CN115504570B - Autotrophic denitrification process device and sewage treatment method - Google Patents
Autotrophic denitrification process device and sewage treatment method Download PDFInfo
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2806—Anaerobic processes using solid supports for microorganisms
-
- 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
- C02F3/2833—Anaerobic digestion processes using fluidized bed reactors
-
- 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
- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
-
- 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
- C02F3/2866—Particular arrangements for anaerobic reactors
-
- 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
- C02F3/2866—Particular arrangements for anaerobic reactors
- C02F3/2873—Particular arrangements for anaerobic reactors with internal draft tube circulation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- 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)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Biological Treatment Of Waste Water (AREA)
Abstract
The invention relates to an autotrophic nitrogen removal process device and a sewage treatment method, wherein the autotrophic nitrogen removal process device comprises the following steps: the device comprises a homogenizing tank, a middle tank and an anaerobic reactor, wherein the homogenizing tank is communicated with the middle tank, and the middle tank is communicated with the anaerobic reactor; the anaerobic reactor is sequentially divided into a water distribution area, a carrier area, a three-phase separation area and a water outlet area from bottom to top; wherein, the water distribution area is provided with a water distribution plate, and the water distribution plate is provided with a filter head; a denitrification carrier is filled in the carrier zone; a central tube and a horn-shaped cover body are arranged in the three-phase separation area; the top of the water outlet area is provided with a water collecting tank and a water outlet weir. According to the autotrophic nitrogen removal process device, an anaerobic reactor is adopted, anti-blocking filter heads are adopted for water distribution, so that the uniformity of water distribution is improved, and the effective utilization rate of a carrier layer is increased; the device occupies small area, runs stably and has high denitrification load.
Description
Technical Field
The invention belongs to the technical field of chemical industry and environmental protection, in particular relates to a wastewater process technology, and further relates to an autotrophic denitrification process device and a wastewater treatment method.
Background
In recent years, nitrogen pollution in the field of water treatment has become one of the social hot spots. Removal of nitrogen from water is one of the key problems of concern in the water treatment field. How to economically, efficiently and safely remove total nitrogen from water, develop a high-efficiency and stable bio-enhanced denitrification technology, and become a problem to be solved in the field of sewage treatment.
Biological denitrification is widely focused on the lower treatment cost, and the traditional biological denitrification approach in the sewage treatment field is autotrophic nitrification-heterotrophic denitrification, but has the defects of long denitrification process, large oxygen consumption, large carbon source consumption and large sludge yield. Autotrophic denitrification is realized without adding any additional carbon source, total nitrogen removal can be realized by utilizing sulfur, iron, nitrite and the like, the flow is short, the cost is low, and the treatment efficiency is high. In the autotrophic denitrification process, the biomembrane method is widely focused due to the characteristics of high treatment efficiency, small sludge yield of residual sludge, convenient operation and management and the like, and has wide application prospect in sewage treatment.
Patent CN110054291A discloses a device and a method for denitrification of urban sewage with low C/N ratio, which can realize deep denitrification of domestic sewage through an anaerobic ammonia oxidation way under the condition of not adding a carbon source additionally, but the process has complicated mode for realizing deep denitrification, longer process flow and poor control.
Patent CN111807610B discloses a method and a system for deeply removing total nitrogen in sewage, which can be used for upgrading and reforming an existing sewage treatment plant, but the process adopts suspended sludge to perform anaerobic ammoxidation, has lower denitrification load, and needs to ensure the total nitrogen concentration with lower concentration in the water inlet.
The carrier in the biomembrane process is used as the important component of the reactor, and is the carrier of the microbial film, and the physical and chemical characteristics, the hydraulic fluidization characteristics and the like of the carrier affect the mass transfer efficiency of the substrate. The quality of the carrier performance directly influences the difficulty of film formation, the adhesion quantity of the biological film and the total nitrogen treatment load, and is important to improving the treatment efficiency of the biological film reactor and reducing the operation cost.
Therefore, development of a denitrification functional carrier is needed to improve the activity of the biological membrane and realize efficient denitrification.
Disclosure of Invention
Aiming at the condition of lacking autotrophic biomembrane denitrification process in the current water treatment, the invention discloses an autotrophic denitrification process device and a denitrification functional carrier matched with the autotrophic biomembrane denitrification process device, which improve biomembrane activity and reactor treatment load, realize high-efficiency denitrification and effectively reduce the operation and running cost of a reactor.
In a first aspect, the present invention provides an autotrophic nitrogen removal process device, which is characterized by comprising: the device comprises a homogenizing tank, a middle tank and an anaerobic reactor, wherein the homogenizing tank is communicated with the middle tank, and the middle tank is communicated with the anaerobic reactor.
The anaerobic reactor is sequentially divided into a water distribution area, a carrier area, a three-phase separation area and a water outlet area from bottom to top; wherein, the water distribution area is provided with a water distribution plate, and the water distribution plate is provided with a filter head; a denitrification carrier is filled in the carrier zone; a central tube and a horn-shaped cover body are arranged in the three-phase separation area; the top of the water outlet area is provided with a water collecting tank and a water outlet weir.
According to the autotrophic nitrogen removal process device, an anaerobic reactor is adopted, anti-blocking filter heads are adopted for water distribution, so that the uniformity of water distribution is improved, and the effective utilization rate of a carrier layer is increased; the device occupies small area, runs stably and has high denitrification load.
The filter heads are arranged on the gas-water distribution plate, the filter heads consist of filter caps, filter gaps and filter rods, and the filter rods are arranged on the gas-water distribution plate through rubber gaskets and threads, so that uniform distribution of water flow and gas at the bottom of the reactor can be realized, and meanwhile, the function of intercepting biological carriers can be achieved.
The filter screen meshes can be wedge-shaped, round holes, square holes and the like, the filter screen cleaning mode can be one or a combination of a plurality of ultrasonic cleaning, rotating brush cleaning, scraping plate cleaning, spraying flushing and the like, the purposes of adhering sludge cleaning, continuous sludge discharge and carrier loss prevention to the outlet filter screen are achieved, and the outlet water enters a circulating pipeline or a discharge system through a water outlet after passing through the filter screen.
Preferably, the apparatus may further comprise a wastewater treatment apparatus comprising an auxiliary line.
As a specific embodiment of the present invention, the ratio of the height to the diameter of the anaerobic reactor is (1-8): 1, preferably (2 to 4): 1.
the bottom of the upflow expansion bed reactor is uniformly distributed by the filter head, carrier region expansion is realized by the circulating system, which is favorable for substrate transmission and blockage prevention, biomembrane self-balancing is realized by friction among carriers, the water flux of the filter screen is kept by the filter screen cleaning system, continuous mud discharge of device water is realized, and carrier loss is prevented.
As a specific embodiment of the present invention, the horn-shaped cover body includes an upper cover body, a lower cover body and a connecting piece, wherein the upper cover body and the lower cover body are connected by the connecting piece and form a flow passage, the flared ends of the upper cover body and the lower cover body face to the lower part, and the necking end of the upper cover body is connected with the lower port of the central tube.
As a specific embodiment of the invention, the loading volume of the denitrification carrier is 20% -80% of the volume of the carrier zone.
As a specific embodiment of the present invention, the average particle diameter of the denitrification carrier is 1mm to 6mm, preferably 2mm to 2.5mm.
As the inventionIn the specific embodiment, the specific surface area is 1m 2 /g～100m 2 /g, preferably 10m 2 /g～60m 2 /g。
As a specific embodiment of the present invention, the apparent density was 0.2g/cm 3 ～0.8g/cm 3 Preferably 0.45g/cm 3 ～0.75g/cm 3 。
In a specific embodiment of the present invention, the closed cell ratio is 1% to 99%, preferably 25% to 60%.
As a specific embodiment of the present invention, the preparation method of the denitrification carrier comprises the following steps:
s101: under the inert gas atmosphere, dissolving a polymerization monomer and an initiator in an organic medium to form a homogeneous solution for polymerization reaction, and separating to obtain a ternary polymerization microsphere filler; wherein the polymeric monomer comprises maleic anhydride, styrene and alpha-methylstyrene, and the initiator is selected from organic peroxy compounds and/or azo compounds;
s102: mixing the filler prepared in the step S101 with an antioxidant and thermoplastic resin, and extruding and granulating;
s103: and (3) impregnating the particles obtained in the step (S102) with supercritical fluid, then releasing pressure, cooling the particles, and regulating and controlling pore channels to obtain the denitrification carrier. Specifically, particles are treated by supercritical fluid, and supercritical gas treatment equipment firstly heats a treatment furnace chamber to a foaming temperature through a temperature control system; then placing the tissue particles into a treatment furnace chamber, pressurizing by a hydraulic system, and introducing supercritical fluid into the furnace chamber by a high-pressure gas conveying system to enable the gas pressure to reach the working pressure; the supercritical fluid diffuses from the material surface into the composition particles and impregnates for a period of time; after reaching dissolution balance, pressure is released once or in a sectional way, and the gas in the furnace chamber is discharged and recovered through a gas recovery system.
The denitrification carrier is prepared by mixing one or more thermoplastic resins as basic resins, antioxidants and fillers according to a certain proportion, granulating and then carrying out supercritical gas treatment. The denitrification carrier has the advantages that the pore wall is rough, the pore structure is controllable, the denitrification carrier can be effectively attached to denitrification functional bacteria, and the reactor is started quickly; the carrier is easy to expand and fluidize, periodic backwashing is not needed, the self-balancing of the biological film can be realized, and the operation is stable.
As a specific embodiment of the present invention, the mass percentage of the polymerized monomer is 4% to 22%, preferably 6% to 19%, based on the mass of the homogeneous solution; the mass percentage of the initiator is 0.4-4%, preferably 0.3-3.6%, more preferably 1-3%.
In a specific embodiment of the present invention, the average particle diameter of the ternary polymerization microsphere is 500nm to 1600nm, preferably 800nm to 1500nm.
As a specific embodiment of the invention, the mole percent of maleic anhydride is 48-51%, the mole percent of styrene is 10-45%, the mole percent of alpha-methyl styrene is 10-45%, and the mole ratio of styrene to alpha-methyl styrene is 9:1-1:9.
In the step S102, the antioxidant is 0.05 to 1 part and the filler is 0.5 to 30 parts based on 100 parts by weight of the thermoplastic resin; preferably, the antioxidant is 0.1 to 0.5 part and the filler is 5 to 15 parts.
In step S102, the granulation may be performed by a twin-screw extruder, or may be performed by injection molding, compression molding, blow molding, die casting, hollow molding, vacuum molding, or other processing methods to obtain molded articles such as sheets, blocks, rods, and hollow tubes.
As a specific embodiment of the present invention, after the step S102, the method further includes the following steps: after extrusion granulation, mixing the obtained granules, molding the mixture by a molding machine, and granulating the mixture by a granulator; wherein the extrusion temperature is in the range of 170 ℃ to 230 ℃, preferably 180 ℃ to 200 ℃, such as 180 ℃,190 ℃,200 ℃, and any combination thereof.
As a specific embodiment of the present invention, the dicing speed is in the range of 100rpm to 500rpm, preferably 200rpm to 300rpm, for example 200rpm,250rpm,300rpm, and any combination thereof.
As a specific embodiment of the present invention, in the step S103, the supercritical fluid impregnation temperature is in a range of 130 to 180 ℃, preferably 140 to 165 ℃, such as 140 ℃,145 ℃,150 ℃,155 ℃,160 ℃,165 ℃, and any combination thereof.
As a specific embodiment of the present invention, the supercritical fluid impregnation pressure is in the range of 1.0MPa to 25.0MPa, preferably 7.3MPa to 15.0MPa, for example, 7.3MPa,8.5MPa,10.0MPa,12.0MPa,15.0MPa, and any combination thereof.
As a specific embodiment of the present invention, the supercritical fluid is immersed for a time ranging from 1min to 1h, preferably from 10min to 30min, for example, 10min,20min,30min, and any combination thereof.
As a specific embodiment of the invention, one pressure relief is adopted during pressure relief, and the pressure relief speed is 0.1 MPa/min-30 MPa/min, preferably 1 MPa/min-10 MPa/min.
As a specific embodiment of the invention, multiple segmented pressure relief is adopted during pressure relief, and the pressure relief speed of each segment is 1 MPa/min-30 MPa/min, preferably 3 MPa/min-15 MPa/min.
As a specific embodiment of the present invention, in the step S101, the antioxidant adopts a mass ratio of 1: (0.8 to 1.2) a hindered phenol antioxidant and a phosphite antioxidant.
Preferably, the hindered phenolic antioxidant is selected from at least one of antioxidant 1010, antioxidant 1076, antioxidant 245 or antioxidant 246.
As a specific embodiment of the present invention, the phosphite antioxidant is selected from at least one of triphenyl phosphate, trimethyl phosphate, or antioxidant 168; and/or the number of the groups of groups,
the thermoplastic resin is at least one selected from the group consisting of polyethylene resin, polypropylene resin, polyethylene compound resin, polystyrene resin, styrene-butadiene rubber resin, ABS resin and polyamide resin.
Preferably, the thermoplastic resin is at least selected from one polyolefin resin.
More preferably, the thermoplastic resin is at least one selected from polypropylene, polyethylene, polybutylene, and polypentene.
As a specific embodiment of the present invention, the organic medium is an organic acid alkyl ester. The general formula of the organic acid alkyl ester is R 1 COOR 2 Wherein R is 1 Selected from H, C 1-4 At least one of alkyl, phenyl and benzyl, R 2 Is C 1-10 Is a hydrocarbon group. Preferably, R 1 Is C 1-4 R is alkyl and/or phenyl 2 Is C 1-7 Is a hydrocarbon group.
As a specific embodiment of the present invention, the inert atmosphere may be provided by inert gases conventional in the art, such as nitrogen.
In a specific embodiment of the present invention, the polymerization temperature is 60℃to 95℃and preferably 65℃to 76 ℃.
In a specific embodiment of the present invention, the polymerization time is 2 to 24 hours, preferably 4 to 8 hours.
In a second aspect, the present invention provides a sewage treatment method, comprising the steps of: and introducing sewage to be treated into the device, and sequentially passing through a homogenizing tank, a middle tank and an anaerobic reactor.
As a specific embodiment of the invention, the total nitrogen concentration of the inlet water of the sewage to be treated is 10 mg/L-3000 mg/L. In the present invention, the total nitrogen concentration means nitrate nitrogen, i.e., nitrate nitrogen, NO 3 -N。
As a specific embodiment of the invention, the ascending flow rate of the material in the carrier zone is 10m/h to 100m/h, preferably 20m/h to 70m/h.
As a specific embodiment of the invention, the hydraulic retention time in the upflow expanded bed reactor is 1 to 48 hours, preferably 5 to 20 hours. In the present invention, the hydraulic retention time in the upflow expanded bed reactor refers to the retention time of wastewater in the reactor, which is a conventional parameter in the art.
As a specific embodiment of the invention, the upflow expanded bed reactor processes a total nitrogen load of 0.5kg/m 3 ·d～10kg/m 3 D, preferably 1kg/m 3 ·d～5kg/m 3 ·d。
In a specific embodiment of the present invention, the carrier in the carrier region has an expansion ratio of 1% to 100%, preferably 10% to 50%.
As shown in FIG. 1, the autotrophic nitrogen removal process of the present invention comprises the following steps:
step one, a homogenizing tank 1 is connected with a feed pump 2, the effluent of the feed pump 2 enters a mixer 14 of a middle tank through a feed inlet 15, is mixed with circulating water and then enters a circulating pump 18 through a middle tank outlet 17, and the effluent of the circulating pump 18 enters an anaerobic reactor through a bottom inlet 3 and enters a carrier zone 6 after being distributed by a distribution plate 19.
And secondly, carrying the carrier into the deflector 5 by upward water flow, wherein carrier particles in the reactor are in a fluidized state along with the water flow under the pushing of the circulating water flow, and performing anaerobic biological reaction.
And thirdly, circulating water flows into the water outlet area 7 after passing through the carrier area 6, carriers leave from the upper part of the diversion channel and are intercepted by the three-phase separator, fine carrier particles carried by the circulating water flow are settled back into the carrier area 6 after the flow speed of the water flow is reduced, and the fine carriers are prevented from being carried out of the fluidized bed by the water flow.
And step four, water flow enters the inlet 13 of the intermediate tank through the water outlet 10 after reaching the water outlet area, is effectively mixed with the inlet water in the mixer 14, and the residual outlet water is discharged out of the system from the outer water discharge outlet 16 through the overflow of the liquid level height difference.
The autotrophic nitrogen removal process device has the following beneficial effects:
(1) The autotrophic denitrification reactor does not need an external organic carbon source, and has low economic cost;
(2) The pore wall of the denitrification carrier is rough, functional denitrification bacteria are easy to attach, the reactor is started quickly, and the biological membrane in the carrier area is high;
(3) The denitrification carrier is easy to fluidize, the solid-liquid two-phase flow state is beneficial to the contact and mass transfer of microorganisms and sewage, and the denitrification efficiency is high;
(4) The denitrification carrier has controllable density range and large specific surface area, controllable pore canal structure, high mechanical strength and long service life;
(5) The autotrophic denitrification reactor adopts an anti-blocking filter head to distribute water, so that the uniformity of water distribution is improved, and the effective utilization rate of a carrier layer is increased;
(6) In the running of the autotrophic denitrification reactor, the denitrification carrier biomembrane quantity can realize self-balancing, a sludge sedimentation tank is not required to be arranged independently, the occupied area of the device is small, and the denitrification load is high.
Drawings
The invention will be described in further detail with reference to the accompanying drawings.
FIG. 1 is a schematic view of the process flow of the autotrophic nitrogen removal process device of the present invention
Reference numerals illustrate:
1. the device comprises a homogenizing tank, 2, a feed pump, 3, a reactor water inlet, 4, an anaerobic reactor, 5, a deflector, 6, a carrier zone, 7, a water outlet zone, 8, a water collecting tank, 9, a water outlet weir, 10, a reactor water outlet, 11, a three-phase separator, 12, a middle tank, 13, a middle tank inlet, 14, a mixer, 15, a feed inlet, 16, an outer drainage outlet, 17, a middle tank outlet, 18, a circulating pump, 19 and a water distribution zone.
Detailed Description
In order that the invention may be more readily understood, the invention will be described in detail below with reference to the following examples and the accompanying drawings, which are given by way of illustration only and are not limiting the scope of application of the invention.
As shown in FIG. 1, the autotrophic nitrogen removal process of the present invention comprises the following steps:
the homogenizing tank 1 is connected with the feed pump 2, the effluent of the feed pump 2 enters the mixer 14 of the intermediate tank through the feed inlet 15, and enters the circulating pump 18 through the intermediate tank outlet 17 after being mixed with circulating water, and the effluent of the circulating pump 18 enters the anaerobic reactor through the bottom inlet 3 and enters the carrier zone 6 after being distributed by the distribution plate 19. The upward water flow carries the carrier into the deflector 5, carrier particles in the reactor are in a fluidized state along with the water flow under the pushing of the circulating water flow, anaerobic biological reaction is carried out, and as the circulating water flow contains the biochemically degradable matrix, microbial films can grow on the fine particle carrier in the carrier area, denitrification reaction is carried out, and organic matters and total nitrogen are removed. The circulating water flow enters the water outlet area 7 after passing through the carrier area 6, the carrier leaves from the upper part of the diversion channel and is intercepted by the three-phase separator, and fine carrier particles carried by the circulating water flow are settled back to the carrier area 6 after the flow speed of the water flow is reduced, so that the fine carrier is prevented from being carried out of the fluidized bed by the water flow. After reaching the water outlet area, the water flow enters the inlet 13 of the intermediate tank through the water outlet 10 and is effectively mixed with the water inlet in the mixer 14, and the residual water is discharged out of the system through the outer water discharge outlet 16 by overflow of the liquid level height difference.
The test methods or criteria used in the following examples are as follows:
(1) Density tester: CPA225D, density accessory YDK01, sartorius company, germany. The testing method comprises the following steps: the apparent density of the thermoplastic resin cellular foam was obtained by a drainage method according to the GB/T6343-2009 standard test using the density attachment of a Satorius balance.
(2) Scanning electron microscope: XL-30, FEI company, USA. The testing method comprises the following steps: quenching the foaming material by liquid nitrogen, spraying metal on the section, and observing the cell structure inside the foaming material by adopting a Scanning Electron Microscope (SEM).
(3) Open-close aperture ratio tester: ULTRAFOAM 1200e, quantachrome instruments, inc., U.S.A.. The testing method comprises the following steps: according to GB/T10799-2008.
(4) Specific surface area tester: ASAP2020Plus specific surface area tester, michael Ratike instruments, inc., USA. The testing method comprises the following steps: according to GB/T19587-2017.
(5) COD concentration test: COD tester, DR-890, from Hash company of America. The testing method comprises the following steps: according to HJ 828-2017.
(6)NO 3 -N concentration test: ion chromatograph, ICS 5000, available from Dynam, USA. The testing method comprises the following steps: according to HJ 84-2016.
(7) Carrier layer expansion ratio: the rest height of the carrier layer is H 0 The carrier layer has a height H after expansion 1 The carrier layer expansion ratio was (H 1 -H 0 )/H 0 。
(8) Carrier layer up flow rate: the flow rate of rising water flow in the reactor, the flow rate of the reactor is Q, and the diameter of the reactorThe carrier layer rising flow rate is Q/(pi.d) 2 /4)。
The sources of materials in the following examples are as follows:
ternary copolymer microspheres SYXQ101, 102, 103, 104, 105: the ternary polymerization microsphere is a self-made ternary polymerization microsphere, and the preparation method comprises the following steps: in inert atmosphere, maleic anhydride, alpha-methyl styrene, styrene and an initiator are dissolved in an organic medium to form a homogeneous solution, and after the homogeneous solution is polymerized to obtain copolymer emulsion suspension, the terpolymer microsphere is obtained by centrifugal separation. The dosage of maleic anhydride and the molar ratio of styrene to alpha-methyl styrene are regulated and controlled, the self-stable dispersion of a polymerization system is realized, the prepared polymer is microsphere with excellent uniformity, no additives such as a stabilizer, a precipitant and the like are required to be added in the polymerization process, and the obtained copolymer microsphere has the characteristics of clean surface, good dispersibility in a medium and no aggregation. The initiator is an organic peroxide and/or azo compound. The organic medium is selected from organic acid alkyl ester.
Other commercial products are commercially available without any particular description.
Embodiment one: taking the ammonia nitrogen concentration of certain industrial wastewater to be 400mg/L, the nitrite nitrogen concentration to be 550mg/L and the total nitrogen treatment load to be 3.1kg/m 3 D, the reactor process parameters range as follows:
1. preparing autotrophic denitrification carrier:
(1) The preparation parameters of the ternary polymerization microsphere are shown in the following table 1-1:
TABLE 1-1 preparation parameters of ternary copolymer microspheres
(2) Mixing HDPE YGH041 with ternary polymerization microsphere, antioxidant 1010 and antioxidant 168 according to the weight ratio of 100:10:0.2:0.1, adding into a feeder of a double-screw extruder, keeping the screw temperature between 180 ℃ and 210 ℃ in the processing process, melting and mixing uniformly by the screw, drawing and extruding, granulating at the granulating speed of 250rpm, and drying at 80 ℃ to obtain material particles with rough surfaces and smooth sections.
(3) Heating the supercritical fluid treatment device to 145 ℃, putting the material particles prepared in the step (2) into the supercritical fluid treatment device, and sealing a furnace chamber. Introducing 10MPa nitrogen into the furnace chamber, and allowing supercritical carbon dioxide to diffuse into the matrix at 145 ℃ and 10 MPa. After saturation for 20min, the diffusion balance is achieved, the pressure in the furnace chamber is reduced to 4MPa in 2 min through a pressure relief valve, then the furnace chamber is opened for pressure relief foaming, cooling and shaping, and the autotrophic nitrogen removal carrier is obtained.
(4) Autotrophic nitrogen removal supports are shown in tables 1-2:
TABLE 1-2 autotrophic denitrification Carrier parameters
| Length/particle size mm | Apparent density g/cm 3 | Closed porosity% | Specific surface area m 2 /g | |
| Example 1 | 4.3/2.5 | 0.60 | 34.7 | 32.68 |
2. Autotrophic denitrification reaction:
the autotrophic denitrification treatment parameters are shown in tables 1-3:
TABLE 1-3 autotrophic denitrification treatment parameters
| Carrier filling rate | Rising flow rate | Hydraulic retention time | |
| Example 1 | 61％ | 30m/h | 12h |
After treatment, ammonia nitrogen in the effluent can be reduced from 400mg/L to below 10mg/L, nitrite nitrogen can be reduced from 550mg/L to below 15mg/L, and the total nitrogen removal rate reaches 97%.
Embodiment two: taking the ammonia nitrogen concentration of certain industrial wastewater to be 500mg/L, the nitrite nitrogen concentration to be 660mg/L and the total nitrogen treatment load to be 4.0kg/m 3 D, total nitrogen treatment load of 2.1kg/m 3 D. The reactor process parameters range as follows:
1. preparing autotrophic denitrification carrier:
(1) The preparation parameters of the ternary polymerization microsphere are shown in Table 2-1:
TABLE 2-1 preparation parameters of ternary copolymer microspheres
(2) Mixing the homo-polypropylene T30s with the ternary polymerization microsphere, the antioxidant 1010 and the antioxidant 168 according to the weight ratio of 100:15:0.2:0.1, adding the mixture into a feeder of a double-screw extruder, keeping the temperature of a screw between 160 ℃ and 200 ℃ in the processing process, melting and mixing the mixture uniformly by the screw, extruding the mixture by a draw bar, granulating the mixture at a granulating speed of 300rpm, and drying the mixture at 80 ℃ to obtain material particles with rough surfaces and smooth sections.
(3) Heating the supercritical fluid treatment device to 160 ℃, putting the material particles prepared in the step (2) into the supercritical fluid treatment device, and sealing a furnace chamber. Introducing 15MPa nitrogen into the furnace chamber, and allowing supercritical nitrogen to diffuse into the substrate at 160 ℃ and 15 MPa. After 15min of saturation, the diffusion balance is achieved, the pressure in the furnace chamber is reduced to 7MPa in 1min through a pressure relief valve, the pressure is maintained for 10min and then reduced to 3MPa in 4 min, and then the furnace chamber is opened for pressure relief foaming, cooling and shaping, so that the denitrification carrier is obtained.
(4) Autotrophic nitrogen removal supports are shown in tables 2-2:
TABLE 2-2 autotrophic denitrification Carrier parameters
| Length/particle size mm | Apparent density g/cm 3 | Closed porosity% | Specific surface area m 2 /g | |
| Example two | 3.9/2.1 | 0.74 | 46.3 | 27.27 |
2. Autotrophic denitrification reaction:
the autotrophic denitrification treatment parameters are shown in tables 2-3:
TABLE 2-3 autotrophic denitrification treatment parameters
| Carrier filling rate | Rising flow rate | Hydraulic retention time | |
| Example two | 60％ | 25m/h | 3h |
The ammonia nitrogen in the treated effluent can be reduced from 500mg/L to below 18mg/L, the nitrite nitrogen can be reduced from 660mg/L to below 25mg/L, and the total nitrogen removal rate reaches 96%.
Embodiment III: taking ammonia nitrogen concentration of certain industrial wastewater as 300mg/L and NO 3 The N concentration was 420mg/L and the total nitrogen treatment load was 3.8kg/m 3 D, the reactor process parameters range as follows:
1. preparing autotrophic denitrification carrier:
(1) The preparation parameters of the ternary polymerization microsphere are shown in Table 3-1:
TABLE 3-1 preparation parameters of ternary copolymer microspheres
(2) Mixing LDPE LD100AC with ternary polymerization microsphere, antioxidant 1010 and antioxidant 168 according to the weight ratio of 100:5:0.2:0.1, adding into a feeder of a double-screw extruder, maintaining the temperature of a screw at 160-200 ℃ in the processing process, melting and mixing uniformly by the screw, drawing and extruding, granulating at a granulating speed of 210rpm, and drying at 80 ℃ to obtain material granules with rough surfaces and smooth sections.
(3) Heating the supercritical fluid treatment device to 140 ℃, putting the material particles prepared in the step (2) into the supercritical fluid treatment device, and sealing a furnace chamber. Introducing 7.5MPa of carbon dioxide into the furnace chamber, so that the supercritical carbon dioxide is diffused into the matrix under the conditions of 140 ℃ and 7.5 MPa. And after saturation for 25min, reaching diffusion balance, opening a furnace chamber to release pressure for foaming, and cooling and shaping to obtain the denitrification carrier.
(4) Autotrophic nitrogen removal supports are shown in Table 3-2:
TABLE 3-2 autotrophic denitrification Carrier parameters
| Length/particle size mm | Apparent density g/cm 3 | Closed porosity% | Specific surface area m 2 /g | |
| Example III | 4.6/2.6 | 0.50 | 25.6 | 23.19 |
2. Autotrophic denitrification reaction:
the autotrophic denitrification treatment parameters are shown in tables 3-3:
TABLE 3-3 autotrophic denitrification treatment parameters
| Carrier filling rate | Rising flow rate | Hydraulic retention time | |
| Example III | 65％ | 40m/h | 5h |
After treatment, ammonia nitrogen in the effluent can be reduced from 300mg/L to below 10mg/L, nitrite nitrogen can be reduced from 420mg/L to below 12mg/L, and the total nitrogen removal rate reaches 97%.
Embodiment four: taking industrial wastewater with nitrate nitrogen concentration of 200mg/L, S/N ratio of 2 and total nitrogen treatment load of 1.5kg/m 3 D, the reactor regulation process parameters range is as follows:
1. preparing autotrophic denitrification carrier:
(1) The preparation parameters of the ternary polymerization microsphere are shown in Table 4-1:
TABLE 4-1 preparation parameters of ternary polymerization microspheres
(2) Mixing high melt strength polypropylene HMS20Z with filler SYXQ104, antioxidant 1010 and antioxidant 168 according to the weight ratio of 100:8:0.2:0.1, adding into a feeder of a double-screw extruder, keeping the temperature of a screw between 160 ℃ and 200 ℃ in the processing process, melting and mixing uniformly by the screw, drawing and extruding, granulating at a granulating speed of 275rpm, and drying at 80 ℃ to obtain material particles with rough surfaces and smooth sections.
(3) Heating the supercritical fluid treatment device to 163 ℃, putting the material particles prepared in the step (2) into the supercritical fluid treatment device, and sealing a furnace chamber. Introducing 15MPa nitrogen into the furnace chamber, and allowing supercritical nitrogen to diffuse into the substrate at 163 ℃ under 15 MPa. After 15min of saturation, the diffusion balance is achieved, the pressure in the furnace chamber is reduced to 6MPa in 3 min through a pressure relief valve, then the furnace chamber is opened for pressure relief foaming, cooling and shaping, and the autotrophic nitrogen removal carrier is obtained.
(4) Autotrophic nitrogen removal supports are shown in Table 4-2:
TABLE 4-2 autotrophic denitrification Carrier parameters
| Length/particle size mm | Apparent density g/cm 3 | Closed porosity% | Specific surface area m 2 /g | |
| Example IV | 4.0/2.1 | 0.69 | 52.0 | 19.35 |
2. Autotrophic denitrification reaction:
the autotrophic denitrification treatment parameters are shown in tables 4-3:
TABLE 4-3 autotrophic denitrification treatment parameters
| Carrier filling rate | Rising flow rate | Hydraulic retention time | |
| Example IV | 70％ | 45m/h | 10h |
The total nitrogen in the treated effluent can be reduced from 200mg/L to below 15mg/L, and the total nitrogen removal rate reaches 93 percent.
Fifth embodiment: taking industrial wastewater with the nitrate nitrogen concentration of 300mg/L, the S/N ratio of 2 and the total nitrogen treatment load of 2.5kg/m 3 D, the reactor regulation process parameters range is as follows:
1. preparing autotrophic denitrification carrier:
(1) The preparation parameters of the ternary polymerization microsphere are shown in Table 5-1:
TABLE 5-1 preparation parameters of ternary polymerization microspheres
(2) LD100AC, EVA V4110J, HMS Z, a filler SYXQ105, an antioxidant 1010 and an antioxidant 168 are mixed according to the weight ratio of 20:10:70:25:0.2:0.1 and then added into a feeder of a double-screw extruder, the temperature of a screw is kept between 160 ℃ and 200 ℃ in the processing process, the mixture is melted and mixed uniformly by the screw, the drawing bar is extruded, the mixture is granulated at a granulating speed of 275rpm, and the mixture is dried at 80 ℃ to obtain material particles with rough surfaces and smooth cut surfaces.
(3) Heating the supercritical fluid treatment device to 158 ℃, putting the material particles prepared in the step (2) into the supercritical fluid treatment device, and sealing a furnace chamber. Introducing 8MPa of carbon dioxide into the furnace chamber, and then introducing nitrogen to enable the pressure to reach 18MPa. The supercritical mixed gas is diffused into the matrix at 158 ℃ and 18MPa. After saturation for 30min, the diffusion balance is achieved, the pressure in the furnace chamber is reduced to 4MPa in 2.5 min through a pressure relief valve, then the furnace chamber is opened for pressure relief foaming, cooling and shaping are carried out, and the autotrophic nitrogen removal carrier is obtained.
(4) Autotrophic nitrogen removal supports are shown in Table 5-2:
TABLE 5-2 autotrophic denitrification Carrier parameters
| Length/particle size mm | Apparent density g/cm 3 | Closed pore rate％ | Specific surface area m 2 /g | |
| Example five | 4.4/2.3 | 0.55 | 30.1 | 48.09 |
2. Autotrophic denitrification reaction:
the autotrophic denitrification treatment parameters are shown in tables 5-3:
TABLE 5-3 autotrophic denitrification treatment parameters
| Carrier filling rate | Rising flow rate | Hydraulic retention time | |
| Example five | 80％ | 49m/h | 15h |
The total nitrogen in the treated effluent can be reduced from 300mg/L to below 20mg/L, and the total nitrogen removal rate reaches 93%.
Example six: taking the total ammonia nitrogen concentration of 400mg/L and the nitrite nitrogen concentration of 550mg/L of certain industrial wastewaterThe nitrogen treatment load was 1.6kg/m 3 D. The same apparatus and process flow as in example one were used to treat it, but the carrier preparation step three was used to prepare a carrier using a chemically foamed extrusion molded body. Mixing the material particles prepared in the second step of carrier preparation and 4 parts of AC foaming agent, adding into a single screw extruder, extruding into strip-shaped foam bodies from a front end nozzle of the extruder, and cutting the foam bodies to obtain carrier with an average particle diameter of 2.3mm and a specific surface area of 0.75m 2 Per g, apparent density of 0.88g/cm 3 The closed porosity was 69.6%. The total nitrogen removal after anaerobic reactor treatment was 50%.
Embodiment seven: taking the ammonia nitrogen concentration of certain industrial wastewater to be 400mg/L, the nitrite nitrogen concentration to be 550mg/L and the total nitrogen treatment load to be 1.9kg/m 3 D. The same apparatus and process flow as in example one were used to treat it, but the carrier preparation step three was used to prepare a carrier using a chemically foamed extrusion molded body. This was treated by the same apparatus and process flow as in example 1, but the carrier preparation step three was carried out by using a chemically foamed extrusion molded body. Mixing the material particles prepared in the second step of carrier preparation and 6 parts of AC foaming agent, adding into a single screw extruder, extruding into strip-shaped foam bodies from a front end nozzle of the extruder, and cutting the foam bodies to obtain carrier with an average particle size of 2.3mm and a specific surface area of 5.11m 2 Per g, apparent density of 0.68g/cm 3 The closed porosity was 27.7%. The total nitrogen removal rate after treatment by the anaerobic reactor was 60%.
Example eight: taking the ammonia nitrogen concentration of certain industrial wastewater to be 400mg/L, the nitrite nitrogen concentration to be 550mg/L and the total nitrogen treatment load to be 2.6kg/m 3 D. The same apparatus and process flow as in example one were used to treat it, but the carrier preparation step three was used to prepare a carrier using a chemically foamed extrusion molded body. This was treated by the same apparatus and process flow as in example 1, but the carrier preparation step three was carried out by using a chemically foamed extrusion molded body. Mixing the material particles prepared in the second step of carrier preparation and 8 parts of AC foaming agent, adding into a single screw extruder, extruding into strip-shaped foam bodies from a front end nozzle of the extruder, and cutting the foam bodies to obtain carrier with an average particle size of 2.9mm and a specific surface area of 8.86m 2 Per gram, apparent density of 0.43g/cm 3 The closed porosity was 15.1%. NO after anoxic expanded bed treatment 3 The N removal rate was 83%.
Example nine: taking the ammonia nitrogen concentration of certain industrial wastewater to be 400mg/L, the nitrite nitrogen concentration to be 550mg/L and the total nitrogen treatment load to be 2.2kg/m 3 D. The same apparatus and process flow as in example one were used to treat it, but the carrier preparation step three was used to prepare a carrier using a chemically foamed extrusion molded body. The same apparatus and process flow as in example one were used to treat it, but the carrier preparation step one did not add filler, and the carrier obtained had an average particle diameter of 2.5mm and a specific surface area of 6.40m 2 Per g, apparent density of 0.58g/cm 3 The closed porosity was 38.2%. The total nitrogen removal rate after treatment by the anaerobic reactor was 70%.
Example ten: taking the ammonia nitrogen concentration of certain industrial wastewater to be 400mg/L, the nitrite nitrogen concentration to be 550mg/L and the total nitrogen treatment load to be 2.7kg/m 3 D. The same apparatus and process flow as in example one were used to treat it, but the carrier preparation step three was used to prepare a carrier using a chemically foamed extrusion molded body. The same equipment and process flow as in example one were used to treat it, but the filler in the carrier preparation step was changed to talc powder, which was produced by DalianFuji mineral company and had a particle size distribution of 2-5. Mu.m, and the obtained carrier had an average particle size of 2.5mm and a specific surface area of 9.63m 2 Per gram, apparent density of 0.65g/cm 3 The closed porosity was 41.5%. The total nitrogen removal rate after anaerobic reactor treatment was 85%.
It should be noted that the above-described embodiments are only for explaining the present invention and do not constitute any limitation of the present invention. The invention has been described with reference to exemplary embodiments, but it is understood that the words which have been used are words of description and illustration, rather than words of limitation. Modifications may be made to the invention as defined in the appended claims, and the invention may be modified without departing from the scope and spirit of the invention. Although the invention is described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, as the invention extends to all other means and applications which perform the same function.
Claims (30)
1. An autotrophic nitrogen removal process device, characterized in that the autotrophic nitrogen removal process device comprises: the device comprises a homogenizing tank, a middle tank and an anaerobic reactor, wherein the homogenizing tank is communicated with the middle tank, and the middle tank is communicated with the anaerobic reactor;
the anaerobic reactor is sequentially divided into a water distribution area, a carrier area, a three-phase separation area and a water outlet area from bottom to top; wherein, the water distribution area is provided with a water distribution plate, and the water distribution plate is provided with a filter head; a denitrification carrier is filled in the carrier zone; a central tube and a horn-shaped cover body are arranged in the three-phase separation area; a water collecting tank and a water outlet weir are arranged at the top of the water outlet area;
the average grain diameter of the denitrification carrier is 1 mm-6 mm, and the specific surface area is 10m 2 /g～60m 2 /g; apparent density of 0.2g/cm 3 ～0.8g/cm 3 The method comprises the steps of carrying out a first treatment on the surface of the The closing rate is 1-99%;
the preparation method of the denitrification carrier comprises the following steps:
s101: under the inert gas atmosphere, dissolving a polymerization monomer and an initiator in an organic medium to form a homogeneous solution for polymerization reaction, and separating to obtain a ternary polymerization microsphere filler; wherein the polymeric monomer comprises maleic anhydride, styrene and alpha-methylstyrene, and the initiator is selected from organic peroxy compounds and/or azo compounds;
s102: mixing the filler prepared in the step S101 with an antioxidant and thermoplastic resin, and extruding and granulating;
s103: impregnating the particles obtained in the step S102 with supercritical fluid, then releasing pressure, cooling the particles, and performing pore canal regulation and control to obtain a denitrification carrier;
the organic medium is organic acid alkyl ester;
the average particle diameter of the ternary polymerization microsphere is 500 nm-1600 nm;
the molar ratio of the styrene to the alpha-methyl styrene is 9:1-1:9.
2. The autotrophic nitrogen removal process device according to claim 1, wherein the anaerobic reactor has an aspect ratio of (1 to 8): 1, a step of; and/or the number of the groups of groups,
the horn-shaped cover body comprises an upper cover body, a lower cover body and a connecting piece, wherein the upper cover body is connected with the lower cover body through the connecting piece and forms a flow passage, the flaring ends of the upper cover body and the lower cover body face to the lower part, and the necking end of the upper cover body is connected with the lower port of the central tube; and/or the number of the groups of groups,
the loading volume of the denitrification carrier is 20% -80% of the volume of the carrier area.
3. The autotrophic nitrogen removal process device according to claim 2, wherein the anaerobic reactor has an aspect ratio of (2 to 4): 1.
4. the autotrophic nitrogen-removal process device according to claim 3, wherein the average particle diameter of the nitrogen-removal carrier is 2mm to 2.5mm; and/or an apparent density of 0.45g/cm 3 ～0.75g/cm 3 The method comprises the steps of carrying out a first treatment on the surface of the And/or the closed porosity is 25% -60%.
5. The autotrophic nitrogen-removal process device according to claim 4, wherein in the step S101, the mass percentage of the polymerized monomer is 4% to 22% based on the mass of the homogeneous solution; the mass percentage of the initiator is 0.4% -4%; and/or the mole percent of maleic anhydride is 48-51%, the mole percent of styrene is 10-45%, and the mole percent of alpha-methyl styrene is 10-45%.
6. The autotrophic nitrogen-removal process device according to claim 5, wherein in the step S101, the mass percentage of the polymerized monomer is 6% to 19% based on the mass of the homogeneous solution; the mass percentage of the initiator is 0.3-3.6%; the average particle diameter of the ternary polymerization microsphere is 800 nm-1500 nm.
7. The autotrophic nitrogen-removal process device according to claim 6, wherein in the step S101, the mass percentage of the initiator is 1% -3% based on the mass of the homogeneous solution.
8. The autotrophic nitrogen-removing process device according to claim 7, wherein in said step S102, the antioxidant is 0.05 to 1 part and the filler is 0.5 to 30 parts based on 100 parts by weight of the thermoplastic resin; and/or the number of the groups of groups,
the step S102 further includes the following steps: after extrusion granulation, mixing the obtained granules, molding the mixture by a molding machine, and granulating the mixture by a granulator; wherein the extrusion temperature is 170-230 ℃; and/or the dicing speed is 100rpm to 500rpm.
9. The autotrophic nitrogen-removing process device according to claim 8, wherein in the step S102, the antioxidant is 0.1 to 0.5 parts and the filler is 5 to 15 parts based on 100 parts by weight of the thermoplastic resin.
10. The autotrophic nitrogen removal process device of claim 9, further comprising the following steps after said step S102: after extrusion granulation, mixing the obtained granules, molding the mixture by a molding machine, and granulating the mixture by a granulator; wherein the extrusion temperature is 180-200 ℃.
11. The autotrophic nitrogen removal process device of claim 10, further comprising the following steps after said step S102: after extrusion granulation, mixing the obtained granules, molding the mixture by a molding machine, and granulating the mixture by a granulator; wherein, the dicing speed is 200 rpm-300 rpm.
12. The autotrophic anammox process device of claim 11, wherein in said step S103, the supercritical fluid impregnation temperature is 130 ℃ to 180 ℃; and/or the supercritical fluid impregnation pressure is 1.0 MPa-25.0 MPa; and/or the time of the supercritical fluid impregnation is 1 min-1 h; and/or, when the pressure is released, one-time pressure release is adopted, and the pressure release speed is 0.1 MPa/min-30 MPa/min; and/or, during pressure relief, multiple segmented pressure relief is adopted, and the pressure relief speed of each segment is 1 MPa/min-30 MPa/min.
13. The autotrophic anammox process apparatus of claim 12, wherein in said step S103, the supercritical fluid impregnation temperature is 140 ℃ to 165 ℃.
14. The autotrophic nitrogen removal process device of claim 13, wherein the supercritical fluid impregnation pressure is 7.3MPa to 15.0MPa.
15. The autotrophic nitrogen removal process device of claim 14, wherein the supercritical fluid is immersed for a period of time ranging from 10 minutes to 30 minutes.
16. The autotrophic nitrogen removal process device of claim 15, wherein the pressure relief is performed once, and the pressure relief speed is 1MPa/min to 10MPa/min.
17. The autotrophic nitrogen removal process device of claim 16, wherein the pressure relief is performed in multiple steps, and the pressure relief speed of each step is 3 MPa/min-15 MPa/min.
18. The autotrophic nitrogen removal process device of claim 17, wherein in the step S101, the antioxidant is used in a mass ratio of 1: (0.8 to 1.2) a hindered phenol antioxidant and a phosphite antioxidant; and/or the phosphite antioxidant is selected from at least one of triphenyl phosphate, trimethyl phosphate or antioxidant 168; and/or the number of the groups of groups,
the thermoplastic resin is at least one selected from the group consisting of polyethylene resin, polypropylene resin, polyethylene compound resin, polystyrene resin, styrene-butadiene rubber resin, ABS resin and polyamide resin.
19. The autotrophic anammox process device of claim 18, wherein the hindered phenolic antioxidant is selected from at least one of antioxidant 1010, antioxidant 1076, antioxidant 245, or antioxidant 246.
20. The autotrophic nitrogen-removing process device of claim 17, wherein the thermoplastic resin is at least one selected from the group consisting of polypropylene, polyethylene, polybutylene, and polypentene.
21. The autotrophic nitrogen-removing process device according to claim 20, wherein,
the polymerization temperature is 60-95 ℃; and/or the number of the groups of groups,
the polymerization time is 2-24 hours.
22. The autotrophic anammox process device of claim 21, wherein the alkyl ester of an organic acid has a formula R 1 COOR 2 Wherein R is 1 Selected from H, C 1-4 At least one of alkyl, phenyl and benzyl, R 2 Is C 1-10 Is a hydrocarbon group.
23. The autotrophic anammox process device of claim 22, wherein the alkyl ester of an organic acid has a formula R 1 COOR 2 Wherein R is 1 Is C 1-4 R is alkyl and/or phenyl 2 Is C 1-7 Is a hydrocarbon group.
24. The autotrophic anammox process device of claim 23, wherein the polymerization temperature is 65 ℃ to 76 ℃.
25. The autotrophic nitrogen-removing process device of claim 24, wherein the polymerization time is 4 h-8 h.
26. The sewage treatment method is characterized by comprising the following steps of: introducing sewage to be treated into an autotrophic denitrification process device according to any one of claims 1-25, and sequentially passing through a homogenizing tank, a middle tank and an anaerobic reactor;
the total nitrogen concentration of the inlet water of the sewage to be treated is 10 mg/L-3000 mg/L; and/or the number of the groups of groups,
the ascending flow rate of the materials in the carrier area is 10 m/h-100 m/h; and/or the number of the groups of groups,
the hydraulic retention time in the anaerobic reactor is 1-48 h; and/or the number of the groups of groups,
the total nitrogen load of the anaerobic reactor treatment is 0.5kg/m 3 ·d～10kg/m 3 D; and/or the number of the groups of groups,
the expansion rate of the carrier in the carrier region is 1% -100%.
27. The wastewater treatment method according to claim 26, wherein the ascending flow rate of the material in the carrier zone is 20m/h to 70m/h.
28. The wastewater treatment method according to claim 27, wherein the hydraulic retention time in the anaerobic reactor is 5 to 20 hours.
29. The wastewater treatment process of claim 28, wherein the anaerobic reactor treatment total nitrogen load is 1kg/m 3 ·d～5kg/m 3 ·d。
30. The wastewater treatment method according to claim 29, wherein the carrier expansion ratio of the carrier region is 10% to 50%.
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