfate is 50mg/L-120 mg/L; controlling the hydraulic retention time of the flocculation area (32) to be 7min-10min, controlling the flow velocity in the guide cylinder (39) to be 0.4m/s-1.2m/s, the flow velocity outside the guide cylinder to be 0.1m/s-0.3m/s, controlling the speed gradient of the stirrer to be 75L/s-250L/s, and controlling the concentration of polyacrylamide to be 0.6mg/L-2.0 mg/L; controlling the sludge concentration time of the settling zone (33) to be 5-10 h and the surface load of the inclined pipe component (312) to be 12m3/(m2·h)-25m3/(m2H) while the sludge in the thickening tank (317) is returned to the sludge return pipes (311 and 318)The reflux ratio of the flocculation area (32) is 2-10%, and the wastewater enters a water collection tank (315) after being subjected to shallow precipitation by an inclined pipe assembly (312) and finally flows out through a flow guide pipe III (314);
step S4: the effluent of the draft tube III (314) enters an inlet channel (411) of the denitrification filter tank (4) through an inlet tube II (413), and the volume load of the denitrification filter tank (4) is controlled to be 0.5 kg/(m)3·d)-3.0kg/(m3D), the hydraulic retention time is 15min to 20min, the filtering speed is 10m/h to 15m/h, the wastewater enters a backwashing drainage tank (42) after being biodegraded and filtered by a filter material layer (47), a part of effluent enters an inlet channel (411) through a backwashing drainage pipe (45) for backwashing, the backwashing period is controlled to be 24h to 48h, and the water washing intensity is 15m3/(m2·h)-25m3/(m2H) air purge strength of 90m3/(m2·h)-150m3/(m2H), the back washing lasts for 10min to 20min, and the other part of the effluent enters the effluent groove (44) and is discharged through the flow guide pipe four (46);
step S5: and leading the effluent of the flow guide pipe IV (46) into the activated carbon adsorption tank (5) through a water inlet pipe III (51), controlling the filtering speed in the activated carbon adsorption tank (5) to be 5-10 m/h and the operating pressure to be 0.1-0.3 MPa, and finally discharging or recycling the wastewater through a drain pipe (58) after the wastewater is adsorbed and filtered by an adsorption layer (53).
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110727236.5A CN113511779A (en) | 2021-06-29 | 2021-06-29 | Organic nitrogen wastewater treatment system and process |
| JP2021162746A JP7149016B2 (en) | 2021-06-29 | 2021-10-01 | Organic nitrogen wastewater treatment system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110727236.5A CN113511779A (en) | 2021-06-29 | 2021-06-29 | Organic nitrogen wastewater treatment system and process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113511779A true CN113511779A (en) | 2021-10-19 |
Family
ID=78066237
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110727236.5A Pending CN113511779A (en) | 2021-06-29 | 2021-06-29 | Organic nitrogen wastewater treatment system and process |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JP7149016B2 (en) |
| CN (1) | CN113511779A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114873876A (en) * | 2022-07-07 | 2022-08-09 | 天津高能时代水处理科技有限公司 | Landfill leachate non-membrane treatment system and method |
| CN115124198A (en) * | 2022-07-22 | 2022-09-30 | 山东辰广环保装备有限公司 | Pretreatment device for solving biological pollution of water treatment membrane |
| CN115403218A (en) * | 2022-08-24 | 2022-11-29 | 中冶赛迪工程技术股份有限公司 | Coal chemical wastewater treatment device and treatment process |
| CN116239263A (en) * | 2023-03-17 | 2023-06-09 | 沈阳环境科学研究院 | Reinforced treatment method for town sewage |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114506980B (en) * | 2022-02-28 | 2023-10-10 | 宝钢湛江钢铁有限公司 | Method for removing organic nitrogen and soluble organic matters in cold rolling emulsion wastewater |
| CN114681966A (en) * | 2022-03-28 | 2022-07-01 | 深圳合续科技开发有限公司 | Rain and sewage mixing overflow sewage treatment device |
| CN115254821A (en) * | 2022-07-26 | 2022-11-01 | 宝武水务科技有限公司 | Cleaning device for inclined tube in inclined tube sedimentation tank |
| CN115466005A (en) * | 2022-08-05 | 2022-12-13 | 中国石油化工股份有限公司 | High-salt high-ammonia nitrogen sewage treatment device and method |
| CN115215439A (en) * | 2022-08-19 | 2022-10-21 | 中建生态环境集团有限公司 | Sewage deep denitrification device based on two-stage AO double-reflux process and operation method |
| CN115745234B (en) * | 2022-11-01 | 2023-07-04 | 同济大学建筑设计研究院(集团)有限公司 | Multi-medium composite filling water treatment system and application method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103204605A (en) * | 2013-05-22 | 2013-07-17 | 徐州工程学院 | Method for treating garlic processing waste water |
| CN104230114A (en) * | 2014-09-24 | 2014-12-24 | 清华大学 | Device and method for treating petrochemical wastewater by using anaerobic hydrolysis acidification-A/O biological membrane method |
| CN111138047A (en) * | 2020-03-03 | 2020-05-12 | 安徽绿衡环保科技有限公司 | Denitrification and dephosphorization device with advanced standard improvement and treatment process thereof |
| CN111268799A (en) * | 2020-03-03 | 2020-06-12 | 南京大学 | Efficient biological treatment system and process for organic nitrogen industrial wastewater |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004097856A (en) * | 2002-09-04 | 2004-04-02 | Masuda Shokai:Kk | Equipment and method for waste liquid treatment |
-
2021
- 2021-06-29 CN CN202110727236.5A patent/CN113511779A/en active Pending
- 2021-10-01 JP JP2021162746A patent/JP7149016B2/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103204605A (en) * | 2013-05-22 | 2013-07-17 | 徐州工程学院 | Method for treating garlic processing waste water |
| CN104230114A (en) * | 2014-09-24 | 2014-12-24 | 清华大学 | Device and method for treating petrochemical wastewater by using anaerobic hydrolysis acidification-A/O biological membrane method |
| CN111138047A (en) * | 2020-03-03 | 2020-05-12 | 安徽绿衡环保科技有限公司 | Denitrification and dephosphorization device with advanced standard improvement and treatment process thereof |
| CN111268799A (en) * | 2020-03-03 | 2020-06-12 | 南京大学 | Efficient biological treatment system and process for organic nitrogen industrial wastewater |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114873876A (en) * | 2022-07-07 | 2022-08-09 | 天津高能时代水处理科技有限公司 | Landfill leachate non-membrane treatment system and method |
| CN115124198A (en) * | 2022-07-22 | 2022-09-30 | 山东辰广环保装备有限公司 | Pretreatment device for solving biological pollution of water treatment membrane |
| CN115403218A (en) * | 2022-08-24 | 2022-11-29 | 中冶赛迪工程技术股份有限公司 | Coal chemical wastewater treatment device and treatment process |
| CN116239263A (en) * | 2023-03-17 | 2023-06-09 | 沈阳环境科学研究院 | Reinforced treatment method for town sewage |
Also Published As
| Publication number | Publication date |
|---|---|
| JP7149016B2 (en) | 2022-10-06 |
| JP2022001368A (en) | 2022-01-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113511779A (en) | Organic nitrogen wastewater treatment system and process | |
| CN102659244B (en) | Integrated internal circulation type denitrification and decarburization bio-membrane reactor and operating method thereof | |
| CN101244883B (en) | High-efficiency low-consumption retexture method for urban sewage | |
| CN108585384B (en) | MBBR high-standard sewage treatment system and treatment process | |
| CN202625927U (en) | Integration internal circulation type denitrification decarburization biological membrane reactor | |
| CN218910039U (en) | Efficient mud membrane symbiotic denitrification and dephosphorization sewage treatment system | |
| CN214528587U (en) | Rural domestic sewage treatment system of nitrogen and phosphorus removal integration | |
| CN104030441A (en) | Horizontal type three-phase biological fluidized bed and sewage treatment method thereof | |
| CN111646649A (en) | Excrement wastewater treatment method for modular railway train excrement collector | |
| CN110776219A (en) | Advanced treatment device for printing and dyeing wastewater pollutants and application thereof | |
| CN102964037A (en) | Novel sewage treatment method by combined utilization of light filter material biological aerated filter and heavy filter material biological aerated filter | |
| CN105923771A (en) | Self-circulation biological denitrification reactor | |
| CN111646648A (en) | Remote treatment method for excrement wastewater of modular railway train excrement collector | |
| CN104803480A (en) | Multistage bioreactor and method for treating sewage with reactor | |
| CN109775936B (en) | Low-energy-consumption domestic sewage treatment system | |
| CN209906446U (en) | Integrated sewage advanced treatment device based on circular tank body | |
| CN112429840A (en) | Improved artificial rapid infiltration integrated device based on agricultural waste carbon slow release enhanced biological nitrogen and phosphorus removal and application thereof | |
| CN101659497A (en) | Processing method of mixed tail water from pharmaceutical industrial park | |
| CN218811022U (en) | Integrated treatment device for deep denitrification of garbage penetration filtrate | |
| CN102372394A (en) | Method for treating rural sewage with effect of removing phosphate and nitrogen | |
| CN201406344Y (en) | Biologic fixed bed reactor | |
| CN212833299U (en) | Modularized long-term treatment device for excrement wastewater of toilet wastewater collector of railway train | |
| CN210367122U (en) | Folded plate flow artificial wetland system for strengthening removal of nitrogen and phosphorus | |
| CN204569547U (en) | Multi-stage biological reactor | |
| CN113880237A (en) | Concentric circle internal circulation aerobic reactor |
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 |