Water-energy-carbon multi-element synergistic water treatment system and method

Abstract

The invention provides a water-energy-carbon multi-element synergistic water treatment system and method. The water treatment system comprises a mud film phase reaction unit group, a pure film phase reaction unit group and a tail water strengthening unit group, the mud film phase reaction unit group comprises a front anoxic reaction purification unit, a mud film aerobic reaction purification unit, a rear anoxic reaction purification unit and a first mud-water precipitation separation unit; the pure membrane phase reaction unit group comprises a suspended water membrane aerobic reaction purification unit and a second micro-flocculation precipitation separation unit; the tail water strengthening unit group comprises a baffling reaction unit provided with a tail water solid matter sieve drawer assembly, a third precipitation separation unit and a tail water receiving unit; the front anoxic reaction purification unit, the mud film aerobic reaction purification unit, the rear anoxic reaction purification unit and the suspended water film aerobic reaction purification unit are all provided with flow guide mechanisms. According to the treatment system provided by the invention, the pollution-reducing and carbon-reducing optimization and synergy targets of small and medium-scale sewage treatment, energy conservation and consumption reduction, and greenhouse gas carbon emission reduction in an operation stage based on water-energy-carbon multi-element coordination are realized.

Description

Technical Field

[0001] This invention relates to the field of water treatment technology, and in particular to a water treatment system and method that integrates water, energy, and carbon. Background Technology

[0002] Existing small and medium-sized wastewater treatment facilities mostly adopt conventional biological treatment processes such as AAO or its modified forms, AOAO, oxidation ditch, MBBR, and IFAS. They generally use single-stage sedimentation and separation units, which lack biomimetic natural purification functions to further intercept pollutants. It is difficult to guarantee the ultimate removal of conventional pollutants in wastewater. The buffer redundancy capacity is insufficient to cope with high and low water volume and quality shock loads, low temperature operation in winter, or the intrusion of industrial wastewater into centralized wastewater treatment facilities. In addition, the energy consumption of high-power equipment such as blowers, agitators, and sludge or mixed liquor internal and external recirculation is high. The single method of adding nitrogen and phosphorus removal chemicals results in inefficient utilization of chemical consumption, leading to increased carbon emissions and failing to meet the green and low-carbon goals of pollution reduction and carbon reduction synergistic efficiency. When using packing-based suspended biofilms and activated sludge in the same biological symbiosis unit, problems often arise: poor packing selection, lack of modification, inconvenient dosing, inability to measure, poor biofilm formation, easy wear and tear, reduced volume, and easy leakage of packing to the next unit, clogging the flow channels. Sludge is also easily lost from the biological system, making it difficult to maintain a certain amount of active biomass and sustain long-term biological operation and purification effects. In biological tanks, complex influent composition and damaged activated sludge microorganisms, coupled with poor aeration and mixing dynamics, excessive or localized turbulent flow, often lead to the accumulation of sludge, scum, and foam on the surface, significantly impacting sensory evaluation and treatment effectiveness. There are no effective and convenient mechanical or manual sludge removal measures. Furthermore, due to flow structure issues, the effluent outlet often easily breeds and accumulates suspended solids, posing a risk of affecting water sample collection and causing excessive levels of suspended solids and total phosphorus during testing. There are currently no effective energy-saving diagnostic methods or index optimization measures for high-power equipment (such as fans). Manual judgment is limited by insufficient professional expertise, and often adopts extensive control methods, which makes it difficult to achieve effective energy-saving results.

[0003] Therefore, a water treatment system and method that integrates water, energy, and carbon is needed to at least partially solve the above-mentioned technical problems. Summary of the Invention

[0004] This invention provides a water treatment system that integrates water, energy, and carbon, achieving the goals of pollution reduction, carbon reduction, and efficiency improvement based on the synergy of water, energy, and carbon during operation, while simultaneously addressing small- to medium-scale wastewater treatment, energy conservation, and greenhouse gas carbon emission reduction.

[0005] In a first aspect, the present invention provides a water treatment system that integrates water, energy, and carbon resources in a synergistic manner, the system comprising:

[0006] The treatment system includes a mud-film phase reaction unit group, a pure membrane phase reaction unit group, and a tailwater enhancement unit group;

[0007] The mud-film phase reaction unit group includes a pre-anoxic reaction purification unit, a mud-film aerobic reaction purification unit, a post-anoxic reaction purification unit, and a first mud-water sedimentation and separation unit, which are sequentially connected by liquids.

[0008] The pure membrane phase reaction unit group includes a suspended membrane aerobic reaction purification unit and a second micro-flocculation sedimentation separation unit connected in series; the liquid of the suspended membrane aerobic reaction purification unit is connected to the first mud-water sedimentation separation unit;

[0009] The tailwater enhancement unit group includes a baffled reaction unit, a third sedimentation separation unit, and a tailwater receiving unit connected to a second micro-flocculation sedimentation separation unit via a first pipeline. The front and rear ends of the first pipeline are sequentially connected to the baffled reaction unit and the third sedimentation separation unit via branch pipelines.

[0010] The tailwater receiving unit includes a tailwater solids sieve assembly installed in the unit body, which is used for diversion, energy dissipation, water distribution and leakage, and interception and removal of suspended solids.

[0011] The pre-anoxic reaction purification unit, the mud film aerobic reaction purification unit, the post-anoxic reaction purification unit, and the suspended film aerobic reaction purification unit are all equipped with:

[0012] The flow guiding mechanism includes a first and a second flow guiding arc wall symmetrically arranged at the inlet of the unit, and a third and a fourth flow guiding arc wall symmetrically arranged near the outlet of the unit; a plurality of straight flow guiding walls extending along the flow direction are also provided between the second and third flow guiding arc walls.

[0013] According to the treatment system of the present invention, two-stage microbial sludge membrane (AOA-anoxic / aerobic / anoxic) and pure membrane treatment are realized, and the two-stage solid-liquid separation cascade operates independently. Each reaction and purification unit adopts a flow-guiding structure, which improves the hydraulic flow pattern, ensures the efficient use of hydraulic retention time, greatly reduces the internal recirculation energy consumption of biological denitrification, and avoids the high dissolved oxygen content entrained by excessive recirculation, which would damage the environmental conditions for anoxic biological denitrification. This ensures the ultimate removal of various conventional pollutants in wastewater, especially the denitrification and phosphorus removal levels. The effluent end is equipped with an effluent solids screen assembly device with functions of diversion, energy dissipation, good water distribution and leakage, and suspended solids interception and stripping. This facilitates online sludge collection and offline cleaning and removal of solid deposits such as garbage collected at the effluent end, greatly improving the interception and purification capacity of effluent for suspended particulate pollutants.

[0014] Secondly, the present invention also provides a water treatment method for the synergistic interaction of water, energy, and carbon elements, and a treatment system based on the above technical solution, the treatment system further including a control device with an embedded artificial intelligence model, the treatment method comprising:

[0015] Obtain the actual air volume, actual air pressure, and actual power of the blower equipment during operation, as well as the depth of the oxygen supply aeration head to the highest liquid level;

[0016] Calculate the rated efficiency of the blower, the actual operating efficiency of the blower, the actual resistance loss of the aeration system, and the economic coefficient of the blower's operating efficiency; among these,

[0017] Rated calculated efficiency of fan = Rated air volume / 60 × Rated air pressure / Rated power;

[0018] Fan actual operating efficiency = actual air volume / 60 × actual air pressure / actual power;

[0019] Actual resistance loss of the aeration system = actual air pressure / 10 - depth from the oxygen supply aeration head to the highest liquid level;

[0020] The economic coefficient of the fan operating efficiency = the actual operating efficiency of the fan / the rated calculated efficiency of the fan;

[0021] The actual wind pressure, the actual resistance loss of the aeration system, and the economic coefficient of the blower operating efficiency are input into the artificial intelligence model, which then performs the following steps:

[0022] Determine if the actual wind pressure exceeds the rated load; if so, reduce the frequency of the fan equipment until it does not exceed the rated load, and adjust the fan equipment to operate in the high-efficiency and energy-saving range; if not, proceed to the next step.

[0023] Determine whether the actual resistance loss of the aeration system exceeds the warning limit; if so, continue to reduce the frequency of the blower equipment or intervene manually to control it until it does not exceed the warning limit; if not, proceed to the next step.

[0024] Determine whether the economic coefficient of the fan's operating efficiency exceeds the set operating energy efficiency coefficient. If yes, the process ends. If no, adjust the fan equipment frequency or intervene manually to control the operation. Iterate the first two steps to ultimately ensure that the actual wind pressure does not exceed the rated load, the actual resistance loss of the aeration system does not exceed the warning limit, and the economic coefficient of the fan's operating efficiency exceeds the set operating energy efficiency coefficient.

[0025] According to the processing method of the present invention, by establishing the relationship between the operating energy efficiency accounting of high-power wind turbine equipment and the evaluation of AI (artificial intelligence) model, the wind turbine equipment can be autonomously optimized through deep thinking of the AI ​​model, which is both efficient and convenient.

[0026] Additional advantages, objects, and features of the invention will be set forth in part in the description which follows, and will also become apparent in part to those skilled in the art upon studying the description, or may be learned by practice of the invention. The objects and other advantages of the invention can be realized and obtained by means of the structures specifically pointed out in the description and drawings.

[0027] Those skilled in the art will understand that the objectives and advantages achievable with the present invention are not limited to those specifically described above, and that the above and other objectives achievable with the present invention will become clearer from the following detailed description. Attached Figure Description

[0028] The accompanying drawings, which are included to provide a further understanding of the invention and form part of this application, are not intended to limit the scope of the invention. The components in the drawings are not drawn to scale but are merely illustrative of the principles of the invention. For ease of illustration and description of certain parts of the invention, corresponding portions in the drawings may be enlarged, i.e., may appear larger relative to other components in an exemplary device actually manufactured according to the invention. In the drawings:

[0029] Figure 1 This is a schematic diagram of a processing system according to an embodiment of the present invention;

[0030] Figure 2 This is a schematic diagram of a processing system according to another embodiment of the present invention;

[0031] Figure 3 This is a schematic diagram of a baffled reaction unit in a processing system according to an embodiment of the present invention;

[0032] Figure 4 This is a schematic diagram of a flow guiding mechanism in a processing system according to an embodiment of the present invention;

[0033] Figure 5 This is a schematic diagram showing the distribution of the suspension membrane constant volume dosing and interception components in the corresponding units of a processing system according to an embodiment of the present invention;

[0034] Figure 6 This is an exploded view of the packing interception and hydraulic flow-through components in a treatment system according to an embodiment of the present invention;

[0035] Figure 7 This is a schematic diagram of a carbon source feeding component in a processing system according to an embodiment of the present invention;

[0036] Figure 8 This is a partial schematic diagram of a sludge connection pipeline component in a treatment system according to an embodiment of the present invention;

[0037] Figure 9This is a schematic diagram of a first-stage filtration component in a processing system according to an embodiment of the present invention;

[0038] Figure 10 An exploded view of the double-layered intercepting net bag of the first-stage filtration component in a processing system according to an embodiment of the present invention;

[0039] Figure 11 This is an exploded view of the second-stage sink component in a processing system according to an embodiment of the present invention;

[0040] Figure 12 This is a schematic diagram of the scum blowing component of a mobile mixed-phase scum removal assembly in a processing system according to an embodiment of the present invention.

[0041] Figure 13 This is another schematic diagram of the scum blowing component of a mobile mixed-phase scum removal assembly in a processing system according to an embodiment of the present invention;

[0042] Figure 14 This is an overall schematic diagram of a moving mixed-phase slag removal component in a processing system according to an embodiment of the present invention;

[0043] Figure 15 A schematic diagram of the circumferential slag blowing fan blade component of a slag isolation element in a processing system according to an embodiment of the present invention; and

[0044] Figure 16 This is a flowchart of a processing method according to an embodiment of the present invention. Detailed Implementation

[0045] The objects and functions of the present invention, as well as the methods for achieving these objects and functions, will be clarified by referring to exemplary embodiments. However, the present invention is not limited to the exemplary embodiments disclosed below; it can be implemented in various forms. The purpose of this specification is merely to help those skilled in the art to comprehensively understand the specific details of the invention.

[0046] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the scope of exemplary embodiments according to the invention. As used herein, the singular form is intended to include the plural form as well, unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms “comprising” and / or “including” are used in this specification, they indicate the presence of features, integrals, steps, operations, elements, and / or components, but do not exclude the presence or addition of one or more other features, integrals, steps, operations, elements, components, and / or combinations thereof.

[0047] The ordinal numbers such as "first" and "second" used in this invention are merely identifiers and do not have any other meaning, such as a specific order. Moreover, for example, the term "first component" does not imply the existence of "second component," and the term "second component" does not imply the existence of "first component."

[0048] It should be noted that the terms “up,” “down,” “front,” “back,” “left,” “right,” “inner,” “outer,” and similar expressions used in this article are for illustrative purposes only and are not intended to be limiting.

[0049] This invention provides a water treatment system 100 that integrates water, energy, and carbon. The system 100 can be applied in the field of water treatment technology, such as for small- to medium-scale wastewater treatment, and can solve the problems of existing small- to medium-scale wastewater treatment methods that struggle to guarantee the ultimate removal of conventional pollutants and have high internal recirculation energy consumption.

[0050] In a preferred embodiment, Figure 1 This is a schematic diagram of a processing system according to an embodiment of the present invention; Figure 2 This is a schematic diagram of a treatment system according to another embodiment of the present invention. The treatment system 100 provided in this embodiment of the present invention includes a mud-film phase reaction unit group, a pure membrane phase reaction unit group, and a tailwater enhancement unit group.

[0051] The mud-film phase reaction unit group, the pure membrane phase reaction unit group, and the effluent enhancement unit group are hydraulically connected. The mud-film phase reaction unit group serves as the first stage of wastewater treatment, the pure membrane phase reaction unit group serves as the second stage of wastewater treatment, and the effluent enhancement unit group serves as the third stage of wastewater treatment.

[0052] Specifically, the mud film phase reaction unit group (or the first mud film phase MBAS reaction unit group) includes a pre-anoxic reaction purification unit 11, a mud film aerobic reaction purification unit 12, a post-anoxic reaction purification unit 13, and a first mud-water sedimentation and separation unit 14, which are sequentially connected by liquids. Figure 1 and Figure 2 As shown. Upstream water is pumped by pressure or gravity and enters this treatment system through pipeline b10. It can then be split into pipelines b11 and b12 (both pipelines are equipped with valves to regulate the flow). Pipeline b11 enters unit 11, and pipeline b12 is further split into pipelines b13 and b14 (both pipelines are equipped with shut-off valves to regulate the flow rate), which enter units 12 and 13 respectively.

[0053] This effective integration and sequential hydraulic connection of AOAS (Activated Biocarrier Activated Sludge and Settling Reactor) based on activated sludge and suspended biofilm loading media for biodegradation and sludge-water separation forms the MBAS section (Moving Biocarrier Activated Sludge and Settling Reactor). This significantly reduces the internal recirculation energy consumption of biological denitrification and avoids excessively high dissolved oxygen content entrained by excessive recirculation, which could disrupt the anaerobic biological denitrification environment. The activated sludge concentration in units 11–13 can be maintained at 1800–4500 mg / L. The suspended biofilm filling volume ratio in units 11 and 13 can be 15%–40%. In unit 12, as an aerobic metabolic unit, the suspended biofilm filling volume ratio can be 25%–50%. The specific surface area of ​​the suspended biofilm in section I is consistently around 600 m². 2 / m 3 The above, supplemented with appropriate amounts of activated coke and magnetic powder (Fe3O4), are used to enhance the activated carbon adsorption, biochar adsorption, and physicochemical micro-magnetic adsorption performance of the biofilm, as well as its function of adhering to and trapping pollutants.

[0054] The pure membrane phase reaction unit group (or the second-stage pure membrane phase MABS reaction unit group) includes a connected suspended membrane aerobic reaction purification unit 21 and a second micro-flocculation sedimentation separation unit 22. The suspended membrane aerobic reaction purification unit 21 is connected to the first mud-water sedimentation separation unit 22. Thus, based on the effective connection and sequential hydraulic series connection of the biodegradation of the packing membrane and the mud-water separation, the pure membrane phase MABS section (Moving Aerobic Biocarrier and Settling Reactor, abbreviated as MABS) is formed. The specifications and performance of the suspended biofilm material in the second stage are the same as those in the first stage.

[0055] The tailwater enhancement unit group (or the third stage tailwater enhancement unit group) includes a baffled reaction unit 31, a third sedimentation separation unit 32, and a tailwater receiving unit 33 connected to a second micro-flocculation sedimentation separation unit 22 via a first pipeline. The front and rear ends of the first pipeline are sequentially connected to the baffled reaction unit 31 and the third sedimentation separation unit 32 via branch pipelines.

[0056] The tailwater receiving unit 33 includes a tailwater solids screen assembly installed in the unit body, which is used for diversion, energy dissipation, water distribution and leakage, and interception and removal of suspended solids.

[0057] Within the baffle reaction unit 31, a predetermined number of baffles may be installed, such as... Figure 3Lines 31a1 and 31a2 (with their long sides close to the inner wall, near the water flow), and lines 31b1 and 31b2 (with their long sides opposite to 31a1 and 31a2, also close to the inner wall, near the water flow) form a meandering, labyrinthine flow channel. This enhances the multiphase mixing reaction gradient of pollutants, chemicals, trace sludge flocs, and return liquid in the water, reduces the power consumption of fluidization within the tank, and eliminates dead zones where mixing is inadequate. 31 receives the effluent from sedimentation and separation at 22, which is then split into b21 and b22 via hydraulic pipe b20 (both branch pipes are equipped with valves for adjusting flow rates; b21 also has a one-way check valve). Figure 2 (Not shown in the image), and enter into 31 and 33 respectively (accessed via gravity flow or pressure flow, with pumped pressure flow in the latter). Figure 2 (Not shown in the text). After hydraulic connection between 31 and 32, the water flows from the end of 32 through pipeline b23 (which is equipped with a one-way check valve and a stop valve for regulating flow) and merges with b211 (from the confluence of b21 and 53) to form pipeline b212. Then it enters the upper part of the first-stage screening component F (described in detail below) in the tailwater solids screening assembly at the beginning of unit 33, and finally flows out from the end of 33.

[0058] Furthermore, the pre-anoxic reaction purification unit 11, the mud film aerobic reaction purification unit 12, the post-anoxic reaction purification unit 13, and the suspended film aerobic reaction purification unit 21 are all equipped with flow guiding mechanisms to increase water flow rate and improve the hydraulic flow state in the pool.

[0059] Specifically, such as Figure 4 As shown, each unit (11, 12, 13, 21) has adjacent and symmetrical first guide arc wall q1 (constant arc side from the inlet side) and second guide arc wall q2 (convex arc side from the inlet side) at a certain distance at the inlet end. Near the outlet end of the corresponding unit, there are adjacent and symmetrical third guide arc wall q1' (constant arc side from the outlet side) and fourth guide arc wall q2' (convex arc side from the outlet side) at a certain distance. Along the water flow direction, the unit also has multiple straight guide walls, such as q3 and q3', at certain distances. 42 is positioned relatively closer to the outlet side of q1' (i.e., 42 is located at the rear end of q1' in the water flow direction).

[0060] According to the treatment system of the present invention, two-stage microbial sludge membrane (AOA-anoxic / aerobic / anoxic) and pure membrane treatment are realized, and the two-stage solid-liquid separation cascade operates independently. Each reaction and purification unit adopts a flow-guiding structure, which improves the hydraulic flow pattern, ensures the efficient use of hydraulic retention time, greatly reduces the internal recirculation energy consumption of biological denitrification, and avoids the high dissolved oxygen content entrained by excessive recirculation, which would damage the environmental conditions for anoxic biological denitrification. This ensures the ultimate removal of various conventional pollutants in wastewater, especially the denitrification and phosphorus removal levels. The effluent end is equipped with an effluent solids screen assembly device with functions of diversion, energy dissipation, good water distribution and leakage, and suspended solids interception and stripping. This facilitates online sludge collection and offline cleaning and removal of solid deposits such as garbage collected at the effluent end, greatly improving the interception and purification capacity of effluent for suspended particulate pollutants.

[0061] In a preferred embodiment, emergent aquatic plant beds are provided in sedimentation and separation units 14, 22, and 32. These emergent aquatic plant beds consist of zipper-type emergent floating beds, each containing aggregates such as expanded clay and aquatic plants. Figure 2 Ceramsite has the function of further filtering and intercepting non-dissolved pollutants in the water, while emergent aquatic plants play a biomimetic natural purification function by intercepting and adsorbing pollutants, and can further absorb nitrogen and phosphorus pollutants in the water as well as the carbon sequestration function of plants that absorb carbon dioxide.

[0062] The suspended membrane constant-volume dosing and interception component 4 may include a floating membrane packing 41, a packing interception and hydraulic flow-through component 42, and a packing quantitative dosing component 43, and is installed in biochemical units 11, 12, 13, and 21. Figure 2 , Figure 5 Among them: 41 is uniformly fluidized and distributed in pools 11, 12, 13, and 21; 42 is located at the end of each pool to intercept the packing 41, and as a uniform outflow hydraulic flow pipe component at the end of the unit; 43 is located on each pool as a quantitative metering volume of the packing and the hopper for adding 41, and is equipped with volume metering graduations. 42 includes two parts: a flow-through cylinder 421 and an airbag inner chamber component 422 for dispersing and removing the packing at the tail end from accumulation, such as... Figure 6421 can be cylindrical or cuboid in structure, with 422 placed inside the cylinder 421. 421 includes a cylinder body 421a and a predetermined number of flow-through holes 421b that can intercept 41 (ensuring the flow rate meets the treatment capacity requirements). The hole diameter is smaller than 41, allowing water to pass through the inner cavity of 421 while the packing is blocked outside the cylinder wall. 422 is a soft airbag that can be expanded or contracted by air-driven force. The airbag has evenly distributed airbag holes. When driven by external airflow, 422 is in an expanded state. When 422 is in its maximum expanded state, its volume occupies approximately one-quarter to one-third of the inner chamber volume of 421. Microbubbles are released from 422 and enter 421, flowing back through its flow-through holes 421b to purge the packing 41, preventing the packing 41 from accumulating near the outer wall of the flow-through holes on 421 and affecting the flow rate. When the external airflow stops, 422 is in its original contracted and shrunken state. The external airflow can alternately drive or stop 422, thereby pulsating and disturbing the packing material to prevent unfavorable accumulation and effectively regulating the different flow rates entering 421. Multiple sets of 42 can be installed on the end walls of 11, 12, 13, and 21, not shown in the figure.

[0063] The reagent feeding components may include a carbon source feeding component 51, a phosphorus removal feeding component 52, a targeted oxidant feeding component 53, and a reducing agent deoxygenation feeding component 54, such as... Figure 2 51 includes parts 511 to 516, such as... Figure 7The components are as follows: 511 for dissolving and pumping the drug; 512 for a flow channel component for uniform distribution of the drug solution via a double weir; 513 for a high-gradient carbon source content drug solution pipe assembly (including fittings, a high-gradient carbon source content drug solution flow meter 513a, and a flow regulating valve); 514 for a low-gradient carbon source content drug solution transfer pipe assembly (including fittings, a pre-dilution drug solution flow meter 514a, and a flow regulating valve); 515 for a dilution water pipe assembly (including the raw water interface and fittings for dilution, and a dilution water flow meter 515a; the dilution water source can be tap water, clean water, or reclaimed water); and 516 for a mixing pipe assembly for the drug solution and dilution water. By using 514 and 515 (and by matching their 514a and 515a metering, the dilution water is adjusted to dilute the high gradient carbon source content ratio to meet the expected ideal target low gradient carbon source content requirements), a quantitatively diluted low gradient carbon source content solution is obtained, and then guided into 21 through 51a (including pipe fittings and flow regulating valves). This allows the high-gradient carbon source solution (generally 450,000 to 750,000 COD equivalent) to enter the post-anoxic purification unit 13 of the first stage MBAS, while the corresponding low-gradient carbon source solution (150,000 to 250,000 COD equivalent) diluted according to target requirements enters the suspension membrane aerobic purification unit 21 of the second stage MABS. This serves as the carbon source nutrients for the biological cells synthesized during the initial culture of the membrane in the 21 packing membrane. It also avoids the possibility of residual COD in the carbon source penetrating the process end due to the incorrect selection of a high-gradient carbon source solution in the second stage, thus avoiding the environmental safety risk of excessive COD effluent. Furthermore, the use of a post-low-gradient carbon source solution greatly reduces the amount of carbon source reagent used in the system units, thereby reducing the indirect carbon emission intensity of reagent consumption. 52 includes a phosphorus removal agent solution and pumping unit 521, and pipelines 522-524 (all including fittings and flow regulating valves), enabling three-point dosing: 522 pumps the agent to the first end of 14, 523 pumps the agent to the first end of 22 (greatly improving the micro-flocculation settling performance in 21), and 524 adds the agent to the middle section of 31 (improving the floc particle size and settling and coagulation performance of unit 31). 53 includes an oxidant (represented by low-content hypochlorite compounds, used to enhance the removal of residual recalcitrant organic matter, nitrogenous pollutants, and specific emerging pollutants remaining in the water after two stages of biochemical microbial treatment) solution and pumping unit, as well as a branch dosing pipeline component, which adds the agent to the first end of 31 or merges with pipeline b21. 54 is a reducing agent liquid dosing system (represented by sodium bisulfite, ferrous sulfate, or ferrous chloride, or a mixture thereof) which is used for emergency dosing in the middle and later stages of 31, and is linked with the residual chlorine monitor installed in the middle of 31 to reduce the oxidation residue at the end of the unit to below the expected threshold.

[0064] The air supply components may include an aeration drive blower component 60, a first air supply pipe component 61, and a second air supply pipe component 61'. 61 then branches to components 611 and 612, 61' further branches to pipe components 62 and 63, and 62 further branches to pipe components 621 and 622, etc. Figure 2 611 serves as the oxygen source for aeration in the uniformly distributed tube within the sludge film aerobic reaction purification unit 12. 612 serves as the driving force for the expansion of the air bladder chamber component 422, which is located at the end of component 42 within 12, to remove the packing material accumulated at the tail end. 63 serves as the driving force for bottom sludge disturbance in the uniformly distributed tube of the first-stage settling unit 14, so that pneumatic stirring and propulsion can be initiated in the early stage of biofilm initiation and cultivation in 21. This allows the first-stage activated sludge portion settled in 14 to be distributed into 21 as its inoculation sludge source. It can also synergize with the readily biodegradable organic carbon source provided by 51a in 51, achieving integrated use of sludge source and carbon source in the early stage of activated sludge acclimatization and cultivation in 21. 62 serves as the air supply source for the suspended membrane aerobic reaction (Oxic) purification unit 21, wherein: 621 serves as the oxygen supply source for the uniformly distributed tube aeration within the suspended membrane aerobic reaction (Oxic) purification unit 21, and 622 serves as the driving force for the slack air source of component 422 located at the end of 21.

[0065] The first small air source component may include fluidization-driven small air source components 70, 71, 72, and 73. 70 is connected in series to branch into 71, 72, and 73. 71 then branches into components 711 and 712, and 73 further branches into components 731 and 732. 711 serves as the uniformly distributed pipe fluidization-driven small air source within the post-anoxic purification unit 13, and 712 serves as the venting air source driving force for component 422 located at the end of unit 13. 731 serves as the uniformly distributed pipe fluidization-driven small air source within the pre-anoxic purification unit 11, and 732 serves as the venting air source driving force for component 422 located at the end of unit 11, thus achieving multi-point use of a single air source. 72 serves as the airlift driving force for the return of sludge mixture from the sludge film aerobic purification unit 12 to unit 11.

[0066] The second small air source component may include fluidization-driven small air source components 80, 81, 82, and 83. 80 is connected in series and split into 81, 82, and 83. 81 serves as the air-lift driving force for the return of bottom settled sludge from the second-stage settling unit 22, 82 serves as the air-lift driving force for the return of bottom settled sludge from the first-stage settling unit 14, and 83 serves as the air-lift driving force for the pumping of bottom settled sludge from the third-stage settling unit 32, thus realizing the use of one air source for multiple points.

[0067] The sludge connecting pipeline component 9 includes 90, 91, 92, 93, and 94. 90, 91, 92, and 93 are respectively the conveying pipelines for the return or discharge of sludge in units 12, 14, 22, and 32. 90, 91, 92, and 93 include air-lift sludge risers installed near the end wall of the corresponding unit pools 12, 14, 22, and 32. These risers are connected to the lower ends of the sludge risers installed in the corresponding unit pools 12, 14, 22, and 32 via air-lift power, facilitating the extraction of sludge or mixed liquor from units 12, 14, 22, and 32 using air-lift power. The sludge-water mixture from unit 12 is circulated back to unit 11 via the air-lift driving force of unit 72, the sludge air-lift riser of unit 90, and its transfer pipeline. The settled sludge from section 14 is extracted to other pipe interfaces via airlift drive (section 82), sludge airlift riser (section 91), and their transfer pipelines. The settled sludge from section 22 is extracted to other pipe interfaces via airlift drive (section 81), sludge airlift riser (section 92), and their transfer pipelines. The settled sludge from section 32 is extracted to other pipe interfaces via airlift drive (section 83), sludge airlift riser (section 93), and their transfer pipelines. The connection of the relevant pipe fittings is as follows: The sludge pipeline from 91 is branched into 91a and 91a' (91a is equipped with a one-way check valve, and 91a' is equipped with a one-way check valve and a shut-off valve for regulating flow). 92 (also equipped with a one-way check valve and a shut-off valve 92a for regulating flow, ensuring unidirectional flow of the sludge liquid phase and preventing backflow) merges with 91a' and connects to pipelines 92b and 912 (each equipped with a shut-off valve for regulating flow). 92b enters unit 21. 912 and 93 (93 is also equipped with a one-way check valve and a shut-off valve 93a for regulating flow, ensuring unidirectional flow of the sludge liquid phase and preventing backflow) merge with pipeline 94, see [link to details]. Figure 2 , Figure 8 94 includes pipe fittings 94a to 94g, a dry pressure pumping unit 940, and a residual sludge receiving unit 941. 93 is connected to 94a and 94b. 94a is connected to 912 and then to 94d and 94c. 94c is connected to 94b and then to 94e. 94e is connected to 94f and 94g via the pumping unit 940. 94d and 94f are connected to the residual sludge receiving unit 941. 91a is branched to 91b and 91f (91f is equipped with a shut-off valve for flow regulation), while 91b is branched to 91c, 91d, and 91e. The pipelines of 91c, 91d, and 91e (each equipped with a shut-off valve for flow regulation) respectively enter units 13, 12, and 11. After 91f and 94g are combined, they are transferred to unit 31 through pipeline 95, thereby enabling the input of activated sludge from section I into 31, achieving enhanced bio-adsorption and degradation of pollutants by the sludge in this unit, eliminating the residual content of the oxidant added at 52, and accelerating the co-precipitation of particulate matter.

[0068] Tailwater solids screen assemblies F and H, such as Figure 2 , Figure 9 The system includes an upper first-stage filtration component F and a lower second-stage sink component H, both located within 33. F includes an upper horizontal and vertical bending type drainage platform 33a1 (the water-blocking drainage platform on the mirror-symmetrical side along the vertical central axis is 33a1'), a curved surface guide plate 33a2 (the mirror-symmetrical side along the vertical central axis is 33a2') with vertical energy dissipation function, and a double-layered intercepting net bag 33a3 and 33a3' with good water distribution, leakage, and suspended solids interception and removal functions. The two ends of 33a3 and 33a3' are bolted to the lower ends of 33a1 and 33a1', and the lower parts of 33a1 and 33a1' are respectively provided with the outlets 33a4 and 33a4' of this component. The inflow from b212 enters the body F through the spatial gap between 33a1 and 33a2, and between 33a1' and 33a2', and then flows out symmetrically through 33a4 and 33a4'. 33a3 is located above 33a3', and the two are closely fitted. The mesh openings of 33a3 are larger than those of 33a3'; the former typically has a mesh opening of 5–15 mm, while the latter typically has a mesh opening of 3–8 mm. Figure 10 Show.

[0069] like Figure 11 The second level H at the bottom includes two sections 331 and 332, with a drawer-like structure. 332 can be embedded in 331 and can be freely pulled out. 331 includes a handle 331a and a cuboid cavity composed of m1-m2-m3-m4 and n1-n2-n3-n4, wherein: n1-n2-m2-m1 (the upper layer) is open, m1-m2-m3-m4 (the right side layer, facing 332) is also open, and the remaining layers are closed plates. A removable sealing part 331b is provided on the lower part of the side such as n1-n4-m4-m1, which is used to clean and remove solid deposits such as garbage accumulated in 331 after 331 is lifted out of 331. Similarly, 332 includes a handle 332a, and a cuboid cavity composed of m1'-m2'-m3'-m4' and n1'-n2'-n3'-n4', wherein: n1'-n2'-m2'-m1' (the upper layer) is open, n1'-n2'-n3'-n4' (the left side layer, facing 331) is also open, and the remaining layers are closed plates, such as n 1’ -n 4’ -m 4’ -m 1’ A removable sealing section 332b is provided on the lower side, which is used to clean and remove solid deposits such as garbage that have accumulated inside 332 after 332 is lifted out of 33.

[0070] The mobile mixed-phase slag removal assembly G includes a slag purging component G1 (G1', another example with a different shape) and a slag-enclosing isolation component G2, such as... Figure 12 , Figure 13 and Figure 14 The G1 body has a sealing baffle near its center to divide the inner cavity into an upper water-bearing zone G11a (serving as the inlet and outlet for the gas-liquid-pharmaceutical multiphase medium) and a lower waterless zone G11b (serving as the float support chamber). At the top center of G11a, there are gas source inlets G12a, water source inlets G13a, and pharmaceutical inlets G14a, each equipped with a control valve. Flexible pipe connectors G12b, G13b, and G14b are also provided. Outlets and fittings, such as G16a and its symmetrical side G16a', are located on the two symmetrical sides of G11a, as well as outlets G16b and G16b' (G16b' is not shown in the diagram) pointing downwards towards the scum. Free-moving traction ropes G15a and G15b are located on both sides of the top of G1. The mobile traction system, G1, achieves shearing, scrubbing, and ablation of the gas-liquid-pharmaceutical mixed phase medium on the pool surface, removing biological and chemical scum and foam. A supporting connector G2a connects the scum isolation component G2 and the scum blowing component G1, allowing G2 to encircle G1 within its ring tube. Around G2, a number of evenly distributed circumferential scum blowing fan blade components G2b are also installed. G2b includes a photovoltaic power generation module G2b1 (serving as the power source for G2b2), a fan blade and fan cover component G2b2 (containing three to four rotatable lateral fan blades with external blade guards), a bottom support connector G2b3 (which adjusts the height and tilt angle of G2b2 and is movably engaged with G2), and a wireless remote control handle. The height and horizontal tilt angle of G2b2 can be adjusted mechanically or remotely (via a remote control handle, the fan blades and shroud are operated at the same frequency to blow away scum and debris), thus achieving the purpose of blowing away biological and chemical scum and foam on the pool surface through horizontal and vertical airflow. The scum blowing component G1 (G1') and the scum enclosure component G2 can adopt a closed circular pipe section or a closed square box structure, which can move freely on the water surface of the sewage pool.

[0071] Table 1 shows the multi-channel system for sludge recirculation, mixed liquor recirculation, and excess sludge discharge in this treatment system.

[0072] Table 1

[0073]

[0074]

[0075] In summary, the treatment system of this invention achieves two-stage microbial sludge membrane (AOA) and pure membrane treatment. The tank adopts a flow-guiding structure, which improves the hydraulic flow pattern, ensures efficient use of hydraulic retention time, greatly reduces the internal recirculation energy consumption of biological denitrification, and avoids excessive dissolved oxygen content entrained by high recirculation, thus preventing the disruption of the anoxic biological denitrification environment. It ensures the ultimate removal of various conventional pollutants in wastewater, especially nitrogen and phosphorus removal levels. Furthermore, the two-stage solid-liquid separation cascade operates independently, and an emergent aquatic plant bed is added, achieving high sludge enrichment flux and low water quality load operation. This saves space, reduces infrastructure investment costs, and improves the ability to withstand high and low water quality and quantity shock loads. It also enhances the buffer redundancy control capacity during low-temperature winter operation or industrial wastewater intrusion, and greatly improves the sludge settling performance and suspended particulate matter interception efficiency, preventing sludge runoff and flocculent floating phenomena in single-stage biological systems. The suspended biofilm packing material possesses a high specific surface area and is supplemented with appropriate amounts of activated coke and magnetic powder (Fe3O4) to enhance the biofilm's activated carbon adsorption, biochar adsorption, and physicochemical micromagnetic adsorption properties, as well as its ability to adhere to and trap pollutants. The suspended biofilm allows for quantitative and rapid dosing of the suspended membrane packing material and facilitates the initial start-up of the pure membrane unit by inoculating sludge and carbon sources for bacterial cultivation and biofilm formation. Effective flow interception at the unit's tail end significantly improves the sludge adhesion capacity and enzyme activity of the biochemical treatment system, reducing the production of excess sludge and the operating costs of subsequent sludge dewatering. A multi-channel system for sludge recirculation, mixed liquor recirculation, and excess sludge discharge between the core units of the system is established, enabling flexible and adjustable process operation. Uniformly adjusting the addition of carbon sources with varying concentrations significantly reduces chemical consumption and prevents exogenous carbon source penetration and exceedances. Multi-point dosing of phosphorus removal agents increases the inorganic components of the system and improves the settling performance of sludge or suspended solids. The selection of oxidants enhances the removal of residual recalcitrant organic matter, nitrogenous pollutants, and specific emerging pollutants remaining in the water after two stages of biochemical microbial treatment. A combined device at the effluent end, featuring diversion, energy dissipation, effective water distribution and leakage, and suspended solids interception and removal, facilitates online sludge collection and offline cleaning and removal of accumulated solid deposits such as garbage at the effluent end, significantly improving the effluent's ability to intercept and purify suspended particulate pollutants. A mobile, traction-based scum blowing and scum isolation device achieves shearing, scrubbing, dissolution, and horizontal and vertical airflow sweeping on the pool surface through a gas-liquid-chemical mixed-phase medium, effectively removing biological and chemical scum and foam.

[0076] Secondly, such as Figure 16 This invention also provides a water treatment method that coordinates multiple elements including water, energy, and carbon, based on the treatment system described in the above embodiments. The treatment system further includes a control device with an embedded artificial intelligence model. The treatment method includes:

[0077] Obtain the actual air volume of the fan equipment during operation (unit: m³) 3 ( / min), actual air pressure (unit: kPa) and actual power (unit: kW), and the depth from the oxygen supply aeration head to the highest liquid level (unit: m).

[0078] Calculate the rated efficiency of the blower, the actual operating efficiency of the blower, the actual resistance loss of the aeration system, and the economic coefficient of the blower's operating efficiency. Among these,

[0079] The rated efficiency of a fan is calculated as follows: Rated air volume / 60 × Rated air pressure / Rated power. Where rated air volume is in cubic meters per second (m³). 3 The rated wind speed ( / min), rated wind pressure (unit: kPa), and rated power (unit: kW) can be directly obtained from the nameplate information of the wind turbine equipment.

[0080] Actual operating efficiency of the fan = actual air volume / 60 × actual air pressure / actual power.

[0081] Actual resistance loss of the aeration system = actual air pressure / 10 - depth from the oxygen supply aeration head to the highest liquid level.

[0082] The economic coefficient of wind turbine operating efficiency = actual operating efficiency of wind turbine / rated calculated efficiency of wind turbine.

[0083] The actual wind pressure, the actual resistance loss of the aeration system, and the economic coefficient of the blower operating efficiency are input into the artificial intelligence model, which then performs the following steps:

[0084] Determine if the actual wind pressure exceeds the rated load; if so, reduce the frequency of the fan equipment until it does not exceed the rated load, and adjust the fan equipment to operate in the energy-saving range; if not, it means there is no overpressure, and proceed to the next step.

[0085] Determine whether the actual resistance loss of the aeration system exceeds the warning limit (unit: m, generally taken as ≤1.5m based on experience); if so, continue to reduce the frequency of the blower equipment or intervene manually to control it until it does not exceed the warning limit; if not, it does not exceed the limit, and proceed to the next step.

[0086] Determine whether the economic efficiency coefficient of the blower exceeds the set energy efficiency coefficient (i.e., the actual operating efficiency of the blower should not be lower than the energy efficiency coefficient of the blower's rated calculated efficiency, generally taken as ≥0.7~0.85). If yes, the operating energy efficiency is reasonable, and this process ends. If no, adjust the blower frequency or intervene manually to control it, and iterate the first two steps to ultimately ensure that the actual wind pressure does not exceed the rated load, the actual resistance loss of the aeration system does not exceed the warning limit, and the economic efficiency coefficient of the blower exceeds the set energy efficiency coefficient.

[0087] By establishing an AI-powered large-scale model for energy efficiency calculation and evaluation of high-power wind turbine equipment, and through in-depth thinking and customized code development of the AI ​​model, machine-written code and functional development of the model interface were achieved. This significantly improved human-computer interaction capabilities and the potential for energy-saving process analysis, enabling the optimization of wind turbine energy consumption and the assessment and optimization of greenhouse gas carbon emission reduction. Through backend expert analysis of the evaluation results, and by extending the reasoning through the knowledge base or information database of the large-scale model, feasible implementation paths for wind turbine energy-saving optimization were further explored.

[0088] The energy efficiency calculation and AI large-scale model evaluation can utilize either code or a large-scale inference model (such as DeepSeek). This involves developing machine-written code and functionalities for the model interface using Excel or WPS. After establishing the computational logic, customized code development requirements are analyzed and uploaded to the AI ​​large-scale model's (e.g., DeepSeek) human-computer dialogue window. The model then generates VBA code similar to an HTML webpage through deep thinking. The webpage interface must at least include command buttons for data entry (supporting numeric or text input), calculation execution, data clearing, and data repair. During this process, the code is tested and run. If errors or deficiencies are found, the development requirements are revised and supplemented to improve and iteratively optimize the code model. The VBA code is copied to a text file (.txt format), renamed to .html format, and saved for testing. The saved file can then be opened for verification. Through expert analysis of the evaluation results, further exploration of feasible implementation paths for wind turbine energy-saving optimization is conducted using the knowledge base or information database of the large-scale inference model.

[0089] Other embodiments of the invention will be readily conceived and understood by those skilled in the art in conjunction with the description and practice of the invention disclosed herein. The descriptions and embodiments are to be considered exemplary only, and the true scope and spirit of the invention are defined by the claims.

Claims

1. A water treatment system with synergistic effects of water, energy, and carbon, characterized in that, The treatment system includes a mud-film phase reaction unit group, a pure membrane phase reaction unit group, and a tailwater enhancement unit group; The mud-film phase reaction unit group includes a pre-anoxic reaction purification unit, a mud-film aerobic reaction purification unit, a post-anoxic reaction purification unit, and a first mud-water sedimentation and separation unit, which are sequentially connected by liquids. The pure membrane phase reaction unit group includes a suspension membrane aerobic reaction purification unit connected to the first mud-water sedimentation separation unit and the second micro-flocculation sedimentation separation unit. The tailwater enhancement unit group includes a baffled reaction unit, a third sedimentation separation unit, and a tailwater receiving unit connected to a second micro-flocculation sedimentation separation unit via a first pipeline. The front and rear ends of the first pipeline are sequentially connected to the baffled reaction unit and the third sedimentation separation unit via branch pipelines. The tailwater receiving unit includes a tailwater solids sieve assembly installed in the unit body, which is used for diversion, energy dissipation, water distribution and leakage, and interception and removal of suspended solids. The pre-anoxic reaction purification unit, the mud film aerobic reaction purification unit, the post-anoxic reaction purification unit, and the suspended film aerobic reaction purification unit are all equipped with: The flow guiding mechanism includes a first and a second flow guiding arc wall symmetrically arranged at the inlet of the unit, a third and a fourth flow guiding arc wall symmetrically arranged near the outlet of the unit, and a straight flow guiding wall extending along the flow direction between the second and third flow guiding arc walls.

2. The processing system according to claim 1, characterized in that, The tailwater solids screening assembly includes a first-stage screening component and a second-stage settling component respectively disposed in the upper part and lower bottom of the unit body; The first-stage filtration component is constructed as a relatively closed structure with liquid flowing in from the top center and liquid flowing out from both sides. It includes symmetrically arranged bent-type flow guiding platforms at the top. Each of the two flow guiding platforms has an outwardly curved arc-shaped flow guiding plate below its inner end to form an inlet with a smaller top and larger bottom that has energy dissipation function. Between the bottom ends of the outer walls of the two flow guiding platforms, a concave double-layered intercepting net bag is provided for water distribution, leakage, and suspended solids interception and removal. Each of the two flow guiding platforms has an outlet on its outer wall to guide the liquid to the second-stage sink component. The second-level sink drawer component is a relatively closed structure with an open top surface, including a first container and a second container, both of which have open top surfaces. The second container is embedded in the first container and can be pulled out horizontally relative to the first container. The first container and the second container are respectively provided with detachable sealing parts on their sides.

3. The processing system according to claim 1, characterized in that, The treatment system further includes a suspended membrane constant-volume dosing and interception component, which is respectively installed in the pre-anoxic reaction purification unit, the mud film aerobic reaction purification unit, the post-anoxic reaction purification unit, and the suspended membrane aerobic reaction purification unit. The suspended membrane constant-volume dosing and interception component includes: Floating membrane packing; Packing interception and hydraulic flow passage components are installed at the end of the unit; Packing material dispensing unit; The packing interception and hydraulic flow-through component includes a flow-through orifice cylinder and an airbag inner chamber component disposed within the flow-through orifice cylinder for expanding and dispersing the tail-end packing material that accumulates around the orifice. The airbag inner chamber component is a soft airbag that can be expanded or contracted by air driving force, and the airbag has uniformly distributed airbag holes.

4. The processing system according to claim 1, characterized in that, The processing system also includes a mobile mixed-phase sludge removal assembly that can move freely on the surface of each unit's pool, the mobile mixed-phase sludge removal assembly comprising: A scum-blowing device is used to shear, scrub, and dissolve biological and chemical scum and foam on the surface of a pool through a gas-liquid-chemical mixed medium. The scum-blowing device includes a scum-blowing device body whose inner cavity is divided into an upper water-bearing zone and a lower waterless zone by a sealing baffle. The top of the upper water-bearing zone is connected to a gas source pipeline, a water source pipeline, and a chemical liquid pipeline, respectively. An outflow pipeline in the direction of downward scum is also provided on the side of the upper water-bearing zone. The scum blowing component surrounds the scum isolation component within its coiled tube, which is used to blow air in the horizontal and vertical directions on the pool surface to remove biological and chemical scum and foam; the coiled tube is surrounded by circumferential scum blowing fan blades with adjustable height and horizontal tilt angle.

5. The processing system according to claim 3, characterized in that, The processing system further includes an air supply component, which includes: Aeration drive blower components, used to provide aeration gas; An air supply pipe component is used to: supply the aeration gas to the mud film aerobic reaction purification unit and the suspended water film aerobic reaction purification unit as an aeration oxygen source; supply the aeration gas to the air bladder chamber component located at the end of the mud film aerobic reaction purification unit and the suspended water film aerobic reaction purification unit as a relaxation air source; and supply the aeration gas to the first mud-water sedimentation separation unit as a driving force for bottom mud disturbance.

6. The processing system according to claim 3, characterized in that, The processing system further includes a first small air source component, the first small air source component comprising: The first fluidized drive air source component is used to provide the drive air source; The driving air pipeline is used for: supplying the driving air source to the rear anoxic reaction purification unit and the front anoxic reaction purification unit as a fluidization stirring driving air source; supplying the driving air source to the airbag chamber component located at the end of the rear anoxic reaction purification unit and the front anoxic reaction purification unit as a relaxation air source; and supplying the driving air source to the sludge film aerobic reaction purification unit as the air lifting driving force for the sludge mixture to flow back from the sludge film aerobic reaction purification unit to the front anoxic reaction purification unit.

7. The processing system according to claim 3 or 6, characterized in that, The processing system further includes a second small air source component, the second small air source component comprising: The second fluidized drive gas source component is used to provide the drive gas source; The driving air pipeline is used to supply the driving air source to the second micro-flocculation sedimentation separation unit, the first sludge-water sedimentation separation unit and the third sedimentation separation unit respectively, so as to serve as the driving force for the air lift of the sludge mixture back to the corresponding unit.

8. The processing system according to claim 1, characterized in that, The processing system further includes a reagent dispensing component, which comprises: The carbon source feeding component is used to add a high-gradient carbon source content solution to the downstream anoxic reaction purification unit and a low-gradient carbon source content solution to the suspended membrane aerobic reaction purification unit. The phosphorus removal feeding unit is used to add phosphorus removal agents to the beginning of the first mud-water sedimentation separation unit, the beginning of the second micro-flocculation sedimentation separation unit, and the middle section of the baffle reaction unit, respectively. A targeted oxidant feeding component is used to feed oxidant to the beginning of the baffled reaction unit and the middle section of the first pipeline, respectively; The reducing agent deoxygenation feeding component is used to add reducing agent solution to the middle and later stages of the baffled reaction unit; The carbon source feeding component includes a drug storage and pumping component, a flow channel component for uniform distribution of drug solution by double weirs, a drug solution pipe assembly with high gradient carbon source content, a drug solution transfer pipe assembly with low gradient carbon source content, a dilution water pipe assembly, and a mixing pipe assembly for drug solution and dilution water. The flow deflector unit is provided with baffles at intervals along the water flow direction to form a meandering flow channel.

9. The processing system according to claim 7, characterized in that, The treatment system also includes a sludge connection pipeline component, which comprises: Pressure pumping components; The sludge conveying pipeline is used to return or discharge sludge from the mud film aerobic reaction purification unit, the first mud-water sedimentation separation unit, the second micro-flocculation sedimentation separation unit, and the third sedimentation separation unit under the action of pressure pumping components or air lift driving force, so that the sludge is returned or discharged to the corresponding pre-anoxic reaction purification unit, mud film aerobic reaction purification unit, post-anoxic reaction purification unit, suspended water film aerobic reaction purification unit, or baffle reaction unit. The waste sludge receiving unit is used to receive waste sludge.

10. A water-energy-carbon multi-element synergistic water treatment method, based on the treatment system as described in any one of claims 1 to 9, characterized in that, It also includes a control device with an embedded artificial intelligence model, and the processing method includes: Obtain the actual air volume, actual air pressure, and actual power of the blower equipment during operation, as well as the depth of the oxygen supply aeration head to the highest liquid level; Calculate the rated efficiency of the blower, the actual operating efficiency of the blower, the actual resistance loss of the aeration system, and the economic coefficient of the blower's operating efficiency; among these, Rated calculated efficiency of fan = Rated air volume / 60 × Rated air pressure / Rated power; Fan actual operating efficiency = actual air volume / 60 × actual air pressure / actual power; Actual resistance loss of the aeration system = actual air pressure / 10 - depth from the oxygen supply aeration head to the highest liquid level; The economic coefficient of the fan operating efficiency = the actual operating efficiency of the fan / the rated calculated efficiency of the fan; The actual wind pressure, the actual resistance loss of the aeration system, and the economic coefficient of the blower operating efficiency are input into the artificial intelligence model, which then performs the following steps: Determine if the actual wind pressure exceeds the rated load; if so, reduce the frequency of the fan equipment until it does not exceed the rated load, and adjust the fan equipment to operate in the energy-saving zone; if not, proceed to the next step. Determine whether the actual resistance loss of the aeration system exceeds the warning limit; if so, continue to reduce the frequency of the blower equipment or intervene manually to control it until it does not exceed the warning limit; if not, proceed to the next step. Determine whether the economic coefficient of the fan's operating efficiency exceeds the set operating energy efficiency coefficient. If yes, the process ends. If no, adjust the fan equipment frequency or intervene manually to control the operation. Iterate the first two steps to ultimately ensure that the actual wind pressure does not exceed the rated load, the actual resistance loss of the aeration system does not exceed the warning limit, and the economic coefficient of the fan's operating efficiency exceeds the set operating energy efficiency coefficient.

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