CN111410313A - Side-flow type enhanced biological phosphorus removal process - Google Patents
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Abstract
The invention belongs to the technical field of biological sewage treatment, and particularly relates to a side-flow type enhanced biological phosphorus removal process, which comprises the following steps: the method comprises the following steps: introducing the wastewater into a primary sedimentation tank for sedimentation, introducing the separated sewage into an anoxic tank, and introducing the separated sludge into a primary sedimentation sludge fermentation tank; step two: introducing the sewage in the anoxic tank into the aerobic tank, reflowing part of nitrified liquid mud water discharged from the aerobic tank to the anoxic tank, and introducing the other part of nitrified liquid mud water into a secondary sedimentation tank; step three: after the sludge and the water of the nitrifying liquid in the secondary sedimentation tank are subjected to sludge-water separation, discharging supernatant, discharging partial sludge, and refluxing the other part of sludge to a bypass flow pre-anoxic tank; step four: adding primary sludge fermentation supernatant into a side-flow pre-anoxic tank, and allowing the mixture to enter a side-flow anaerobic tank after mixed reaction; and discharging the sludge after fermentation in the bypass anaerobic tank, and allowing the sludge to enter the main anoxic tank. The process gets rid of or reduces the dependence on the influent carbon source to a certain extent, and improves the dephosphorization effect and stability of the process.
Description
Technical Field
The invention belongs to the technical field of biological sewage treatment, and particularly relates to a side-flow type enhanced biological phosphorus removal process.
Background
With the rapid development of production industry and urbanization and the growth of population, the discharge amount of various domestic and industrial sewage is gradually increased, the problem of water eutrophication is increasingly prominent, and the water pollution condition is increasingly serious, so that the water resource crisis form in China is more severe. Wherein, the discharge of nitrogen and phosphorus nutrient elements is the main reason of the eutrophication of the receiving water body.
At present, the removal mode of phosphorus in wastewater is mainly divided into a chemical method and a biological method. The chemical method is mainly characterized in that some chemical agents, such as common iron salt, calcium salt and aluminum salt, are added into the wastewater, so that the chemical agents react with phosphorus in the wastewater to generate insoluble phosphate precipitate, and phosphorus is removed through a solid-liquid separation mode. The biological method (EBPR) is to remove phosphorus in wastewater by utilizing the characteristics of anaerobic phosphorus release and aerobic excessive phosphorus absorption of phosphorus accumulating bacteria of activated sludge under the condition of anaerobic and aerobic alternate operation, and to remove phosphorus by discharging phosphorus-containing excess sludge. Compared with a chemical method, the biological method has the advantages of environmental friendliness, low economic cost, small carbon footprint and the like. However, in the implementation of the EBPR process in a specific sewage plant, the growth and activity of phosphorus accumulating bacteria are often inhibited due to the lack of carbon source in the influent water and the fluctuation of water quality, so that the requirement of continuous and effective phosphorus removal performance cannot be met, and some sewage plants have to rely on the chemical phosphorus removal method more and more. Although the chemical method is simple and efficient, the dosage is large, the treatment cost is high, a large amount of chemical sludge is generated, and secondary pollution is easily caused if the chemical method is not properly treated. In addition, the chemical addition method also reduces the recovery efficiency of phosphorus in struvite.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a side-flow type enhanced biological phosphorus removal process. The technical problem to be solved by the invention is realized by the following technical scheme:
a side-flow type enhanced biological phosphorus removal process comprises a primary sedimentation tank, a primary sedimentation sludge fermentation tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a side-flow pre-anoxic tank and a side-flow anaerobic tank, and comprises the following steps:
the method comprises the following steps: introducing the wastewater into a primary sedimentation tank for sedimentation, introducing the separated sewage into an anoxic tank, and introducing the separated sludge into a primary sedimentation sludge fermentation tank;
step two: introducing the sewage in the anoxic tank into the aerobic tank, reflowing part of nitrified liquid mud water discharged from the aerobic tank to the anoxic tank, and introducing the other part of nitrified liquid mud water into a secondary sedimentation tank;
step three: after the sludge and the water of the nitrifying liquid in the secondary sedimentation tank are subjected to sludge-water separation, discharging supernatant, discharging partial sludge, and refluxing the other part of sludge to a bypass flow pre-anoxic tank;
step four: adding a certain amount of primary sludge fermentation supernatant into a bypass flow pre-anoxic tank, and making returned sludge enter a bypass flow anaerobic tank after mixed reaction; and discharging the sludge after deep fermentation and phosphorus accumulating bacteria reinforced screening in the bypass anaerobic tank, and entering the main anoxic tank.
Further, stirring devices are arranged in the primary sedimentation tank, the primary sedimentation sludge fermentation tank, the anoxic tank, the aerobic tank, the side-flow pre-anoxic tank and the side-flow anaerobic tank.
Further, an aeration device is arranged in the aerobic tank.
Further, the temperature of the muddy water is 5-35 ℃, the pH value is 6.5-8.0, and the sludge concentration is 2500-5000 mg/L.
Furthermore, the water temperature of the anoxic tank is 0.2-0.6 mg/L of dissolved oxygen, the reflux ratio of the nitrifying liquid is 100-400%, and the hydraulic retention time is 0.5-3 h.
Furthermore, the dissolved oxygen of the aerobic pool is not less than 2.0 mg/L, and the hydraulic retention time is 6.5-12 h.
Further, the sludge reflux ratio of the secondary sedimentation tank in the third step is 50-100%.
Further, the chemical oxygen demand of the supernatant obtained by fermenting the primary sludge in the fourth step is 50-300 mg/L.
Furthermore, the oxidation-reduction potential of the side-flow anaerobic tank is below-200 mV, and the retention time of the returned sludge is 1-4 h.
Compared with the prior art, the invention has the beneficial effects that:
1. the by-pass flow reactor can easily reach deep anaerobic conditions, is beneficial to fermentation acid production and screening reinforcement of phosphorus accumulating bacteria, and creates favorable conditions for the phosphorus accumulating bacteria to dominate in competition with the glycan bacteria, thereby enhancing the phosphorus removal performance of the process;
2. compared with the traditional biological phosphorus removal system, the side-stream process has more stable phosphorus removal performance, and phosphorus release and substrate absorption of phosphorus-accumulating bacteria under anaerobic conditions do not directly depend on the carbon-phosphorus ratio of inlet water;
3. because a certain amount of primary sludge fermentation supernatant is supplemented in the bypass pre-anoxic tank, the requirement on the fermentation acid production amount of the return sludge is reduced, and the requirement on the retention time of the return sludge in the bypass process is shortened, so that the design size and the occupied area of the bypass reactor are reduced, and more return sludge is subjected to carbon source supplement and screening acclimation through the bypass reactor and then flows back to the main process;
4. the influent carbon source is mainly supplied to the main flow process for denitrification, and meanwhile, the supplement of primary sludge fermentation liquor and the acid production by return sludge fermentation also promote denitrification, so that the nitrogen and phosphorus removal performance and stability of the whole process are enhanced;
5. the process structure is simple and flexible, and is easy to combine and reform with various processes of the existing sewage plant with a primary sludge fermentation tank, an anaerobic tank and an aerobic tank;
6. the side-flow reactor performs anaerobic fermentation on the returned sludge, and has a certain sludge reduction effect.
Drawings
FIG. 1 is a schematic view of the process flow.
In the figure: 1-primary settling tank; 2-primary sludge fermentation tank; 3-an anoxic pond; 4, an aerobic tank; 5-secondary sedimentation tank; 6-a side-stream pre-anoxic tank; 7-a side-stream anaerobic tank.
Detailed Description
The present invention will be described in further detail with reference to specific examples, but the embodiments of the present invention are not limited thereto.
Example 1:
a side-flow type enhanced biological phosphorus removal process comprises a primary sedimentation tank, a primary sedimentation sludge fermentation tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a side-flow pre-anoxic tank and a side-flow anaerobic tank, and comprises the following steps:
the method comprises the following steps: introducing the wastewater into a primary sedimentation tank for sedimentation, introducing the separated sewage into an anoxic tank, and introducing the separated sludge into a primary sedimentation sludge fermentation tank;
step two: introducing the sewage in the anoxic tank into the aerobic tank, reflowing part of nitrified liquid mud water discharged from the aerobic tank to the anoxic tank, and introducing the other part of nitrified liquid mud water into a secondary sedimentation tank;
step three: after the sludge and the water of the nitrifying liquid in the secondary sedimentation tank are subjected to sludge-water separation, discharging supernatant, discharging partial sludge, and refluxing the other part of sludge to a bypass flow pre-anoxic tank;
step four: adding a certain amount of primary sludge fermentation supernatant into a bypass flow pre-anoxic tank, and making returned sludge enter a bypass flow anaerobic tank after mixed reaction; and discharging the sludge after deep fermentation and phosphorus accumulating bacteria reinforced screening in the bypass anaerobic tank, and entering the main anoxic tank.
The primary sedimentation tank, the primary sedimentation sludge fermentation tank, the anoxic tank, the aerobic tank, the side-flow pre-anoxic tank and the side-flow anaerobic tank are all provided with stirring devices.
An aeration device is arranged in the aerobic tank.
The temperature of the muddy water is 5-35 ℃, the pH value is 6.5-8.0, and the sludge concentration is 2500-5000 mg/L.
The water temperature of the anoxic tank is 0.2-0.6 mg/L of dissolved oxygen, the reflux ratio of the nitrifying liquid is 100-400%, and the hydraulic retention time is 0.5-3 h.
The dissolved oxygen of the aerobic pool is not less than 2.0 mg/L, and the hydraulic retention time is 6.5-12 h.
And the sludge reflux ratio of the secondary sedimentation tank in the third step is 50-100%.
And in the fourth step, the chemical oxygen demand of the primary sludge fermentation supernatant is 50-300 mg/L after the primary sludge fermentation supernatant is added.
The oxidation-reduction potential of the side-flow anaerobic tank is below-200 mV, and the retention time of the returned sludge is 1-4 h.
As shown in figure 1, the device used in the process comprises a primary sedimentation tank, a primary sedimentation sludge fermentation tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a side-flow pre-anoxic tank and a side-flow anaerobic tank. The discharge of the primary sedimentation tank is divided into two parts of sludge and sewage, the sludge enters the primary sedimentation sludge fermentation tank and is connected by a pipeline, a water inlet pipeline is connected between the primary sedimentation tank and the anoxic tank, the water inlet pipeline is connected with a pump, the anoxic tank and the aerobic tank run in a plug flow mode, the tail end of the aerobic tank is provided with a nitrifying liquid return port, be connected to the oxygen deficiency pond through drain pipe and pump, the upper portion in good oxygen pond is equipped with the delivery port, through drain pipe connection to two heavy ponds, and good oxygen pond exhaust muddy water gets into two heavy ponds and carries out mud-water separation, and the bottom is equipped with mud return port and mud discharging port, and the mud discharging port is outside mud discharge system, and mud return port is equipped with the pump and flows back mud to the bypass and advances the oxygen deficiency pond in advance, and the bypass advances the oxygen deficiency pond and receives backward flow mud and a certain amount and come from leading-in bypass anaerobism pond with mud behind the fermentation supernatant of primary sedimentation mud fermentation pond, and the bypass anaerobism pond carries out the anaerobic fermentation and releases the phosphorus back with mud and flows back to the mainstream oxygen. Except the secondary sedimentation tank, each reaction tank is provided with a stirring device, and each aerobic tank is provided with an aeration device.
The process has the following functions:
primary sedimentation tank: the primary sedimentation tank is used for removing settleable matters and floating matters in the wastewater and separating mud from water, sewage enters the anoxic tank, and sludge enters the primary sedimentation sludge fermentation tank.
Primary sludge fermentation tank: the primary sludge fermentation tank is used for fermenting sludge discharged from the primary sludge fermentation tank, decomposing original organic matters in the sewage difficult to degrade again and providing a carbon source for the reaction of the biological tank.
An anoxic tank: the anoxic pond receives the inlet water and the nitrate from the aerobic pond, and the Chemical Oxygen Demand (COD) in the inlet water provides sufficient nutrients for denitrification, so the denitrification effect of the anoxic pond is superior to that of the traditional A2O reactor; the denitrifying phosphorus accumulating bacteria in the anoxic pond can absorb phosphorus synchronously.
An aerobic tank: an aeration head is arranged in the aerobic tank, so that the dissolved oxygen required by aerobic microorganisms and the condition of full contact of activated sludge are met, organic pollutants are degraded, and COD is further utilized and consumed; the phosphorus-accumulating bacteria absorb phosphorus, and synthesized polyphosphate is stored in cells, so that phosphorus-enriched activated sludge is formed.
A secondary sedimentation tank: the secondary sedimentation tank is used for separating mud and water to enable effluent to be clear and sludge to be concentrated, one part of separated sludge is taken as residual sludge to be discharged out of the system to realize biological phosphorus removal, the other part of separated sludge flows back to the bypass flow pre-anoxic tank, and the secondary sedimentation tank effect directly influences the effluent quality and the concentration of returned sludge.
Side-stream pre-anoxic zone: as the return sludge of the secondary sedimentation tank contains nitrate and is difficult to reach a deep anaerobic state, a side-flow pre-anoxic tank is arranged, and a certain amount of sludge fermentation liquor of the primary sedimentation tank or an external carbon source (methanol, sodium acetate, saccharides and the like) is added to promote denitrification, so that the influence of the nitrate on the anaerobic condition is reduced.
A side-flow anaerobic tank: the dissolved oxygen in the reaction zone is zero, the sludge is hydrolyzed, fermented and produced into acid, extra volatile fatty acid can be generated due to the deep anaerobic environment, the phosphorus-accumulating bacteria can absorb available carbon sources such as volatile fatty acid and the like, assimilate into intracellular carbon energy storage substance Polyhydroxyalkanoate (PHA), and store necessary carbon sources and energy for subsequent aerobic excess phosphorus absorption, the energy required by anaerobic biochemical reaction comes from the hydrolysis and glycolysis processes of intracellular polyphosphate, and the phosphate generated by hydrolysis can be diffused to the outside of cells to increase the phosphorus concentration.
Example 2:
the process is characterized in that sludge at a backflow section of a certain sewage treatment plant is taken, and is cleaned and domesticated, and the process is applied as follows:
firstly, raw sewage enters an anoxic tank, COD of the raw sewage is 180 mg/L, Total Nitrogen (TN) is 30 mg/L, Total Phosphorus (TP) is 6.8 mg/L, water temperature is 23 ℃, Hydraulic Retention Time (HRT) of the anoxic tank is 1.9h, and sludge concentration is 3500 mg/L;
secondly, the aerobic tank receives the sludge-water mixed liquor discharged by the anoxic tank, the HRT of the aerobic tank is 7.7h, the DO is more than 2 mg/L, and the reflux ratio of the nitrifying liquid is 300 percent;
thirdly, the sludge-water mixed liquor discharged from the aerobic tank 4 enters a secondary sedimentation tank for sludge-water separation, the sedimentation time of the secondary sedimentation tank is 1.9h, and the sludge concentration is 8000 mg/L;
the fourth step: after mud-water separation is carried out in the secondary sedimentation tank, supernatant is directly discharged out of the system, the precipitated activated sludge is divided into two parts, one part is discharged out of the system as residual sludge, the other part enters a bypass flow pre-anoxic tank as return sludge, and the sludge reflux ratio is 50%;
fifthly, anaerobic fermentation and phosphorus accumulating bacteria screening are carried out on the returned sludge through a bypass flow pre-anoxic tank and a bypass flow anaerobic tank, then the returned sludge flows back to an anoxic tank at a water inlet end, the HRT of the bypass flow pre-anoxic tank is 1.9h, the HRT of the bypass flow anaerobic tank is 3.8h, and a certain amount of sludge fermentation liquor of a primary sedimentation tank is added into the bypass flow pre-anoxic tank, so that the COD reaches 200 mg/L.
The method comprises the steps of enabling effluent of a primary sedimentation tank to enter an anoxic tank to provide a carbon source for denitrifying bacteria, removing nitrate flowing back from an aerobic tank to achieve the purpose of denitrification, enabling sludge-water mixed liquor in the anoxic tank to enter the aerobic tank, further decomposing organic matters by means of microorganisms, enabling phosphorus-accumulating bacteria to absorb phosphorus, transferring phosphorus from a water phase to a sludge phase, enabling ammonia nitrogen to be converted into nitrate nitrogen under the action of nitrifying bacteria, enabling the sludge-water mixed liquor in the aerobic tank to flow into a secondary sedimentation tank, discharging the phosphorus out of a system through sedimentation, enabling the phosphorus to flow into a bypass pre-anoxic tank, enabling the returned sludge to flow into the bypass pre-anoxic tank, adding primary sludge fermentation liquor to promote denitrification in the tank to minimize the nitrate, enabling the sludge to enter a bypass anaerobic tank, performing hydrolytic fermentation on the sludge to produce acid under deep anaerobic conditions, and achieving screening and domestication of the phosphorus-accumulating bacteria, wherein COD (12.8 mg/L) is equal to 6.8 mg/L equal to 0.13 mg/L, and all indexes of effluent meet the discharge index of pollutants in a municipal sewage treatment plant (GB18918-2002) discharge standard.
Example 3:
firstly, raw sewage enters an anoxic tank, wherein COD of the raw sewage is 250 mg/L and 40 mg/L is 10 mg/L, the water temperature is 23 ℃, HRT of the anoxic tank is 1.9h, and the sludge concentration is 3200 mg/L;
secondly, the aerobic tank receives the sludge-water mixed liquor discharged by the anoxic tank, the HRT of the aerobic tank is 7.7h, the DO is more than 2.7 mg/L, and the reflux ratio of the nitrifying liquid is 300 percent;
thirdly, the sludge-water mixed liquor discharged from the aerobic tank enters a secondary sedimentation tank for sludge-water separation, the sedimentation time of the secondary sedimentation tank is 1.9h, and the sludge concentration is 8200 mg/L;
the fourth step: after mud-water separation is carried out in the secondary sedimentation tank, supernatant is directly discharged out of the system, the precipitated activated sludge is divided into two parts, one part is discharged out of the system as residual sludge, the other part enters a bypass flow pre-anoxic tank as return sludge, and the sludge reflux ratio is 50%;
fifthly, anaerobic fermentation and phosphorus accumulating bacteria screening are carried out on the returned sludge through a bypass flow pre-anoxic tank and a bypass flow anaerobic tank, then the returned sludge flows back to an anoxic tank at a water inlet end, the HRT of the bypass flow pre-anoxic tank is 1.9h, the HRT of the bypass flow anaerobic tank is 3.8h, and a certain amount of sludge fermentation liquor of a primary sedimentation tank is added into the bypass flow pre-anoxic tank, so that the COD reaches 200 mg/L.
The method comprises the steps of enabling effluent of a primary sedimentation tank to enter an anoxic tank to provide a carbon source for denitrifying bacteria, removing nitrate flowing back from an aerobic tank to achieve the purpose of denitrification, enabling sludge-water mixed liquor in the anoxic tank to enter the aerobic tank, further decomposing organic matters by means of microorganisms, enabling phosphorus-accumulating bacteria to absorb phosphorus, transferring phosphorus from a water phase to a sludge phase, enabling ammonia nitrogen to be converted into nitrate nitrogen under the action of nitrifying bacteria, enabling the sludge-water mixed liquor in the aerobic tank to flow into a secondary sedimentation tank, discharging sludge through sedimentation, enabling the phosphorus to be removed out of a system to achieve the purpose of phosphorus removal, enabling backflow sludge to flow into a bypass pre-anoxic tank, adding primary sludge fermentation liquor into the secondary sedimentation tank to promote denitrification to minimize nitrate, enabling the sludge to enter a bypass anaerobic tank to be subjected to hydrolytic fermentation to produce acid under deep anaerobic conditions, and achieving screening and domestication of the phosphorus-accumulating bacteria, wherein each index of the effluent is COD (22.6 mg/L) -8.7 mg/L-0.21 mg/L, and each index meets the discharge standard of pollutants in urban sewage treatment plant (1GB 18-2002A).
According to the scheme, the by-pass anaerobic fermentation tank is arranged, anaerobic hydrolysis fermentation treatment is carried out on the returned sludge, an extra internal carbon source is generated and provided for phosphorus-accumulating bacteria, and then the sludge is returned to the main flow process for biological phosphorus removal. Meanwhile, primary sludge fermentation liquor is supplemented in the process, and the available carbon source of the phosphorus-accumulating bacteria is further improved, so that the dependence on a water inlet carbon source is eliminated or reduced to a certain extent, and the phosphorus removal effect and stability of the process are improved. Due to the supplement of the carbon source, the retention time of the return sludge of the by-pass flow process is greatly shortened, and the size and the occupied area of the by-pass flow anaerobic tank are reduced.
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several simple deductions or substitutions can be made without departing from the spirit of the invention, and all shall be considered as belonging to the protection scope of the invention.
Claims (9)
1. A side-flow type enhanced biological phosphorus removal process comprises a primary sedimentation tank, a primary sedimentation sludge fermentation tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a side-flow pre-anoxic tank and a side-flow anaerobic tank, and is characterized in that: the method comprises the following steps:
the method comprises the following steps: introducing the wastewater into a primary sedimentation tank for sedimentation, introducing the separated sewage into an anoxic tank, and introducing the separated sludge into a primary sedimentation sludge fermentation tank;
step two: introducing the sewage in the anoxic tank into the aerobic tank, reflowing part of nitrified liquid mud water discharged from the aerobic tank to the anoxic tank, and introducing the other part of nitrified liquid mud water into a secondary sedimentation tank;
step three: after the sludge and the water of the nitrifying liquid in the secondary sedimentation tank are subjected to sludge-water separation, discharging supernatant, discharging partial sludge, and refluxing the other part of sludge to a bypass flow pre-anoxic tank;
step four: adding a certain amount of primary sludge fermentation supernatant into a bypass flow pre-anoxic tank, and making returned sludge enter a bypass flow anaerobic tank after mixed reaction; and discharging the sludge after deep fermentation and phosphorus accumulating bacteria reinforced screening in the bypass anaerobic tank, and entering the main anoxic tank.
2. The side-stream enhanced biological phosphorus removal process of claim 1, wherein: and stirring devices are arranged in the primary sedimentation tank, the primary sedimentation sludge fermentation tank, the anoxic tank, the aerobic tank, the side-flow pre-anoxic tank and the side-flow anaerobic tank.
3. The side-stream enhanced biological phosphorus removal process of claim 1, wherein: an aeration device is arranged in the aerobic tank.
4. The side-flow enhanced biological phosphorus removal process of claim 1, wherein the temperature of the muddy water is 5-35 ℃, the pH value is 6.5-8.0, and the sludge concentration is 2500-5000 mg/L.
5. The side-flow type enhanced biological phosphorus removal process of claim 1, wherein the dissolved oxygen at the water temperature of the anoxic tank is 0.2-0.6 mg/L, the reflux ratio of the nitrifying liquid is 100-400%, and the hydraulic retention time is 0.5-3 h.
6. The side-stream biological phosphorus removal process of claim 1, wherein:
the dissolved oxygen of the aerobic pool is not less than 2.0 mg/L, and the hydraulic retention time is 6.5-12 h.
7. The side-stream enhanced biological phosphorus removal process of claim 1, wherein: and the sludge reflux ratio of the secondary sedimentation tank in the third step is 50-100%.
8. The side-flow type enhanced biological phosphorus removal process of claim 1, wherein the chemical oxygen demand of the primary sludge fermentation supernatant in the fourth step after addition is 50-300 mg/L.
9. The side-stream enhanced biological phosphorus removal process of claim 1, wherein: the oxidation-reduction potential of the side-flow anaerobic tank is below-200 mV, and the retention time of the returned sludge is 1-4 h.
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| CN114426373B (en) * | 2020-10-10 | 2023-01-20 | 中国石油化工股份有限公司 | Method and device for improving nitrogen and phosphorus removal effect of AO system |
| CN114477422A (en) * | 2022-02-28 | 2022-05-13 | 两山生态科技(山东)有限公司 | System and process for enhancing denitrification effect of sewage with low C/N ratio by utilizing fermentation |
| CN114671526A (en) * | 2022-04-12 | 2022-06-28 | 中国市政工程华北设计研究总院有限公司 | Method for recovering biological phosphorus removal function of chemical synergistic phosphorus removal sewage treatment system |
| CN115057534A (en) * | 2022-07-27 | 2022-09-16 | 中国市政工程华北设计研究总院有限公司 | Low-carbon sewage nitrogen and phosphorus removal system and process |
| CN115057534B (en) * | 2022-07-27 | 2022-11-18 | 中国市政工程华北设计研究总院有限公司 | Low-carbon sewage nitrogen and phosphorus removal system and process |
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