Method for rapidly stabilizing and improving denitrification efficiency of shortcut nitrification coupled anaerobic ammonia oxidation (PN / A) system

Abstract

The invention provides a method for rapidly stabilizing and improving the denitrification efficiency of a shortcut nitrification coupled anaerobic ammonia oxidation (PN / A) system, and aims to stabilize a continuous packed fixed bed PN / A reactor in a mainstream state and improve the denitrification performance of the continuous packed fixed bed PN / A reactor at the same time. 2.0 mg N / L of free nitrous acid (FNA) and 30.0 mg N / L of free ammonia (FA) are used for treating and inhibiting nitrite oxidizing bacteria (NOB) in the system so as to reduce the concentration of nitrate nitrogen (NO3 <->-N) in effluent, and 3.0 mg N / L of FNA needs to be used for further inhibiting the nitrate nitrogen (NO3 <->-N) when the high aeration flow speed (30 mL / min) is adopted. Experiments show that by means of the method, nitrate nitrogen in effluent is reduced from 15.64 mg N / L to 3.10 mg N / L, and the total nitrogen removal rate is increased from 143.43 mg N / L / d to 589.25 mg N / L / d and is increased by 4.11 times. Besides, the reactor used in the invention is a continuous filler fixed bed reactor, so that the sewage treatment load is improved, the sludge biomass retention capability is good, the operation is simple, and the method is environment-friendly. The overall efficiency of the sewage treatment system is greatly improved, the stability of the continuous PN / A system is also improved, and the continuous PN / A system is suitable for sewage treatment scenes with efficient denitrification requirements.

Description

Technical Field

[0001] This invention belongs to the field of wastewater treatment technology, specifically relating to a method for rapidly stabilizing and improving the denitrification efficiency of a continuous packed bed PN / A system under mainstream conditions. Technical Background

[0002] Anaerobic ammonia oxidation (Anammox) technology is a highly efficient nitrogen removal process that has attracted much attention in the field of wastewater treatment in recent years. Its core mechanism is that anaerobic ammonia oxidizing bacteria decompose NH4+ under anaerobic conditions. + -N and NO2 - -N is simultaneously converted into nitrogen gas (N2), achieving direct removal of nitrogen from wastewater. This technology overcomes the limitations of traditional biological nitrogen removal, which relies on aerobic nitrification and anoxic denitrification in steps, and has significant technological advantages. However, under normal circumstances, actual wastewater does not contain nitrite, resulting in a lack of substrate for anaerobic ammonia oxidation and its inability to proceed. The PN / A technology, by constructing a coupled system of "short-cut nitrification-anaerobic ammonia oxidation," utilizes the sensitive regulation of environmental factors such as dissolved oxygen (DO) and temperature by ammonia-oxidizing bacteria (AOB) to convert ammonia nitrogen (NH4) into nitrogen gas. + -N is selectively oxidized to NO2 - -N (instead of nitrification to NO3) - The PN / A process provides the necessary substrate for the Anammox reaction, forming a closed metabolic loop for autotrophic denitrification. Compared to the traditional nitrification-denitrification process, the PN / A process can reduce organic carbon source requirements by 100%, sludge production by 90%, and oxygen consumption by 60%, significantly reducing energy consumption and substantially lowering denitrification costs.

[0003] The denitrification rate of a PN / A denitrification system hinges on whether the short-cut nitrification (PN) stage can achieve NO2 removal. - Stable enrichment of -N. Under aerobic conditions, AOB will partially enrich NH4+. + -N is nitrated into NO2 in a short path. - -N, anaerobic ammonia oxidizing bacteria (AnAOB) will convert the remaining NH4+ into nitrogen. + -N and the generated NO2 - -N is oxidized to harmless N2 and produces a small amount of NO3. - -N. AnAOB and AOB form a symbiotic relationship of metabolic interaction; the excessive proliferation of nitrite-oxidizing bacteria (NOB) will increase NO2. - -N is oxidized to NO3 - -N disrupts the substrate supply of Anammox, therefore, it is necessary to suppress the niche competition of NOB through the regulation of environmental parameters (such as DO≤0.5mg / L, FA / FNA, etc.) to ensure the dominant position of AOB and AnAOB.

[0004] To address these challenges and improve the nitrogen removal rate of the PN / A system while maintaining its stability, effective strategies are crucial. Among these, the differentiated toxicity effects of FA and FNA on NOB and AOB, and the creation of a short-range nitrification environment favorable to AOB dominance, are particularly important, thus providing a stable source of NO2 for AnAOB. - -N substrates. FA technology inhibits NOB nitrification activity by lowering the pH of the reaction system, increasing the acidity of the environment. AOB, on the other hand, is more adaptable to acidic environments and is less inhibited. FNA technology, however, promotes the formation of free nitrite (HNO2) by maintaining a high nitrite concentration in the reaction system and appropriately adjusting the pH. Free nitrite is considered a toxic substance of NOB and can effectively inhibit its activity by interfering with its metabolic processes. In the PN / A process, an appropriate amount of FNA can selectively inhibit NOB growth while having little impact on AOB, thereby increasing the nitrite concentration and providing better substrate conditions for the anaerobic ammonium oxidation reaction. Both FA and FNA technologies inhibit NOB growth, stopping the nitrification stage at NO2. - The generation of -N prevents NO2. - -N is further oxidized, thus providing a reaction substrate for the Anammox process.

[0005] Achieving efficient nitrogen removal and NOB suppression in mainstream continuous packed fixed-bed PN / A reactors faces multiple challenges. Low temperature (10-25℃) and low NH4 content are key requirements. + -N (50-100 mg N / L) environment significantly inhibits the activity of AOB and AnAOB, while NOB proliferates easily under high aeration conditions due to its high oxygen affinity. Mass transfer resistance of biofilm and uneven spatial distribution of bacterial community in fixed bed further limit reaction efficiency.

[0006] Therefore, to address the above situation, a method needs to be developed that can rapidly inhibit the activity of NOB while ensuring a stable supply of NO2 in the system. - The method of supplying nitrogen and performing efficient nitrogen removal is of vital importance for improving wastewater treatment efficiency in mainstream environments. Summary of the Invention

[0007] In view of this, the object of the present invention is to provide a method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system. This method aims to rapidly suppress the activity of NOB in the system and provide stable NO2 by using FNA and FA treatment in a continuous packed fixed-bed PN / A reactor. - -N supply ensures long-term stable and efficient operation, thereby improving the overall efficiency and environmental friendliness of wastewater treatment.

[0008] Specifically, this invention provides a method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system, comprising the following steps:

[0009] S1. The reactor is inoculated with anaerobic ammonia oxidation packing biofilm sludge, and the initial flow rate of aeration (air) is controlled at 10 mL / min, and the influent flow rate is 5 mL / min.

[0010] S2, when the reactor ammonia nitrogen (NH4) + The effluent concentration of NO3- (N) remained stable below 40 mg N / L. - -N was maintained at 15 mg N / L for 1 day, followed by three FNA treatments at 2.0 mg N / L, with each FNA treatment spaced 2 days apart.

[0011] S3. During the three 2.0 mg N / L FNA treatments in step S2, the NH4+ effluent from the reactor during this period... + -N concentration increased slightly, NO3 in effluent - -N concentration decreased to below 7 mg N / L. NO3 concentration was expected to decrease after three FNA treatments. - After maintaining the -N concentration in the effluent below 10 mg N / L for T3 days, three FA treatments of 30.0 mg N / L were performed, with an interval of T4 days between each FA treatment.

[0012] S4. During the three FA treatments at 30.0 mg N / L in step S3, the NH4+ effluent from the reactor during this period... + -N concentration fluctuated slightly, NO3 in effluent - After the -N concentration was stabilized below 10 mg N / L and maintained for T5 days, the aeration rate was increased from 10 mL / min to 30 mL / min.

[0013] S5. After increasing the aeration flow rate in step S4, NH4 + -N concentration decreased to 2 mg N / L, and NO3 - When the -N concentration rises to 12 mg N / L, three FNA treatments of 3.0 mg N / L are performed, with each treatment spaced 6 days apart.

[0014] S6. During the three 3.0 mg N / L FNA treatments in step S5, the NH4+ effluent from the reactor during this period... + -N concentration increased slightly, NO3 in effluent - -N concentration decreased to below 5 mg N / L. After treatment, the effluent NH4+... + -N concentration remained stable below 2 mgN / L and NO3 - When the -N concentration is stable below 5 mg N / L, it indicates that the FNA and FA treatment was successful.

[0015] In some specific embodiments of the present invention, the FNA is provided by NaNO2.

[0016] In some specific embodiments of the present invention, FA is provided by NH4CI.

[0017] In some specific embodiments of the present invention, the FNA treatment time is 4 hours, during which the pH is 6.0±0.1.

[0018] In some specific embodiments of the present invention, the FA treatment time is 4 hours, during which the pH is 8.0±0.1.

[0019] In some specific embodiments of the present invention, T1 = 10, T2 = 7, T3 = 7, T4 = 7, T5 = 7, and T6 = 7.

[0020] In some specific embodiments of the present invention, the reactor is a continuous packed fixed-bed reactor.

[0021] In some specific embodiments of the present invention, the sludge in the reactor is the packing biofilm sludge from the mainstream anaerobic ammonia oxidation wastewater treatment system.

[0022] In some specific embodiments of the present invention, the biofilm sludge in the mainstream anaerobic ammonia oxidation wastewater treatment system in the reactor has the following characteristics: the reactor for cultivating anaerobic ammonia oxidation fluidized bed packing is an SBR reactor, the operating environment is as follows: influent ammonia nitrogen concentration 45±5mg N / L, hydraulic retention time 6h, operating pH 7.5, temperature room temperature, dissolved oxygen less than 0.5mg / L, and effluent ammonia nitrogen concentration stably less than 2mg / L.

[0023] The present invention has the following significant advantages and effects compared with the prior art:

[0024] 1. This invention has been successfully controlled in a continuous packed fixed bed reactor under mainstream conditions, overcoming the shortcomings of this type of reactor such as weak shock resistance and difficulty in parameter adjustment, and has high wastewater treatment capacity and significantly improved denitrification efficiency.

[0025] 2. Under the mainstream conditions, after treatment with FNA and FA, NOB in the system is effectively suppressed. Further, the use of high-concentration FNA after aeration significantly increases the denitrification rate of the system.

[0026] 3. Optimize aeration control: The initial aeration flow rate is 10 mL / min, allowing sufficient aeration space to allow the system to adapt to aeration while reducing excessive NOB proliferation. Subsequently, the aeration flow rate is increased to 30 mL / min, resulting in a dissolved oxygen concentration of approximately 0.5 mg / L in the system. This maximizes AOB activity while minimizing the inhibition of AnAOB activity due to excessive aeration.

[0027] 4. Stabilizing the dominant position of anaerobic ammonia oxidizing bacteria: Through dual treatment with FNA and FA, the activity of NOB in the system was further inhibited. The improved denitrification performance under high concentration FNA treatment indicates that AnAOB occupies a dominant position in the system.

[0028] 5. Environmentally friendly: FNA and FA are relatively environmentally friendly treatment methods that do not introduce new harmful substances and have a small impact on the environment, thus meeting environmental protection requirements.

[0029] In summary, the method for rapidly restoring the denitrification efficiency of an anaerobic ammonia oxidation system provided by this invention effectively enhances the dominant position of anaerobic ammonia oxidizing bacteria, increases the denitrification rate and overall treatment efficiency of the system, while also improving the stability of the bacterial community, inhibiting the growth of harmful microorganisms, and is simple to operate and environmentally friendly, demonstrating significant technical effects and application prospects. Attached Figure Description

[0030] Appendix Figure 1 This is a photograph of the packing biofilm sludge in the mainstream anaerobic ammonia oxidation wastewater treatment system used in the embodiments of the present invention.

[0031] Appendix Figure 2 This is an image of a continuous packed fixed-bed reactor constructed in an embodiment of the present invention.

[0032] Appendix Figure 3 This is a graph showing ammonia nitrogen monitoring data in a continuous reactor in an embodiment of the present invention.

[0033] Appendix Figure 4 This is a graph showing the monitoring data of nitrite nitrogen in a continuous reactor in an embodiment of the present invention.

[0034] Appendix Figure 5 This is a graph showing the monitoring data of nitrate nitrogen in a continuous reactor in an embodiment of the present invention.

[0035] Appendix Figure 6 This is a graph showing the monitoring data of total nitrogen removal rate and dissolved oxygen concentration in the system during the experiment in the continuous reactor in this embodiment of the invention. Detailed Implementation

[0036] The present invention will be further illustrated below with reference to specific embodiments. It should be understood that these embodiments are for illustrative purposes only and are not intended to limit the scope of the invention. Furthermore, it should be understood that after reading the teachings of this invention, those skilled in the art can make various alterations or modifications to the invention, and these equivalent forms also fall within the scope defined in this application.

[0037] Example 1: A method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system.

[0038] A method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system includes the following steps:

[0039] S1. Add anaerobic ammonia oxidation packing sludge to the reactor and simultaneously aerate (air) in the reactor. The initial flow rate is 10 mL / min, and aeration continues thereafter. The reactor influent flow rate is always 5 mL / min.

[0040] S2, when the reactor NH4 + -N concentration in effluent remained stable below 40 mg N / L, NO3 - After maintaining -N at 15 mg N / L for 10 days, three FNA treatments of 2.0 mg N / L were performed, each lasting 4 hours, with an interval of 7 days between treatments;

[0041] S3. During the three 2.0 mg N / L FNA treatments in step S2, the NH4+ effluent from the reactor during this period... + -N concentration increased slightly, NO3 in effluent - -N concentration dropped significantly to below 7 mg N / L. After three FNA treatments, NO3... - After the -N effluent concentration slightly rebounded and remained below 10 mg N / L for 7 days, three FA treatments of 30.0 mg N / L were performed, each lasting 4 hours, with an interval of 7 days between treatments.

[0042] S4. During the three FA treatments at 30.0 mg N / L in step S3, the NH4+ effluent from the reactor during this period... + -N concentration fluctuated slightly, NO3 in effluent - After the -N concentration was stabilized below 10 mg N / L for 7 days, the aeration rate was increased from 10 mL / min to 30 mL / min.

[0043] S5. After increasing the aeration flow rate in step S4, NH4 + -N concentration dropped significantly to 2 mg N / L, and NO3- concentration decreased significantly. -When the -N concentration rises to 12 mg N / L, three FNA treatments of 3.0 mg N / L are performed, each lasting 4 hours, with an interval of 7 days between treatments.

[0044] S6. During the three 3.0 mg N / L FNA treatments in step S5, the NH4+ effluent from the reactor during this period... + -N concentration will increase slightly, and NO3 in the effluent will... - -N concentration dropped significantly to below 5 mg N / L. The effluent NH4+ concentration will be released after treatment. + -N concentration remained stable below 2 mg N / L and NO3 in the effluent - When the -N concentration stabilizes below 5 mg N / L, it indicates that the FNA and FA treatment was successful.

[0045] Example 2: Testing of a method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-path nitrification coupled anaerobic ammonium oxidation (PN / A) system.

[0046] The required reactor is a continuous reactor, constructed from a 1.5L transparent acrylic cylinder with an inner diameter of 7cm, an outer diameter of 8cm, and a height of 40cm. Water enters from the bottom, and an outlet is located 1L above the bottom. The influent flow rate is maintained at 5mL / min throughout the experiment. The reactor is placed indoors at a temperature of 22–27℃, and is sealed at the top to isolate it from oxygen, with a small opening for sample measurement. Throughout the experiment, the pH of the influent is adjusted to 7.2±0.1 using 1mol / L HCl. The influent matrix contains the following components and concentrations:

[0047] KH2PO4 0.028 g·L -1 CaCl2·2H2O 0.185g·L -1 NaHCO3 1.68 g·L -1 MgSO4·7H2O 0.2 g·L -1 NH4 + -N 80mg·L -1 Trace element solution I 1 ml·L -1 Trace element solution II 1 ml·L -1 .

[0048] Trace element solution I includes: EDTA 5 g / L, FeSO4·7H2O 5 g / L

[0049] Trace element solution II includes: EDTA 15 g / L, H3BO3 0.011 g / L, MnCl2·4H2O 0.99 g / L, CuSO4·5H2O 0.25 g / L, ZnSO4·7H2O 0.43 g / L, NiCl2·6H2O 0.19 g / L, (NH4)6Mo7O24 ·4H2O0.16g / L, CoCl2·6H2O 0.24g / L, Na2SeO3·5H2O 0.1596g / L

[0050] The reactor was operated according to the aeration flow rate and influent flow rate in Table 1.

[0051] Table 1

[0052]

[0053] The reactor is processed according to the FNA and FA in Table 2.

[0054] Table 2

[0055]

[0056] Mainstream anaerobic ammonia oxidation fluidized bed packing: The reactor used for cultivation in this experiment was an SBR reactor, and the operating environment was an influent NH4+. + The nitrogen concentration was 45±5 mg / L, the hydraulic retention time was 6 h, the operating pH was 7.5, the temperature was room temperature, the dissolved oxygen was less than 0.5 mg / L, and the effluent ammonia nitrogen concentration was consistently less than 3 mg / L in the given environment. The sludge in this reactor can be considered the mainstream anaerobic ammonia oxidation fluidized bed packing sludge used in this experiment.

[0057] After filtration through a 0.45 μm water filter, ammonia nitrogen was determined using the N-Schönlein reagent colorimetric method, nitrite nitrogen was determined using the N-(1-naphthyl)-ethylenediamine spectrophotometric method, and nitrate nitrogen was determined using the ultraviolet spectrophotometric method. pH and dissolved oxygen were measured using a pH meter and a dissolved oxygen meter, respectively.

[0058] The total nitrogen removal rate (TNRR), total nitrogen removal efficiency (TNRE), FNA, and FA mentioned in the text are calculated using the following formulas.

[0059] TNRR=ΔC N / HRT (1)

[0060] In equation (1), ΔC N The difference in substance concentration between the influent and effluent (mg / L) is represented by HRT, which represents the hydraulic retention time (d).

[0061]

[0062] In equation (2), ΔC N The difference in substance concentration between the influent and effluent (mg / L) is represented by HRT, which represents the hydraulic retention time (d).

[0063]

[0064] In formula (3), [NO2] - [] represents the nitrite concentration, T represents the temperature, and pH represents the pH value inside the reactor.

[0065]

[0066] In formula (4), [NH4] + [] represents ammonium concentration, T represents temperature, and pH represents the pH value inside the reactor. Experimental results:

[0067] The influent and effluent concentrations of ammonia nitrogen, nitrite nitrogen, and nitrate nitrogen in the continuous reactor, the nitrogen removal / generation rate, the total nitrogen removal rate, and the dissolved oxygen concentration during the experiment are shown in the attached figures. Figure 3-6 As shown.

[0068] The reactor was first inoculated with anaerobic ammonia oxidation biofilm sludge from a mainstream wastewater treatment plant. Aeration was then carried out in the reactor for 10 days at an aeration rate of 10 mL / min. At this time, the NH4+ content in the reactor... + The nitrogen removal efficiency was 55.47±4.08%, and the total nitrogen removal rate (TNRR) was 200.68±30.91 mg N / L / d. At this point, the effluent NO3... - The -N concentration was significantly too high, at 14.15 ± 0.57 mg N / L, indicating that aeration caused NOB proliferation within the system, leading to the oxidation of NH4 by AOB. + -N was further oxidized by NOB to NO3. - -N makes Anammox require the substrate NO2 --N was competed for, affecting the Anammox process. Therefore, on day 11, a 2.0 mg N / L FNA treatment was performed, with each treatment lasting 4 hours, for three treatments, with an interval of 7 days between each treatment. The FNA treatment steps were as follows: 2 L of distilled water was placed in a 2 L beaker, the temperature was measured, and the required mass of NaNO2 was calculated according to formula (3). The NaNO2 was dissolved in the beaker, and the pH of the solution was adjusted to 6.0 using 1 mol / L HCl. After draining the inlet water in the reactor, the reactor was rinsed three times with this solution. After draining the reactor again, the inlet and outlet water holes were connected by a pump pipe, and a peristaltic pump was connected to achieve internal circulation. 1.2 L of the prepared FNA solution was slowly poured into the reactor, ensuring that the solution completely covered all the packing material and that the solution could circulate. The peristaltic pump was turned on, and the circulation flow rate was 230 mL / min. The pH inside the reactor was monitored in real time using a pH meter. During the treatment process, the pH inside the reactor would rise. A certain amount of 1 mol / L HCl was added to the reactor using a 5 mL syringe to maintain a stable pH of 6.0. After 4 hours, the FNA solution was drained, and the reactor was rinsed three times with the influent solution before normal operation. At this point, the FNA treatment was complete. The effluent from the reactor after FNA treatment contained NO3. - The -N concentration decreased significantly to 7.17±1.69 mg N / L, indicating that the FNA treatment was effective. However, due to the small but recoverable adverse effect of FNA on AnAOB, the effluent NH4 concentration decreased. + -N showed a slight increase, to 44.54±4.78 mg N / L.

[0069] Subsequently, to further inhibit NOB activity, FA at a concentration of 30.0 mg N / L was used on day 32 to further inhibit NOB activity. Each treatment lasted 4 hours, and three treatments were performed with an interval of 7 days between each treatment. The FA treatment steps were as follows: 2L of distilled water was placed in a 2L beaker, the temperature was measured, and the required mass of NH4Cl was calculated according to formula (4). The NH4Cl was dissolved in the beaker, and the pH of the solution was adjusted to 8.0 using 1mol / L HCl and NaOH solution. After draining the inlet water in the reactor, the reactor was rinsed three times with this solution. After draining the reactor again, the inlet and outlet water holes were connected by a pump pipe, and a peristaltic pump was connected to achieve internal circulation. 1.2L of the prepared FA solution was poured into the reactor, ensuring that the solution completely submerged all the packing material and that the solution could circulate. The peristaltic pump was turned on, and the circulation flow rate was 230mL / min. The pH inside the reactor was monitored in real time using a pH meter. A certain amount of 1 mol / L HCl or 1 mol / L NaOH solution was added to the reactor using a 5 mL syringe to maintain a stable pH of 8.0. After 4 hours, the FA solution was drained, and the reactor was rinsed three times with the influent solution before normal operation. At this point, the FA treatment was completed. The effluent from the reactor after FA treatment contained NH4+. + -N and NO3- -N was relatively stable, at 37.53±0.7 mg N / L and 8.34±0.34 mg N / L respectively, indicating that FA treatment was successful.

[0070] Subsequently, to further reduce effluent ammonia nitrogen, the aeration rate was increased from 10 mL / min to 30 mL / min on day 53. At this point, the effluent NH4 content was reduced. + -N decreased significantly to 8.51±7.88 mg N / L, while the increase in aeration further reduced NO3 in the effluent. - -N increased to 11.00±1.75 mg N / L. Therefore, in order to suppress NOB activity under high aeration intensity, a higher concentration of 3.0 mg N / L FNA was applied on day 63, with each treatment lasting 4 hours, for three treatments, with an interval of 7 days between each treatment. The FNA treatment steps were the same as above, except for the required NaNO2 mass. After the high-concentration FNA treatment, the NO3 in the reactor effluent decreased. - -N decreased significantly to 4.04 ± 0.94 mg N / L, indicating that the high-concentration FNA treatment was successful. After two weeks without adjustment, in the final stage of the experiment, because NOB had been sufficiently suppressed and the bacterial communities within the system had stabilized, NH4+... + -N is oxidized to NO2 by AOB. - -N is then fully utilized by AnAOB to carry out the Anammox reaction, thus producing NH4+ in the effluent. + -N is removed to the maximum extent possible. Reactor effluent NH4 + -N is stable below 1 mg N / L, and the effluent NO3 - -N concentration remained stable below 5 mg N / L, TNRR reached 589.25 mg N / L / d, and TNRE reached 95%.

[0071] The above results indicate that, under mainstream conditions, treatment combining FNA and FA in a continuous packed fixed-bed PN / A reactor can effectively suppress the activity of NOB in the system; under high aeration rates, NH4+... + -N is almost completely removed, and high-concentration FNA treatment is required to further inhibit NOB activity, maintain system stability, and obtain higher denitrification performance.

Claims

1. A method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system, characterized in that, Includes the following steps: S1. The reactor is inoculated with anaerobic ammonia oxidation packing biofilm sludge, and the initial flow rate of aeration (air) is controlled at 10 mL / min, and the influent flow rate is 5 mL / min. S2, when the reactor ammonia nitrogen (NH4) + The effluent concentration of NO3- (N) remained stable below 40 mg N / L. - After maintaining -N at 15 mg N / L for T1 days, three treatments with FNA at a concentration of 2.0 mg were performed, with each FNA treatment spaced at T2 days apart. S3. During the three 2.0 mg FNA treatments in step S2, the NH4 in the reactor effluent... + -N concentration increased slightly, NO3 in effluent - -N concentration decreased to below 7 mg N / L. NO3 concentration was expected to decrease after three FNA treatments. - After maintaining the -N effluent concentration below 10 mg N / L for T3 days, three FA treatments with a concentration of 30.0 mg were performed, with an interval of T4 days between each FA treatment. S4. During the three 30.0 mg FA treatments in step S3, the NH4 in the effluent from the reactor during this period... + -N concentration fluctuated slightly, effluent NO3 - After the -N concentration was stabilized below 10 mg N / L and maintained for T5 days, the aeration rate was increased from 10 mL / min to 30 mL / min. S5. After increasing the aeration flow rate in step S4, NH4 + -N concentration decreased to 2 mg N / L, and NO3 - When the -N concentration rises to 12 mg N / L, three treatments with 3.0 mg FNA are performed, with each treatment spaced 6 days apart. S6. During the three 3.0 mg FNA treatments in step S5, the NH4+ effluent from the reactor during this period... + -N concentration increased slightly, NO3 in effluent - -N concentration decreased to below 5 mg N / L. After treatment, the effluent NH4+... + -N concentration remained stable below 2 mg N / L and NO3- - When the -N concentration is stable below 5 mg N / L, it indicates that the FNA and FA treatment was successful.

2. The method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system according to claim 1, characterized in that, The values ​​are T1 = 10, T2 = 7, T3 = 7, T4 = 7, T5 = 7, and T6 = 7.

3. The method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-range nitrification coupled anaerobic ammonium oxidation (PN / A) system according to claim 1, characterized in that, In steps S2 and S5, the FNA treatment lasts for 4 hours, during which the pH is maintained at 6 ± 0.

1. In step S3, the FA treatment lasts for 4 hours, during which the pH is maintained at 8 ± 0.

1.

4. The method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-range nitrification coupled anaerobic ammonium oxidation (PN / A) system according to claim 1, characterized in that, When the aeration flow rate is low, a low concentration of FNA should be used to suppress NOB; when the aeration flow rate is high, a high concentration of FNA should be used to suppress NOB.

5. The method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system according to claim 1, characterized in that, The reactor is a continuous packed fixed-bed PN / A reactor in the mainstream state.

6. The method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system according to any one of claims 1-5, characterized in that, The anaerobic ammonia oxidation packing biofilm sludge inoculated in the reactor comes from mainstream anaerobic ammonia oxidation wastewater treatment systems.

7. The method for rapidly stabilizing and improving the nitrogen removal efficiency of a short-cut nitrification coupled anaerobic ammonium oxidation (PN / A) system according to any one of claims 1-5, characterized in that, The anaerobic ammonia oxidation packing biofilm sludge inoculated in the reactor has the following characteristics: the reactor for cultivating the anaerobic ammonia oxidation packing biofilm sludge is an SBR reactor, the operating environment is as follows: influent ammonia nitrogen concentration 45±5mg / L, hydraulic retention time 6h, operating pH 7.5, temperature room temperature, dissolved oxygen less than 0.5mg / L, and effluent ammonia nitrogen concentration consistently less than 2mg / L.

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