A reactor and method for simultaneously achieving denitrification and production of anammox granular sludge

Abstract

The present application belongs to the field of sewage biological treatment technology, and particularly relates to a reactor and a method for simultaneously achieving denitrification and production of anaerobic ammonia oxidation granular sludge. The reactor for simultaneously achieving denitrification and production of anaerobic ammonia oxidation granular sludge comprises a reactor shell, the inside of the reactor shell is sequentially divided into an upper light filler zone, a middle complete mixing zone and a lower granular sludge production zone from top to bottom, a stirring mechanism is arranged at the top of the reactor shell, the stirring mechanism is used for stirring the middle complete mixing zone, the bottom of the reactor shell is in a conical structure, a sludge discharge valve is arranged at the middle position of the bottom of the conical structure, a water inlet is arranged at the side of the bottom of the reactor shell, and a water outlet is arranged at the side of the top of the reactor shell. The present application realizes effective control of the biomass in the reactor by regular mechanical cyclone disturbance of the stirring mechanism and quantitative sludge discharge, avoids blockage and short flow caused by excessive growth of the granular sludge and the biofilm in the reactor, and realizes stable denitrification under a super-high load of middle nitrogen concentration.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of sewage biological treatment, and particularly relates to a reactor and a method for simultaneously achieving denitrification and production of anaerobic ammonia oxidation granular sludge. BACKGROUND

[0002] In recent years, on the basis of the concept of pursuing sustainable development in economic and environmental fields, the demand for high-quality effluent and energy-saving reconstruction in sewage treatment is increasing. There are various methods for nitrogen removal, such as full nitrification-denitrification, short nitrification, short denitrification, and anaerobic ammonia oxidation. Among them, anaerobic ammonia oxidation as an autotrophic denitrification method has attracted more and more attention in sewage treatment due to its high denitrification efficiency, no need for aeration, no need for additional carbon source, and small sludge yield. However, as a chemotrophic autotrophic bacteria, the slow growth rate and long generation cycle of anaerobic ammonia oxidation bacteria have become a major problem for large-scale application in industrial and municipal sewage treatment.

[0003] Currently, in the cultivation and production of anaerobic ammonia oxidation microorganisms, activated sludge method is often used, and the method of adding carriers to cultivate biofilm is used for enrichment and retention of bacteria. According to the movement mode of the carrier, it is generally divided into moving bed biofilm system and fixed bed biofilm system. In the moving bed system, the biofilm filler moves with the water flow and can fully contact and mass transfer with the substrate, but the slow-growing functional bacteria are difficult to colonize on the surface of the filler, and the collision and friction between the fillers will cause the biomass colonized to fall off and lose again. In the fixed bed biofilm system, the fillers can well maintain the biomass, but under high hydraulic load, the limited ecological space is continuously squeezed by the continuous growth of microorganisms, and inert substances are also easily accumulated and deposited in the reactor, causing internal blockage and short flow problems in the reactor. Even if the backwashing system is configured, it is also difficult to effectively and regularly solve the blockage problem, ultimately leading to unstable effluent quality. In the prior art, the produced anaerobic ammonia oxidation sludge granules have a large particle diameter, the mass transfer efficiency is reduced, and gas pockets are formed in the sludge, blocking the nitrogen channel and causing the granular sludge to float, resulting in unavoidable granular floating and loss. SUMMARY

[0004] In view of the above problems, the present application aims to provide a reactor and a method for simultaneously achieving denitrification and production of anaerobic ammonia oxidation granular sludge, wherein the interior of the reactor shell is sequentially divided into an upper lightweight filler zone, a middle complete mixing zone and a lower granular sludge production zone from top to bottom, the upper lightweight filler zone effectively retains biomass, the middle complete mixing zone simultaneously achieves biofilm shedding in the upper lightweight filler zone, prevents the upper lightweight filler zone from being blocked and the granular sludge material in the gas hole channel from floating, and the lower granular sludge production zone produces anaerobic ammonia oxidation granular sludge through a sludge discharge valve. Through the division of different functional zones, the reactor effectively maintains the biomass in the reactor while solving the problem of easy blockage of the fixed bed biofilter column, and achieves stable nitrogen removal in the actual operation of the anaerobic ammonia oxidation process, and can have a high nitrogen load, effectively reduce the addition of carbon source, the production of excess sludge and the emission of greenhouse gases.

[0005] The technical scheme of the present application is as follows: a reactor for simultaneously achieving denitrification and production of anaerobic ammonia oxidation granular sludge, comprising a reactor shell, wherein the interior of the reactor shell is sequentially divided into an upper lightweight filler zone, a middle complete mixing zone and a lower granular sludge production zone from top to bottom, a stirring mechanism is arranged at the top of the reactor shell, the stirring mechanism is used for stirring in the middle complete mixing zone, the bottom of the reactor shell is in a conical structure, a sludge discharge valve is arranged at the middle position of the bottom of the conical structure, a water inlet is arranged on the side of the bottom of the reactor shell, the water inlet is connected with a peristaltic pump through a pipeline, the peristaltic pump is connected with a wastewater supply end, a water outlet is arranged on the side of the top of the reactor shell, and the water outlet is connected with a wastewater outlet end through a pipeline.

[0006] The upper lightweight filler zone is provided with lightweight fillers, the specific gravity of the lightweight fillers is less than that of water, the lightweight fillers are high-density polyethylene, the particle size of the lightweight fillers is less than 1.0 cm, and the lightweight fillers are in the shape of a cylinder or a sphere and have a hollow or porous structure.

[0007] The volume of the upper lightweight filler zone accounts for 1 / 5 to 1 / 3 of the volume of the interior of the reactor shell, the volume of the middle complete mixing zone accounts for 1 / 5 to 1 / 3 of the volume of the interior of the reactor shell, the reactor shell is a cylindrical shell, and the height-diameter ratio of the reactor shell is 10.

[0008] A first water sample collection port is arranged at a position on the outside of the reactor shell and above the lower granular sludge production zone, a second water sample collection port is arranged at a position on the outside of the reactor shell and in the middle of the middle complete mixing zone, and a gas collection port is arranged at a position on the outside of the reactor shell and above the upper lightweight filler zone.

[0009] The reactor shell is provided with a bottom sludge sampling port at a lower position of the lower granular sludge production zone, a first filler collection port at an upper position of the lower granular sludge production zone, and a second filler collection port at a middle position of the middle completely mixed zone.

[0010] The stirring mechanism comprises a motor, and the output end of the motor is provided with a paddle located in the middle completely mixed zone, and the power range of the motor is 5-25 W.

[0011] A method for simultaneously achieving denitrification and production of anaerobic ammonia oxidation granular sludge, using a reactor for simultaneously achieving denitrification and production of anaerobic ammonia oxidation granular sludge as described above, comprising the following steps:

[0012] Step one: starting anaerobic ammonia oxidation of the reactor, specifically: + wastewater with NH4 — N concentration of 53±10 mg / L is pumped into the reactor shell from the bottom inlet, and under normal temperature and anoxic conditions, the wastewater runs from bottom to top in the reactor shell and is discharged from the outlet, and under the conditions of a hydraulic retention time HRT of 12 h and 31±3℃, the reactor is continuously operated, and when the NH4 + -N and NO2 — N concentration <1 mg / L, and the total nitrogen removal rate TN reaches more than 86%, and the reactor anaerobic ammonia oxidation is successfully started;

[0013] Step two: formation of anaerobic ammonia oxidation bacteria enrichment and biofilm in the reactor, specifically: + -N, NO2 - -N concentration of 48±2 mg / L and 53±3 mg / L, so that the total nitrogen removal rate NTR is stably maintained at more than 86% and can be maintained for 10 days;

[0014] Step three: domestication and stable operation of anaerobic ammonia oxidation granular sludge under high hydraulic load in the reactor, specifically: 3 suddenly shortening the hydraulic retention time HRT from 3 h to 40 min, at which time the nitrogen load NLR in the reactor shell is suddenly increased from 0.8 kgN / (m 3TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m 3 TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m 3 TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m 3 TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m - TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m + TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m - TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m + TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m

[0015] TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m 3 TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m TN removal rate again recovered to 86% and could be stably operated, further abruptly reducing HRT from 40 min to 20 min and 10 min, corresponding nitrogen loading NLR from 3.6 kgN / (m

[0016] In the step one, the reactor is started and continuously operated under the condition of temperature controlled by heating wire at 31±3℃. In the step two, the hydraulic retention time is gradually shortened by 2 times.

[0017] In the step two, the hydraulic retention time is gradually shortened by 2 times. In the step four, the sludge discharge valve discharges sludge periodically, and the sludge discharge period is every three days, and the sludge discharge amount is 50 mL each time.

[0018] In the step four, the sludge discharge valve discharges sludge periodically, and the sludge discharge period is every three days, and the sludge discharge amount is 50 mL each time. In the step four, the sludge discharge valve discharges sludge periodically, and the sludge discharge period is every three days, and the sludge discharge amount is 50 mL each time.

[0019] The technical effect of the present application is that: 1. The reactor shell inside the present application is sequentially divided into an upper light filler area, a middle complete mixing area and a lower granular sludge production area from top to bottom. The upper light filler area realizes effective retention of biomass; the middle complete mixing area can realize the functions of biological membrane peeling in the upper light filler area, preventing the upper light filler area from being blocked and the gas hole channel from being blocked by the granular sludge material, through the stirring of the stirring mechanism; the lower granular sludge production area realizes the production of anaerobic ammonia oxidation granular sludge through the sludge discharge valve. Through the division of different functional areas, the problem of easy blockage of the fixed bed biological filter column is solved, the biomass in the reactor is effectively maintained, stable nitrogen removal is realized in the actual operation of the anaerobic ammonia oxidation process, and a higher nitrogen load can be achieved. Carbon source addition, residual sludge production and greenhouse gas emission can be effectively reduced; 2. The light filler in the upper part of the reactor is disturbed by the rotation of the paddle to rub against each other in the reserved blank area. The biological membrane on the surface of the filler is peeled off and naturally sinks under the action of gravity. At the same time, the large particle floating sludge is naturally sunk by physical shearing, which becomes high-activity biomass together, plays an excellent anaerobic ammonia oxidation function, and realizes extremely high denitrification efficiency and hydraulic load bearing.

[0020] Further description will be made below in combination with the drawings. BRIEF DESCRIPTION OF DRAWINGS

[0021] Figure 1 It is a structure schematic diagram of a reactor for simultaneously realizing denitrification and anaerobic ammonia oxidation granular sludge production according to an embodiment of the present application.

[0022] The drawings show that: 1-wastewater supply end, 2-peristaltic pump, 3-reactor shell, 31-sludge discharge valve, 32-water inlet, 33-first water sample collection port, 34-second water sample collection port, 35-gas collection port, 36-light filler, 37-water outlet, 38-second filler collection port, 39-first filler collection port, 310-bottom sludge sampling port, 4-stirring mechanism, 41-motor, 42-paddle, 5-wastewater outlet end. DETAILED DESCRIPTION

[0023] Example 1

[0024] As Figure 1As shown, a reactor for realizing denitrification and anaerobic ammonia oxidation granular sludge production simultaneously comprises a reactor shell 3, the inside of the reactor shell 3 is sequentially divided into an upper light filler area, a middle complete mixing area and a lower granular sludge production area from top to bottom, a stirring mechanism 4 is arranged at the top of the reactor shell 3, the stirring mechanism 4 is used for stirring the middle complete mixing area, the bottom of the reactor shell 3 is in a conical structure, a sludge discharge valve 31 is arranged at the middle position of the bottom of the conical structure, a water inlet 32 is arranged at the side of the bottom of the reactor shell 3, the water inlet 32 is connected with a peristaltic pump 2 through a pipeline, the peristaltic pump 2 is connected with a wastewater supply end 1, a water outlet 37 is arranged at the side of the top of the reactor shell 3, the water outlet 37 is connected with a wastewater outlet end 5 through a pipeline.

[0025] In actual use, the inside of the reactor shell 3 is sequentially divided into an upper light filler area, a middle complete mixing area and a lower granular sludge production area from top to bottom, the upper light filler area realizes effective retention of biomass, the middle complete mixing area realizes biofilm shedding of the upper light filler area, prevents the upper light filler area from being blocked and the granular sludge material bodies floating up from blocking the air hole channel through stirring of the stirring mechanism, and the lower granular sludge production area realizes anaerobic ammonia oxidation granular sludge production through the sludge discharge valve.

[0026] Embodiment 2

[0027] Preferably, based on embodiment 1, in the present embodiment, the upper light filler area is provided with light fillers 36, the light fillers 36 have a specific gravity less than water, the particle size of the light fillers 36 is less than 1.0 cm, the light fillers 36 are high-density polyethylene, and the light fillers 36 are in a cylindrical or spherical shape and have a hollow or porous structure.

[0028] In actual use, the light fillers 36 have a specific gravity less than water, the particle size of the light fillers 36 is less than 1.0 cm, and the light fillers 36 are in a cylindrical or spherical shape and have a hollow or porous structure, which can effectively intercept large-particle-size granular sludge floating up due to air hole blockage.

[0029] Embodiment 3

[0030] Preferably, based on embodiment 1 or embodiment 2, in the present embodiment, the volume of the upper light filler area accounts for 1 / 5-1 / 3 of the internal volume of the reactor shell 3, the volume of the middle complete mixing area accounts for 1 / 5-1 / 3 of the internal volume of the reactor shell 3, the reactor shell 3 is a cylindrical shell, and the height-diameter ratio of the reactor shell 3 is 10.

[0031] In actual use, the volume of the upper lightweight filler zone accounts for 1 / 5-1 / 3 of the internal volume of the reactor shell 3, which provides attachment sites for anaerobic ammonia oxidation microorganisms and realizes biomass retention of anaerobic ammonia oxidation microorganisms, thereby ensuring low suspended solids concentration of effluent and maximum retention of anaerobic ammonia oxidation bacteria generated by the system. The volume of the middle completely mixed zone accounts for 1 / 5-1 / 3 of the internal volume of the reactor shell 3 and is located below the upper lightweight filler zone. The middle completely mixed zone is stirred by the stirring mechanism 4, and the lightweight filler can move to the area to rotate and collide, so that the overgrown biofilm on the filler falls off. This area is a temporary active area for the filler to fall off, and can also decompose large-particle sludge into small-particle sludge through physical collision and shearing action, thereby ensuring mass transfer efficiency.

[0032] Example 4

[0033] Preferably, based on example 1 or example 3, in this embodiment, a first water sample collection port 33 is arranged on the outer side of the reactor shell 3 at a position above the lower granular sludge production zone, a second water sample collection port 34 is arranged on the outer side of the reactor shell 3 at a position in the middle of the middle completely mixed zone, and a gas collection port 35 is arranged on the outer side of the reactor shell 3 at a position above the upper lightweight filler zone.

[0034] In actual use, the first water sample collection port 33, the second water sample collection port 34 and the gas collection port 35 collect wastewater samples of the lower granular sludge production zone, the middle completely mixed zone and gas samples of the upper lightweight filler zone, respectively, which facilitates the judgment of the reaction in the reactor shell 3.

[0035] Example 5

[0036] Preferably, based on example 1 or example 4, in this embodiment, a bottom mud sampling port 310 is arranged on the outer side of the reactor shell 3 at a position below the lower granular sludge production zone, a first filler collection port 39 is arranged on the outer side of the reactor shell 3 at a position above the lower granular sludge production zone, and a second filler collection port 38 is arranged on the outer side of the reactor shell 3 at a position in the middle of the middle completely mixed zone.

[0037] In actual use, the bottom mud sampling port 310 arranged on the outer side of the reactor shell 3 at a position below the lower granular sludge production zone is used to detect the production of granular sludge in the reactor shell 3, and the first filler collection port 39 and the second filler collection port 38 are used to detect the distribution of lightweight filler in the reactor shell 3.

[0038] Example 6

[0039] Preferably, based on Embodiment 1, in this embodiment, the stirring mechanism 4 includes a motor 41, the output end of the motor 41 is provided with a blade 42, the blade 42 is located in the middle of the fully mixed zone, and the power range of the motor 41 is 5 to 25W.

[0040] In actual use, the present invention periodically activates the motor 41, which rotates the blades 42 to create a hydraulic vortex in the middle of the reactor, and periodically discharges sludge in a measured manner. The rotation of the blades 42 disturbs the lightweight packing material at the top of the reactor, causing it to rub against each other in the reserved blank area. The excessively grown biofilm on the surface of the packing material is peeled off and naturally sinks under gravity. At the same time, large particles of floating sludge naturally sink under physical shearing, together forming highly active biomass, exerting excellent anaerobic ammonia oxidation function, and achieving extremely high denitrification efficiency and hydraulic load capacity.

[0041] Example 7

[0042] A method for simultaneously producing granular sludge from denitrification and anammox is disclosed. The method utilizes a reactor, as described above, for simultaneously producing granular sludge from denitrification and anammox. The reactor is made of plexiglass, with a height of 51.5 cm, an inner diameter of 5 cm, and a height-to-diameter ratio of 10. Its effective working volume is 0.785 L. The reactor is filled with K1 packing material, which is high-density polyethylene, with a height of 1.0 cm and a diameter of 1.0 cm, filling 1 / 5 of the effective volume. The reactor is started up and operated at 31°C according to the following steps:

[0043] Step 1: Start the anaerobic ammonium oxidation process in the reactor, specifically: [The process involves reacting substances containing NH4+ with nitrogen and sulfur dioxide]. + -N concentration was 48±10 mg / L and NO2 — Wastewater with an nitrogen concentration of 53±10 mg / L is pumped into reactor shell 3 through bottom inlet 32. Under normal temperature and anoxic conditions, the wastewater flows upward within reactor shell 3 and is discharged from outlet 37. The reactor operates continuously at a hydraulic retention time (HRT) of 12 h and a temperature of 31±3 °C until the NH4+ effluent from reactor shell 3 is discharged. + -N and NO2 — With a nitrogen concentration of <1 mg / L, the total nitrogen (TN) removal rate in the water body reached over 86%, and the anaerobic ammonia oxidation reactor was successfully started up.

[0044] Step 2: Enrichment and biofilm formation of anaerobic ammonia oxidizing bacteria within the reactor. Specifically, this involves gradually shortening the hydraulic retention time (HRT) from 12 h to 6 h and then to 3 h, allowing the anaerobic ammonia oxidizing bacteria inside the reactor shell 3 to be progressively enriched and purified. At each HRT, the influent NH4+ level is maintained at a certain level. + -N, NO2 --N concentrations of 48±2 mg / L and 53±3 mg / L ensured that the total nitrogen removal rate (NTR) remained stable at over 86% for 10 days.

[0045] Step 3: Acclimation and stable operation of anaerobic ammonia oxidation granular sludge under high hydraulic loading in the reactor. The specific process is as follows: The hydraulic retention time (HRT) is abruptly shortened from 3 hours to 40 minutes. At this time, the nitrogen load (NLR) inside the reactor shell (3) decreases from 0.8 kg N / (m³) 3 ·d) Instantaneously increased to 3.6 kgN / (m 3 ·d), once the total nitrogen (TN) removal rate in the water body recovers to 86% and can operate stably, the HRT is further drastically reduced from 40 min to 20 min and then to 10 min, corresponding to a nitrogen load (NLR) of 3.6 kg N / (m³). 3 ·d) Doubled to 7.2 kgN / (m 3 ·d) and 14.4 kgN / (m 3 ·d) When the total nitrogen (TN) removal rate in the water body remains stable above 86%, and NO2 - -N / NH4 + -N and NO3 - -N / NH4 + -N meets the theoretical stoichiometric ratios of 1.32 and 0.26 for anaerobic ammonia oxidation, indicating that anaerobic ammonia oxidation operates stably and efficiently under high load.

[0046] Step 4: Stable production of granular sludge in the reactor. The specific process is as follows: maintain hydraulic retention time (HRT) = 10 min and nitrogen load (NLR) at 14.4 kg N / (m³). 3 Under the conditions of ·d), the motor 41 is turned on every day to physically rotate and mix and disturb the sludge through the blades 42. The sludge is discharged periodically by the sludge discharge valve 31 to control the biomass inside the biological filter column reactor, so that the sludge retention time is 15 to 30 days. This achieves a stable TN removal rate of 86% for the total nitrogen in the water, thereby achieving efficient and stable denitrification and simultaneous production of anaerobic ammonia oxidation granular sludge.

[0047] In step one, the reactor is started and the temperature is controlled by heating wire to operate continuously at 31±3℃.

[0048] In step two, the hydraulic residence time is gradually shortened in increments of two times.

[0049] In step four, the sludge discharge valve 31 discharges sludge periodically every three days, with a discharge volume of 50 mL each time.

[0050] The application can efficiently realize and stably operate the anaerobic ammonia oxidation process, and the operation method of regularly rotating disturbance by the stirring mechanism and quantitative sludge discharge can solve the blockage problem commonly existing in the fixed bed biofilm system in the reactor, while avoiding the mass loss of biomass in the reactor and the mass transfer uneven problem of the large particle size granular sludge floating up. The application can realize efficient and stable denitrification of the medium nitrogen concentration anaerobic ammonia oxidation granular sludge in the ultra-short hydraulic retention time, and realize efficient and homogeneous production of the anaerobic ammonia oxidation granular sludge.

[0051] The above is only the preferred specific embodiment of the application, but the protection scope of the application is not limited to this. Any change or replacement easily thought of by those skilled in the art within the technical range disclosed by the application should be covered within the protection scope of the application.

Claims

1. A reactor that simultaneously realizes denitrification and anaerobic ammonia oxidation granular sludge production, characterized in that: The reactor includes a reactor shell (3), which is divided into an upper light packing zone, a middle fully mixed zone, and a lower granular sludge production zone from top to bottom. A stirring mechanism (4) is provided at the top of the reactor shell (3) for stirring the middle fully mixed zone. The bottom of the reactor shell (3) is a conical structure with a sludge discharge valve (31) located in the middle of the bottom. An inlet (32) is provided on the side of the bottom of the reactor shell (3), and the inlet (32) is connected to a peristaltic pump (2) via a pipe. The peristaltic pump (2) is connected to a wastewater supply end (1). An outlet (37) is provided on the side of the top of the reactor shell (3). The outlet (37) is connected to the wastewater outlet (5) through a pipe. Lightweight filler (36) is provided in the upper lightweight filler area. The specific gravity of the lightweight filler (36) is less than that of water. The lightweight filler (36) is high-density polyethylene. The particle size of the lightweight filler (36) is less than 1.0 cm. The lightweight filler (36) is cylindrical or spherical and has a hollow or porous structure. The volume of the upper lightweight filler area accounts for 1 / 5 to 1 / 3 of the internal volume of the reactor shell (3). The volume of the middle fully mixed area accounts for 1 / 5 to 1 / 3 of the internal volume of the reactor shell (3). The reactor shell (3) is a cylindrical shell. The height-to-diameter ratio of the reactor shell (3) is 10.

2. The reactor for simultaneously realizing denitrification and anaerobic ammonia oxidation granular sludge production according to claim 1, characterized in that: The reactor shell (3) has a first water sample collection port (33) located on the outside of the lower granular sludge production area, a second water sample collection port (34) located on the outside of the reactor shell (3) located in the middle of the middle fully mixed area, and a gas collection port (35) located on the outside of the reactor shell (3) located in the upper part of the upper light packing area.

3. The reactor for simultaneously realizing denitrification and anaerobic ammonia oxidation granular sludge production according to claim 1, characterized in that: A bottom sludge sampling port (310) is provided on the outside of the reactor shell (3) at the lower part of the lower granular sludge production area. A first packing material collection port (39) is provided on the outside of the reactor shell (3) at the upper part of the lower granular sludge production area. A second packing material collection port (38) is provided on the outside of the reactor shell (3) at the middle part of the middle fully mixed area.

4. The reactor for simultaneously realizing denitrification and anaerobic ammonia oxidation granular sludge production according to claim 1, characterized in that: The stirring mechanism (4) includes a motor (41), and the output end of the motor (41) is provided with a blade (42). The blade (42) is located in the middle of the fully mixed zone, and the power range of the motor (41) is 5 to 25W.

5. A method for simultaneously producing granular sludge from denitrification and anammox, using a reactor as described in any one of claims 1 to 4, characterized in that: Includes the following steps: Step 1: Start the anaerobic ammonium oxidation process in the reactor. The specific process is as follows: [The text abruptly ends here, likely due to an incomplete sentence or a formatting error.] + Wastewater with a NO-N concentration of 48±10 mg / L and a NO2-N concentration of 53±10 mg / L was pumped into the reactor shell (3) through the bottom inlet (32). Under normal temperature and anoxic conditions, the wastewater flowed upwards within the reactor shell (3) and was discharged from the outlet (37). The reactor operated continuously at a hydraulic retention time (HRT) of 12 h and a temperature of 31±3 °C until the NH4+ effluent from the reactor shell (3) was discharged. + -N and NO2-N concentrations <1mg / L, the total TN removal rate of various forms of nitrogen in the water body reached over 86%, and the anaerobic ammonia oxidation reactor was successfully started up; Step 2: Enrichment and biofilm formation of anaerobic ammonia oxidizing bacteria in the reactor. Specifically, the process involves: gradually shortening the hydraulic retention time (HRT) from 12h to 6h and then to 3h, so that the anaerobic ammonia oxidizing bacteria inside the reactor shell (3) are gradually enriched and purified. Under each hydraulic retention time (HRT), the influent NH4+ is maintained at a constant level. + The concentrations of -N and NO2-N were 48±2 mg / L and 53±3 mg / L, respectively, which ensured that the total nitrogen removal rate (NTR) remained stable at over 86% for 10 days. Step 3: Acclimation and stable operation of anaerobic ammonia oxidation granular sludge under high hydraulic load in the reactor. The specific process is as follows: The hydraulic retention time (HRT) is suddenly shortened from 3 hours to 40 minutes. At this time, the nitrogen load (NLR) in the reactor shell (3) is reduced from 0.8 kg N / (m³) 3 ·d) Instantaneously increased to 3.6 kgN / (m 3 ·d), once the total nitrogen (TN) removal rate in the water body recovers to 86% and can operate stably, the HRT is further drastically reduced from 40 min to 20 min and then to 10 min, corresponding to a nitrogen load (NLR) of 3.6 kg N / (m³). 3 ·d) Doubled to 7.2 kgN / (m 3 ·d) and 14.4 kgN / (m 3 ·d) When the total nitrogen (TN) removal rate in the water body remains stable above 86%, and the NO2-N / NH4 ratio is... + -N and NO3-N / NH4 + -N meets the theoretical stoichiometric ratios of 1.32 and 0.26 for anaerobic ammonia oxidation, indicating that anaerobic ammonia oxidation operates stably and efficiently under high load. Step 4: Stable production of granular sludge in the reactor. The specific process is as follows: maintain hydraulic retention time (HRT) = 10 min and nitrogen load (NLR) at 14.4 kg N / (m³). 3 Under the conditions of ·d), the motor (41) is turned on every day to physically rotate and mix and disturb the water through the blades (42). The sludge is discharged periodically by the sludge discharge valve (31) to control the biomass inside the biological filter column reactor, so that the sludge retention time is 15 to 30 days. This achieves a stable TN removal rate of 86% for the total nitrogen in the water, thereby achieving efficient and stable denitrification and synchronous production of anaerobic ammonia oxidation granular sludge.

6. The method for simultaneously producing granular sludge from denitrification and anaerobic ammonia oxidation according to claim 5, characterized in that: In step one, the reactor is started and the temperature is controlled by heating wire to operate continuously at 31±3℃.

7. The method for simultaneously producing granular sludge from denitrification and anaerobic ammonia oxidation according to claim 5, characterized in that: In step two, the hydraulic residence time (HRT) is gradually shortened in increments of two times.

8. The method for simultaneously producing granular sludge from denitrification and anaerobic ammonia oxidation according to claim 5, characterized in that: In step four, the mud discharge valve (31) discharges mud periodically every three days, with a mud discharge volume of 50 mL each time.

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