Fermentation pharmaceutical wastewater advanced treatment system device and method based on internal and external source synergistic denitrification

Abstract

The invention discloses a fermentation pharmaceutical wastewater advanced treatment system device and method based on internal and external source synergistic denitrification, belongs to the field of sewage treatment, is used for sewage treatment, and is characterized in that a sequencing batch reactor is provided with an aeration disc, a sampling port, a water inlet, a water outlet, a sludge discharge port and a heating rod; the fermentation pharmaceutical wastewater inlet tank is communicated with the water inlet through a pipeline and a peristaltic pump, the water outlet is communicated with the fermentation pharmaceutical wastewater outlet tank through a pipeline, the aeration disc is located in the sequencing batch reactor and communicated with the aeration pump through a pipeline and a rotor flow meter, and a thermometer and a mechanical stirrer are further arranged in the sequencing batch reactor. The method can stably operate under high ammonia nitrogen and antibiotic pollution conditions, can realize deep denitrification without additional carbon sources, has the advantages of quick start, low energy consumption, high toxicity resistance, stable and standard effluent and the like, and provides a new way for efficient, low-carbon and sustainable treatment of fermentation pharmaceutical wastewater.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of wastewater treatment, and in particular, relates to a fermentation pharmaceutical wastewater advanced treatment system device and method based on internal-external source synergistic denitrification. BACKGROUND

[0002] Fermentation pharmaceutical wastewater has the characteristics of high ammonia nitrogen, high organic load and strong antibiotic toxicity, and is a typical refractory industrial wastewater. The traditional A / O process or nitrification-denitrification system has problems such as insufficient carbon source, high nitrification energy consumption and poor system stability in the treatment of such wastewater. Because the denitrification process is often limited by the supply of external carbon source, the operation cost is high and is easily affected by the fluctuation of influent water quality, which makes it difficult to meet the standard of total nitrogen in effluent. In addition, the toxicity of antibiotics can inhibit the activity of nitrifying bacteria and denitrifying bacteria, further reducing the denitrification performance of the system, and increasing the production of excess sludge and the operation and maintenance cost.

[0003] In recent years, endogenous denitrification (ED) process has become an important direction of energy-saving wastewater treatment because it can utilize the polymers stored in microorganisms (such as polyhydroxyalkanoates PHA and glycogen Gly) as electron donors to achieve denitrification without external carbon source. However, the single endogenous denitrification rate is low, which is difficult to deal with high-nitrogen and high-toxicity fermentation pharmaceutical wastewater. On the other hand, the simultaneous nitrification and denitrification (SND) technology can realize nitrification and denitrification reactions in the same reaction environment, which not only shortens the treatment process, but also effectively reduces the aeration energy consumption.

[0004] Therefore, the organic coupling of exogenous denitrification and endogenous denitrification process forms a complementary multi-path denitrification mechanism, which is the key to realizing efficient advanced denitrification of fermentation pharmaceutical wastewater. Based on this idea, the present application proposes a composite biological denitrification process under the synergistic action of exogenous-endogenous denitrification. SUMMARY

[0005] The present application aims to provide a fermentation pharmaceutical wastewater advanced treatment system device and method based on internal-external source synergistic denitrification, which can stably operate under high ammonia nitrogen and antibiotic pollution conditions, achieve deep denitrification without additional carbon source, has the advantages of fast start-up, low energy consumption, strong antibiotic resistance and stable effluent, and provides a new way for efficient, low-carbon and sustainable treatment of fermentation pharmaceutical wastewater.

[0006] To achieve the above-mentioned purpose, the present application is realized by the following technical scheme:

[0007] This application describes a deep treatment system for fermentation-based pharmaceutical wastewater based on synergistic denitrification from internal and external sources. The system includes a fermentation-based pharmaceutical wastewater inlet tank, a sequencing batch reactor (SBR), and a fermentation-based pharmaceutical wastewater effluent tank. The SBR is equipped with an aeration disc, sampling port, inlet, outlet, sludge outlet, and heating rod. The fermentation-based pharmaceutical wastewater inlet tank is connected to the inlet via pipelines and a peristaltic pump. The outlet is connected to the fermentation-based pharmaceutical wastewater effluent tank via pipelines. The aeration disc is located inside the SBR and connected to the aeration pump via pipelines and a rotor flow meter. The SBR also includes a thermometer and a mechanical stirrer. The mechanical stirrer has a drive device and a stirring device, which is located inside the SBR and driven by the drive device. The probe of the dissolved oxygen / pH meter is located inside the SBR. The heating rod is used to heat and maintain the temperature of the liquid inside the SBR. The temperature inside the SBR is monitored by the thermometer to ensure it is maintained at 24±1℃.

[0008] The method for a deep treatment system for fermentation-based pharmaceutical wastewater based on synergistic denitrification from internal and external sources, as described in this application, includes a sequencing batch reactor (SBR) operation mode with an influent COD of 800-1000 mg / L and NH4+ of... + -N is 100~120 mg / L, TN is 120~135 mg / L, the influent volume and effluent volume of the sequencing batch reactor should not exceed 50% of the total wastewater volume in the reactor, and the following steps should be followed for operation:

[0009] Phase I: Take activated sludge mixture from the aerobic tank of the AO reactor used for treating fermented pharmaceutical wastewater. After sedimentation, decant the supernatant and inject it into the sequencing batch reactor (SBR). After inoculation, control the sludge concentration in the SBR to MLSS = 3500 mg / L. The SBR operates in the following mode: influent stage → anaerobic stage → aerobic stage I → anoxic stage → aerobic stage II → sedimentation stage → effluent stage. During the anaerobic stage, inject the fermented pharmaceutical wastewater into the SBR for 5 minutes using a peristaltic pump. Simultaneously, start the mechanical agitator in the SBR and perform anaerobic agitation for 2 hours at a stirring speed of 70-90 rpm. In the aerobic stage I, the aeration pump provides aerobic aeration through pump pipes and aeration discs, controlling the dissolved oxygen at 3.0 mg / L~3.4 mg / L for 6 hours. During the anoxic stage of the sequencing batch reactor (SBR), mechanical agitation is used for 12 hours. In the aerobic stage II, the aeration pump provides aerobic aeration through pump pipes and aeration discs, controlling the dissolved oxygen at 2.0±0.3 mg / L for 2 hours. After sedimentation for 1 hour, water is discharged through the aeration discs. This stage operates for 31 cycles, each cycle lasting 1 day. Once the SBR's effluent meets the ammonia nitrogen limit requirements in the fermentation-based pharmaceutical industry wastewater discharge standards, the nitrification-denitrification system is successfully started after the completion of stage I.

[0010] Phase II: The sequencing batch reactor (SBR) operates in the following manner: influent stage → anaerobic stage → aerobic stage I → anoxic stage → aerobic stage II → sedimentation stage → effluent stage. In the anaerobic stage, fermentation-type pharmaceutical wastewater is injected into the SBR for 5 minutes using a peristaltic pump, simultaneously activating the mechanical agitator. Anaerobic aeration is performed for 3 hours using the mechanical agitator at a speed of 70-90 rpm. In the aerobic stage I, aeration pumps provide aerobic aeration through pump pipes and aeration discs, maintaining dissolved oxygen at 2.0 ± 0.3 mg / L. During this stage, as the system's nitrification performance improves, the aeration time is gradually shortened from 6 hours to 5.5 hours, then to 5 hours, and finally to 4.5 hours, ultimately settling at 4.5 hours. In the anoxic stage, mechanical agitation lasts for 12 hours. In the aerobic stage II, aeration pumps provide aerobic aeration through pump pipes and aeration discs, maintaining dissolved oxygen at 2.0 ± 0.3 mg / L. mg / L, the aeration time was shortened from 2h in stage I to 30min, followed by 1h of sedimentation and drainage through the aeration disc. This stage ran for 40 cycles, with each cycle lasting 1 day. The efficiency of sludge storage of internal carbon sources was significantly improved in this stage. When the internal carbon source storage efficiency reached 77%, stage II ended.

[0011] Phase III: The sequencing batch reactor (SBR) operates in the following manner: influent stage → anaerobic stage → aerobic stage I → anoxic stage → aerobic stage II → sedimentation stage → effluent stage. In the anaerobic stage, fermentation-based pharmaceutical wastewater is injected into the SBR for 5 minutes using a peristaltic pump, while the mechanical agitator is activated for 3 hours of anaerobic agitation at a speed of 70-90 rpm. In the aerobic stage I, aeration pumps provide aerobic aeration through pump pipes and aeration discs, maintaining oxygen levels at 2.0 ± 0.3 mg / L. Due to increased intracellular carbon source storage efficiency in the anaerobic stage, COD consumption increases; therefore, to prevent over-aeration, the aeration time is shortened from 4.5 hours to 3.5 hours. In the anoxic stage, mechanical agitation lasts for 12 hours. In the aerobic stage II, aeration pumps provide aerobic aeration through pump pipes and aeration discs, maintaining dissolved oxygen at 0.8 ± 0.2 mg / L. mg / L, aeration time was further shortened to 10 min, followed by 1 h of sedimentation and drainage through the aeration disc. This stage was run for 49 cycles, with each cycle lasting 1 day; effluent COD and NH4... + -N, NO2 - -N and NO3 - -N further decreased, and when the average ARE, NAR and TNRE were 95.3%, 94.4% and 94.8% respectively, and the internal carbon source storage was significantly improved, Phase III ended.

[0012] As one of the preferred technical solutions of this application, the sequencing batch reactor operates in cycles, and each cycle includes an influent stage, an anaerobic stage, an aerobic I stage, an anoxic stage, an aerobic II stage, a sedimentation stage, and a drainage stage in sequence; the aeration time of the aerobic II stage is less than 30 min, ensuring that the remaining available carbon source is reduced and the sludge is kept in a starved state before entering the anaerobic stage of the next cycle.

[0013] As one of the preferred technical solutions of this application, the short-cut nitrification time in the third stage does not exceed 4.5 h, and the nitrite accumulation rate is maintained at no less than 80% through the inhibitory effect of free ammonia and / or oxytetracycline on nitrite-oxidizing bacteria; at the same time, during the domestication operation, denitrifying polysaccharide bacteria GAO are enriched, so that the intracellular carbon source storage efficiency is gradually increased to more than 77%, and can reach more than 90% at the highest.

[0014] As one of the preferred technical solutions of this application, the dissolved oxygen concentration in the aerobic stage I of the third stage is controlled at 2.0±0.3mg / L, and the duration of the aerobic stage I is gradually shortened to 3.5-4.5h; the dissolved oxygen concentration in the aerobic stage II is controlled at 0.8±0.2mg / L, and the aeration duration of the aeration stage in the aerobic stage II is 30-10 min.

[0015] Compared with the prior art, the beneficial effects of this application are:

[0016] 1. This invention significantly reduces the dependence on external carbon sources by coupling external denitrification and internal denitrification to achieve a synchronous nitrification-denitrification denitrification process, thereby reducing operating costs and energy consumption.

[0017] 2. This invention employs an alternating operation mode of anaerobic, aerobic I stage, anoxic, and aerobic II stage, which can effectively enrich denitrifying polysaccharide bacteria (DGAO). This allows intracellular polyhydroxyalkanoates (PHA) and glycogen to be fully converted into carbon sources required for denitrification during the anoxic stage, thereby significantly improving nitrogen removal efficiency. Subsequently, by implementing short-term aeration in the aerobic II stage, the remaining available organic carbon sources in the system are further consumed, putting the sludge in a "starved" state. When entering a new anaerobic stage, the high sensitivity of the sludge to starvation promotes its metabolic activity, allowing the influent organic matter to be quickly and fully absorbed and stored in the cells. This strengthens endogenous denitrification while avoiding excessive consumption of organic matter in the aerobic stage, ensuring that the short-cut nitrification (PN) process is not affected. In this invention, alternating anoxic / aerobic operating conditions and a relatively long anoxic hydraulic retention time (HRT) are the main process factors for achieving stable PN. Free ammonia (FA) and oxytetracycline (OTC) in the raw water further inhibit nitrite-oxidizing bacteria (NOB), which is conducive to the accumulation of nitrite. At the same time, the use of nitrification system sludge with some nitrite accumulation characteristics as inoculum sludge further shortens the start-up time of PN.

[0018] 3. This invention exhibits excellent denitrification performance. In actual operation, the total nitrogen removal rate can reach 89.8%, the ammonia nitrogen removal rate reaches 96.2%, and the chemical oxygen demand removal rate reaches 52.3%. The effluent quality consistently meets the requirements of the "Water Pollutant Discharge Standard for Fermentation Pharmaceutical Industry," and the overall system energy consumption is less than 1.0 kWh·m³. -3 It also has a strong resistance to antibiotic shocks and can operate stably for a long time even under OTC concentrations of 10 mg / L.

[0019] In summary, this invention achieves efficient and stable denitrification of fermentation-based pharmaceutical wastewater under low energy consumption and without external carbon sources, demonstrating good economic efficiency and engineering application value. Attached Figure Description

[0020] Figure 1 This is a schematic diagram of a deep treatment system for fermentation-based pharmaceutical wastewater based on synergistic denitrification from internal and external sources, as described in this application.

[0021] Figure 2 This describes the pollutant removal effect under long-term operation of this application.

[0022] Figure 3This is a graph showing the change in the proportion of nitrogen removal contribution during the long-term operation of this application.

[0023] Figure 4 This is a diagram of contaminant removal and intracellular carbon source conversion during a typical cycle in this application.

[0024] In the diagram: 1. Inlet tank for fermentation-type pharmaceutical wastewater; 2. Peristaltic pump; 3. Aeration pump; 4. Rotor flow meter; 5. Thermometer; 6. Mechanical stirrer; 7. Dissolved oxygen / pH meter; 8. Outlet tank for fermentation-type pharmaceutical wastewater; 9. Aeration disc; 10. Sequencing batch reactor; 11. Sampling port; 12. Inlet; 13. Outlet; 14. Sludge discharge port; 15. Heating rod. Detailed Implementation

[0025] The technical solutions described in this application will be further described below with reference to the accompanying drawings and embodiments.

[0026] Example 1

[0027] See Figure 1 A deep treatment system for fermentation-based pharmaceutical wastewater based on synergistic denitrification from internal and external sources is disclosed. The system comprises a fermentation-based pharmaceutical wastewater inlet tank 1, a peristaltic pump 2, an aeration pump 3, a rotor flowmeter 4, a thermometer 5, a mechanical stirrer 6, a dissolved oxygen / pH meter 7, a fermentation-based pharmaceutical wastewater outlet tank 8, an aeration disc 9, a sequencing batch reactor 10, a sampling port 11, an inlet 12, an outlet 13, a sludge discharge port 14, and a heating rod 15. The fermentation-based pharmaceutical wastewater inlet tank 1, driven by the peristaltic pump 2, feeds the fermentation-based pharmaceutical wastewater into the sequencing batch reactor 10 through the inlet 12. The sequencing batch reactor 10 is equipped with a mechanical stirrer 6, which has a drive device and a stirring device. The stirring device is located inside the sequencing batch reactor 10 and is driven by the drive device to agitate the fermentation-based pharmaceutical wastewater within the reactor 10. The sequencing batch reactor 10 is further equipped with an aeration disc 9, which is connected to an aeration pump 3 via a pump pipe and a rotor flow meter 4. The aeration pump 3 delivers the required gas to the aeration disc 9, and the rotor flow meter 4 measures the gas pumped by the aeration pump 3. The sequencing batch reactor 10 is also equipped with a sampling port 11, a water inlet 12, a drain outlet 13, and a sludge discharge outlet 14, arranged sequentially from top to bottom. The dissolved oxygen / pH meter 7 has a probe that extends into the sequencing batch reactor 10. The probe is connected to the dissolved oxygen / pH meter 7 via an electrical signal to measure the pH and dissolved oxygen levels of the liquid inside the sequencing batch reactor 10. The heating rod 15 heats and maintains the temperature of the liquid inside the sequencing batch reactor 10. A thermometer 5 monitors the water temperature inside the sequencing batch reactor 10 to ensure that the temperature inside the sequencing batch reactor 10 is maintained at 24±1℃.

[0028] Example 2

[0029] The reaction system of this invention adopts a sequencing batch reactor (SBR) operation mode, running one cycle per day (i.e., one cycle equals one day). Each cycle includes the following seven stages: influent stage → anaerobic stage → aerobic stage I → anoxic stage → aerobic stage II → sedimentation stage → effluent stage, running for a total of 120 days. Actual fermentation-based pharmaceutical wastewater contains a large amount of oxytetracycline and a small amount of other antibiotics. The influent COD is 800~1000 mg / L, and NH4+... + -N is 100~120 mg / L, TN is 120~135 mg / L, and the influent-to-effluent ratio is 50%. That is, the influent and effluent volumes of the sequencing batch reactor 10 should not exceed 50% of its total internal wastewater volume. According to different operating conditions, the entire operating cycle is divided into three stages, and the specific steps are as follows:

[0030] Phase 1 (1-31 days): The system operates in the following mode: influent stage → anaerobic stage → aerobic stage I → anoxic stage → aerobic stage II → sedimentation stage → effluent stage. The mixed liquor of sludge from the aerobic tank of an actual antibiotic treatment plant is inoculated into the SBR reactor, controlling the sludge concentration (MLSS) to approximately 3500 mg / L. First, influent is pumped in for 5 minutes, followed by the anaerobic stage with mechanical stirring for 2 hours at 70-90 rpm. During this stage, microorganisms store organic matter in the water as PHA and glycogen within their cells. In the anoxic stage, mixing is carried out for 12 hours, utilizing the PHA and glycogen stored by the microorganisms in the anaerobic stage for denitrification. Finally, in the aerobic stage II, the DO concentration is controlled at 2.0 ± 0.3 mg / L, and aeration is performed for 2 hours to remove residual ammonia nitrogen. After sedimentation for 1 hour, effluent is discharged through drain valve 9. After 31 cycles of this phase, the effluent from the sequencing batch reactor 10 should meet the ammonia nitrogen limit requirements of the wastewater discharge standards for fermentation-based pharmaceutical industries, with a stable and compliant ammonia nitrogen removal rate. The main purpose of this stage is to allow the seed mud to adapt to the experimental operating conditions, while stabilizing the nitrification and denitrification performance.

[0031] Phase Two (32-71 days): The system continued to operate in the following pattern: influent stage → anaerobic stage → aerobic stage I → anoxic stage → aerobic stage II → sedimentation stage → effluent stage. The anaerobic stage was extended to 3 hours to further promote the storage of intracellular carbon sources. With the improvement of short-cut nitrification performance, the duration of aerobic stage I was adjusted (6 h → 5.5 h → 5 h → 4.5 h), ultimately controlling the nitrification time of aerobic stage I at 4.5 hours, with DO maintained at 2.0 ± 0.3 mg / L. The anoxic stage remained at 12 hours, and the HRT of the final short aeration stage, i.e., aerobic stage II, was shortened from 2 hours to 30 minutes. Initially, the system's sludge storage capacity for intracellular carbon sources was still relatively limited, and COD...intra，efficiency The efficiency of intracellular carbon source storage increased by only 15% compared to stage I, reaching 77.8% at the end of stage II (71 days). After long-term acclimatization, the efficiency of intracellular carbon source storage was significantly improved in this stage. The main purpose of this stage is to improve the endogenous denitrification performance of the system.

[0032] Phase 3 (71-120 days): The system continues to operate in the following pattern: influent stage → anaerobic stage → aerobic stage I → anoxic stage → aerobic stage II → sedimentation stage → effluent stage. The anaerobic stage is still controlled for 3 hours, the anoxic stage for 12 hours, and the aeration time in aerobic stage II is further shortened from 30 minutes in phase 2 to 10 minutes. After changing the operating conditions, the COD consumption in the anaerobic stage increases, and the COD... intra，efficiency The efficiency was above 94.8%. Furthermore, due to the reduction in effluent COD at the end of the anaerobic stage, the HRT of the aerobic I stage was further shortened to 3.5 h, reducing system operating energy consumption while ensuring system effectiveness. At the end of the third stage (100-120 days), the effluent NH4... + -N, NO2 - -N and NO3 - The concentrations of nitrogen oxides (NOx) and nitrogen (N) were 5.1 mg / L, 0.8 mg / L, and 3.5 mg / L, respectively; the average ARE, NAR, and TNRE were 95.3%, 94.4%, and 94.8%, respectively. This indicates a significant improvement in the system's treatment efficiency, achieving highly efficient nitrogen removal.

[0033] In this application, the discharge volume and influent volume of the sequencing batch reactor 10 are 50% of the total wastewater volume in the sequencing batch reactor 10.

[0034] Based on the above embodiments, see the appendix of this application. Figure 2 and appendix Figure 3 Using the apparatus described in Example 1 and the method described in Example 2, a denitrification experiment was conducted on actual fermentation-based pharmaceutical wastewater. The effective volume of the SBR reactor used was 5L, and the effluent ratio was 50%. Start-up and operation results showed stable denitrification performance, and the system operated for 120 days. Typical cycle analysis was performed during stable system operation, considering influent COD and NH4... + When the concentrations of -N and TN are 786 mg / L, 112 mg / L, and 117 mg / L respectively, the effluent COD and NH4 can be reduced. + -N and TN concentrations were 381 mg / L, 5 mg / L, and 9 mg / L, respectively. Simultaneously, typical cycle nitrogen metabolism was analyzed, showing endogenous denitrification accounting for 68%, exogenous denitrification for 7.3%, and simultaneous nitrification and denitrification for 20.3%. (See [reference needed]). Figure 3 The removal rates of ammonia nitrogen and total nitrogen can reach 95.5% and 92.3%, respectively.

[0035] Finally, although this specification describes embodiments, not every embodiment contains only one independent technical solution. This way of describing the specification is only for clarity. Those skilled in the art should regard the specification as a whole. The technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

Claims

1. A fermentation pharmaceutical wastewater advanced treatment system device based on endogenous and exogenous synergistic denitrification, characterized by: The device includes fermentation pharmaceutical wastewater inflow tank (1), sequencing batch reactor (10), fermentation pharmaceutical wastewater effluent tank (8), the sequencing batch reactor (10) is provided with aeration disc (9), sampling port (11), water inlet (12), drainage (13), sludge outlet (14), heating rod (15), the fermentation pharmaceutical wastewater inflow tank (1) is communicated with water inlet (12) by pipeline, peristaltic pump (2), the drainage (13) is communicated with fermentation pharmaceutical wastewater effluent tank (8) by pipeline, the aeration disc (9) is located in the inside of sequencing batch reactor (10) and is communicated with aeration pump (3) by pipeline, rotor flowmeter (4), the sequencing batch reactor (10) is also provided with thermometer (5), mechanical stirrer (6), the mechanical stirrer (6) has driving device and stirring device, and stirring device is located in the inside of sequencing batch reactor (10) and is driven by driving device;The probe of dissolved oxygen / PH measuring instrument (7) is located in the inside of sequencing batch reactor (10), the heating rod (15) is used for heating and heat preservation to the liquid in the inside of sequencing batch reactor (10), and the water temperature in the inside of sequencing batch reactor (10) is monitored by thermometer (5) to ensure that the temperature is maintained at 24±1 ℃.

2. A method for the advanced treatment of fermentation pharmaceutical wastewater based on the synergistic denitrification of endogenous and exogenous sources, characterized by the fact that it comprises the following steps: The influent COD is 800-1000 mg / L, NH4 + -N is 100-120 mg / L, TN is 120-135 mg / L, the influent volume and effluent volume of the sequencing batch reactor (10) should not exceed 50% of the total volume of sewage in the sequencing batch reactor (10), and the following steps are used for operation: The first stage: from the actual treatment fermentation pharmaceutical wastewater AO reactor, the activated sludge mixed liquor of aerobic tank is taken, after precipitation, the supernatant is decanted, and is injected into sequencing batch reactor (10), after inoculation, the sludge concentration in sequencing batch reactor (10) is controlled to be MLSS=3500mg / L;The sequencing batch reactor (10) adopts the operation mode of water inlet stage→anaerobic stage→oxygen I section→anoxic stage→oxygen II section→precipitation stage→drainage stage, wherein the anaerobic stage of sequencing batch reactor (10) is injected with fermentation pharmaceutical wastewater by peristaltic pump (2) for 5min, and the mechanical stirrer (6) of sequencing batch reactor (10) is started, anaerobic stirring is carried out by mechanical stirrer (6) for 2h, and the stirring speed of mechanical stirrer (6) is 70rmp~90rmp;In the oxygen I section of sequencing batch reactor (10), aeration pump (3) carries out aerobic aeration through pump pipe and aeration disc (9), the dissolved oxygen is controlled to be 3.0mg / L~3.4mg / L, and the aeration time is 6h;In the anoxic stage of sequencing batch reactor (10), the stirring is carried out by mechanical stirrer (6) for 12 hours;In the oxygen II section of sequencing batch reactor (10), aeration pump (3) carries out aerobic aeration through pump pipe and aeration disc (9), the dissolved oxygen is controlled to be 2.0±0.3mg / L, and the aeration time is 2h, then 1h is precipitated, and the water is discharged through aeration disc (9), and the operation of this stage is 31 cycles, and each cycle is 1 day;When the water discharge of sequencing batch reactor (10) meets the ammonia nitrogen limit requirement in fermentation pharmaceutical industrial water discharge standard, the first stage is ended, and the nitrification and denitrification system is successfully started in the operation stage. In the second stage, the sequencing batch reactor (10) is operated in the mode of influent stage, anaerobic stage, aerobic stage I, anoxic stage, aerobic stage II, sedimentation stage and effluent stage. The anaerobic stage of the sequencing batch reactor (10) is injected with fermentation pharmaceutical wastewater for 5 minutes by the peristaltic pump (2), and the mechanical stirrer (6) of the sequencing batch reactor (10) is started to stir anaerobically for 3 hours. The stirring speed of the mechanical stirrer (6) is 70 rmp-90 rmp. In the aerobic stage I of the sequencing batch reactor (10), the aeration pump (3) performs aerobic aeration through the pump pipe and the aeration disc (9), and the dissolved oxygen is controlled at 2.0±0.3 mg / L. In this stage, the aeration time is gradually shortened from 6 hours to 5.5 hours, 5 hours and 4.5 hours, and finally controlled at 4.5 hours, along with the improvement of the nitrification performance of the system. In the anoxic stage of the sequencing batch reactor (10), the mechanical stirrer (6) is stirred for 12 hours. In the aerobic stage II of the sequencing batch reactor (10), the aeration pump (3) performs aerobic aeration through the pump pipe and the aeration disc (9), and the dissolved oxygen is controlled at 2.0±0.3 mg / L. The aeration time is shortened from 2 hours in the first stage to 30 minutes, and then the effluent is discharged through the aeration disc (9) after 1 hour of sedimentation. This stage is operated for 40 cycles, and each cycle is 1 day. In this stage, the efficiency of sludge storage of internal carbon source is significantly improved. When the efficiency of internal carbon source storage reaches 77%, the second stage ends. Stage III: The sequencing batch reactor (10) adopts the operation mode of water feeding stage → anaerobic stage → aerobic I stage → anoxic stage → aerobic II stage → sedimentation stage → drainage stage, wherein the anaerobic stage of the sequencing batch reactor (10) is injected with fermentation pharmaceutical wastewater for 5 min by the peristaltic pump (2), at the same time, the mechanical stirrer (6) of the sequencing batch reactor (10) is started, anaerobic stirring is carried out by the mechanical stirrer (6), the time is controlled for 3 h, and the stirring speed of the mechanical stirrer (6) is 70 rmp~90 rmp; in the aerobic I stage of the sequencing batch reactor (10), the aeration pump (3) carries out aerobic aeration through the pump pipe and the aeration disc (9), the oxygen control is controlled at 2.0±0.3 mg / L, due to the improvement of the intracellular carbon source storage efficiency in the anaerobic stage, the COD consumption in the anaerobic stage is increased, in order to prevent excessive aeration, the aeration time is shortened from 4.5 h to 3.5 h; in the anoxic stage of the sequencing batch reactor (10), the mechanical stirrer (6) is stirred for 12 hours; in the aerobic II stage of the sequencing batch reactor (10), the aeration pump (3) carries out aerobic aeration through the pump pipe and the aeration disc (9), the dissolved oxygen is controlled at 0.8±0.2 mg / L, the aeration time is further shortened to 10 min, and then the water is drained through the aeration disc (9) after 1 h of sedimentation, the operation of this stage is 49 cycles, each cycle is 1 day; the effluent COD, NH4 + -N, NO2 - -N and NO3 - -N is further reduced, when the average ARE, NAR and TNRE are 95.3%, 94.4% and 94.8% respectively, and the intracellular carbon source storage is significantly improved, the stage III is ended.

3. The method of claim 2, wherein the system is characterized in that: The sequencing batch reactor (10) is operated in cycles, and each cycle includes the influent stage, the anaerobic stage, the aerobic stage I, the anoxic stage, the aerobic stage II, the sedimentation stage and the effluent stage in turn. The aeration time of the aerobic stage II is less than 30 minutes, which ensures that the remaining available carbon source is reduced and the sludge starvation state is maintained before entering the anaerobic stage of the next cycle.

4. The method of claim 2 or 3, wherein the system is characterized in that: In the third stage, the duration of short-cut nitrification is not more than 4.5 hours, and the accumulation rate of nitrite is maintained at not less than 80% through the inhibition of free ammonia and / or oxytetracycline on nitrite oxidizing bacteria. At the same time, the enrichment of denitrifying polysaccharide bacteria GAO during the domestication operation gradually improves the intracellular carbon source storage efficiency to more than 77%, and the highest can reach more than 90%.

5. The method of claim 3, wherein the system is characterized in that: In the third stage, the dissolved oxygen concentration in the aerobic stage I is controlled at 2.0±0.3 mg / L, and the duration of the aerobic stage I is gradually shortened to 3.5-4.5 hours. In the third stage, the dissolved oxygen concentration in the aerobic stage II is controlled at 0.8±0.2 mg / L, and the aeration duration in the aerobic stage II is 30-10 minutes.

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