Ammonia-nitrogen wastewater treatment method

Abstract

The invention belongs to the field of wastewater treatment, and particularly relates to an ammonia-nitrogen wastewater treatment method which is characterized in that ammonia-nitrogen wastewater treatment is carried out in an MBBR-MBR reactor, and the specific process of the MBBR-MBR reactor starting stage comprises the following steps: adding ammonia-nitrogen wastewater, sodium succinate and direct ammoxidation functional bacteria Acinetobacter sp.SC3T into the MBBR-MBR reactor, and not inoculating activated sludge; in the starting stage, the concentration of dissolved oxygen in the MBBR-MBR is controlled to be 1-10 mg / L, the temperature is controlled to be 25-35 DEG C, the concentration of ammonia nitrogen is controlled to be 150-300 mg / L, and the addition amount of sodium succinate is controlled to be 1-3 g / L. The method provided by the invention effectively overcomes the defects that the cost is increased and the effect is unstable due to the fact that direct ammoxidation functional bacteria are easy to lose and need to be fed regularly, and has an excellent removal effect on high-ammonia-nitrogen organic matter wastewater.

Description

Technical Field

[0001] The invention belongs to the field of wastewater treatment, and in particular relates to a method for treating ammonia nitrogen wastewater. Background Art

[0002] Existing biological denitrification technologies mainly rely on the coupling of nitrification and denitrification processes, and remove ammonia nitrogen by consuming a large amount of oxygen and an external carbon source. This method is widely used in the treatment of low-concentration ammonia nitrogen wastewater, but its operation is complicated, the system occupies a large area, and its efficiency in the treatment of high-concentration ammonia nitrogen and organic wastewater is low. Nitrifying bacteria are easily affected by environmental changes and have poor shock resistance, resulting in fluctuations in the system's denitrification efficiency. In addition, the denitrification process requires an external carbon source to maintain the carbon-nitrogen ratio, which increases operating costs.

[0003] In response to the shortcomings of existing technologies, recent studies have shown that the microbial direct ammonia oxidation (Dirammox) process is a new ammonia nitrogen removal pathway that can directly convert ammonia nitrogen into nitrogen gas under aerobic conditions through functional bacteria such as Alcaligenes. This pathway does not rely on the multi-stage treatment steps of traditional nitrification / denitrification, and can significantly reduce the complexity and footprint of the system. In addition, Dirammox functional bacteria have strong growth ability and environmental adaptability, and can still efficiently remove pollutants under conditions of high ammonia nitrogen and organic matter coexistence, showing great application potential.

[0004] However, how to maintain the high abundance and stability of Dirammox functional bacteria is a key issue in the engineering application of this technology. Summary of the invention

[0005] In view of this, the purpose of the present invention is to provide a method for treating ammonia nitrogen wastewater. The present invention combines the MBBR (moving bed biofilm reactor) coupling MBR (membrane bioreactor) process with the microbial direct ammonia oxidation process (Dirammox), effectively overcoming the shortcomings of direct ammonia oxidation functional bacteria that are easy to lose and require regular dosing of bacteria, resulting in increased costs and unstable effects, and has excellent removal effect on high ammonia nitrogen organic wastewater.

[0006] The present invention provides a method for treating ammonia nitrogen wastewater, and the ammonia nitrogen wastewater is treated in an MBBR-MBR reactor;

[0007] The MBBR-MBR reactor comprises: a reactor body, on which a water inlet, a water outlet and a mud outlet are arranged; an MBBR carrier and an aeration device arranged in the reactor body; and an MBR membrane assembly, wherein the MBR membrane assembly is connected to the water outlet of the reactor body and is arranged in the reactor body or connected to the outside of the reactor body;

[0008] The specific process of the MBBR-MBR reactor startup phase includes:

[0009] Adding ammonia nitrogen wastewater, sodium succinate and direct ammonia oxidizing functional bacteria Acinetobacter sp.SC3T into the MBBR-MBR reactor, without inoculating activated sludge, and starting in aeration or continuous flow mode;

[0010] During the startup phase, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35° 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.

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

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

[0013] Preferably, the amount of the MBBR carrier loaded 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, the reactor body is also provided with an overflow port.

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

[0020] Compared with the prior art, the present invention provides a method for treating ammonia nitrogen wastewater, and the ammonia nitrogen wastewater is treated in an MBBR-MBR reactor; the MBBR-MBR reactor comprises: a reactor body, on which a water inlet, a water outlet and a mud outlet are arranged; an MBBR carrier and an aeration device arranged in the reactor body; and an MBR membrane assembly, wherein the MBR membrane assembly is connected to the water outlet of the reactor body, and is arranged in the reactor body or externally connected to the reactor body; the specific process of the startup phase 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, without inoculating activated sludge, and starting in a suffocating or continuous flow mode; in the startup phase, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35° 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 invention combines MBBR (moving bed biofilm reactor) coupling MBR (membrane bioreactor) process with microbial direct ammonia oxidation process (Dirammox) to develop a method that can efficiently and stably treat high ammonia nitrogen wastewater. The key point of this method is to use Dirammox functional bacteria Acinetobacter sp.SC3T as the core functional bacterial community, and achieve its enrichment and interception in the reactor through MBBR-MBR technology, solving the problem that the traditional nitrification / denitrification process has poor treatment effect on high ammonia nitrogen wastewater. In addition, the present invention is adapted to higher influent ammonia concentrations, inhibits the growth of other competitive microorganisms, ensures the dominant position of Dirammox functional bacteria in the system, and effectively improves denitrification efficiency and system stability. Ultimately, it is possible to achieve efficient denitrification and organic matter removal under high ammonia nitrogen and high organic load conditions. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying creative work.

[0022] Figure 1 is a schematic structural diagram of an MBBR-MBR reactor provided in Example 1 of the present invention;

[0023] Figure 2 is a schematic structural diagram of an MBBR-MBR reactor provided in Example 2 of the present invention;

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

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

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

[0027] Figure 6 It is a schematic diagram of the structure of the MBBR-MBR reactor provided in Example 6 of the present invention.

[0028] Explanation of the reference numerals: 1 is the water outlet, 2 is the drainage pump, 3 is the vacuum gauge, 4 is the aeration device, 5 is the water inlet pump, 6 is the water inlet, 7 is the overflow port, 8 is the mud discharge port, 9 is the MBBR carrier, and 10 is the MBR membrane assembly. DETAILED DESCRIPTION

[0029] The technical solutions in the embodiments of the present invention are described clearly and completely below. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0030] The present invention provides a method for treating ammonia nitrogen wastewater, and the ammonia nitrogen wastewater is treated in an MBBR-MBR reactor;

[0031] The MBBR-MBR reactor comprises: a reactor body, on which a water inlet, a water outlet and a mud outlet are arranged; an MBBR carrier and an aeration device arranged in the reactor body; and an MBR membrane assembly, wherein the MBR membrane assembly is connected to the water outlet of the reactor body and is arranged in the reactor body or connected to the outside of the reactor body;

[0032] The specific process of the MBBR-MBR reactor startup phase includes:

[0033] Adding ammonia nitrogen wastewater, sodium succinate and direct ammonia oxidizing functional bacteria Acinetobacter sp.SC3T into the MBBR-MBR reactor, without inoculating activated sludge, and starting in aeration or continuous flow mode;

[0034] During the startup phase, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35° 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.

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

[0036] (1) Sample collection:

[0037] Take an appropriate amount of activated sludge from the sewage treatment plant and determine the basic parameters of the sludge; perform PCR gene determination on the batch of sludge to detect whether the batch of sludge contains the Dirammox gene.

[0038] (2) Domestication and cultivation:

[0039] In a sterile environment, take 100mL of sludge mixed liquid with Dirammox gene dnfA and place it in a conical flask and shake it by hand for 10 minutes. After the granular sample is broken, take 10mL and inoculate it into 3 100mL HNM liquids respectively; culture at 28-30℃ for 24h. When the culture time is over, determine the indicators such as ammonia nitrogen, nitrate nitrogen and nitrite nitrogen, and carry out the second round of domestication. The domestication inoculation amount is 2%, and the subsequent steps are consistent with the first round of domestication; after the water quality index is determined, carry out the third domestication with an inoculation amount of 2%, and determine the water quality index; after the three rounds of domestication are completed, take samples of three types of culture medium for dnfA gene determination;

[0040] HNM medium: (NH4)2SO40.66g (5mM), sodium succinate 2.84g, KH2PO40.5g, MgSO4·7H2O0.2g, Na2HPO40.5g, trace element solution 2.00mL, pH=7.5;

[0041] 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 ·4H2O1.10g, CuSO4·5H2O 1.60g, CoCl2·6H2O 1.60g, pH=6.0;

[0042] Solid culture medium: The composition is the same as that of liquid culture medium, plus 1.5% agar.

[0043] (3) Sample dilution:

[0044] Take 20 mL of the culture medium after the culture is completed, rinse with PBS buffer, centrifuge at 4000 r / min for 2 min, repeat three times, and resuspend with PBS buffer to make a bacterial suspension; then take 10 mL of the bacterial suspension and add it to a conical flask containing 90 mL of sterile water, pipette it three times, shake it by hand for 10 min, dilute it to a bacterial solution with a concentration of 10-1, and then dilute it by 10 -2 , 10 -3 , 10 -4 Concentration of bacterial solution.

[0045] (4) Plate separation:

[0046] Take 30 plates and draw 10 samples in sequence under sterile operation. -2 , 10 -3 , 10 -4 0.5mL of bacterial solution of different concentrations was inoculated onto the plate; there were three types of culture media, each with three concentrations, each with three plates, and the last one was a control; cultured at 28-30°C for 24-48h; then a single colony was picked out from the plate where culture had ended using an inoculation loop and inoculated onto a new plate, and the operation was repeated until pure bacteria appeared; if the colonies on the plate grew densely, the bacterial solution was continued to be diluted.

[0047] (5) Strain identification:

[0048] The cultivated strain was tested for dnf gene cluster, and the result showed that the strain was the strain numbered txid1820089 in the NCBI database.

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

[0050] In the present invention, during the startup phase, the temperature in the MBBR-MBR reactor can be specifically controlled to be 25°C, 26°C, 27°C, 28°C, 29°C, 30°C, 31°C, 32°C, 33°C, 34°C or 35°C.

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

[0052] In the present invention, during the startup phase, the amount of sodium succinate added in the MBBR-MBR reactor can be specifically 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 invention, the water inlet is preferably located at the bottom of the reactor body to ensure that the incoming water is in full contact with the microorganisms at the bottom.

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

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

[0056] In the present invention, the pore size of the filter membrane of the MBR membrane assembly is preferably 0.05-0.2 μm, more preferably 0.1 μm, to ensure that the direct ammonia oxidizing functional bacteria are fully retained.

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

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

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

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

[0061] In the present invention, after the MBBR-MBR reactor completes the startup phase and runs stably, it is preferred to gradually increase the treatment load of ammonia nitrogen wastewater.

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

[0063] (1) The reactor includes key units such as the reactor body, MBBR carrier, MBR membrane assembly, aeration device, water inlet / outlet and pump, vacuum gauge, overflow port, and mud outlet. These components ensure the stable operation and efficient denitrification of the reactor in the treatment of high ammonia nitrogen wastewater.

[0064] (2) The outlet of the reactor is passed through the MBR membrane assembly to retain microorganisms, ensuring that the Dirammox functional bacteria in the reactor will not be lost and maintaining efficient denitrification capacity.

[0065] (3) The reactor should provide sufficient mixed growth space for the bacterial community to ensure that the Dirammox functional bacteria can form a biofilm by attaching to the MBBR carrier, thereby improving the biomass and denitrification performance in the system.

[0066] (4) The MBR membrane components ensure that the Dirammox functional bacteria are fully retained in the reactor to promote the formation of flocs, particles or biofilms, while extending the sludge age and improving the stability and treatment capacity of the reactor.

[0067] (5) By installing a vacuum gauge at the outlet of the reactor, the membrane fouling condition can be monitored in real time, and then cleaning and adjustment can be carried out in time according to the membrane fouling condition to ensure the long-term stable operation of the system.

[0068] (6) The aeration device can be used to accurately adjust the dissolved oxygen content in the reactor to ensure that the Dirammox functional bacteria maintain efficient ammonia oxidation capacity in the reactor.

[0069] (7) The sludge discharge port can be used to adjust the sludge retention time (SRT) in the reactor to prevent the occurrence of sludge bulking problems and ensure the stable operation of the reactor.

[0070] (8) The inlet / outlet water pump can be used to control the discharge volume at the outlet to be consistent with the water inlet volume, thereby maintaining the volume balance of the reactor and ensuring that the system can operate continuously and stably.

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

[0072] (1) Inoculation and startup: In the startup phase of the reactor, the traditional domesticated activated sludge is not inoculated, but the pure cultured Dirammox functional bacteria Acinetobacter sp. SC3T is directly inoculated. In this phase, the environmental conditions, such as dissolved oxygen and temperature, are strictly controlled to promote the rapid enrichment and efficient biofilm formation of Dirammox functional bacteria.

[0073] (2) Bacterial flora retention and attachment growth: Through the physical retention of the MBR membrane components, Dirammox functional bacteria can achieve rapid attachment to the MBBR carrier in the reactor and maintain a high biomass. With the advantages of fast growth rate and strong environmental adaptability, Dirammox functional bacteria can maintain a high abundance state in the reactor to ensure efficient ammonia nitrogen removal.

[0074] (3) The promoting effect of high ammonia nitrogen: The high ammonia nitrogen concentration in the initial influent and the exogenous addition of sodium succinate as the optimal carbon source in the initial stage promote the rapid growth of Dirammox functional bacteria Acinetobacter sp. SC3T. The high ammonia nitrogen concentration 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 denitrification efficiency and maintains the stability and efficiency of the system.

[0075] (4) Biofilm formation: As the reactor runs, nutrients enter the reactor through the influent, and the Dirammox functional bacteria use these nutrients to 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 ability to treat 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 process of high ammonia nitrogen and high COD wastewater, significantly simplifying the traditional denitrification process and reducing treatment costs.

[0077] For the purpose of greater clarity, the invention is described in detail through the following embodiments.

[0078] Example 1

[0079] The structure of the MBBR-MBR reactor used in this example is as follows Figure 1 The specific instructions are as follows:

[0080] The main body of the reactor is a cylindrical reactor with a volume of 1L, with a water inlet 6 and an aeration device 4 at the bottom. The aeration device 4 uses a microporous aeration head to ensure continuous aeration and sufficient mixing of the solution in the reactor. The middle part of the reactor body is fixed with 1 / 3 volume of K5 filler through a microporous plate. As an MBBR carrier 9, K5 filler not only provides a carrier for the growth of biofilm, but also has the ability to adsorb ammonia ions; an MBR membrane assembly 10 is installed on the upper part of the reactor body, and the MBR membrane assembly 10 adopts a hollow fiber membrane with a membrane pore size of 0.1μm; the water outlet of the MBR membrane assembly 10 is connected to the water outlet 1 of the reactor, and the water outlet is driven by suction through a drainage pump 2 installed at the water outlet 1; due to the large size of microorganisms, they cannot pass through the filter membrane of the MBR membrane assembly 10, so that the functional bacteria (direct ammonia oxidizing functional bacteria) can 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, which is used to monitor the membrane contamination in real time. When the membrane is blocked, it can be cleaned in time; an overflow port 7 is also provided on the top of the reactor body, and a mud discharge port 8 and a water inlet 6 are also provided at the bottom, and an inlet pump 5 is installed at the water inlet 6.

[0081] During the startup phase of the MBBR-MBR reactor, ammonia nitrogen wastewater, sodium succinate and direct ammonia oxidizing functional bacteria Acinetobacter sp.SC3T (NCBI: txid1820089) are added to the MBBR-MBR reactor, activated sludge is not inoculated, and the reactor is started in a continuous flow mode; during the startup phase, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 3-6 mg / L, the temperature is controlled at 27-33° C., the ammonia nitrogen concentration is controlled at 200 mg / L, and the amount of sodium succinate added is controlled at 1.8 g / L.

[0082] After the MBBR-MBR reactor completes the startup phase and runs stably, simulated sewage is continuously introduced into the reactor for treatment; during sewage treatment, the reactor adopts continuous aeration, the dissolved oxygen concentration is controlled at 3-6 mg / L, and the operating temperature is controlled at 27-33°C. The treatment effect of the reactor is evaluated by monitoring the COD and ammonia nitrogen concentrations 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 as follows Figure 2 As shown, the difference between the reactor in Example 1 is that the reactor body is a 2L rectangular container, and the MBBR carrier 9 is replaced by K1 filler. The MBR membrane module 10 uses a flat membrane.

[0085] The other operating conditions were the same as those in Example 1. The treatment effect of the reactor was 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 as follows Figure 3 As shown, the difference between it and the reactor of Example 1 is that the reactor body is a columnar reactor with a long diameter of 5, and it is operated in a discontinuous aeration SBR mode to form aerobic granular sludge.

[0088] The other operating conditions were the same as those in Example 1. The treatment effect of the reactor was 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 as follows Figure 4 As shown, the difference between it and the reactor of Example 1 is that the MBR membrane assembly 10 is externally connected to the reactor body.

[0091] The other operating conditions were the same as those in Example 1. The treatment effect of the reactor was 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 as follows Figure 5 As shown, the difference between it and the reactor of Example 1 is that the aeration device 4 uses a hollow fiber membrane for bubble-free aeration, and the MBR membrane assembly 10 is externally connected to the reactor body.

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

[0095] Example 6

[0096] The structure of the MBBR-MBR reactor used in this example is as follows Figure 6 As shown, the difference between the reactor of Example 1 is that the MBBR carrier 9 uses a mixture of K1 filler and K5 filler, and the volume ratio of the two is 1:1.

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

[0098] Table 1 Summary of COD removal efficiency and denitrification performance of reactors in Examples 1 to 6

[0099]

[0100] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principle of the present invention. These improvements and modifications should also be regarded as the scope of protection of the present invention.

Claims

1. A method for treating ammonia nitrogen wastewater, characterized in that: Ammonia nitrogen wastewater treatment in MBBR-MBR reactor; The MBBR-MBR reactor comprises: a reactor body, on which a water inlet, a water outlet and a mud outlet are arranged; an MBBR carrier and an aeration device arranged in the reactor body; and an MBR membrane assembly, wherein the MBR membrane assembly is connected to the water outlet of the reactor body and is arranged in the reactor body or connected to the outside of the reactor body; The specific process of the MBBR-MBR reactor startup phase includes: Adding ammonia nitrogen wastewater, sodium succinate and direct ammonia oxidizing functional bacteria Acinetobacter sp.SC3T into the MBBR-MBR reactor, without inoculating activated sludge, and starting in aeration or continuous flow mode; During the startup phase, the dissolved oxygen concentration in the MBBR-MBR reactor is controlled at 1-10 mg / L, the temperature is controlled at 25-35° 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.

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 amount of the MBBR carrier loaded in the reactor body accounts for 1 / 4 to 1 / 2 of the volume of the reactor body.

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

5. The processing method according to claim 1, characterized in that: The pore size of the filter membrane of the MBR membrane assembly is 0.05-0.2 μm.

6. The processing method according to claim 5, characterized in that: The pore size of the filter membrane of the MBR membrane assembly is 0.1 μm.

7. The processing method according to claim 1, characterized in that: A water inlet pump is installed at the water inlet of the reactor body.

8. The processing method according to claim 1, characterized in that: The water outlet of the reactor body is equipped with a drainage pump and a vacuum gauge.

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

10. The processing method according to claim 1, characterized in that: After the MBBR-MBR reactor completes the startup phase and runs stably, the treatment load of ammonia nitrogen wastewater is gradually increased.

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