A method for treating ammonia-nitrogen wastewater

Abstract

The present application belongs to the field of wastewater treatment, and particularly relates to a treatment method of ammonia-nitrogen wastewater, which is carried out in an MBBR-MBR reactor for ammonia-nitrogen wastewater treatment. The specific process in the start-up stage of the MBBR-MBR reactor comprises: adding ammonia-nitrogen wastewater, sodium succinate and direct ammonia-oxidizing functional bacteria Acinetobacter sp.SC3T into the MBBR-MBR reactor, and not inoculating activated sludge; in the start-up stage, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35 DEG C, the ammonia-nitrogen concentration is controlled at 150-300 mg / L, and the sodium succinate addition amount is controlled at 1-3 g / L. The method provided by the present application effectively overcomes the shortcomings that the direct ammonia-oxidizing functional bacteria are prone to loss, need to be inoculated regularly, and cause cost increase and unstable effect, and has excellent removal effect on high-ammonia-nitrogen organic wastewater.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of wastewater treatment, and particularly relates to a treatment method of ammonia-nitrogen wastewater. BACKGROUND

[0002] The existing biological denitrification technology mainly relies on the coupling of nitrification and denitrification process, and ammonia-nitrogen removal is achieved by consuming a large amount of oxygen and adding carbon source. This method is widely used in low-concentration ammonia-nitrogen wastewater treatment, but it is complex to operate, occupies a large area, and has low efficiency in high-concentration ammonia-nitrogen and organic wastewater treatment. Nitrobacteria are easily affected by environmental changes and have poor impact resistance, resulting in fluctuation of system denitrification efficiency. In addition, the denitrification process requires additional carbon source to maintain the carbon-nitrogen ratio, increasing the operation cost.

[0003] In view of the deficiencies of the prior art, recent studies have shown that the microbial direct ammonia oxidation (Dirammox) process is a new ammonia-nitrogen removal approach, which can convert ammonia-nitrogen into nitrogen gas under aerobic conditions through functional bacteria such as Alcaligenes. This approach does not rely on the traditional multi-stage nitrification / denitrification process, which can significantly reduce the complexity and area occupied by the system. In addition, Dirammox functional bacteria have strong growth ability and environmental adaptability, and can still efficiently remove pollutants under the condition of coexistence of high ammonia-nitrogen and organic matter, showing great application potential.

[0004] However, how to maintain the high abundance and stability of Dirammox functional bacteria is a key problem for the engineering application of this technology. SUMMARY

[0005] Therefore, the purpose of the present application is to provide a treatment method of ammonia-nitrogen wastewater. The present application combines the MBBR (moving bed biofilm reactor) process with the MBR (membrane bioreactor) process and the microbial direct ammonia oxidation process (Dirammox), effectively overcoming the shortcomings of the easy loss of direct ammonia oxidation functional bacteria and the increase in cost and instability of the effect caused by periodic inoculation, and having excellent removal effect on high-ammonia-nitrogen organic wastewater.

[0006] The present application provides a treatment method of ammonia-nitrogen wastewater, which is carried out in an MBBR-MBR reactor.

[0007] The MBBR-MBR reactor comprises a reactor body provided with a water inlet, a water outlet and a sludge discharge port, an MBBR carrier and an aeration device arranged in the reactor body, and an MBR membrane assembly connected with the water outlet of the reactor body and arranged in or externally connected with the reactor body.

[0008] The specific process of the start-up stage of the MBBR-MBR reactor comprises:

[0009] The ammonia-nitrogen wastewater, sodium succinate and direct ammonia-oxidation functional bacteria Acinetobacter sp. SC3T are added into the MBBR-MBR reactor, and no activated sludge is inoculated, so as to start the reactor in a batch or continuous flow mode;

[0010] During the starting stage, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35℃, the ammonia-nitrogen concentration is controlled at 150-300 mg / L, and the addition amount of sodium succinate is controlled at 1-3 g / L.

[0011] Preferably, the MBBR carrier is K1 plastic carrier and / or K5 plastic carrier.

[0012] Preferably, the loading amount of the MBBR carrier in the reactor body accounts for 1 / 4-1 / 2 of the volume of the reactor body.

[0013] Preferably, the loading amount of the MBBR carrier in the reactor body accounts for 1 / 3 of the volume of the reactor body.

[0014] Preferably, the pore size of the filter membrane of the MBR membrane assembly is 0.05-0.2 μm.

[0015] Preferably, the pore size of the filter membrane of the MBR membrane assembly is 0.1 μm.

[0016] Preferably, a water inlet pump is installed at the water inlet of the reactor body.

[0017] Preferably, a drainage pump and a vacuum gauge are installed at the water outlet of the reactor body.

[0018] Preferably, an overflow port is further arranged on the reactor body.

[0019] Preferably, after the MBBR-MBR reactor completes the starting stage and runs stably, the treatment load of the ammonia-nitrogen wastewater is gradually increased.

[0020] Compared with the prior art, the present application provides a treatment method for ammonia-nitrogen wastewater, which is carried out in an MBBR-MBR reactor; the MBBR-MBR reactor comprises: a reactor main body, which is provided with a water inlet, a water outlet and a sludge discharge port; an MBBR carrier and an aeration device arranged in the reactor main body; and an MBR membrane assembly connected with the water outlet of the reactor main body, arranged in the reactor main body or externally connected with the reactor main body; the specific process of the start-up stage of the MBBR-MBR reactor comprises: adding ammonia-nitrogen wastewater, sodium succinate and direct ammonia oxidation functional bacteria Acinetobactersp.SC3T into the MBBR-MBR reactor, without inoculating activated sludge, and starting in a muffled exposure or continuous flow mode; in the start-up stage, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35 DEG C, the ammonia-nitrogen concentration is controlled at 150-300 mg / L, and the addition amount of sodium succinate is controlled at 1-3 g / L. The present application combines the MBBR (moving bed biofilm reactor) process and the MBR (membrane bioreactor) process with the direct ammonia oxidation process (Dirammox) of microorganisms, and develops a method capable of efficiently and stably treating high-ammonia-nitrogen wastewater, the key point of which is to use Dirammox functional bacteria Acinetobactersp.SC3T as the core functional bacterial group, and to realize the enrichment and interception of the Dirammox functional bacteria in the reactor through the MBBR-MBR technology, thereby solving the problem of poor treatment effect of the traditional nitrification / denitrification process on high-ammonia-nitrogen wastewater. In addition, the present application is suitable for higher influent ammonia concentration, inhibits the growth of other competitive microorganisms, ensures the dominant position of the Dirammox functional bacteria in the system, and thus effectively improves the denitrification efficiency and the system stability. Finally, efficient denitrification and organic matter removal can be realized under the conditions of high ammonia-nitrogen and high organic load. BRIEF DESCRIPTION OF DRAWINGS

[0021] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the following will briefly introduce the drawings needed to be used in the embodiments or the prior art description. Obviously, the drawings in the following description are only embodiments of the present application, and other drawings can also be obtained by those skilled in the art without any creative effort on the basis of the provided drawings.

[0022] Figure 1 is a structural schematic diagram of the MBBR-MBR reactor provided by Embodiment 1 of the present application;

[0023] Figure 2 is a structural schematic diagram of the MBBR-MBR reactor provided by Embodiment 2 of the present application;

[0024] Figure 3is a structural schematic diagram of the MBBR-MBR reactor provided in Embodiment 3 of the present application;

[0025] Figure 4 is a structural schematic diagram of the MBBR-MBR reactor provided in Embodiment 4 of the present application;

[0026] Figure 5 is a structural schematic diagram of the MBBR-MBR reactor provided in Embodiment 5 of the present application;

[0027] Figure 6 is a structural schematic diagram of the MBBR-MBR reactor provided in Embodiment 6 of the present application.

[0028] Legend: 1 is a water outlet, 2 is a drainage pump, 3 is a vacuum gauge, 4 is an aeration device, 5 is a water inlet pump, 6 is a water inlet, 7 is an overflow port, 8 is a sludge discharge port, 9 is an MBBR carrier, and 10 is an MBR membrane assembly. DETAILED DESCRIPTION

[0029] The technical solutions in the embodiments of the present application will be described clearly and completely below. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative work fall within the scope of protection of the present application.

[0030] The present application provides a treatment method for ammonia-nitrogen wastewater, which is carried out in an MBBR-MBR reactor.

[0031] The MBBR-MBR reactor comprises: a reactor main body, on which a water inlet, a water outlet and a sludge discharge port are arranged; an MBBR carrier and an aeration device arranged in the reactor main body; and an MBR membrane assembly connected with the water outlet of the reactor main body and arranged in the reactor main body or externally connected with the reactor main body.

[0032] The specific process of the start-up stage of the MBBR-MBR reactor comprises:

[0033] Ammonia-nitrogen wastewater, sodium succinate and direct ammonia-oxidizing functional bacteria Acinetobactersp.SC3T are added into the MBBR-MBR reactor, and no activated sludge is inoculated, so as to start up in a muffled exposure or continuous flow mode.

[0034] In the start-up stage, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35℃, the ammonia-nitrogen concentration is controlled at 150-300 mg / L, and the addition amount of sodium succinate is controlled at 1-3 g / L.

[0035] In the present application, the direct ammonia oxidation functional bacteria Acinetobacter sp. SC3T is numbered as txid1820089 in the NCBI database, and the above strain can be cultivated according to the following steps:

[0036] (1) Sample collection:

[0037] An appropriate amount of activated sludge is taken from a sewage treatment plant, and the sludge basic parameters are determined; pcr gene determination is performed on the batch of sludge to detect whether the batch of sludge has Dirammox gene.

[0038] (2) Domestication culture:

[0039] Under sterile environment, 100 mL of sludge mixed solution with Dirammox gene dnfA is placed in a conical flask and shaken by hand for 10 min, and after the granular sample is broken, 10 mL is inoculated into each of 3 100 mL HNM liquids; cultivate at 28-30℃ for 24h. When the cultivation time is over, the indexes such as ammonia nitrogen, nitrate nitrogen and nitrite nitrogen are determined, and the second domestication is carried out, the domestication inoculation amount is 2%, the subsequent steps are consistent with the first domestication; after the water quality indexes are determined, the third domestication is carried out, the inoculation amount is 2%, and the water quality indexes are determined; after the three rounds of domestication are over, three types of culture medium samples are taken, and dnfA gene determination is carried out;

[0040] The HNM culture medium is: (NH4)2SO40.66g (5mM), sodium succinate 2.84g, KH2PO40.5g, MgSO4·7H2O 0.2g, Na2HPO40.5g, trace element solution 2.00mL, pH=7.5;

[0041] The trace element solution is: EDTA·2Na 57.10g, ZnSO4·7H2O 3.90g, CaCl2·2H2O 7.00g, MnCl2·4H2O 1.00g, FeSO4·7H2O 5.00g, (NH4)6Mo7O 24 ·4H2O 1.10g, CuSO4·5H2O 1.60g, CoCl2·6H2O 1.60g, pH=6.0;

[0042] Solid culture medium: the composition is consistent with the liquid culture medium, and 1.5% agar is additionally added.

[0043] (3) Sample dilution:

[0044] 20mL from the culture medium after the completion of the culture, rinsing with PBS buffer, centrifugation at 4000r / min for 2min, repeated three times, and then resuspended with PBS buffer to prepare a bacterial suspension; then 10mL of the bacterial suspension was added to a conical flask containing 90mL of sterile water, blown three times with a pipette, shaken by hand for 10min, and then diluted to a concentration of 10-1 of the bacterial solution, and then sequentially diluted to a concentration of 10 -2 -3 -4

[0045] (4) Plate separation:

[0046] 30 plates were taken, and 0.5mL of bacterial solution with concentrations of 10 -2 -3 -4 mL was inoculated into the plates under sterile operation; a total of three types of culture medium, three concentrations for each culture medium, and three plates for each concentration, and the last one was a control; incubated at 28-30℃ for 24-48h; then a single colony was picked from the plate with the completed culture using a inoculation loop and inoculated into a new plate, and the operation was repeated until pure bacteria appeared; if the colonies on the plate grew densely, the bacterial solution was further diluted.

[0047] (5) Strain identification:

[0048] The dnf gene cluster of the cultivated strain was detected, and the results showed that the strain was the strain with the number txid1820089 in the NCBI database.

[0049] In the present application, in the start-up phase, the dissolved oxygen concentration in the MBBR-MBR reactor can be controlled to be 1mg / L, 2mg / L, 3mg / L, 4mg / L, 5mg / L, 6mg / L, 7mg / L, 8mg / L, 9mg / L or 10mg / L.

[0050] In the present application, in the start-up phase, the temperature in the MBBR-MBR reactor can be controlled to be 25℃, 26℃, 27℃, 28℃, 29℃, 30℃, 31℃, 32℃, 33℃, 34℃ or 35℃.

[0051] In the present application, in the start-up phase, the ammonia nitrogen concentration in the MBBR-MBR reactor can be controlled to be 150mg / L, 160mg / L, 170mg / L, 180mg / L, 190mg / L, 200mg / L, 210mg / L, 220mg / L, 230mg / L, 240mg / L, 250mg / L, 260mg / L, 270mg / L, 280mg / L, 290mg / L or 300mg / L.

[0052] ​​​​​In the present application, the amount of sodium succinate added in the MBBR-MBR reactor during the start-up phase can be controlled to be 1 g / L, 1.1 g / L, 1.2 g / L, 1.3 g / L, 1.4 g / L, 1.5 g / L, 1.6 g / L, 1.7 g / L, 1.8 g / L, 1.9 g / L, 2 g / L, 2.1 g / L, 2.2 g / L, 2.3 g / L, 2.4 g / L, 2.5 g / L, 2.6 g / L, 2.7 g / L, 2.8 g / L, 2.9 g / L, or 3 g / L.

[0053] In the present application, the water inlet is preferably located at the bottom of the reactor body to ensure sufficient contact between the influent and the microorganisms at the bottom.

[0054] In the present application, the MBBR carrier is preferably a K1 plastic carrier and / or a K5 plastic carrier.

[0055] In the present application, the loading amount of the MBBR carrier in the reactor body is preferably 1 / 4 to 1 / 2 of the volume of the reactor body, and more preferably 1 / 3.

[0056] In the present application, the pore size of the filter membrane of the MBR membrane module is preferably 0.05 to 0.2 μm, and more preferably 0.1 μm, to ensure sufficient retention of direct ammonia-oxidizing functional bacteria.

[0057] In the present application, the aeration device preferably uses a microporous aeration head and is preferably installed at the bottom of the reactor body, which not only provides sufficient oxygen for the reactor but also has good mixing effect, helping to improve the oxygen transfer efficiency.

[0058] In the present application, the water inlet of the reactor body is preferably equipped with a water inlet pump.

[0059] In the present application, the water outlet of the reactor body is preferably equipped with a drainage pump and a vacuum gauge.

[0060] In the present application, the reactor body is preferably also provided with an overflow port.

[0061] In the present application, after the MBBR-MBR reactor completes the start-up phase and runs stably, the treatment load of ammonia-nitrogen wastewater is preferably gradually increased.

[0062] In the present application, for the MBBR-MBR reactor used, the following key points need to be emphasized:

[0063] (1) The reactor includes reactor body, MBBR carrier, MBR membrane module, aeration device, water inlet / outlet and pump, vacuum gauge, overflow port, sludge discharge port, and other key units, which ensure the stable operation and efficient denitrification of the reactor in high ammonia-nitrogen wastewater treatment.

[0064] (2) The effluent end of the reactor passes through the MBR membrane assembly to intercept microorganisms, ensuring that the Dirammox functional bacteria in the reactor do not flow out, maintaining high-efficiency denitrification capacity.

[0065] (3) The reactor should provide sufficient mixed growth sites for the bacterial population, ensuring that Dirammox functional bacteria can form biofilms by attaching to MBBR carriers, thereby increasing biomass and denitrification performance within the system.

[0066] (4) The MBR membrane assembly ensures that Dirammox functional bacteria are sufficiently intercepted within the reactor to promote the formation of flocs, granules or biofilms, while extending the sludge age, improving the stability and treatment capacity of the reactor.

[0067] (5) By setting a vacuum gauge at the effluent outlet of the reactor, membrane fouling can be monitored in real time, and timely cleaning and adjustment can be performed according to the membrane fouling situation to ensure long-term stable operation of the system.

[0068] (6) The dissolved oxygen content in the reactor can be precisely adjusted using an aeration device to ensure that Dirammox functional bacteria maintain high-efficiency ammonia oxidation capacity within the reactor.

[0069] (7) The sludge retention time (SRT) in the reactor can be adjusted using the sludge discharge port to prevent sludge bulging and ensure stable operation of the reactor.

[0070] (8) The water inlet and outlet pumps can be used to control the water discharge volume at the effluent outlet to be consistent with the water inlet volume, thereby maintaining the volume balance of the reactor and ensuring continuous and stable operation of the system.

[0071] In the present application, for the ammonia-nitrogen wastewater treatment process, the following key points need to be emphasized:

[0072] (1) Inoculation and start-up: During the start-up phase of the reactor, instead of inoculating traditional domesticated activated sludge, Dirammox functional bacteria Acinetobacter sp. SC3T are directly inoculated. During this phase, strict control of environmental conditions such as dissolved oxygen and temperature is used to promote rapid enrichment and efficient biofilm formation of Dirammox functional bacteria.

[0073] (2) Bacterial population interception and attachment growth: Through the physical interception effect of the MBR membrane assembly, Dirammox functional bacteria can rapidly attach to MBBR carriers in the reactor and maintain a high biomass. Dirammox functional bacteria, with their fast growth rate and strong environmental adaptability, can maintain a high abundance in the reactor, ensuring efficient ammonia-nitrogen removal.

[0074] (3) The promoting effect of high ammonia nitrogen: By adding a high concentration of ammonia nitrogen in the initial influent and adding sodium succinate as the optimal carbon source, the growth of Dirammox functional bacteria Acinetobacter sp. SC3T is promoted. A high concentration of ammonia nitrogen can inhibit the growth of other non-target microorganisms, thereby reducing competition and ensuring the dominant position of Dirammox functional bacteria in the reactor. This measure effectively avoids the interference of competitive microorganisms on the denitrification efficiency, maintaining the stability and efficiency of the system.

[0075] (4) Formation of biofilm: As the reactor operates, nutrients enter the reactor through the influent, and Dirammox functional bacteria rapidly proliferate and attach to the filler carrier to form a biofilm system. The coupling of the filter membrane and the biofilm further enhances the accumulation of biomass and improves the system's treatment capacity for pollutants.

[0076] (5) Efficient denitrification and organic matter removal: Through the above process control, Dirammox functional bacteria can achieve efficient and stable denitrification and organic matter removal in the treatment of wastewater with high ammonia nitrogen and high COD, significantly simplifying the traditional denitrification process and reducing treatment costs.

[0077] For a clearer understanding, the following examples are provided for further illustration.

[0078] Example 1

[0079] The structure of the MBBR-MBR reactor used in this example is shown in Figure 1 , and is specifically described as follows:

[0080] The main body of the reactor is a cylindrical reactor with a volume of 1L, and the bottom is provided with an influent inlet 6 and an aeration device 4. The aeration device 4 uses a microporous aeration head to ensure continuous aeration and thorough mixing of the solution in the reactor. In the middle of the reactor main body, 1 / 3 of the volume of K5 filler is fixed by a microporous plate as the MBBR carrier 9, which not only provides a carrier for biofilm growth but also has the ability to adsorb ammonia ions. The upper part of the reactor main body is installed with an MBR membrane assembly 10, which uses hollow fiber membranes with a pore size of 0.1 μm. The water outlet of the MBR membrane assembly 10 is connected to the water outlet 1 of the reactor, and the water is driven out by suction through the drainage pump 2 installed at the water outlet 1. Since the volume of microorganisms is large, they cannot pass through the filter membrane of the MBR membrane assembly 10, thereby allowing the functional bacteria (direct ammonia-oxidizing functional bacteria) to be retained in the reactor. A vacuum gauge 3 is provided between the drainage pump 2 and the water outlet of the MBR membrane assembly 10 for real-time monitoring of membrane fouling. The top of the reactor main body is also provided with an overflow port 7, and the bottom is provided with a sludge discharge port 8 and an influent inlet 6. The influent inlet 6 is installed with an influent pump 5.

[0081] In the start-up phase of the MBBR-MBR reactor, ammonia-nitrogen wastewater, sodium succinate and direct ammonia-oxidizing functional bacteria Acinetobacter sp. SC3T (NCBI:txid1820089) were added into the MBBR-MBR reactor, and no activated sludge was inoculated to start in a continuous flow mode; in the start-up phase, the dissolved oxygen concentration in the MBBR-MBR reactor was controlled at 3-6 mg / L, the temperature was controlled at 27-33℃, the ammonia-nitrogen concentration was controlled at 200 mg / L, and the addition amount of sodium succinate was controlled at 1.8 g / L.

[0082] After the MBBR-MBR reactor completed the start-up phase and ran stably, simulated wastewater was continuously fed into the reactor for treatment; during the wastewater treatment, the reactor was continuously aerated, the dissolved oxygen concentration was controlled at 3-6 mg / L, and the running temperature was controlled at 27-33℃. The treatment effect of the reactor was evaluated by monitoring the COD and ammonia-nitrogen concentration in the effluent, and the results are shown in Table 1.

[0083] Example 2

[0084] The structure of the MBBR-MBR reactor used in this example is shown in Figure 2 The difference between the reactor of this example and the reactor of Example 1 is that the reactor body is a 2L cuboid container, and the MBBR carrier 9 is replaced with K1 filler The MBR membrane assembly 10 uses flat sheet membranes.

[0085] The other operating conditions are the same as those of Example 1, and the treatment effect of the reactor is evaluated, and the results are shown in Table 1.

[0086] Example 3

[0087] The structure of the MBBR-MBR reactor used in this example is shown in Figure 3 The difference between the reactor of this example and the reactor of Example 1 is that the reactor body is a column reactor with a length-diameter ratio of 5, and the SBR mode of discontinuous aeration is used to form aerobic granular sludge.

[0088] The other operating conditions are the same as those of Example 1, and the treatment effect of the reactor is evaluated, and the results are shown in Table 1.

[0089] Example 4

[0090] The structure of the MBBR-MBR reactor used in this example is shown in Figure 4 The difference between the reactor of this example and the reactor of Example 1 is that the MBR membrane assembly 10 is connected to the reactor body.

[0091] The other operating conditions are the same as those of Example 1, and the treatment effect of the reactor is evaluated, and the results are shown in Table 1.

[0092] Example 5

[0093] The structure of the MBBR-MBR reactor used in this example is shown in Figure 5 Figure 2, which differs from the reactor of Example 1 in that the aeration device 4 uses a hollow fiber membrane for bubbleless aeration, and the MBR membrane assembly 10 is connected to the outside of the reactor body.

[0094] The other operating conditions are the same as in Example 1, and the treatment effect of the reactor is evaluated, with the results shown in Table 1.

[0095] Example 6

[0096] The structure of the MBBR-MBR reactor used in this example is shown in Figure 6 Figure 2, which differs from the reactor of Example 1 in that the MBBR carrier 9 is replaced with a mixture of K1 filler and K5 filler, with a volume ratio of 1:1.

[0097] The other operating conditions are the same as in Example 1, and the treatment effect of the reactor is evaluated, with the results shown in Table 1.

[0098] Table 1 Summary of COD removal efficiency and nitrogen removal performance results of the reactors of Examples 1-6

[0099]

[0100] The above description is only preferred embodiments of the present application, and it should be noted that for those skilled in the art, without departing from the principles of the present application, a number of improvements and refinements can be made, which should also be considered within the scope of protection of the present application.

Claims

1. A method for treating ammonia nitrogen wastewater, characterized in that, Ammonia nitrogen wastewater is treated in an MBBR-MBR reactor; The MBBR-MBR reactor includes: a reactor body with an inlet, an outlet and a sludge discharge outlet; an MBBR carrier and an aeration device disposed within the reactor body; and an MBR membrane module connected to the outlet of the reactor body, disposed within the reactor body or connected to the outside of the reactor body. The specific process of the MBBR-MBR reactor start-up phase includes: Ammonia nitrogen wastewater, sodium succinate, and Acinetobacter sp. SC3T, a direct ammonia oxidation functional bacteria, are added to the MBBR-MBR reactor. No activated sludge is inoculated. The reactor is started up using either aeration or continuous flow. During the start-up phase, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1~10 mg / L, the temperature is controlled at 25~35℃, the ammonia nitrogen concentration is controlled at 150~300 mg / L, and the amount of sodium succinate added is controlled at 1~3 g / L. After the MBBR-MBR reactor has completed the start-up phase and is operating stably, the treatment load of ammonia nitrogen wastewater is gradually increased.

2. The processing method according to claim 1, characterized in that, The MBBR carrier is a K1 plastic carrier and / or a K5 plastic carrier.

3. The processing method according to claim 1, characterized in that, The MBBR carrier is filled in the reactor body in an amount that accounts for 1 / 4 to 1 / 2 of the reactor body volume.

4. The processing method according to claim 3, characterized in that, The MBBR carrier is filled in a volume of 1 / 3 of the reactor body.

5. The processing method according to claim 1, characterized in that, The filter membrane of the MBR membrane module has a pore size of 0.05~0.2μm.

6. The processing method according to claim 5, characterized in that, The filter membrane of the MBR membrane module has a pore size of 0.1 μm.

7. The processing method according to claim 1, characterized in that, The reactor body is equipped with a water inlet pump.

8. The processing method according to claim 1, characterized in that, The reactor body is equipped with a drain pump and a vacuum gauge at its outlet.

9. The processing method according to claim 1, characterized in that, The reactor body is also equipped with an overflow port.

Images