Method for treating wastewater using a moving bed biofilm reactor

Abstract

This invention discloses a method for treating wastewater using a moving bed biofilm reactor. Wastewater is placed in the reactor and aeration is controlled, causing the microorganisms within the reactor to sequentially enter an anaerobic, aerobic, and anaerobic phase. Wastewater treatment is completed after the aeration control ends. The aeration control consists of a cycle of stopping aeration, aeration, and stopping aeration, with the ratio of the time spent stopping aeration, aeration, and stopping aeration within one cycle being (1.8-2.2):1:(1.8-2.2). When wastewater enters the reactor, the aeration control program is initiated. As the aeration control program proceeds, the microorganisms within the reactor sequentially enter the anaerobic, aerobic, and anaerobic phases. In the aerobic phase, carbon removal, nitrification, and phosphorus uptake occur; in the anaerobic phase, denitrification and phosphorus release occur, thereby achieving the goals of carbon removal, nitrogen removal, and phosphorus removal. This reduces energy consumption for wastewater treatment and eliminates the need for additional equipment.

Description

Technical Field

[0001] This invention relates to the field of wastewater treatment technology, and more specifically, to a method for treating wastewater using a moving bed biofilm reactor. Background Technology

[0002] The discharge of large amounts of nitrogen and phosphorus-containing substances into water bodies from human life and production can lead to eutrophication, which in turn prevents aquatic plants and fish and shrimp from living and reproducing normally, and may even indirectly affect human health. Therefore, we need to treat nitrogen and phosphorus wastewater. The treated water can be recycled or discharged directly in compliance with standards, thereby reducing the impact on nature, human health, or the living environment.

[0003] For the biological treatment of nitrogen and phosphorus wastewater, traditional nitrogen and phosphorus removal processes require the addition of large amounts of carbon sources or combination with other processes, which increases reagent costs and investment costs. Compared with traditional nitrogen and phosphorus removal processes that use multiple tanks, simultaneous nitrification and denitrification in an MBBR reactor can reduce the footprint and equipment investment. Most simultaneous nitrification and denitrification processes control dissolved oxygen at a low concentration to promote simultaneous nitrification and denitrification. However, low dissolved oxygen concentrations are difficult to control and can lead to poor carbon and phosphorus removal. In addition, the low aeration disturbance results in low microbial activity and slow regeneration.

[0004] In view of this, the present invention is proposed. Summary of the Invention

[0005] The purpose of this invention is to provide a method for treating wastewater using a moving bed biofilm reactor.

[0006] This invention is implemented as follows:

[0007] In a first aspect, the present invention provides a method for treating wastewater using a moving bed biofilm reactor, wherein the wastewater is placed in the reactor and aeration is controlled, so that the microorganisms in the reactor are sequentially in an anaerobic stage, an aerobic stage and an anaerobic stage, and the wastewater treatment is completed after the aeration control is completed; wherein the aeration control is based on a cycle of stopping aeration, aeration and stopping aeration, and the ratio of the time of stopping aeration, aeration and stopping aeration in one cycle is (1.8-2.2):1:(1.8-2.2).

[0008] In an optional implementation, one cycle of the aeration control is 35h-45h.

[0009] In an optional implementation, the dissolved oxygen concentration in the reactor water during the aeration stage is 4 mg / L-5 mg / L.

[0010] In an optional embodiment, the sludge concentration in the reactor is 3g / L-5g / L, the pH is 7-8, and the temperature is 20±5℃.

[0011] In an optional embodiment, the wastewater has a C / N ratio of <4;

[0012] Preferably, the wastewater has a COD of 150 mg / L-400 mg / L, a total nitrogen of 50-150 mg / L, an ammonia nitrogen of 5 mg / L-20 mg / L, and a total phosphorus of 2.0 mg / L-5.0 mg / L.

[0013] In an optional embodiment, the concentration of carbon source in the water within the reactor is 1 / 16 g / L to 1 / 8 g / L.

[0014] In an optional embodiment, the biofilm culture method in the reactor includes:

[0015] Facultative sludge was inoculated into the reactor and artificial water was added to make the sludge concentration in the sludge mixture in the reactor 3g / L-5g / L. Then, packing material was added into the reactor.

[0016] Biofilm cultivation involves mixing packing material, artificial water, and sludge, and controlling aeration. One cultivation cycle consists of artificial water inflow, aeration control, and effluent discharge, and this process is repeated until the ammonia nitrogen removal rate is above 60% and the COD removal rate is above 80%, at which point the biofilm cultivation is complete.

[0017] In an optional embodiment, the C:N:P mass-volume concentration ratio in the artificially prepared water is (95-105):(4-6):1, and the P element concentration is 2.8 mg / L-3.2 mg / L.

[0018] In an optional embodiment, after the biofilm culture is completed, a large number of Vorticella, Paramecium and Paramecium are observed on the carrier under a microscope, and the biofilm is light yellowish-brown.

[0019] Preferably, the packing material is at least one of BioNest biological nest packing, PE packing, and biological curtain packing; the filling rate of the packing material in the reactor is 40%-50%;

[0020] Preferably, the dominant bacterial groups in the sludge attached to the packing material are *Pseudomonas mexicans* and *Hydrogenobacterium*.

[0021] In an optional embodiment, when the reactor first treats wastewater, the proportion of wastewater in the influent is 15%-25%, and the proportion of wastewater in the influent is gradually increased from 15%-25% until the proportion of wastewater in the influent reaches 100%.

[0022] The present invention has the following beneficial effects:

[0023] When wastewater enters the reactor, the aeration control program is activated. As the aeration control program proceeds, the microorganisms in the reactor sequentially enter the anaerobic stage, the aerobic stage, and the anaerobic stage. In this way, carbon removal, nitrification, and phosphorus uptake occur in the aerobic stage, while denitrification and phosphorus release occur in the anaerobic stage. This achieves the purpose of carbon removal, nitrogen removal, and phosphorus removal, reducing the energy consumption of wastewater treatment and eliminating the need for additional equipment. Detailed Implementation

[0024] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. Where specific conditions are not specified in the embodiments, conventional conditions or conditions recommended by the manufacturer shall apply. Reagents or instruments whose manufacturers are not specified are all conventional products that can be purchased commercially.

[0025] This invention provides a method for treating wastewater using a moving bed biofilm reactor. The wastewater is placed in the reactor and aeration is controlled, so that the microorganisms in the reactor are sequentially in an anaerobic stage, an aerobic stage, and an anaerobic stage. The wastewater treatment is completed after the aeration control is completed. The aeration control consists of a cycle of stopping aeration, aeration, and stopping aeration, and the ratio of the time of stopping aeration, aeration, and stopping aeration in one cycle is (1.8-2.2):1:(1.8-2.2).

[0026] In this embodiment, when wastewater enters the reactor, the aeration control program is started. As the aeration control program proceeds, the microorganisms in the reactor are in the anaerobic stage, the aerobic stage, and the anaerobic stage in sequence. In this way, carbon removal, nitrification and phosphorus uptake are carried out in the aerobic stage, and denitrification and phosphorus release are carried out in the anaerobic stage, thereby achieving the purpose of carbon removal, nitrogen removal and phosphorus removal.

[0027] It should be noted that in this embodiment, during the initial period after wastewater enters the reactor and during the period after aeration is completed, a small amount of oxygen remains dissolved in the reactor water. Therefore, even without aeration, there will be a brief period of anoxic conditions. Consequently, within a complete aeration control cycle, the microorganisms in the reactor may sequentially be in the anoxic, anaerobic, aerobic, anoxic, and anaerobic phases. During the anoxic phase, denitrification and phosphorus release can still occur in the reactor, which is still beneficial for achieving carbon, nitrogen, and phosphorus removal.

[0028] In this embodiment, the ratio of the time for stopping aeration, the time for aeration, and the time for stopping aeration within one cycle is set to (1.8-2.2):1:(1.8-2.2). Specifically, it can be any value between 1.8:1:2.2, 1.9:1:2.1, 2:1:2, 2.1:1:1.9, 2.2:1:1.8, 1.8:1:1.8, 1.9:1:1.9, 2.1:1:2.1, 2.2:1:2.2, or (1.8-2.2):1:(1.8-2.2). The allocation of aeration and stopping aeration time is conducive to the rational allocation of time for carbon removal, digestion, denitrification, phosphorus absorption, and phosphorus release, thereby achieving a better wastewater purification effect. In addition, the aeration time in this embodiment is relatively short, which helps to reduce the operating cost of the reactor.

[0029] In an optional implementation, the aeration control cycle is 35-45 hours, specifically 35, 36, 37, 38, 39, 40, 41, 425, 43, 44, 45 hours, or any value between 35 and 45 hours. For example, aeration can be stopped for 16 hours, followed by 8 hours of aeration, and then stopped for another 16 hours to complete one aeration control cycle. After the reactor stabilizes and completes one cycle, the COD removal efficiency is above 60%, the ammonia nitrogen removal efficiency is above 80%, the total nitrogen removal efficiency is above 90%, the simultaneous nitrification / denitrification rate (SND rate) is around 50%, and the total phosphorus removal efficiency is above 60%. The total phosphorus concentration in the effluent is maintained within the range of 0.5 mg / L-1.0 mg / L, and phosphate is discharged in the form of sludge. If the aeration control cycle is too short, the water treatment effect will be poor; if the aeration control cycle is too long, the water treatment cost will increase.

[0030] In an optional implementation, the dissolved oxygen concentration in the reactor water during the aeration stage is 4 mg / L-5 mg / L.

[0031] Biofilm reactors are relatively effective at treating wastewater, but the problem of easy clogging of biological packing materials limits their application.

[0032] In this embodiment, the dissolved oxygen concentration in the reactor is controlled at a high level during aeration. On the one hand, this is beneficial for the carbon removal, nitrification, and phosphorus uptake processes. On the other hand, the higher dissolved oxygen requires a higher aeration intensity, which helps to increase the flow rate of the water in the reactor, thereby enhancing the water's ability to scour the packing material. This facilitates the shedding and renewal of microorganisms on the packing material, and ultimately helps to maintain the reactor's wastewater treatment effect.

[0033] In an optional embodiment, the sludge concentration in the reactor is 3 g / L-5 g / L, specifically any value between 3 g / L, 3.5 g / L, 4 g / L, 4.5 g / L, 5 g / L, or 3 g / L-5 g / L; the pH is 7-8, specifically any value between 7, 7.2, 7.4, 7.6, 7.8, 8, or 7-8; and the temperature is 20±5℃, specifically any value between 15℃, 17℃, 19℃, 21℃, 23℃, 25℃, or 20±5℃.

[0034] In an optional embodiment, the wastewater has a C / N ratio of <4, and the wastewater treatment method in this embodiment is suitable for wastewater with a low C / N ratio.

[0035] Preferably, the wastewater has a COD of 150 mg / L-400 mg / L, a total nitrogen of 50-150 mg / L, an ammonia nitrogen of 5 mg / L-20 mg / L, and a total phosphorus of 2.0 mg / L-5.0 mg / L.

[0036] In an optional embodiment, the concentration of carbon source in the water in the reactor is 1 / 16 g / L to 1 / 8 g / L, specifically any value between 1 / 16, 1 / 14, 1 / 12, 1 / 10, 1 / 8 or 1 / 16-1 / 8.

[0037] In the treatment of low C / N wastewater, it is usually necessary to add an additional carbon source to the water as an electron donor. The method of this application only requires the addition of about 0.5 times the amount of organic carbon source of traditional nitrification-denitrification processes after aeration, and the denitrification process can proceed smoothly. The nitrate nitrogen and nitrite nitrogen in the reactor effluent can both reach below 1.0 mg / L, which will not lead to a large accumulation of nitrate nitrogen and nitrite nitrogen. Compared with traditional nitrification-denitrification, it greatly reduces the cost of reagents.

[0038] In an optional embodiment, the biofilm culture method in the reactor includes:

[0039] Facultative sludge was inoculated into the reactor and artificial water was added to make the sludge concentration in the sludge mixture in the reactor 3g / L-5g / L. Then, packing material was added into the reactor.

[0040] Biofilm cultivation involves mixing packing material, artificially prepared water, and sludge, and controlling aeration. One cultivation cycle consists of artificially prepared water intake, controlled aeration, and effluent discharge, and this process is repeated until ammonia nitrogen removal rate exceeds 60% and COD removal rate exceeds 80%, at which point biofilm cultivation is complete. Typically, biofilm cultivation can be completed in 5 cycles, making it relatively easy and time-efficient.

[0041] In an optional embodiment, the C:N:P mass-volume concentration ratio in the artificially prepared water is (95-105):(4-6):1, and the P element concentration is 2.8 mg / L-3.2 mg / L.

[0042] By adjusting the composition of the artificially prepared water, the needs of the microorganisms within the reactor are met, thereby improving the effectiveness of subsequent wastewater treatment. Specifically, the phosphorus (P) concentration can be any value between 2.8 mg / L, 2.9 mg / L, 3.0 mg / L, 3.1 mg / L, 3.2 mg / L, or 2.8 mg / L-3.2 mg / L; the nitrogen (N) concentration can be any value between 14 mg / L, 14.5 mg / L, 15 mg / L, 15.5 mg / L, 16 mg / L, or 14 mg / L-16 mg / L; and the carbon (C) concentration can be any value between 280 mg / L, 290 mg / L, 300 mg / L, 310 mg / L, 320 mg / L, or 280 mg / L-320 mg / L.

[0043] In an optional embodiment, after the biofilm culture is completed, a large number of Vorticella, Paramecium and Paramecium are observed on the carrier under a microscope, and the biofilm is light yellowish-brown.

[0044] Preferably, the packing material is at least one of BioNest biological nest packing, PE packing, and biological curtain packing; the filling rate of the packing material in the reactor is 40%-50%, specifically, it can be any value between 40%, 42%, 44%, 46%, 48%, 50%, or 40%-50%.

[0045] Preferably, the dominant bacterial groups in the sludge attached to the packing material are *Pseudomonas mexicans* and *Hydrogenobacterium*, both of which have denitrification capabilities. *Hydrogenobacterium*, in particular, has a denitrification effect, which improves the efficiency of subsequent wastewater treatment.

[0046] In an optional embodiment, when the reactor first treats wastewater, the proportion of wastewater in the influent is 15%-25%. The proportion of wastewater in the influent is gradually increased from 15%-25% until the proportion of wastewater in the influent reaches 100%, thereby gradually reducing the amount of artificially prepared water and playing a transitional role.

[0047] The features and performance of the present invention will be further described in detail below with reference to embodiments.

[0048] Example 1

[0049] This embodiment provides a method for treating wastewater using a moving bed biofilm reactor, including:

[0050] Biofilm cultivation in the reactor involved inoculating facultative sludge from the Wuhu wastewater treatment plant into the reactor after two rounds of washing, followed by the addition of artificial water to achieve a sludge concentration of 5 g / L in the sludge mixture. BioNest bio-nest packing material was then added, with the packing volume occupying 50% of the total reactor volume. The packing material, artificial water, and sludge were mixed, and aeration was controlled. One cultivation cycle consisted of artificial water inflow, aeration control, and effluent discharge, and this process was repeated until ammonia nitrogen removal exceeded 60% and COD removal exceeded 80%, indicating successful biofilm cultivation. The artificial water had a C:N:P ratio of 100:5:1, with C, N, and P concentrations of 300 mg / L, 15 mg / L, and 3 mg / L, respectively. Aeration control included stopping aeration for 16 hours, aerating for 8 hours, and then stopping aeration again for 16 hours.

[0051] Wastewater treatment was performed on caprolactam wastewater from a coal chemical plant with a C / N ratio of 3.33 and a B / C ratio of 0.10. The influent COD was 200 mg / L, total nitrogen was 60 mg / L, ammonia nitrogen was 5.0 mg / L, and total phosphorus was 3.0 mg / L. 4 L of wastewater was initially fed into the reactor without any further operation (aeration was stopped for 16 hours) for denitrification. Aeration was then initiated for 8 hours until the dissolved oxygen concentration stabilized at approximately 4 mg / L, allowing the wastewater to fully contact the substrate with attached microorganisms for carbon removal, nitrification, and phosphorus uptake. After aeration, 0.25 g of sodium acetate was added to the reactor, and aeration was stopped for another 16 hours. This constituted one operating cycle, after which the wastewater was discharged. After the reactor had been running stably for five cycles, the effluent water quality was tested. The effluent COD was 60 mg / L, total nitrogen was 5.0 mg / L, ammonia nitrogen was 0.8 mg / L, total phosphorus was 1.0 mg / L, nitrate nitrogen and nitrite nitrogen were both 1.0 mg / L, and the SND rate was 52%, indicating that the reactor was undergoing simultaneous nitrification and denitrification. After the reactor had been running stably for ten cycles, the effluent water quality was tested again. The effluent COD was 60 mg / L, total nitrogen was 5.0 mg / L, ammonia nitrogen was 1.0 mg / L, total phosphorus was 1.2 mg / L, nitrate nitrogen and nitrite nitrogen were both 1.0 mg / L, and the SND rate was 50%, indicating that the reactor could operate stably for a long period of time.

[0052] Comparative Example 1

[0053] This comparative example provides a method for treating wastewater using a moving bed biofilm reactor, including:

[0054] Biofilm culture in the reactor was the same as in Example 1;

[0055] The wastewater treatment differed from Example 1 only in that: 4L of water was initially fed into the reactor, aeration was initiated to achieve a dissolved oxygen concentration of approximately 2mg / L, and aeration continued for 24 hours. Then, 0.25g of sodium acetate was added to the reactor, and aeration continued for another 16 hours. This constituted one operating cycle, after which the wastewater was discharged. After the reactor had operated stably for five cycles, the effluent quality was tested. The effluent COD was 100mg / L, total nitrogen was 20mg / L, ammonia nitrogen was 2.5mg / L, total phosphorus was 2.0mg / L, nitrate nitrogen was 3.0mg / L, and nitrite nitrogen was 10mg / L. The reactor did not achieve simultaneous nitrification and denitrification. After the reactor had been running stably for 10 cycles, the effluent water quality was tested. The effluent COD was 100 mg / L, total nitrogen was 25 mg / L, ammonia nitrogen was 4.0 mg / L, total phosphorus was 2.5 mg / L, nitrate nitrogen was 3.0 mg / L, and nitrite nitrogen was 10 mg / L. The reactor did not achieve simultaneous nitrification and denitrification. As the reactor's operating time increased, the removal efficiency of total nitrogen, ammonia nitrogen, and total phosphorus gradually deteriorated.

[0056] Example 2

[0057] This embodiment provides a method for treating wastewater using a moving bed biofilm reactor, including:

[0058] Biofilm culture in the reactor was the same as in Example 1;

[0059] Wastewater treatment was performed on petrochemical caprolactam wastewater with a C / N ratio of 2.67 and a B / C ratio of 0.12. The influent COD was 400 mg / L, total nitrogen was 150 mg / L, ammonia nitrogen was 15 mg / L, and total phosphorus was 5.0 mg / L. 4 L of wastewater was initially fed into the reactor without any further operation (aeration was stopped for 16 hours) for denitrification. Aeration was then initiated for 8 hours until the dissolved oxygen concentration stabilized at approximately 4 mg / L, allowing the wastewater to fully contact the packing material with attached microorganisms for carbon removal, nitrification, and phosphorus uptake. After aeration, 0.5 g of sodium acetate was added to the reactor, and aeration was stopped for another 16 hours. This constituted one operating cycle, after which the wastewater was discharged. After the reactor had been running stably for five cycles, the effluent quality was tested. The effluent COD was 100 mg / L, total nitrogen was 15 mg / L, ammonia nitrogen was 3.0 mg / L, total phosphorus was 2.0 mg / L, nitrate nitrogen and nitrite nitrogen were both 2.0 mg / L, and the SND rate was 67%, indicating that the reactor was undergoing simultaneous nitrification and denitrification. After the reactor had been running stably for ten cycles, the effluent quality was tested again. The effluent COD was 100 mg / L, total nitrogen was 18 mg / L, ammonia nitrogen was 3.0 mg / L, total phosphorus was 2.5 mg / L, nitrate nitrogen and nitrite nitrogen were both 2.5 mg / L, and the SND rate was 58%, indicating that the reactor could operate stably for a long period of time.

[0060] Comparative Example 2

[0061] This comparative example provides a method for treating wastewater using a moving bed biofilm reactor, including:

[0062] Biofilm culture in the reactor was the same as in Example 2;

[0063] The wastewater treatment differed from Example 2 only in that: 4L of water was initially fed into the reactor, aeration was initiated to achieve a dissolved oxygen concentration of approximately 2mg / L, and aeration continued for 24 hours. Then, 0.5g of sodium acetate was added to the reactor, and aeration continued for another 16 hours. This constituted one operating cycle, after which the wastewater was discharged. After the reactor had operated stably for five cycles, the effluent quality was tested. The effluent COD was 250mg / L, total nitrogen was 50mg / L, ammonia nitrogen was 8.0mg / L, total phosphorus was 4.0mg / L, nitrate nitrogen was 5.0mg / L, and nitrite nitrogen was 15mg / L. The reactor did not achieve simultaneous nitrification and denitrification.

[0064] Comparative Example 3

[0065] The only difference from Example 1 is that in the wastewater treatment step, after the water is completely fed into the reactor, aeration is carried out for 8 hours and then stopped for 16 hours.

[0066] After the reactor had been running stably for five cycles, the effluent water quality was tested. The effluent COD was 80 mg / L, total nitrogen was 20 mg / L, ammonia nitrogen was 2.0 mg / L, total phosphorus was 2.5 mg / L, nitrate nitrogen was 5 mg / L, and nitrite nitrogen was 8 mg / L. The reactor did not achieve the simultaneous nitrification and denitrification process.

[0067] Comparative Example 4

[0068] The only difference from Example 1 is that in the wastewater treatment step, after the water is completely fed into the reactor, the aeration is stopped for 12 hours, aeration is carried out for 6 hours, and then the aeration is stopped for another 12 hours.

[0069] After the reactor had been running stably for five cycles, the effluent water quality was tested. The effluent COD was 80 mg / L, total nitrogen was 8.0 mg / L, ammonia nitrogen was 1.0 mg / L, total phosphorus was 2.5 mg / L, nitrate nitrogen was 2.0 mg / L, and nitrite nitrogen was 2.0 mg / L. The reactor did not achieve the simultaneous nitrification and denitrification process.

[0070] Comparative Example 5

[0071] The only difference from Example 1 is that in the wastewater treatment step, after the water is completely fed into the reactor, the aeration is stopped for 10 hours, then aerated for 20 hours, and then stopped for another 10 hours.

[0072] After the reactor had been running stably for five cycles, the effluent water quality was tested. The effluent COD was 70 mg / L, total nitrogen was 6.0 mg / L, ammonia nitrogen was 1.0 mg / L, total phosphorus was 1.5 mg / L, nitrate nitrogen was 2.0 mg / L, and nitrite nitrogen was 1.0 mg / L. The reactor did not achieve the simultaneous nitrification and denitrification process.

[0073] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A method for treating wastewater using a moving bed biofilm reactor, characterized by, Wastewater is placed in a reactor and aeration is controlled, so that the microorganisms in the reactor are in the anaerobic stage, the aerobic stage and the anaerobic stage in sequence. The wastewater treatment is completed after the aeration control is completed. The aeration control is based on a cycle of stopping aeration, aeration and stopping aeration, and the ratio of the time of stopping aeration, aeration and stopping aeration in one cycle is (1.8-2.2):1:(1.8-2.2). The biofilm culture method in the reactor includes: Facultative sludge was inoculated into the reactor and artificial water was added to make the sludge concentration in the sludge mixture in the reactor 3 g / L - 5 g / L. Then packing material was added into the reactor. Biofilm cultivation involves mixing packing material, artificial water, and sludge, and controlling aeration. One cultivation cycle consists of artificial water inlet, aeration control, and effluent discharge, and this process is repeated until the ammonia nitrogen removal rate is above 60% and the COD removal rate is above 80%, at which point the biofilm cultivation is complete. After the biofilm culture was completed, a large number of Vorticella, Paramecium and spirochetes were observed on the carrier under a microscope, and the biofilm was light yellowish-brown.

2. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, characterized by, The aeration control cycle is 35h-45h.

3. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, characterized by, During the aeration stage, the dissolved oxygen concentration in the reactor water is 4 mg / L - 5 mg / L.

4. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, characterized by, The sludge concentration in the reactor is 3 g / L - 5 g / L, the pH is 7-8, and the temperature is 20±5℃.

5. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, characterized in that, The wastewater has a C / N ratio of <4.

6. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, wherein The wastewater has a COD of 150 mg / L - 400 mg / L, a total nitrogen of 50 mg / L - 150 mg / L, an ammonia nitrogen of 5 mg / L - 20 mg / L, and a total phosphorus of 2.0 mg / L - 5.0 mg / L.

7. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, characterized in that, The concentration of carbon source in the water within the reactor is 1 / 16 g / L to 1 / 8 g / L.

8. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, wherein The artificially prepared water has a C:N:P mass-volume concentration ratio of (95-105):(4-6):1, and a P element concentration of 2.8 mg / L -3.2 mg / L.

9. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, wherein, The packing material is at least one of BioNest biological nest packing, PE packing, and biological curtain packing; the filling rate of the packing material in the reactor is 40%-50%.

10. The method for treating wastewater using a moving bed biofilm reactor according to claim 1, wherein When the reactor first treats wastewater, the proportion of wastewater in the influent is 15%-25%. The proportion of wastewater in the influent is gradually increased from 15%-25% until the proportion of wastewater in the influent reaches 100%.