CN114671514A - Sewage electrochemical nitrogen and phosphorus removal device and method based on intelligent conductivity judgment - Google Patents
Sewage electrochemical nitrogen and phosphorus removal device and method based on intelligent conductivity judgment Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/005—Combined electrochemical biological processes
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/009—Apparatus with independent power supply, e.g. solar cells, windpower, fuel cells
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4616—Power supply
- C02F2201/46165—Special power supply, e.g. solar energy or batteries
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/002—Apparatus and plants for the biological treatment of water, waste water or sewage comprising an initial buffer container
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/05—Conductivity or salinity
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
The invention discloses a sewage electrochemical nitrogen and phosphorus removal device and method based on intelligent conductivity judgment. The AO biochemical reaction system main body comprises a water inlet adjusting tank, an anoxic tank, an aerobic tank and a water outlet sedimentation tank; the main body of the electrochemical enhanced nitrogen and phosphorus removal system comprises an active metal anode plate, a carbon-based material cathode net and a direct current power supply; the intelligent conductivity judgment system comprises a conductivity electrode, a conductivity on-line monitor and a PLC (programmable logic controller), wherein the PLC regulates and controls the operation modes of the AO biochemical reaction system and the electrochemical enhanced nitrogen and phosphorus removal system according to conductivity data; the solar power supply device provides auxiliary power. The invention can be reconstructed on the basis of the original facilities, has the advantages of high treatment efficiency, low construction cost, long service life of the electrode, convenient operation and maintenance management, capability of realizing unmanned autonomous regulation and control and the like, and is close to the actual rural domestic sewage treatment.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a sewage electrochemical nitrogen and phosphorus removal device and method based on intelligent conductivity judgment.
Background
At present, China adopts A2O, AO, the rural domestic sewage treatment stations of the process account for more than 80 percent of the total amount, and the carbon-nitrogen ratio of the rural domestic sewage is generally low, so that the treatment effect of the pure biochemical process is unstable, and the removal rate of nitrogen and phosphorus is low; in addition, the rural domestic sewage quality and water quantity change in China is large, the number of terminal stations is large, the dispersibility is high, and the like, so that the facility operation and maintenance management difficulty is high, and the consumption of manpower and material resources is high. All the reasons promote that rural domestic sewage treatment facilities in China are difficult to reach the first-level standard of relevant water pollutant discharge.
The electrochemical technology is combined with the traditional biochemical treatment process, the nitrogen and phosphorus removal efficiency of the sewage treatment facility can be effectively improved through the anodic electrocoagulation phosphorus removal and the cathodic autotrophic denitrification, and the method has the remarkable advantages of convenient operation and maintenance management, low sludge yield, no need of additional carbon source and the like. In recent years, the combined process is gradually applied to the technical field of rural domestic sewage treatment, but the related technologies cannot be well adapted to the actual situation of rural domestic sewage treatment, and the combined process has the defects of excessive electrolysis, high power consumption, excessive electrode loss, high construction cost and the like.
The patent with publication number CN201817307U discloses an integrated denitrification and dephosphorization electrolysis device, which adds a mesh metal electrode pair consisting of noble metal alloy and iron electrode in an electrolysis bath, and realizes the high-efficiency completion of the electrolytic denitrification and the electrolytic dephosphorization process in the same electrolysis bath by intermittently changing the polarity of the electrode. But the denitrification and dephosphorization processes of the device can not be synchronously carried out, and the device uses a noble metal electrode, so that the construction cost is high, and the device is not suitable for rural domestic sewage treatment terminals with small monomers and large quantity; in addition, the device does not distinguish the quality of the inlet water, thereby possibly causing the over-high voltage application, accelerating the electrode loss and excessively accumulating nitrite.
The patent with publication number CN205856074U discloses an electrolytic phosphorus removal device, which comprises an aeration tank, a total phosphorus on-line monitor, a programmable logic controller, a direct current power supply, an aluminum plate electrode, an iron plate electrode and the like, wherein the total phosphorus on-line monitor transmits a total phosphorus concentration signal into the programmable logic controller, and the programmable logic controller controls the current change of the direct current power supply, so that the unattended and intelligent impact resistance effect can be realized. However, the device cannot give consideration to other water quality indexes, and the treatment effect is limited; if other water quality index monitors are added, the construction cost is greatly improved.
Disclosure of Invention
In order to make the electrochemical-biochemical coupling process closer to the actual rural domestic sewage treatment, the invention provides a sewage electrochemical nitrogen and phosphorus removal device and method based on intelligent conductivity judgment, and aims to reduce electrochemical energy consumption and electrode loss and reduce operation and maintenance management difficulty and construction cost while realizing efficient synchronous nitrogen and phosphorus removal.
The invention adopts the following specific technical scheme:
the invention provides a sewage electrochemical nitrogen and phosphorus removal device based on intelligent conductivity judgment, which comprises an AO biochemical reaction system, an electrochemical enhanced nitrogen and phosphorus removal system, an intelligent conductivity judgment system and solar power supply equipment;
the AO biochemical reaction system comprises a water inlet adjusting tank, an anoxic tank, an aerobic tank and a water outlet sedimentation tank which are sequentially communicated along the water flow direction; a plurality of fillers for loading microorganisms are uniformly filled in the anoxic tank and the aerobic tank, stirring equipment is arranged in the anoxic tank, aeration equipment externally connected with a fan is arranged at the bottom of the aerobic tank, and a water outlet of the aerobic tank is communicated with a water inlet of the anoxic tank through a return pipeline provided with a return pump;
the electrochemical enhanced nitrogen and phosphorus removal system comprises an active metal anode plate, a carbon-based material cathode mesh and a direct current power supply; the active metal anode plate and the carbon-based material cathode mesh are arranged in the aerobic tank and can be contacted with water flow, and the plate surfaces of the active metal anode plate and the carbon-based material cathode mesh are perpendicular to the direction of the water flow and are arranged in parallel; the active metal anode plate and the carbon-based material cathode mesh are both connected with a direct current power supply arranged outside the aerobic pool;
the intelligent conductivity discrimination system comprises a first conductivity electrode, a second conductivity electrode, a conductivity on-line monitor and a PLC (programmable logic controller); the first conductivity electrode is arranged at the water inlet end of the AO biochemical reaction system, the second conductivity electrode is arranged at the water outlet end of the AO biochemical reaction system, and the first conductivity electrode and the second conductivity electrode are both connected with the conductivity on-line monitor and are used for monitoring the water inlet conductivity and the water outlet conductivity of the AO biochemical reaction system; the PLC is connected with the conductivity on-line monitor, the reflux pump and the direct-current power supply; the solar power supply equipment is used for supplying power to the electric equipment.
Preferably, the filler is a PP suspension ball with a built-in polyurethane sponge, the outer diameter of the suspension ball is 80-150 mm, and the filling volume of the filler is 75% of the total volume of the pool body.
Preferably, the aeration equipment is a micro-nano aeration disc which is positioned under the active metal anode plate and the carbon-based material cathode mesh and is used for supplying oxygen to the upper area.
Preferably, the active metal anode plate is an aluminum plate, the effective sectional area A is 1-3 times of sewage flow, the plate width B is 0.4-0.6 times of the tank body width along the water flow direction, and the plate thickness h is 1-10 mm; wherein the unit of the effective sectional area A is m2The unit of sewage flow is t/d, the unit of plate width B is m, and the unit of tank body width is m.
Preferably, the carbon-based material cathode mesh is prepared by taking carbon fiber filaments as a base material, and the preparation method comprises the following steps:
1) firstly, heating the carbon fiber yarn at 90 ℃ in a 10% hydrogen peroxide water bath for 2 hours to increase the number of oxygen-containing functional groups and micropores on the surface of the carbon fiber yarn and complete surface activation treatment on the carbon fiber yarn;
2) placing the carbon fiber filaments subjected to surface activation treatment in distilled water, heating in a 90 ℃ water bath for 2 hours to clean, and drying in a 105 ℃ drying oven after cleaning;
3) cutting the dried carbon fiber filaments into lengths of 10-20 cm;
4) weaving carbon fiber wires into a net by taking stainless steel wires with the diameter of 2-3 mm as a framework to obtain a carbon-based material cathode net;
the stainless steel wire framework and the active metal anode plate have the same size; in the carbon-based material cathode mesh, the mass ratio of the stainless steel wires to the carbon fiber wires is 1: 1; the effective sectional area ratio of the active metal anode plate to the carbon-based material cathode mesh is 1: (1-3).
Further, the carbon fiber yarns are 24K carbon fiber yarns.
Preferably, the center distance between the active metal anode plate and the carbon-based material cathode mesh is 10-20 cm, and the top ends of the active metal anode plate and the carbon-based material cathode mesh are at least 20cm higher than the effective water depth of the aerobic pool body.
Preferably, the first conductivity electrode and the second conductivity electrode are fixed by stainless steel supports and are respectively 10-20 cm away from the inner wall of the cell body; probes of the first conductivity electrode and the second conductivity electrode are immersed in the effective water depth of 30-50 cm, and perforated PVC protective sleeves are fixed on the outer portions of the probes.
Preferably, the conductivity online monitor is used for acquiring water quality data monitored by the first conductivity electrode and the second conductivity electrode in real time, and the conductivity value can be automatically corrected to be a correction value at 25 ℃.
In a second aspect, the invention provides a rural domestic sewage treatment method using the electrochemical nitrogen and phosphorus removal device for sewage in the first aspect, which specifically comprises the following steps:
1) in the device starting stage, the reflux pump is controlled by the PLC controller to adjust the internal reflux ratio to 200%, the direct current power supply continuously outputs constant current, and the current density between the active metal anode plate and the carbon-based material cathode net is from 0.25A/m2Gradually increase to 1.25A/m2And finally stably maintained at 1.25A/m2The filler in the anoxic tank is loaded with the hydrogen autotrophic denitrifying bacteria, the heterotrophic denitrifying bacteria and the heterotrophic bacteria capable of degrading organic matters, and the filler in the aerobic tank and the carbon-based material cathode net are loaded with the nitrobacteria, the hydrogen autotrophic denitrifying bacteria and the heterotrophic bacteria capable of degrading organic matters; when the effluent index of the AO biochemical reaction system tends to be stable, the device is started;
2) after the device is started, entering a formal operation stage, controlling the operation mode of the device by the PLC according to the conductivity value sigma 1 and the conductivity value sigma 2 respectively monitored by the first conductivity electrode and the second conductivity electrode, wherein the formal operation stage comprises the following specific steps:
s1: when sigma 1 is less than 500mS/cm and sigma 2 is less than 500mS/cm, the direct current power supply is turned off, and the reflux pump does not run; the sewage can be discharged after physical interception and biodegradation of an AO biochemical reaction system;
s2: when the sigma 1 is less than 500mS/cm and less than or equal to 900mS/cm, if the sigma 2 is less than 750mS/cm, the direct current power supply outputs low current, and the internal reflux ratio of the reflux pump is adjusted to be 0-150%;
s3: when the sigma 1 is less than or equal to 900mS/cm and the sigma 2 is more than 750mS/cm, the direct-current power supply outputs low current, and the internal reflux ratio of the reflux pump is adjusted to be 150-300%;
s4: when the sigma 1 is larger than 900mS/cm, if the sigma 2 is smaller than 750mS/cm, the direct-current power supply outputs high current, and the internal reflux ratio of the reflux pump is adjusted to be 0-150%;
s5: when sigma 1 is larger than 900mS/cm, if sigma 2 is larger than 750mS/cm, the direct-current power supply outputs high current, and the internal reflux ratio of the reflux pump is adjusted to be 150-300%;
the low current is to keep the current density between the active metal anode plate and the carbon-based material cathode net within 0.5-1.5A/m2The current of (a); the high current is to keep the current density between the active metal anode plate and the carbon-based material cathode net within 1.5-2.5A/m2The current of (a);
when the operation mode of the device is in any one of S2-S5, the sewage enters the anoxic tank through the water inlet adjusting tank, and the heterotrophic bacteria preliminarily degrade organic matters; meanwhile, the heterotrophic denitrifying bacteria and the hydrogen autotrophic denitrifying bacteria carry out denitrification reaction on the sewage by using an organic substrate in the sewage as a carbon source and a hydrogen electron donor carried in the nitrifying liquid returned by the return pipeline; after the sewage enters the aerobic tank, the small molecular organic matters are further degraded by heterotrophic bacteria, and NH in the sewage is treated by nitrobacteria3Oxidation of-N to NO3 -N, flocculating metal ions generated by the electrolysis of the active metal anode plate and phosphate ions in the sewage to generate phosphate precipitates so as to realize the removal of phosphorus; the carbon-based material cathode net is electrolyzed to generate hydrogen, so that a rich micro-anaerobic environment is formed nearby the carbon-based material cathode net, and the autotrophic denitrifying denitrification by the hydrogen autotrophic denitrifying bacteria is facilitated(ii) a Incompletely utilized hydrogen electron donor and incompletely reduced NO in sewage3 --N re-enters the anoxic tank through the return line for further reaction.
Compared with the prior art, the invention has the following beneficial effects:
(1) based on the design idea of the invention, the method can be reconstructed on the basis of most of domestic constructed rural domestic sewage treatment facilities, and the electrode material and the conductivity monitoring equipment are cheap and easy to obtain, the construction cost is low, and the method is suitable for rural actual conditions;
(2) in the electrochemical enhanced nitrogen and phosphorus removal system, the phosphorus removal of the anode (active metal anode plate) and the denitrification of the cathode (carbon-based material cathode mesh) can be synchronously and efficiently carried out, so that the reflux quantity of the nitrified liquid is greatly reduced, even the reflux of the nitrified liquid is not needed, and the reflux energy consumption in the AO process is reduced;
(3) the device can realize the automatic switching of the operation mode, avoid the problems of increased power consumption, excessively fast electrode loss and nitrite accumulation caused by excessive electrolysis and effectively reduce the operation and maintenance management difficulty and cost of the device;
(4) the solar power supply equipment provides power for the electrochemical enhanced nitrogen and phosphorus removal system and the conductivity intelligent judgment system, and the power consumption of the original AO process cannot be increased.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment of an electrochemical wastewater denitrification and dephosphorization apparatus based on intelligent conductivity discrimination.
FIG. 2 is a schematic structural diagram of a cathode mesh made of carbon-based material in an embodiment of an electrochemical nitrogen and phosphorus removal device for wastewater based on intelligent determination of conductivity.
The reference numerals shown in the figures are as follows:
1-a water inlet adjusting tank; 2-an anoxic tank; 3-an aerobic tank; 4-a water outlet sedimentation tank; 5-a filler; 6-stirring equipment; 7-aeration equipment; 8-a fan; 9-a lift pump; 10-reflux pump; 11-an active metal anode plate; 12-carbon-based material cathode mesh; 13-a direct current power supply; 141-a first conductivity electrode; 142-a second conductivity electrode; 15-conductivity on-line monitor; 16-a PLC controller; 17-a solar powered device; 18-stainless steel wire; 19-carbon fiber filaments.
Detailed Description
The invention will be further elucidated and described with reference to the drawings and the detailed description. The technical features of the embodiments of the present invention can be combined correspondingly without mutual conflict.
As shown in fig. 1, the electrochemical nitrogen and phosphorus removal device for sewage based on intelligent conductivity judgment provided by the present invention mainly comprises an AO biochemical reaction system, an electrochemical enhanced nitrogen and phosphorus removal system, an intelligent conductivity judgment system and a solar power supply device 17.
The AO biochemical reaction system mainly comprises a water inlet adjusting tank 1, an anoxic tank 2, an aerobic tank 3 and a water outlet sedimentation tank 4, wherein the water inlet adjusting tank 1, the anoxic tank 2, the aerobic tank 3 and the water outlet sedimentation tank 4 are sequentially communicated along the water flow direction. The water inlet adjusting tank 1 is used for preliminarily storing the sewage to be treated so as to adjust the quality and quantity of the sewage entering the anoxic tank 2. The water outlet of the water inlet adjusting tank 1 is communicated with the water inlet of the anoxic tank 2 through a pipeline provided with a lift pump 9, and the water outlet of the anoxic tank 2 is communicated with the water inlet of the aerobic tank 3 through a pipeline. A plurality of fillers 5 used for loading microorganisms are uniformly filled in the anoxic tank 2 and the aerobic tank 3, and in practical application, the fillers 5 can adopt PP suspension balls with built-in polyurethane sponge, the outer diameter of each suspension ball is 80-150 mm, and the filling volume of each filler 5 is 75% of the total volume of the tank body. The anoxic tank 2 is internally provided with a stirring device 6 which ensures that the anoxic tank 2 is completely mixed with fluid state by stirring. The bottom of the aerobic tank 3 is provided with an aeration device 7 externally connected with a fan 8, and in practical application, the aeration device 7 can adopt a micro-nano aeration disc which is positioned under an active metal anode plate 11 and a carbon-based material cathode mesh 12 and is used for supplying oxygen for the upper area. The water outlet of the aerobic tank 3 is communicated with the water inlet of the anoxic tank 2 through a return pipeline provided with a return pump 10, and the return ratio is controlled between the anoxic tank 2 and the aerobic tank 3 through the return pump 10.
In practical application, the AO biochemical reaction system runs in a continuous flow mode, the retention time of the anoxic tank 2 is 2-3 h, and the dissolved oxygen concentration is controlled below 0.5 mg/L; the retention time of the aerobic tank 3 is 8-12 h, and the dissolved oxygen concentration is controlled to be 2-4 mg/L.
Effluent treated by the aerobic tank 3 enters the effluent sedimentation tank 4 through a pipeline, a sludge outlet is formed in the bottom of the effluent sedimentation tank 4 and is externally connected with two sludge pipelines, the first sludge pipeline can discharge residual sludge periodically, and the second sludge pipeline can return partial sludge to the anoxic tank 2 periodically.
The electrochemical enhanced nitrogen and phosphorus removal system comprises an active metal anode plate 11, a carbon-based material cathode mesh 12 and a direct current power supply 13. The active metal anode plate 11 and the carbon-based material cathode mesh 12 are both arranged in the aerobic tank 3, and the surfaces of the active metal anode plate and the carbon-based material cathode mesh are perpendicular to the water flow direction and are arranged in parallel. The active metal anode plate 11 and the carbon-based material cathode mesh 12 are partially exposed out of the water surface, and the lower parts of the active metal anode plate and the carbon-based material cathode mesh can be in contact reaction with water flow. In practical application, the distance between the centers of the active metal anode plate 11 and the carbon-based material cathode mesh 12 is 10-20 cm, and the top ends of the active metal anode plate and the carbon-based material cathode mesh are at least 20cm higher than the effective depth of the aerobic pool 3. The active metal anode plate 11 and the carbon-based material cathode net 12 are both connected with a direct current power supply 13 arranged outside the aerobic pool 3, the active metal anode plate 11 is connected with the positive pole of the direct current power supply 13, and the carbon-based material cathode net 12 is connected with the negative pole of the direct current power supply 13.
In this embodiment, the active metal anode plate is an aluminum plate, and the size of the aluminum plate is adjusted correspondingly according to the sewage flow and the width of the tank body. Effective sectional area A (m) of aluminum plate2) (1-3) sewage flow rate (t/d), plate width (b) (m) (0.4-0.6) tank width (m, along water flow direction), and plate thickness (h) 1-10 mm. The carbon-based material cathode mesh 12 is prepared by taking carbon fiber filaments 19 as a basic material, and the specific preparation method comprises the following steps:
(1) firstly, carrying out surface activation treatment on carbon fiber yarns: heating the carbon fiber filaments in 10% hydrogen peroxide water bath for 2 hours at 90 ℃ to increase the number of oxygen-containing functional groups and micropores on the surfaces of the carbon fiber filaments, so that autotrophic denitrifying bacteria can be better and faster enriched; (2) placing the carbon fiber filaments 19 subjected to surface activation treatment in distilled water, heating in a water bath at 90 ℃ for 2 hours for cleaning, and drying in a drying oven at 105 ℃ after cleaning; (3) cutting the dried carbon fiber into small sections of 10-20 cm; (4) a stainless steel wire 18 with the diameter of 2-3 mm is used as a framework, and carbon fiber wires are woven into a net as shown in figure 2. After weaving, the mass ratio of the stainless steel wires to the carbon fiber wires is 1:1, the outline of the cathode stainless steel wire framework is the same as the size of the active metal anode plate, and the effective sectional area ratio of the anode plate to the cathode mesh is 1: (1-3).
Specifically, the carbon fiber yarn is preferably 24K carbon fiber yarn having the highest number of filaments per strand on the market. In order to enhance the treatment effect of the aerobic tank 3, the number of the active metal anode plates and the number of the carbon-based material cathode nets can be increased in pairs according to the actual water quality and water quantity conditions, so that the cathodes and the anodes are connected in series in pairs to form a closed loop; or the number of the carbon-based material cathode nets is increased independently, and the carbon-based material cathode nets are connected in parallel.
The intelligent conductivity discrimination system comprises a first conductivity electrode 141, a second conductivity electrode 142, a conductivity on-line monitor 15 and a PLC 16. The first conductivity electrode 141 is disposed at a water inlet end of the AO biochemical reaction system (which can be disposed in the water inlet regulation tank 1 or the water inlet of the anoxic tank 2), the second conductivity electrode 142 is disposed at a water outlet end of the AO biochemical reaction system (which can be disposed at the water outlet of the aerobic tank 3 or the water outlet sedimentation tank 4), and both the first conductivity electrode 141 and the second conductivity electrode 142 are connected to the conductivity on-line monitor 15 for monitoring the water inlet conductivity and the water outlet conductivity of the AO biochemical reaction system. The PLC 16 is connected with the conductivity on-line monitor 15, the reflux pump 10 and the DC power supply 13. The solar power supply device 17 is used for supplying power to the electric devices.
In practical application, the first conductivity electrode 141 and the second conductivity electrode 142 are fixed by stainless steel supports and are respectively 10-20 cm away from the inner wall of the cell body. Probes of the first conductivity electrode 141 and the second conductivity electrode 142 are immersed in the effective water depth (the lowest water level in the regulating reservoir) of 30-50 cm, and perforated PVC protective sleeves are fixed outside the probes. The conductivity online monitor 15 is used for acquiring the water quality data monitored by the first conductivity electrode 141 and the second conductivity electrode 142 in real time, and the conductivity value can be automatically corrected to a correction value at 25 ℃.
In practical application, the real-time conductivity data measured by the first conductivity electrode 141 and the second conductivity electrode 142 is transmitted to the PLC controller 16 through the conductivity on-line monitor 15, and the PLC controller 16 regulates and controls the operation modes of the AO biochemical reaction system and the electrochemical enhanced nitrogen and phosphorus removal system according to a preset conductivity threshold and an operation program corresponding to the conductivity threshold, and autonomously adjusts the output current of the dc power supply 13 and the operation state of the reflux pump 10, thereby ensuring that the coupling effect between the electrochemical process and the biochemical process is maximized, and realizing low-consumption and high-efficiency nitrogen and phosphorus removal.
The rural domestic sewage treatment method utilizing the sewage electrochemical nitrogen and phosphorus removal device specifically comprises the following steps:
1) in the device starting stage, the reflux pump 10 is controlled to be in a closed state by the PLC 16, the direct current power supply 13 continuously outputs constant current, and the current density between the active metal anode plate 11 and the carbon-based material cathode mesh 12 is from 0.25A/m2Gradually increase to 1.25A/m2(increase 0.25A/m every 3 days2) And finally stably maintained at 1.25A/m2The filler 5 in the anoxic pond 2 is loaded with the hydrogen autotrophic denitrifying bacteria, the heterotrophic denitrifying bacteria and the heterotrophic bacteria capable of degrading organic matters, and the filler 5 in the aerobic pond 3 and the carbon-based material cathode net 12 are loaded with the nitrifying bacteria, the hydrogen autotrophic denitrifying bacteria and the heterotrophic bacteria capable of degrading organic matters. When various water quality indexes such as COD, ammonia nitrogen, TN, TP and the like of the effluent tend to be stable, the device is started.
2) After the device is started, entering a formal operation stage, the PLC controller 16 controls an operation mode of the device according to the conductivity value σ 1 and the conductivity value σ 2 respectively monitored by the first conductivity electrode 141 and the second conductivity electrode 142, specifically as follows:
s1: when σ 1<500mS/cm and σ 2<500mS/cm, the DC power supply 13 is turned off and the reflux pump 10 is not operated. At the moment, the water inflow of the device can cause the great dilution of pollutants due to rain and sewage mixed flow, and the sewage can be discharged after physical interception and simple biodegradation of an AO biochemical reaction system.
S2: when the 500mS/cm < sigma 1 is less than or equal to 900mS/cm, if the sigma 2 is less than 750mS/cm, the direct current power supply 13 outputs low current, and the internal reflux ratio of the reflux pump 10 is adjusted to be 0-150%.
S3: when the 500mS/cm < sigma 1 is less than or equal to 900mS/cm, if sigma 2 is more than 750mS/cm, the direct current power supply 13 outputs low current, and the internal reflux ratio of the reflux pump 10 is adjusted to be 150-300%.
S4: when the sigma 1 is larger than 900mS/cm, if the sigma 2 is smaller than 750mS/cm, the direct current power supply 13 outputs high current, and the internal reflux ratio of the reflux pump 10 is adjusted to be 0-150%.
S5: when the sigma 1 is more than 900mS/cm, if the sigma 2 is more than 750mS/cm, the direct current power supply 13 outputs high current, and the internal reflux ratio of the reflux pump 10 is adjusted to be 150-300%.
In the modes S2-S5, the low current is such that the current density between the active metal anode plate 11 and the carbon-based material cathode mesh 12 is maintained at 0.5-1.5A/m2The current of (2). The high current is to keep the current density between the active metal anode plate 11 and the carbon-based material cathode mesh 12 at 1.5-2.5A/m2The current of (2).
When the operation mode of the device is in any one of S2-S5, sewage enters the anoxic tank 2 through the water inlet adjusting tank 1, and organic matters are primarily degraded by heterotrophic bacteria. Meanwhile, the heterotrophic denitrifying bacteria and the hydrogen autotrophic denitrifying bacteria carry out denitrification reaction on the sewage by using an organic substrate in the sewage as a carbon source and using a hydrogen electron donor carried in the nitrifying liquid returned by the return pipeline. After the sewage enters the aerobic tank 3, the small molecular organic matters are further degraded by heterotrophic bacteria, and NH in the sewage is treated by nitrifying bacteria3Oxidation of-N to NO3 -And N, flocculating metal ions generated by the electrolysis of the active metal anode plate 11 and phosphate ions in the sewage to generate phosphate precipitates, and removing phosphorus. The carbon-based material cathode net 12 generates hydrogen through electrolysis, so that a rich micro-anaerobic environment is formed nearby, and the autotrophic denitrification by the hydrogen autotrophic denitrifying bacteria is facilitated. Incompletely utilized hydrogen electron donor and incompletely reduced NO in sewage3 -N re-enters the anoxic tank 2 through the return line for further reaction.
In actual use, the water quality can be appropriately adjusted according to the specific water quality, but the invention concept of the modes S1 to S5 should not be deviated. The results of the pilot test for sewage treatment using the above-described apparatus are given below.
Example 1
Formula for artificially simulating sewage by water inflowThe following were used: NaAc (200-250 mg/L), NH4Cl(100～120 mg/L)，KNO3(25～35mg/L)，KH2PO4(7.5～11.5mg/L)，NaCl(0.5mg/L)， MgSO4·7H2O(25mg/L)，CaCl2(15mg/L)，NaHCO3(0.5mg/L), trace element solution (0.5 mL/L). The formula of the trace element solution is as follows: FeCl3·6H2O(1.5g/L)，MnCl2·4H2O (0.12g/L)，CoCl2·6H2O(0.15g/L)，H3BO3(0.15g/L)，Na2MoO4·2H2O(0.06 g/L)，CuSO4·5H2O(0.03g/L)，KI(0.18g/L)，ZnSO4·7H2O(0.12g/L)， Na2EDTA·2H2O(2.0g/L)。
The sewage flow Q is 6L/d, and the effective sectional area A of the aluminum plate is 180cm2The plate thickness h is 1 mm. The retention time of the anoxic tank is 3h, and the dissolved oxygen concentration is controlled below 0.5 mg/L; the retention time of the aerobic tank is 12 hours, and the dissolved oxygen concentration is controlled to be 2-4 mg/L.
The inlet water meets 500mS/cm<Sigma 1 is less than or equal to 900mS/cm, the adjusting device operates in an S2 mode, and the specific parameters are as follows: the DC power supply outputs a constant current of 25mA (the current density between the polar plates is about 1.14A/m)2) The nitrified liquid does not flow back. After the device is stable in an S2 mode, the device continuously runs for a week, the water inlet sigma 1 is 796-806 mS/cm, the water outlet sigma 2 is 528-618 mS/cm, and sigma 2 is always satisfied<750mS/cm, the mode of operation is unchanged. The specific indexes of the influent water concentration and the treatment result are as follows:
the pH value of inlet water is 7.63-7.81, and the pH value of outlet water is 7.40-7.61; the COD water inlet value is 185-248 mg/L, the water outlet value is 2.6-30.9 mg/L, and the removal rate is 83.7% -98.7%; the ammonia nitrogen inflow value is 30.08-32.75 mg/L, the outflow value is 0.05-2.10 mg/L, and the removal rate is 93.35% -99.84%; the TN water inlet value is 35.79-37.09 mg/L, the water outlet value is 13.07-17.99 mg/L, and the removal rate is 49.72-64.46%; the TP water inlet value is 2.64-2.99 mg/L, the water outlet value is 0-0.05 mg/L, and the removal rate is 98.33-100%; the nitrite accumulation amount is 0-0.71 mg/L, and no obvious accumulation effect exists.
According to the discharge standard of water pollutants of rural domestic sewage treatment facilities in Shanghai city (DB 31/T1163-2019), the effluent of the device basically meets the first-class A discharge standard. According to the environmental quality standard of surface water (GB3838-2002), the TP of the device effluent meets the II-class water standard, and the COD and ammonia nitrogen of the effluent basically meet the IV-class water standard.
Example 2
The formula of the artificial simulated sewage for water inlet is as follows: NaAc (200-250 mg/L), NH4Cl(140～150 mg/L)，KNO3(140～150mg/L)，KH2PO4(25～35mg/L)，NaCl(0.5mg/L)， MgSO4·7H2O(25mg/L)，CaCl2(15mg/L)，NaHCO3(0.5mg/L), trace element solution (0.5 mL/L). The formulation of the trace element solution was the same as in example 1.
The sewage flow, the device structure and the operation parameters are the same as those in example 1.
The inlet water satisfies sigma 1>900mS/cm, the adjusting device runs in an S4 mode, and the specific parameters are as follows: the DC power supply outputs a constant current of 48mA (the current density between the polar plates is about 2.20A/m)2) The nitrified liquid does not flow back. After the device is stable in the S4 mode, the device continuously runs for a week, the water inlet sigma 1 is 901-926 mS/cm, the water outlet sigma 2 is 516-735 mS/cm, and the sigma 2 is always met<750mS/cm, the mode of operation is unchanged. The specific indexes of the influent water concentration and the treatment result are as follows:
the pH value of inlet water is 7.39-7.57, and the pH value of outlet water is 7.53-8.48; the COD water inlet value is 200-227 mg/L, the water outlet value is 4.4-11.6 mg/L, and the removal rate is 94.2% -98.1%; the ammonia nitrogen inflow value is 38.49-39.56 mg/L, the outflow value is 0.66-3.24 mg/L, and the removal rate is 91.71-98.30%; TN water inlet value is 55.14-58.55 mg/L, water outlet value is 14.48-28.57 mg/L, and removal rate is 51.20% -74.54%; the TP water inlet value is 7.47-7.67 mg/L, the water outlet value is 0.02-0.20 mg/L, and the removal rate is 97.31% -99.75%; the nitrite accumulation amount is 0.56-1.55 mg/L, and no obvious accumulation effect exists.
According to the discharge standard of water pollutants for rural domestic sewage treatment facilities in Shanghai city (DB 31/T1163-2019), the effluent TN of the device basically meets the first-class B discharge standard, and the other indexes meet the first-class A discharge standard. According to the environmental quality standard of surface water (GB3838-2002), COD and TP of the device effluent basically meet the II-class water standard.
The invention can be reconstructed on the basis of the original facilities, has the advantages of high treatment efficiency, low construction cost, long service life of the electrode, convenient operation and maintenance management, capability of realizing unmanned autonomous regulation and control and the like, and is close to the actual rural domestic sewage treatment.
The above-described embodiments are merely preferred embodiments of the present invention, which should not be construed as limiting the invention. Various changes and modifications may be made by one of ordinary skill in the pertinent art without departing from the spirit and scope of the present invention. Therefore, the technical scheme obtained by adopting the mode of equivalent replacement or equivalent transformation is within the protection scope of the invention.
Claims (10)
1. An electrochemical nitrogen and phosphorus removal device for sewage based on intelligent conductivity judgment is characterized by comprising an AO biochemical reaction system, an electrochemical enhanced nitrogen and phosphorus removal system, an intelligent conductivity judgment system and a solar power supply device (17);
the AO biochemical reaction system comprises a water inlet adjusting tank (1), an anoxic tank (2), an aerobic tank (3) and a water outlet sedimentation tank (4) which are sequentially communicated along the water flow direction; a plurality of fillers (5) for loading microorganisms are uniformly filled in the anoxic tank (2) and the aerobic tank (3), stirring equipment (6) is arranged in the anoxic tank (2), aeration equipment (7) externally connected with a fan (8) is arranged at the bottom of the aerobic tank (3), and a water outlet of the aerobic tank (3) is communicated with a water inlet of the anoxic tank (2) through a return pipeline provided with a return pump (10);
the electrochemical enhanced nitrogen and phosphorus removal system comprises an active metal anode plate (11), a carbon-based material cathode mesh (12) and a direct current power supply (13); the active metal anode plate (11) and the carbon-based material cathode mesh (12) are arranged in the aerobic pool (3) and can be contacted with water flow, and the plate surfaces of the active metal anode plate and the carbon-based material cathode mesh are perpendicular to the water flow direction and are arranged in parallel; the active metal anode plate (11) and the carbon-based material cathode mesh (12) are both connected with a direct current power supply (13) arranged outside the aerobic pool (3);
the conductivity intelligent discrimination system comprises a first conductivity electrode (141), a second conductivity electrode (142), a conductivity online monitor (15) and a PLC (programmable logic controller) (16); the first conductivity electrode (141) is arranged at the water inlet end of the AO biochemical reaction system, the second conductivity electrode (142) is arranged at the water outlet end of the AO biochemical reaction system, and the first conductivity electrode (141) and the second conductivity electrode (142) are both connected with the conductivity on-line monitor (15) and are used for monitoring the water inlet conductivity and the water outlet conductivity of the AO biochemical reaction system; the PLC (16) is connected with the conductivity online monitor (15), the reflux pump (10) and the direct current power supply (13); the solar power supply equipment (17) is used for supplying power to electric equipment.
2. The electrochemical nitrogen and phosphorus removal device for sewage water as claimed in claim 1, wherein the filler (5) is a PP suspension ball with a built-in polyurethane sponge, the outer diameter of the suspension ball is 80-150 mm, and the filling volume of the filler (5) is 75% of the total volume of the tank body.
3. The electrochemical denitrification and dephosphorization apparatus for sewage water according to claim 1, wherein said aeration equipment (7) is a micro-nano aeration disk, located right below the active metal anode plate (11) and the carbon-based material cathode mesh (12), for supplying oxygen to the upper region.
4. The electrochemical nitrogen and phosphorus removal device for sewage as claimed in claim 1, wherein the active metal anode plate (11) is an aluminum plate, the effective sectional area A is 1-3 times of the sewage flow, the plate width B is 0.4-0.6 times of the tank body width along the water flow direction, and the plate thickness h is 1-10 mm; wherein the unit of the effective sectional area A is m2The unit of sewage flow is t/d, the unit of plate width B is m, and the unit of tank body width is m.
5. The electrochemical denitrification and dephosphorization apparatus for sewage according to claim 1, wherein said carbon-based material cathode mesh (12) is prepared by using carbon fiber filament (19) as a base material, and the preparation method is as follows:
1) firstly, heating the carbon fiber filaments (19) in a water bath with 10% hydrogen peroxide at 90 ℃ for 2 hours to increase the number of oxygen-containing functional groups and micropores on the surface of the carbon fiber filaments (19), and completing surface activation treatment on the carbon fiber filaments (19);
2) placing the carbon fiber filaments (19) subjected to surface activation treatment in distilled water, heating in a water bath at 90 ℃ for 2 hours to clean, and drying in a drying oven at 105 ℃ after cleaning;
3) cutting the dried carbon fiber filaments (19) into lengths of 10-20 cm;
4) weaving carbon fiber wires (19) into a net by taking stainless steel wires (18) with the diameter of 2-3 mm as a framework to obtain a carbon-based material cathode net (12);
the size of the framework of the stainless steel wire (18) is the same as that of the active metal anode plate (11); in the carbon-based material cathode net (12), the mass ratio of the stainless steel wires (18) to the carbon fiber wires (19) is 1: 1; the effective sectional area ratio of the active metal anode plate (11) to the carbon-based material cathode mesh (12) is 1: (1-3).
6. The electrochemical nitrogen and phosphorus removal device for sewage as claimed in claim 5, wherein the carbon fiber wires (19) are 24K carbon fiber wires.
7. The electrochemical nitrogen and phosphorus removal device for sewage as claimed in claim 1, wherein the center-to-center distance between the active metal anode plate (11) and the carbon-based material cathode mesh (12) is 10-20 cm, and the top ends of the active metal anode plate and the carbon-based material cathode mesh are at least 20cm higher than the effective depth of the aerobic pool (3) in water.
8. The electrochemical nitrogen and phosphorus removal device for sewage according to claim 1, wherein the first conductivity electrode (141) and the second conductivity electrode (142) are fixed by stainless steel brackets and are respectively 10-20 cm away from the inner wall of the tank body; probes of the first conductivity electrode (141) and the second conductivity electrode (142) are immersed in the effective water depth of 30-50 cm, and perforated PVC protective sleeves are fixed on the outer portions of the probes.
9. The electrochemical denitrification and dephosphorization apparatus for sewage according to claim 1, wherein said conductivity on-line monitor (15) is configured to obtain data of water quality monitored by the first conductivity electrode (141) and the second conductivity electrode (142) in real time, and the obtained conductivity value can be automatically corrected to a corrected value at 25 ℃.
10. A rural domestic sewage treatment method using the electrochemical nitrogen and phosphorus removal device for sewage of any one of claims 1 to 9 is characterized by comprising the following steps:
1) in the device starting stage, the reflux pump (10) is controlled by the PLC (16) to adjust the internal reflux ratio to 200%, the direct current power supply (13) continuously outputs constant current, and the current density between the active metal anode plate (11) and the carbon-based material cathode mesh (12) is from 0.25A/m2Gradually increase to 1.25A/m2And finally stably maintained at 1.25A/m2The filler (5) in the anoxic pond (2) is loaded with the hydrogen autotrophic denitrifying bacteria, the heterotrophic denitrifying bacteria and the heterotrophic bacteria capable of degrading organic matters, and the filler (5) and the carbon-based material cathode net (12) in the aerobic pond (3) are loaded with the nitrobacteria, the hydrogen autotrophic denitrifying bacteria and the heterotrophic bacteria capable of degrading organic matters; when the effluent index of the AO biochemical reaction system tends to be stable, the device is started;
2) after the device is started, entering a formal operation stage, the PLC (16) controls the operation mode of the device according to the conductivity value sigma 1 and the conductivity value sigma 2 respectively monitored by the first conductivity electrode (141) and the second conductivity electrode (142), and the method specifically comprises the following steps:
s1: when sigma 1<500mS/cm and sigma 2<500mS/cm, the direct current power supply (13) is turned off and the reflux pump (10) is not operated; the sewage can be discharged after physical interception and biodegradation of an AO biochemical reaction system;
s2: when the 500mS/cm is less than or equal to sigma 1 and less than or equal to 900mS/cm, if the sigma 2 is less than 750mS/cm, the direct current power supply (13) outputs low current, and the internal reflux ratio is adjusted to be 0-150% by the reflux pump (10);
s3: when the sigma 1 is less than or equal to 500mS/cm and the sigma 2 is more than or equal to 750mS/cm, the direct current power supply (13) outputs low current, and the internal reflux ratio of the reflux pump (10) is adjusted to be 150-300%;
s4: when the sigma 1 is larger than 900mS/cm, if the sigma 2 is smaller than 750mS/cm, the direct current power supply (13) outputs high current, and the internal reflux ratio is adjusted to be 0-150% by the reflux pump (10);
s5: when sigma 1 is larger than 900mS/cm and sigma 2 is larger than 750mS/cm, the direct current power supply (13) outputs high current, and the internal reflux ratio of the reflux pump (10) is adjusted to be 150-300%;
the low current is to keep the current density between the active metal anode plate (11) and the carbon-based material cathode mesh (12) at 0.5-1.5A/m2The current of (a); the high current is to keep the current density between the active metal anode plate (11) and the carbon-based material cathode mesh (12) at 1.5-2.5A/m2The current of (a);
when the operation mode of the device is in any one of S2-S5, sewage enters the anoxic tank (2) through the water inlet adjusting tank (1), and organic matters are primarily degraded by heterotrophic bacteria; meanwhile, the heterotrophic denitrifying bacteria and the hydrogen autotrophic denitrifying bacteria carry out denitrification reaction on the sewage by using an organic substrate in the sewage as a carbon source and a hydrogen electron donor carried in the nitrifying liquid returned by the return pipeline; after the sewage enters the aerobic tank (3), the small molecular organic matters are further degraded by heterotrophic bacteria, and NH in the sewage is treated by nitrifying bacteria3Oxidation of-N to NO3 -N, metal ions generated by the electrolysis of the active metal anode plate (11) and phosphate ions in the sewage generate flocculation to generate phosphate precipitates, so that phosphorus is removed; the carbon-based material cathode net (12) is electrolyzed to generate hydrogen, so that an abundant micro-anaerobic environment is formed nearby the carbon-based material cathode net, and the autotrophic denitrification by the hydrogen autotrophic denitrifying bacteria is facilitated; incompletely utilized hydrogen electron donor and incompletely reduced NO in sewage3 --N re-enters the anoxic tank (2) through the return line for further reaction.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008264659A (en) * | 2007-04-19 | 2008-11-06 | Blue Aqua Industry Kk | Waste water treatment device |
| CN102010091A (en) * | 2010-12-27 | 2011-04-13 | 北京碧水源膜科技有限公司 | Advanced treatment method of sewage |
| CN107863536A (en) * | 2017-10-16 | 2018-03-30 | 香港科技大学 | Multiple dimensioned porous electrode applied to flow battery and its preparation method and application |
| CN109336328A (en) * | 2018-10-29 | 2019-02-15 | 浙江利欧环保科技有限公司 | A kind of bioelectrochemistry synchronous denitrification dephosphorizing devices and methods therefor |
| CN111925044A (en) * | 2020-01-10 | 2020-11-13 | 重庆大学 | Sequencing batch biofilm-electrolysis treatment and recycling device and method for domestic sewage |
| CN215712429U (en) * | 2021-03-23 | 2022-02-01 | 成都环能德美环保装备制造有限公司 | Small-size domestic sewage sequencing batch activated sludge-electrolysis equipment |
| CN114162974A (en) * | 2021-12-03 | 2022-03-11 | 哈尔滨工业大学（深圳） | Weak current intervention constructed wetland system for efficiently degrading parachloronitrobenzene and operation method |
| CN114314809A (en) * | 2021-12-16 | 2022-04-12 | 中国科学院生态环境研究中心 | Decentralized sewage treatment device and method |
-
2022
- 2022-04-20 CN CN202210417699.6A patent/CN114671514B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008264659A (en) * | 2007-04-19 | 2008-11-06 | Blue Aqua Industry Kk | Waste water treatment device |
| CN102010091A (en) * | 2010-12-27 | 2011-04-13 | 北京碧水源膜科技有限公司 | Advanced treatment method of sewage |
| CN107863536A (en) * | 2017-10-16 | 2018-03-30 | 香港科技大学 | Multiple dimensioned porous electrode applied to flow battery and its preparation method and application |
| CN109336328A (en) * | 2018-10-29 | 2019-02-15 | 浙江利欧环保科技有限公司 | A kind of bioelectrochemistry synchronous denitrification dephosphorizing devices and methods therefor |
| CN111925044A (en) * | 2020-01-10 | 2020-11-13 | 重庆大学 | Sequencing batch biofilm-electrolysis treatment and recycling device and method for domestic sewage |
| CN215712429U (en) * | 2021-03-23 | 2022-02-01 | 成都环能德美环保装备制造有限公司 | Small-size domestic sewage sequencing batch activated sludge-electrolysis equipment |
| CN114162974A (en) * | 2021-12-03 | 2022-03-11 | 哈尔滨工业大学（深圳） | Weak current intervention constructed wetland system for efficiently degrading parachloronitrobenzene and operation method |
| CN114314809A (en) * | 2021-12-16 | 2022-04-12 | 中国科学院生态环境研究中心 | Decentralized sewage treatment device and method |
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