SPNEDA control method and system

Abstract

The invention relates to the technical field of wastewater treatment, and discloses an SPNEDA control method and system, and the method comprises the steps: 1, an anaerobic stage: adding sewage into an SPNEDA reactor, enabling the liquid level to reach a preset position, then controlling the SPNEDA reactor to operate in an anaerobic mode, carrying out anaerobic treatment for 60 min, storing a carbon source by denitrifying bacteria in the SPNEDA reactor, and heating the SPNEDA reactor; step 2, aerobic stage: carrying out aerobic aeration in the SPNEDA reactor for 360 minutes, and carrying out autotrophic short-cut nitrification on ammonia oxidizing bacteria in the SPNEDA reactor; and step 3, an anoxic stage: carrying out anoxic treatment for 210 minutes, then precipitating for 35 minutes, then draining water, carrying out anaerobic ammonium oxidation reaction by anaerobic ammonium oxidation bacteria, and carrying out endogenous denitrification by denitrifying bacteria. According to the scheme, the SPNA technology and the endogenous denitrification technology are combined, nitrogen removal is achieved through the denitrification technology without additionally adding a carbon source, it can be effectively avoided that denitrifying bacteria excessively grow to compete with anaerobic ammonium oxidation bacteria for a substrate, and the anaerobic ammonium oxidation SPNEDA reactor can be rapidly started.

Description

Technical Field

[0001] The present invention relates to the field of wastewater, and in particular to a SPNEDA control method and a system thereof. Background Art

[0002] As a coupling method, denitrification has been studied as a coupling process to achieve further treatment of nitrogen in water. The denitrification process requires the use of organic carbon sources, which usually come from three sources: internal carbon sources, raw water carbon sources, and external carbon sources. When using traditional nitrification and denitrification processes to treat low C / N wastewater, during the denitrification stage, additional carbon sources need to be added due to the lack of organic carbon sources required for denitrification, which incurs the cost of adding external carbon sources. Summary of the invention

[0003] The present invention is intended to provide a SPNEDA control method and system thereof to solve the problem that the current sewage denitrification requires the addition of additional carbon sources, which results in high costs.

[0004] To achieve the above object, the present invention provides a SPNEDA control method and system thereof, comprising:

[0005] Step 1: Anaerobic stage: Add sewage to the SPNEDA reactor to make the liquid level reach the preset position, and then control the SPNEDA reactor to operate in anaerobic mode for 60 minutes. The denitrifying bacteria in the SPNEDA reactor store carbon sources and heat the SPNEDA reactor. 25 minutes to 35 minutes before the end of the anaerobic stage, add 4 to 8 mg / L NH 2 OH (hydroxylamine).

[0006] Step 2: Aerobic stage: aerobic aeration is performed in the SPNEDA reactor for 360 min, and the ammonia oxidizing bacteria in the SPNEDA reactor perform autotrophic short-range nitrification;

[0007] Step 3: Anoxic stage: After 210 minutes of anoxic period, the water is discharged after sedimentation for 35 minutes. The anaerobic ammonium oxidizing bacteria in the SPNEDA reactor carry out anaerobic ammonium oxidation reaction, and the denitrifying bacteria carry out endogenous denitrification.

[0008] Preferably, in step 1, NH 2 at a concentration of 6 mg / L is added to the SPNEDA reactor 25 min before the end of the anaerobic stage. 2 OH.

[0009] Preferably, the method further includes controlling the dissolved oxygen content in the SPNEDA reactor at each stage to be less than 0.8 mg / L and the pH value to be 7.2-8.2.

[0010] Preferably, in step 2, the wastewater from the SPNEDA reactor is refluxed and stirred.

[0011] Preferably, in step 1, the temperature of the SPNEDA reactor is maintained at 28-32°C.

[0012] Preferably, in step 2, the sewage at the top of the SPNEDA reactor is returned to the bottom of the SPNEDA reactor by external reflux, so that the sewage of the SPNEDA reactor is fully in contact with the granular sludge, the mass transfer process is increased, and the internal hydraulic dead zone is achieved, so that the fluidity of the sludge is good and the operation is stable; at the same time, oxygen is transported to the bottom of the SPNEDA reactor to control the dissolved oxygen content at the bottom of the SPNEDA reactor.

[0013] In order to achieve the above-mentioned purpose, the present scheme also provides a SPNEDA system, comprising: a DO / pH probe, a constant temperature water tank, an aeration pump, and an inlet tank, a SPNEDA reactor and an outlet tank connected in sequence, the constant temperature water tank and the interlayer between the inner and outer walls of the SPNEDA reactor are connected, the aeration pump is used to aerate the SPNEDA reactor, and the DO / pH probe is used to detect the dissolved oxygen content and pH value of the sewage in the SPNEDA reactor.

[0014] Preferably, a reflux pump is also included, and the reflux pump is used to return the sewage from the top of the SPNEDA reactor to the bottom of the SPNEDA reactor, so that the sewage from the SPNEDA reactor is fully in contact with the granular sludge, the mass transfer process is increased, and there is no hydraulic dead zone inside, so that the fluidity of the sludge is good and the operation is stable; at the same time, oxygen is transported to the bottom of the SPNEDA reactor to control the dissolved oxygen content at the bottom of the SPNEDA reactor.

[0015] Preferably, an aeration plate is further included, the aeration plate being located at the top of the SPNEDA reactor and being connected to an aeration pump. The aeration plate increases the dissolved oxygen in the water by releasing air (usually compressed air) into the water in the form of fine bubbles, and introduces air or oxygen into the water uniformly, thereby promoting the dissolution of oxygen in the water, improving water quality, and promoting the growth of microorganisms and the degradation of organic matter.

[0016] The SPNA process refers to synchronous nitrification coupled with anaerobic ammonium oxidation. First, ammonia nitrogen is converted into nitrite nitrogen under the action of ammonia oxidizing bacteria, and then ammonia nitrogen and nitrite nitrogen are converted into nitrogen gas and nitrate nitrogen through the anaerobic ammonium oxidation process. SPNEDA is an integrated short-range nitrification coupled anaerobic ammonium oxidation endogenous denitrification process. The SPNEDA process of this scheme combines the SPNA process with endogenous denitrification technology. Under low DO conditions, AOB converts part of NH 4 + -N is converted to NO 2- -N, then AnAOB uses NH4 + -N and NO 2 - -N Generate N 2 , and produces some NO 3 - -N, finally DGAOs will remove the remaining NO 2- -N and NO 3- -N denitrification to N 2 , the whole process is accompanied by the removal of organic matter. Denitrification is carried out under the condition of making full use of the carbon source of raw water, and the denitrification process without adding additional carbon source can achieve nitrogen removal; and effectively avoid the competition between denitrifying bacteria and anaerobic ammonia oxidizing bacteria. Due to the low endogenous denitrification rate, the growth rate of denitrifying bacteria is also low, which can effectively avoid the overgrowth of denitrifying bacteria and the competition with anaerobic ammonia oxidizing bacteria for substrates, and can quickly start the anaerobic ammonia oxidizing SPNEDA reactor. Specifically, in the anaerobic stage, the substrate substances of denitrifying bacteria are nitrite nitrogen and nitrate nitrogen, and the substrate substances of anaerobic ammonia oxidizing bacteria are nitrite nitrogen and ammonia nitrogen. Due to the low endogenous denitrification rate, anaerobic ammonia oxidizing bacteria give priority to nitrite nitrogen, and the nitrate nitrogen produced at the same time provides substrate substances for endogenous denitrifying bacteria to achieve the purpose of deep denitrification; NH is added in the anaerobic stage 2 OH inhibits the activity of NOB, reduces the influence of NOB on the activity of AOB, restores the denitrification performance of the system and realizes long-term continuous sewage treatment. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 The figure is a schematic diagram of the structure of a SPNEDA system according to an embodiment of the present invention. DETAILED DESCRIPTION

[0018] The following is further described in detail through specific implementation methods:

[0019] The reference numerals in the drawings of the specification include:

[0020] Inlet pool 1, water inlet pump 2, reflux pump 3, SPNEDA reactor 4, DO / pH probe 5, aeration pipe 6, constant temperature water tank 7, water bath circulation pump 8, aeration pump 9, heating rod 10.

[0021] Example:

[0022] Endogenous denitrification technology can fully utilize the carbon source of raw water and remove nitrogen without adding additional carbon source. For example, glycogen accumulating organisms (GAOs) will consume glycogen (Glycogen, Gly) in the anaerobic stage and absorb external carbon sources into the body to form polyhydroxyalkanoate (PHAs) and store them. In the aerobic stage, PHAs will be decomposed to synthesize Gly. There is a branch of GAOs that has denitrification function. It can decompose PHAs to synthesize Gly under anaerobic conditions and use NO as the catalyst. 3 - -N and NO 2 - -N is used as an electron acceptor for denitrification, thereby achieving denitrification under the condition of fully utilizing the carbon source of the raw water. This type of bacteria is named endogenous denitrifying bacteria (Denitrifying glycogen accumulating organisms, DGAOs).

[0023] In order to develop a SPNEDA reactor with faster start-up of anaerobic ammonium oxidation, this study combined the SPNA process with endogenous denitrification technology. Under low DO (dissolved oxygen) conditions, AOB (aerobic ammonia oxidizing bacteria) converted part of the NH 4 + -N is converted to NO 2 - -N, then AnAOB (anaerobic ammonium oxidizing bacteria) uses NH 4 + -N and NO 2 - -N Generate N 2 , and produces some NO 3- -N, and finally DGAOs (denitrifying bacteria) remove the remaining NO in the system 2- -N and NO 3- -N denitrification to N 2 The whole process is accompanied by the removal of organic matter. In the anaerobic stage, the substrates of denitrifying bacteria are nitrite nitrogen and nitrate nitrogen, and the substrates of anaerobic ammonium-oxidizing bacteria are nitrite nitrogen and ammonia nitrogen. Due to the low endogenous denitrification rate, anaerobic ammonium-oxidizing bacteria preferentially utilize nitrite nitrogen. The nitrate nitrogen produced at the same time provides substrates for endogenous denitrifying bacteria, achieving the purpose of deep denitrification and effectively avoiding the overgrowth of denitrifying bacteria and competition with anaerobic ammonium-oxidizing bacteria for substrates.

[0024] A SPNEDA system control method comprises the following steps:

[0025] Step 1: Anaerobic stage: Add sewage to the SPNEDA reactor 4 to make the liquid level reach the preset position, and then control the SPNEDA reactor 4 to operate in anaerobic mode for 60 minutes. The denitrifying bacteria in the SPNEDA reactor 4 store carbon sources and heat the SPNEDA reactor 4.

[0026] In this step, denitrifying bacteria consume glycogen (Glycogen, Gly) under anaerobic conditions and absorb external carbon sources into the body to form polyhydroxyalkanoates (Polyhldroxyalkanoate, PHAs) and store them.

[0027] In this step, NH4+ with a concentration of 4 to 8 mg / L is added to the SPNEDA reactor 4 25 to 35 minutes before the end of the anaerobic stage. 2 OH. NH 4 at a concentration of 6 mg / L was preferably added to the SPNEDA reactor 4 25 min before the end of the anaerobic phase. 2 The SPNEDA process, which is a combination of the SPNA process and the endogenous denitrification technology in this application, has the inherent application bottleneck of the SPNA process: the increase in NOB makes it difficult to maintain short-range nitrification. In the SPNEDA system, when the NOB activity increases, it will not only affect the activity of AOB and AnAOB, but also NO 2- -N competition has an adverse effect on DGAOs. In this scheme, NH 2 OH inhibits the activity of NOB, reduces the influence of NOB on the activity of AOB, restores the denitrification performance of the system and realizes long-term continuous sewage treatment.

[0028] Among them, NH 2 The proof that OH inhibits NOB activity is as follows:

[0029] This short-term test is divided into 6 groups of parallel tests:

[0030] No. 1 Test condition is NH 2 The OH addition time was 25 min, and the addition concentration was 4 mg / L; the test condition for No. 2 was NH 2 The OH addition time was 25 min, and the addition concentration was 6 mg / L; the test condition for No. 3 was NH 2 The OH addition time was 25 min, and the addition concentration was 8 mg / L; the test condition numbered 4 was NH 2 The OH addition time was 35 min, and the addition concentration was 4 mg / L; the test condition numbered 5 was NH 2 The OH addition time was 35 min, and the addition concentration was 6 mg / L; the test condition numbered 6 was NH 2The OH addition time was 35 min, and the addition concentration was 8 mg / L. No. 1, 2, and 3 were tested under anaerobic conditions; No. 4, 5, and 6 were tested under aerobic conditions.

[0031] In the pilot tests of groups 1, 2, and 3, as NH 2 The increase in OH concentration and the NO 3 - -N concentration gradually decreased to 15.6, 13.2, and 11.66 mg / L, respectively. However, with the addition of NH 2 The increase of OH concentration will lead to NO 3- The decreasing trend of -N also indicated that the activity of NOB was effectively inhibited.

[0032] In the 4th, 5th and 6th aerobic dosing point groups, the effluent NO 3- -N concentration also decreased significantly, to 16.5, 12.98, and 11.60 mg / L respectively. 2 After OH, the effluent NH 4 + -N concentration did not decrease significantly. 2 After OH, the denitrification performance of the system did not change significantly. 2 OH treatment will have an adverse effect on AOB and hinder the nitrification process of the system.

[0033] Whether adding NH at aerobic or anaerobic points 2 The inhibition degree of OH and NOB activity was greater than that of AOB. Based on the two groups of experiments under anaerobic conditions and aerobic conditions, anaerobic addition was the best addition condition, and the best NH 2 The OH addition concentration was 6 mg / L and the addition time was 25 min.

[0034] Step 2: Aerobic stage: aerobic aeration is performed in the SPNEDA reactor 4 for 360 minutes, and the ammonia oxidizing bacteria in the SPNEDA reactor 4 perform autotrophic short-range nitrification.

[0035] In this step, denitrifying bacteria will decompose PHAs to synthesize Gly in the aerobic stage, and ammonia oxidizing bacteria will carry out autotrophic short-term nitrification.

[0036] In this step, the DO value in the SPNEDA reactor 4 was maintained at 0.8 mg / L.

[0037] In this step, the sewage of the SPNEDA reactor 4 is refluxed and stirred to make the sewage fully contact with the granular sludge in the SPNEDA reactor 4. Specifically, the sewage at the top of the SPNEDA reactor 46 is refluxed to the bottom of the SPNEDA reactor 46 by external reflux. The sewage of the SPNEDA reactor 4 is fully contacted with the granular sludge, the mass transfer process is increased, and the internal hydraulic dead zone is achieved, so that the fluidity of the sludge is good and the operation is stable; at the same time, oxygen is transported to the bottom of the SPNEDA reactor 4 to control the dissolved oxygen content at the bottom of the SPNEDA reactor 4. In this scheme, a peristaltic pump is used to reflux sewage.

[0038] Step 3: Anoxic stage: Drain after 35 minutes of sedimentation, anaerobic ammonia oxidizing bacteria carry out anaerobic ammonia oxidation reaction, denitrifying bacteria carry out endogenous denitrification, and drain after sedimentation is completed.

[0039] In this step, denitrifying bacteria decompose PHAs to synthesize Gly under anoxic conditions, using NO 3 - -N and NO 2 - -N is used as an electron acceptor for denitrification, thereby achieving denitrification under the condition of fully utilizing the raw water carbon source. Since the endogenous denitrification rate is low, the growth rate of denitrifying bacteria is also low, thus effectively avoiding the overgrowth of denitrifying bacteria and competing with anaerobic ammonia oxidizing bacteria for substrates.

[0040] The drainage ratio in this step is 50%. Reasonable drainage avoids water flow that is too fast or too slow, maintains stable operation of the system, and avoids poor treatment effect due to excessive load.

[0041] DO, pH, temperature, etc. in the system will affect the effect of hydroxylamine. In this scheme, the temperature of SPNEDA reactor 4 is maintained at 28-32°C, preferably 30°C, at each stage. Specifically, water bath heating and other methods can be used to maintain the temperature in SPNEDA reactor 4. At each stage, the dissolved oxygen in SPNEDA reactor 4 is monitored and controlled to be below 0.8 mg / L, and the pH value is between 7.2-8.2.

[0042] This scheme combines the SPNA process with endogenous denitrification technology. The SPNEDA reactor 4 operates in AOA mode (anaerobic-aerobic-anoxic). In the anaerobic stage, DGAOs absorb external carbon sources for storage, in the aerobic stage, GAOs decompose PHAs to synthesize Gly, and in the anoxic stage, GAOs decompose PHAs to synthesize Gly. 3 - -N and NO 2 - -N acts as an electron acceptor for denitrification, thereby achieving denitrification under the condition of fully utilizing the carbon source of the raw water; under low DO conditions, AOB converts part of NH 4+ -N is converted to NO 2- -N, then AnAOB uses NH 4 + -N and NO 2- -N Generate N 2 , and produces some NO 3- -N, finally DGAOs will remove the remaining NO 2- -N and NO 3- -N denitrification to N 2 The whole process is accompanied by the removal of organic matter. The denitrification process without adding additional carbon source is used to achieve nitrogen removal. Due to the low endogenous denitrification rate, the growth rate of denitrifying bacteria is also low, which can effectively avoid the overgrowth of denitrifying bacteria and the competition with anaerobic ammonium oxidizing bacteria for substrates, and can quickly start the anaerobic ammonium oxidizing SPNEDA reactor 4; adding NH 2 OH inhibits the activity of NOB, reduces the influence of NOB on the activity of AOB, restores the denitrification performance of the system and realizes long-term continuous sewage treatment.

[0043] like Figure 1 As shown, the present solution also provides a SPNEDA system for implementing the above method, specifically including a DO / pH probe 5, a constant temperature water tank 7, an aeration pump 9, and a water inlet tank 1, a SPNEDA reactor 4 and a water outlet tank connected in sequence, the constant temperature water tank 7 and the interlayer between the inner and outer walls of the SPNEDA reactor 4 are connected, the aeration pump 9 is used to aerate the SPNEDA reactor 4, and the DO / pH probe 5 is used to detect the dissolved oxygen content and pH value of the sewage in the SPNEDA reactor 4. In this embodiment, the DO / pH probe 5 is specifically a WTW-DO / pH probe, and the WTW Multi340i is specifically used to detect and record the pH, temperature and DO value in the SPNEDA reactor.

[0044] Among them, the SPNEDA reactor used in this embodiment has an upper cylindrical sleeve and a lower conical structure. The inner diameter of the cylindrical part of the SPNEDA reactor is 100 mm and the height is 400 mm. The 40mm-60mm below the overflow weir at the reactor outlet is filled with polyurethane sponge filler, and an aeration head is arranged in the hollow part. The height of the lower cone of the SPNEDA reactor is 60 mm, and the total volume of the SPNEDA reactor is 3.3L.

[0045] The constant temperature water tank 7 is provided with a heating rod 10, which is used to heat the constant temperature water tank to maintain the temperature of the water in the constant temperature water tank, thereby achieving the temperature of the mixed liquid in the SPNEDA reactor being maintained at 30±2°C.

[0046] It also includes a reflux pump 3, which is used to return the sewage from the top of the SPNEDA reactor 4 to the bottom of the SPNEDA reactor 4. The sewage from the SPNEDA reactor is fully contacted with the granular sludge, the mass transfer process is increased, and there is no hydraulic dead zone inside, so that the fluidity of the sludge is good and the operation is stable; at the same time, oxygen is transported to the bottom of the SPNEDA reactor to control the dissolved oxygen content at the bottom of the SPNEDA reactor. The discharge port of the outlet pipeline connected to the reflux pump 3 is tilted on the SPNEDA reactor 4, and the tilt direction of the discharge port of the outlet pipeline is adjustable. The feed port of the inlet pipeline connected to the reflux pump 3 is tilted downward on the SPNEDA reactor 4.

[0047] It also includes an aeration plate and an aeration pipe 6. The aeration plate is located in the SPNEDA reactor 4. The aeration plate is connected to the aeration pump 9 through the aeration pipe 6. The aeration plate increases the dissolved oxygen in the water by releasing air (usually compressed air) into the water in the form of fine bubbles, and introduces air or oxygen into the water uniformly, thereby promoting the dissolution of oxygen in the water, improving the water quality, and promoting the growth of microorganisms and the degradation of organic matter. It also includes a gas flow meter, and the aeration intensity is controlled by using the gas flow meter.

[0048] The connection port between the outlet tank and the SPNEDA reactor 4 is located above the connection port between the inlet pipeline connected to the reflux pump 3 and the SPNEDA reactor 4. The connection port between the inlet tank 1 and the SPNEDA reactor 4 is located at the bottom of the SPNEDA reactor 4, and the connection port between the outlet tank and the SPNEDA reactor 4 is located at the top of the SPNEDA reactor 4.

[0049] It also includes a water inlet pump 2, which is used to pump sewage from the water inlet pool 1 into the SPNEDA reactor 4; a water bath circulation pump 8, the water inlet end of the water bath circulation pump 8 is connected to the constant temperature water tank 7, and the water inlet end of the water bath circulation pump 8 is connected to the interlayer between the inner and outer walls of the SPNEDA reactor 4. The connection point between the water bath circulation pump 8 and the SPNEDA reactor 4 is located at the bottom of the SPNEDA reactor 4, and the connection point between the constant temperature water tank 7 and the SPNEDA reactor 4 is located at the top of the SPNEDA reactor 4. In this way, water enters the top of the interlayer between the inner and outer walls of the SPNEDA reactor 4, and drains from the bottom, the water circulation speed is faster, and the temperature fluctuation of the SPNEDA reactor 4 is reduced.

[0050] In the scheme of this embodiment, peristaltic pumps are used for water bath circulation pump 8, water inlet pump 2 and reflux pump 3. In this scheme, a timer switch is used to control the operation time of the water inlet reflux and water outlet pumps to convert into a CSBR (Cycle-flow Sequencing Batch Reactor) operation mode with a drainage ratio of 50%.

[0051] The test system involved in this embodiment can be scaled up in the same proportion for industrial use by correspondingly scaling up relevant facilities, such as the volume of the SPNEDA reactor, the water inlet pool, the water bath pool, and the flow rate of the pump, which will not be described in detail.

[0052] The above is only an embodiment of the present invention, and the common knowledge such as the known specific technical schemes and / or characteristics in the scheme is not described in detail here. It should be pointed out that for those skilled in the art, several variations and improvements can be made without departing from the technical scheme of the present invention. In the present invention, unless otherwise clearly specified and limited, the terms "install", "connect", "connect", "fix" and the like should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be directly connected, or indirectly connected through an intermediate medium, or it can be the internal connection of two components. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to the specific circumstances. The scope of protection claimed in this application shall be based on the content of its claims, and the specific implementation methods and other records in the specification can be used to interpret the content of the claims.

Claims

1. A SPNEDA system control method, characterized in that: include: Step 1: Anaerobic stage: Add sewage to the SPNEDA reactor to make the liquid level reach the preset position, and then control the SPNEDA reactor to operate in anaerobic mode for 60 minutes. The denitrifying bacteria in the SPNEDA reactor store carbon sources and heat the SPNEDA reactor. 25 minutes to 35 minutes before the end of the anaerobic stage, add NH2OH with a concentration of 4 to 8 mg / L to the SPNEDA reactor; Step 2: Aerobic stage: aerobic aeration is performed in the SPNEDA reactor for 360 min, and ammonia oxidizing bacteria in the SPNEDA reactor perform autotrophic short-range nitrification; Step 3: Anoxic stage: After 210 minutes of anoxic period, the water is discharged after settling for 35 minutes. The anaerobic ammonium oxidizing bacteria in the SPNEDA reactor carry out anaerobic ammonium oxidation reaction, and the denitrifying bacteria carry out endogenous denitrification.

2. The method according to claim 1, characterized in that: 25 min before the end of the anaerobic stage in step 1, NH2OH with a concentration of 6 mg / L was added to the SPNEDA reactor.

3. The method according to claim 1, characterized in that: It also includes controlling the dissolved oxygen content in the SPNEDA reactor to less than 0.8 mg / L and the pH value to 7.2-8.2 at each stage.

4. The method according to claim 1, characterized in that: In the step 2, the wastewater of the SPNEDA reactor is refluxed and stirred.

5. The method according to claim 1, characterized in that: In step 1, the temperature of the SPNEDA reactor is maintained at 28-32°C.

6. The method according to claim 1, characterized in that: In the step 2, the wastewater at the top of the SPNEDA reactor is refluxed to the bottom of the SPNEDA reactor by external reflux.

7. A SPNEDA system implementing the method of claim 1, characterized in that: include: A DO / pH probe, a constant temperature water tank, an aeration pump, and a water inlet tank, a SPNEDA reactor and a water outlet tank are connected in sequence. The constant temperature water tank is connected to the interlayer between the inner and outer walls of the SPNEDA reactor. The aeration pump is used to aerate the SPNEDA reactor. The DO / pH probe is used to detect the dissolved oxygen content and pH value of the sewage in the SPNEDA reactor.

8. A SPNEDA system according to claim 7, characterized in that: The system also includes a return pump, which is used to return wastewater from the top of the SPNEDA reactor to the bottom of the SPNEDA reactor.

9. A SPNEDA system according to claim 7, characterized in that: The device also includes an aeration plate, which is located on the top of the SPNEDA reactor and is connected to an aeration pump.

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