Automatic recovery and operation regulation method and system of double-source sludge of MBGS reactor

Abstract

The application discloses a kind of MBGS reactor dual-source sludge automatic collection and operation regulation method and system, it is related to activated sludge treatment technical field, method includes: by online monitoring unit acquisition bacteria algae sludge particle size, sludge concentration, settling characteristics and reaction working condition parameter;By central controller identification particle nucleation, bacteria algae domestication growth, particle screening maturity or stable operation stage, and adjust water load, gas-liquid mass transfer, light supplement and circulation intensity in culture stage;In stable operation stage, determine mature MBGS particle collection condition or flocculent bacteria algae sludge enhanced collection condition, respectively control particle collection and small particle size particle reflux, or switch flocculent bacteria algae sludge enhanced collection state;After executing regulation, continue monitoring and update control instruction.The technical scheme of the application realizes the closed-loop cooperation of particle culture, dual-source sludge differential collection and operation regulation, and improves the stability of particle system and sludge collection efficiency.

Description

Technical Field

[0001] This invention relates to the field of activated sludge treatment technology, and in particular to an automatic method for collecting and controlling the operation of dual-source sludge in an MBGS (Microalgae-Bacterial Granular Sludge) reactor, as well as an automatic system for collecting and controlling the operation of dual-source sludge in an MBGS reactor. Background Technology

[0002] Microbial-algae granular sludge technology utilizes the synergistic effect between bacteria and microalgae to form symbiotic microbial particles with specific particle size and settling properties within a reactor. These particles can be used for the biological treatment of organic pollutants, nitrogen, and phosphorus in wastewater. Compared to conventional flocculent activated sludge, microbial-algae symbiotic particles offer advantages such as faster settling speed, higher sludge concentration, and easier solid-liquid separation. Modular MBGS reactors show promise in particle cultivation, stable operation, and sludge resource recovery.

[0003] However, the formation and stable maintenance of algal-microbe symbiotic particles are influenced by a variety of factors, including influent load, dissolved oxygen, carbon dioxide supply, light intensity, circulation intensity, and sludge concentration. The requirements for gas-liquid mass transfer, supplemental lighting, and hydraulic conditions differ at different stages, such as particle nucleation, algal-microbe acclimatization and growth, and particle selection and maturation. Existing reactor operations typically rely on manual experience or adjustments to single parameters, making it difficult to promptly identify the actual operating stage of the reactor by combining particle size distribution, sludge concentration, and settling performance, and to implement adaptive synergistic adjustments. This can easily lead to slow particle formation, structural instability, or fluctuations in operating conditions.

[0004] Furthermore, sludge during stable operation typically includes mature MBGS particles, fine particles, and flocculent bacterial and algal sludge. Using uniform sludge discharge or fixed collection methods may result in the discharge of small-to-medium-sized particles with retention value, or the inability to remove excessive flocculent bacterial and algal sludge in a timely manner, thereby damaging particle size distribution and sludge settling performance. Current technologies also lack a closed-loop operation control mechanism that integrates online monitoring, operational phase identification, cultivation condition adjustment, differentiated collection of sludge from both sources, and post-collection status feedback.

[0005] Therefore, there is a need for an automated operation control method that can automatically identify the particle cultivation and stable operation stages based on the reactor's operating status, and coordinate the adjustment of cultivation conditions and the separation and harvesting of the two types of sludge, in order to improve the reliability of bacterial-algae symbiotic particle cultivation and stable maintenance, reduce human intervention, and improve the long-term stability of the reactor. Summary of the Invention

[0006] To address the aforementioned issues, this invention provides a method and system for automatic sludge harvesting and operation control in a dual-source MBGS reactor. By acquiring sludge state parameters and reaction operating parameters online, a central controller identifies particle nucleation, bacterial and algal acclimatization and growth, particle screening for maturity, and stable operation. It also coordinates and adjusts influent load, gas-liquid mass transfer, supplemental lighting, and circulation intensity at different stages. This method updates cultivation conditions as the particle formation process changes, facilitating the formation of bacterial particle skeletons, promoting microalgal attachment and growth, and screening for mature bacterial-algal symbiotic particles. During stable operation, the method controls the harvesting of MBGS particles and intensifies the harvesting of flocculent bacterial and algal sludge based on harvesting conditions, while also allowing small- and medium-sized MBGS particles to be recirculated. This reduces the ineffective loss of particles of suitable size, inhibits the accumulation of flocculent sludge, and improves sludge particle size structure and settling performance. By continuously monitoring and updating adjustment commands after harvesting, a closed-loop control system is formed, reducing manual intervention and improving reactor operational stability.

[0007] To achieve the above objectives, this invention provides an automatic sludge collection and operation control method for a dual-source MBGS reactor. The MBGS reactor is equipped with a flocculent bacteria and algae sludge separation and collection unit for separating and collecting flocculent bacteria and algae sludge, and an MBGS particle separation and collection unit for separating and collecting MBGS particles. The method includes: The operating status parameters of the reactor are collected by the online monitoring unit and sent to the central controller. The operating status parameters include sludge status parameters that characterize the particle size, sludge concentration and settling characteristics of the bacterial and algal sludge, as well as reaction condition parameters that characterize the reaction environment, influent load, gas-liquid mass transfer and circulation status. The central controller identifies whether the reactor is in the particle nucleation stage, the bacterial and algal acclimatization and growth stage, the particle screening and maturation stage, or the stable operation stage based on the sludge state parameters. The central controller, in accordance with the particle nucleation stage, the bacterial and algal acclimatization and growth stage, and the particle screening and maturation stage, controls the operation and regulation execution unit to adjust the influent load, gas-liquid mass transfer conditions, supplemental lighting conditions, and circulation intensity according to the particle cultivation objectives of the corresponding stage, so as to form a bacterial particle skeleton, promote microalgal attachment and growth, and screen mature bacterial-algal symbiotic particles. The operation and regulation execution unit includes an influent regulation execution unit, a gas-liquid mass transfer regulation execution unit, a supplemental lighting regulation execution unit, a circulation separation regulation execution unit, and a harvesting regulation execution unit. During the stable operation phase, the central controller determines whether the mature MBGS particle harvesting conditions or the enhanced harvesting conditions of flocculent bacterial and algal sludge are met based on the sludge state parameters and the reaction condition parameters, and generates corresponding operation adjustment commands. When the conditions for harvesting mature MBGS particles are met, the harvesting regulation execution unit controls the MBGS particle separation and harvesting unit to harvest mature MBGS particles, and controls the circulating separation regulation execution unit to return the separated small and medium-sized MBGS particles to the MBGS reactor. When the conditions for enhanced harvesting of flocculent algae sludge are met, the harvesting adjustment execution unit controls the flocculent algae sludge separation and harvesting unit to switch from the normal operation state to the enhanced operation state, so as to improve the separation and harvesting efficiency of flocculent algae sludge. After executing the operation adjustment command, the operation status parameters continue to be collected, and the central controller updates the reactor operation stage, harvesting conditions and operation adjustment command to form a closed-loop automatic operation control.

[0008] In the above technical solution, preferably, the online monitoring unit includes a pH and temperature monitor, a first light intensity monitor, a second light intensity monitor, a dissolved oxygen meter, a dissolved carbon dioxide detector, a suspended solids concentration detector, an online particle size analyzer, an online sludge volume index monitor, an influent flow meter, a circulating separation flow meter, a carbon dioxide gas flow meter, an air flow meter, and a nitrogen flow meter. The central controller is connected to the online monitoring unit, the water intake regulation execution unit, the gas-liquid mass transfer regulation execution unit, the supplementary lighting regulation execution unit, the circulation separation regulation execution unit, and the harvesting regulation execution unit, respectively.

[0009] In the above technical solution, preferably, identifying the reactor operation stage includes: When the proportion of particles with a diameter of 0.2 mm to 0.5 mm is greater than 50%, it is determined that the nucleation of particles is complete, and the process transitions from the particle nucleation stage to the bacterial and algal acclimatization and growth stage. When the proportion of particles with a diameter of 0.5 mm to 3.0 mm is greater than 60% and the particle settling velocity is greater than 20 m / h, it is determined that the domestication and growth of bacteria and algae is completed, and the process transitions from the domestication and growth stage of bacteria and algae to the particle screening and maturity stage. When the proportion of particles with a diameter of 0.8 mm to 2.0 mm is greater than 70%, the particle settling velocity is 30 m / h to 80 m / h, and the concentration of bacterial and algal sludge is 5 g / L to 10 g / L, it is determined that stable bacterial and algal symbiotic particles have been formed and the stable operation stage has been entered.

[0010] In the above technical solution, preferably, during the particle nucleation stage, the dissolved oxygen is controlled to 0.5 mg / L to 2.0 mg / L, the light intensity is controlled to zero, and the upward flow velocity is controlled to 2 m / h to 5 m / h. During the acclimatization and growth stage of bacteria and algae, dissolved oxygen was controlled at 2.0 mg / L to 4.0 mg / L, and light intensity was gradually increased to 50 μmol / (m²). 2·s) to 200μmol / (m 2 •s), the volume fraction of gaseous carbon dioxide is controlled to be 1% to 5%, and the upflow velocity is controlled to be 5 m / h to 10 m / h; During the particle screening and maturation stage, dissolved oxygen was controlled at 4.0 mg / L to 8.0 mg / L, and light intensity was controlled at 300 μmol / (m²). 2 ·s) to 500μmol / (m 2 •s), the volume fraction of gaseous carbon dioxide is controlled to be 5% to 15%, and the upward flow rate is controlled to be 8m / h to 15m / h.

[0011] In the above technical solution, preferably, the mature MBGS particle harvesting conditions include: the proportion of particles with a diameter greater than 2 mm exceeds 20%, and the concentration of bacteria and algae sludge is greater than 10 g / L; The enhanced harvesting conditions for the flocculent bacterial and algal sludge include any of the following: The concentration of bacterial and algal sludge is greater than 10 g / L, and the proportion of particles with a diameter of less than 0.8 mm is greater than the proportion of particles with a diameter of greater than 2 mm. Online sludge volume index (SVI5) is greater than 50 mL / g or SVI30 is greater than 80 mL / g; When the mature MBGS particle harvesting conditions are met, the external circulation reflux is activated, and the MBGS particle separation and harvesting unit is controlled to harvest mature MBGS particles, increasing the upward flow velocity by 10%, wherein the upward flow velocity does not exceed 15 m / h. When the enhanced harvesting conditions for flocculent algae sludge are met, the flocculent algae sludge separation and harvesting unit is switched from normal operation to enhanced operation to improve the separation and harvesting efficiency of flocculent algae sludge and enhance the washing and separation of fine MBGS particles and flocculent algae sludge.

[0012] In the above technical solution, preferably, during the stable operation phase, the operation adjustment based on the reaction condition parameters includes: When dissolved oxygen is greater than 4 mg / L, reduce the air aeration rate and increase the water inflow rate; when dissolved oxygen is less than 2 mg / L, increase the carbon dioxide supply and air aeration rate, reduce the water inflow rate and increase the supplemental lighting intensity. When the pH is greater than 8.5 or the dissolved carbon dioxide concentration is less than 50 μL / L, increase the carbon dioxide supply; when the dissolved carbon dioxide concentration is greater than 70 μL / L, decrease the carbon dioxide supply. When the detection value of the first or second light intensity monitor is less than 300 μmol / (m 2 When ·s), increase the supplementary light power after determining the concentration of bacterial and algal sludge and the sludge settling performance; when either the first light intensity monitor or the second light intensity monitor has a detection value greater than 500 μmol / (m2 When ·s), reduce the supplementary light power; When the temperature deviates from 25℃ to 30℃, an inlet water temperature adjustment command is output.

[0013] In the above technical solution, preferably, the upward flow velocity V is determined based on the internal circulation flow rate Q0, satisfying: V = Q0 / S; Q0=Q1+Q2+24×(Q3+Q4+Q5); Where S is the cross-sectional area of ​​the main reaction guide tube of the reactor, Q1 is the influent flow rate, Q2 is the external circulation return flow rate, Q3 is the carbon dioxide gas flow rate, Q4 is the air flow rate, Q5 is the nitrogen replenishment flow rate, and 24 is the thrust gain coefficient formed by the gas source. The central controller regulates the upward flow rate V by adjusting at least one of Q1, Q2, Q3, Q4 and Q5.

[0014] In the above technical solution, preferably, during the stable operation phase, the ratio of the internal circulation return flow to the inflow flow is 50% to 500%, and the internal circulation return is continuously activated. The ratio of external circulation return flow to influent flow is 50%. External circulation return is activated when the mature MBGS pellet harvesting conditions are met and deactivated when the mature MBGS pellet harvesting conditions are not met. When harvesting MBGS pellets, the daily mud discharge rate is 5% / d to 30% / d. The flocculent bacteria and algae sludge separation and collection unit operates with a separation and collection efficiency of 60% to 70% under normal operating conditions, and increases the separation and collection efficiency to 100% under enhanced operating conditions.

[0015] In the above technical solution, preferably, the central controller integrates a multi-parameter automatic priority control model based on the response surface methodology (RSM). The multi-parameter automatic priority control model is based on the operating state parameters and, according to the response relationship between multiple candidate control parameters among the influent load, gas-liquid mass transfer conditions, supplementary lighting conditions, and circulation intensity and the preset operating indicators, determines the candidate control parameter with the highest degree of influence on the preset operating indicators as the priority control parameter, and outputs the corresponding priority control command.

[0016] The present invention also proposes an automatic sludge collection and operation control system for an MBGS reactor, characterized in that it includes an MBGS reactor, an online monitoring unit, a central controller, and an operation control execution unit; The MBGS reactor is equipped with a flocculent bacteria and algae sludge separation and harvesting unit for separating and harvesting flocculent bacteria and algae sludge and an MBGS particle separation and harvesting unit for separating and harvesting MBGS particles. The online monitoring unit is used to collect the operating status parameters of the reactor and send them to the central controller. The operating status parameters include sludge status parameters and reaction condition parameters. The operation adjustment execution unit includes a water intake adjustment execution unit, a gas-liquid mass transfer adjustment execution unit, a supplementary lighting adjustment execution unit, a circulation separation adjustment execution unit, and a harvesting adjustment execution unit; The harvesting adjustment execution unit is connected to the flocculent bacteria and algae sludge separation and harvesting unit and the MBGS particle separation and harvesting unit respectively to adjust the corresponding separation and harvesting operation status. The central controller is connected to the online monitoring unit and the operation adjustment execution unit respectively, and is used to output operation adjustment instructions to the operation adjustment execution unit according to the operation status parameters, and is configured to execute any of the automatic operation control methods disclosed in the above technical solutions.

[0017] Compared with the prior art, the beneficial effects of the present invention are as follows: (1) By monitoring the particle size, sludge concentration, settling characteristics and reaction parameters of bacterial and algal sludge online, the central controller identifies the state of particle nucleation, bacterial and algal acclimatization and growth, particle screening maturity or stable operation of the reactor, and outputs operation adjustment instructions according to the stage. This allows the influent load, gas-liquid mass transfer, supplemental lighting and circulation conditions to be adapted to the particle cultivation process, reducing the mismatch of cultivation conditions caused by relying on manual experience or fixed parameter operation, which is conducive to improving the reliability of bacterial and algal symbiotic particle formation and stable maintenance.

[0018] (2) By setting strategies for dissolved oxygen, light, carbon dioxide supply, and upflow velocity adjustment corresponding to different cultivation stages, and combining particle size distribution, settling velocity, and sludge concentration to determine stage transitions, continuous control can be provided for bacterial particle skeleton formation, microalgae attachment and growth, and mature particle screening. The circulation velocity is further determined by the coordinated flow of influent, external circulation return, and air supply, which is conducive to maintaining suitable hydraulic shear and gas-liquid mass transfer conditions.

[0019] (3) During the stable operation phase, differentiated separation and collection of the two types of sludge are carried out according to the collection conditions of mature MBGS particles and the enhanced collection conditions of flocculent bacteria and algae sludge. When collecting mature MBGS particles, small and medium-sized MBGS particles are returned to the reactor. When flocculent sludge accumulates or its settling performance deteriorates, the separation and collection intensity of flocculent bacteria and algae sludge is increased. This avoids the ineffective loss of particles of suitable size due to uniform sludge discharge and inhibits the accumulation of fine particles and flocculent bacteria and algae sludge, which is conducive to improving the sludge particle size structure and settling performance.

[0020] (4) By adjusting parameters such as dissolved oxygen, pH, dissolved carbon dioxide, dual-point light intensity, temperature and circulation flow rate, the aeration, carbon dioxide supply, water intake, supplementary lighting and circulation conditions can be adjusted in a timely manner according to the actual working conditions of the reactor, reducing the impact of operational fluctuations on the algal symbiosis system. The limitation of internal and external circulation and harvesting operation parameters enables stable operation and separation harvesting to have executable control boundaries.

[0021] (5) By using a multi-parameter automatic priority control model based on response surface methodology, the response relationship between multiple candidate control parameters and operating indicators is analyzed and priority control parameters are determined, which can reduce the mutual interference caused by simultaneous adjustment of multiple parameters; the online monitoring unit, central controller and operation control execution unit form a closed-loop control chain of monitoring, judgment, execution and feedback update, which improves the continuity and consistency of automatic operation control and reduces the need for manual intervention. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of the control logic of the automatic collection and operation control method of dual-source sludge in an MBGS reactor disclosed in one embodiment of the present invention; Figure 2 This is a schematic diagram of the overall assembly of the automatic sludge collection and operation control method for the MBGS reactor according to an embodiment of the present invention.

[0023] In the diagram, the correspondence between the components and the reference numerals is as follows: 1. MBGS reactor; 11. Wastewater inlet; 12. Integrated gas source inlet; 13. Main reaction guide tube; 14. Supplemental lighting assembly; 15. Integrated gas source distribution assembly; 16. Inlet water distribution assembly; 17. Return cone; 18. Standard water outlet; 19. MBGS circulating separation outlet; 2. Flocculent bacteria and algae sludge separation and harvesting unit; 21. Water distribution structure; 22. Separation reaction zone; 23. Dissolved gas release assembly; 24. Flocculent sludge collection section; 25. Sludge scraping assembly; 26. Standard water discharge assembly; 27. Sludge discharge assembly; 28. Collector dosing assembly; 3. MBGS particle separation and harvesting unit 31. Circulating separation pump and separation pipeline; 32. Hydraulic screen; 33. Separated water storage unit; 34. Particle collection unit; 4. Online monitoring unit; 41. pH and temperature monitor; 42. First light intensity monitor; 43. Second light intensity monitor; 44. Dissolved oxygen meter; 45. Dissolved carbon dioxide detector; 46. Suspended solids concentration detector; 47. Online particle size analyzer; 48. Online sludge volume index monitor; 49. Influent flow meter; 410. Circulating separation flow meter; 411. Carbon dioxide gas flow meter; 412. Air flow meter; 413. Nitrogen flow meter; 5. Central controller. Detailed Implementation

[0024] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0025] The present invention will now be described in further detail with reference to the accompanying drawings: like Figure 1 and Figure 2 As shown, according to the present invention, an automatic sludge harvesting and operation control method for a dual-source MBGS reactor is provided. The MBGS reactor 1 is equipped with a flocculent bacteria and algae sludge separation and harvesting unit 2 and an MBGS particle separation and harvesting unit 3. The former is used to separate fine MBGS particles and flocculent bacteria and algae sludge entrained in the reactor effluent, while the latter is used to separate mature MBGS particles according to particle size and settling performance, and to return small and medium-sized MBGS particles that have not met the harvesting conditions to the reactor for continued cultivation.

[0026] During operation, the operating status parameters of the reactor are continuously or periodically collected by the online monitoring unit 4 and sent to the central controller 5. The operating status parameters include sludge status parameters that characterize the particle size distribution, sludge concentration and settling performance of bacterial and algal sludge, as well as reaction condition parameters that characterize the reaction environment (temperature, pH), influent load, gas-liquid mass transfer, light and circulation status.

[0027] The central controller 5 performs correlation analysis based on sludge state parameters to identify the current operating stage of the reactor as the particle nucleation stage, the bacterial and algal acclimatization and growth stage, the particle screening and maturation stage, or the stable operation stage. The particle nucleation stage, the bacterial and algal acclimatization and growth stage, and the particle screening and maturation stage constitute the start-up cultivation process in sequence. After the particle screening and maturation are completed, the reactor enters the stable operation stage.

[0028] The central controller 5, in accordance with the particle cultivation objectives of the corresponding stages—nucleation, bacterial-algal acclimatization and growth, and particle screening and maturation—controls the operation and regulation execution units to adjust the influent load, gas-liquid mass transfer conditions, supplemental lighting conditions, and circulation intensity, in order to form a bacterial particle framework, promote microalgal attachment and growth, and screen mature bacterial-algal symbiotic particles. Specifically, the particle nucleation stage aims to establish a dominant bacterial community, promote extracellular polymer secretion, and form a particle framework; the bacterial-algal acclimatization and growth stage gradually introduces the light and carbon dioxide required for microalgal growth, enabling microalgae to attach and colonize on the bacterial particle framework; the particle screening and maturation stage uses hydraulic shear and sedimentation differentials to wash away loosely structured and slowly settling particles, retaining densely structured bacterial-algal symbiotic particles with good settling performance. The operation and regulation execution units include an influent regulation execution unit, a gas-liquid mass transfer regulation execution unit, a supplemental lighting regulation execution unit, a circulation separation regulation execution unit, and a harvesting regulation execution unit.

[0029] During the stable operation phase, the central controller 5 determines whether the mature MBGS particle harvesting conditions or the enhanced harvesting conditions of flocculent bacteria and algae sludge are met based on sludge state parameters (particle size, sludge concentration) and reaction condition parameters (sedimentation performance), and generates corresponding operation adjustment commands. When the conditions for harvesting mature MBGS particles are met, the MBGS particle separation and harvesting unit 3 is controlled by the harvesting regulation execution unit to harvest mature MBGS particles, and the circulating separation regulation execution unit is controlled to return the separated small and medium-sized MBGS particles to the MBGS reactor 1. When the conditions for enhanced harvesting of flocculent algae sludge are met, the flocculent algae sludge separation and harvesting unit 2 is switched from normal operation to enhanced operation by the harvesting adjustment execution unit to improve the separation and harvesting efficiency of flocculent algae sludge. After executing the operation adjustment command, the system continues to collect operating status parameters, and the central controller 5 updates the reactor operating stage, harvesting conditions, and operation adjustment commands to form a closed-loop automatic operation control system of monitoring-analysis-decision-execution-feedback. This closed loop can also coordinate the control of pollutant degradation, nitrogen and phosphorus absorption, carbon dioxide fixation, in-situ oxygen supply, and bacterial and algal biomass harvesting, so that wastewater treatment, carbon sequestration, and biomass production are in dynamic equilibrium.

[0030] In this embodiment, the cultivation conditions can be dynamically changed with the particle formation process, and mature particles and flocculent bacterial and algal sludge can be harvested differently. This reduces the loss of small and medium-sized seed particles and the accumulation of flocculent sludge, improves the long-term stability of the bacterial and algal particle system, reduces the dependence on human experience, helps to shorten the adjustment lag under abnormal operating conditions, and improves the stability of the particle system and the resource harvesting efficiency.

[0031] In the above embodiments, preferably, the online monitoring unit 4 includes a pH and temperature monitor 41, a first light intensity monitor 42, a second light intensity monitor 43, a dissolved oxygen meter 44, a dissolved carbon dioxide detector 45, a suspended solids concentration detector 46, an online particle size analyzer 47, an online sludge volume index monitor 48, an influent flow meter 49, a circulating separation flow meter 410, a carbon dioxide gas flow meter 411, an air flow meter 412, and a nitrogen flow meter 413; Specifically, the pH and temperature monitor 41, dissolved oxygen meter 44, and dissolved carbon dioxide detector 45 can be installed at a slightly above-center position between the main reaction guide tube 13 and the inner wall of the reactor to obtain the reaction environment parameters of the circulating liquid outside the main reaction zone. The first light intensity monitor 42 can be installed at a slightly below-center position in the center of the main reaction guide tube 13, and the second light intensity monitor 43 can be installed at a position equidistant from the main reaction guide tube 13 and the inner wall of the reactor to reflect the difference in illumination between the central and peripheral areas of the reactor.

[0032] The suspended solids concentration detector 46 can be installed at the center of the bottom reflux cone 17 of the reactor; the online particle size analyzer 47 and the online sludge volume index monitor 48 can be installed at the center of the main reaction guide tube 13. The influent flow meter 49 is installed at the wastewater inlet 11, and the circulation separation flow meter 410 is installed at the MBGS circulation separation outlet 19; the carbon dioxide gas flow meter 411, air flow meter 412, and nitrogen flow meter 413 are respectively installed at their respective gas source inlets and connected to the integrated gas source inlet 12. The carbon dioxide gas can be carbon dioxide-rich flue gas; the carbon dioxide gas flow meter 411 corresponds to a carbon dioxide flow control valve, the air flow meter 412 corresponds to an air flow control valve, and the nitrogen flow meter 413 corresponds to a nitrogen flow control valve; the influent flow meter 49 is installed in conjunction with the influent pump, and the circulation separation flow meter 410 is installed in conjunction with the circulation separation pump.

[0033] The central controller 5 is connected to the online monitoring unit 4, the water intake regulation execution unit, the gas-liquid mass transfer regulation execution unit, the supplementary lighting regulation execution unit, the circulation separation regulation execution unit, and the harvesting regulation execution unit, respectively.

[0034] The central controller 5 is also connected to the inlet pump, carbon dioxide flow control valve, air flow control valve, nitrogen flow control valve, supplemental lighting unit 14, circulating separation pump, and dual-source sludge harvesting equipment. Particle size data can be used to generate flow rate adjustment and external circulation start / stop commands; sludge concentration and sludge volume index can be used to generate circulation, harvesting, and necessary inoculation prompts; dissolved oxygen data can be used to adjust carbon dioxide, air, inlet water, and supplemental lighting; pH, temperature, dissolved carbon dioxide, and dual-point light intensity are used to generate corresponding gas source, temperature, and supplemental lighting adjustment commands, respectively.

[0035] The online particle size analyzer 47 is used to trigger the adjustment of the upward flow rate and the opening and closing of the external circulation; the suspended solids concentration detector 46 is used to trigger the adjustment of the upward flow rate, external circulation, carbon dioxide supply, influent flow rate and separation and harvesting efficiency; the online sludge volume index monitor 48 is used to trigger the adjustment of screening intensity, reinoculation prompt and flocculent bacteria and algae sludge harvesting; the dissolved oxygen meter 44 is used to trigger the adjustment of carbon dioxide, air, influent and supplemental lighting; the pH and temperature monitor 41 is used to trigger carbon dioxide adjustment, temperature alarm and influent temperature adjustment; the dissolved carbon dioxide detector 45 is used to trigger the adjustment of carbon dioxide supply; and two light intensity monitors are used to trigger the verification of sludge concentration and sludge volume index and the adjustment of supplemental lighting power.

[0036] In this embodiment, multidimensional operating information within the reactor is obtained through online instruments of different locations and types, reducing the deviation caused by single-point detection or single-parameter judgment, and enabling the central controller 5 to directly convert the monitoring results into the adjustment actions of the corresponding execution equipment.

[0037] In the above embodiments, preferably, identifying the reactor operation stage includes: After the reactor completes water filling, circulation, aeration startup, and inoculation with aerobic activated sludge, it enters the particle nucleation stage. When the proportion of particles with a diameter of 0.2 mm to 0.5 mm is greater than 50%, particle nucleation is considered complete, and the central controller 5 determines that it has transitioned from the particle nucleation stage to the bacterial and algal acclimatization and growth stage. As an auxiliary judgment criterion, at this time, the sludge settling time can decrease from 60 min to 120 min in the initial startup phase to 30 min to 60 min, the settling velocity of the retained particles can be greater than 5 m / h, the bacterial and algal sludge concentration can be between 3 g / L and 5 g / L, and extracellular polymers begin to form a particle-bonded skeleton.

[0038] During the acclimatization and growth stage of microorganisms and algae, when the proportion of particles with a diameter of 0.5 mm to 3.0 mm is greater than 60% and the particle settling velocity is greater than 20 m / h, it indicates that the microalgae attachment and particle growth have met the screening and cultivation requirements, and the acclimatization and growth stage of microorganisms and algae is determined to be completed. The stage then transitions to the particle screening and maturity stage. At this time, the sludge settling time can be reduced to 10 min to 30 min, the concentration of microorganisms and algae in the sludge reaches 4 g / L to 8 g / L, and the rapid accumulation of extracellular polymers and the stable colonization of microalgae in the particles can be used for further confirmation.

[0039] When the proportion of particles with a diameter of 0.8 mm to 2.0 mm is greater than 70%, the particle settling velocity is 30 m / h to 80 m / h, and the concentration of bacterial-algae sludge is 5 g / L to 10 g / L, it is determined that stable bacterial-algae symbiotic particles have been formed and the system has entered a stable operation stage. As an auxiliary state, the sludge settling time can be stabilized at 10 min to 20 min, forming a clear sludge-water interface, with extracellular polymers remaining stable, and microalgae accounting for approximately 20% to 40% of the bacterial-algae sludge.

[0040] During the particle nucleation stage, the particle control strategy involves retaining small seed particles and employing a conservative culture method, focusing on determining MLSS, particle size, and settling time. During the algal acclimatization and growth stage, the particle control strategy involves weeding out weak particles and promoting extracellular polymer formation, focusing on determining extracellular polymer, sludge volume index, and particle size growth. In the particle screening and maturation stage, automatic screening and harvesting are performed using settling differences, focusing on determining MLSS, particle size distribution, sludge volume index, and harvesting volume. The control objectives for the three stages are, in order, to avoid initial shock, dynamically enhance algal symbiosis, and balance particle growth, screening, and harvesting.

[0041] Specifically, the core maturity assessment methods for the above three stages are shown in Table 1 below: Table 1. Core Maturity Indicators for the Three Stages

[0042] Specifically, the three-stage control strategies and actions are shown in Table 2 below: Table 2. Three-stage control strategies and actions

[0043] In this embodiment, the stage transition is identified by combining the results of particle size distribution, settling velocity, and sludge concentration, avoiding switching cultivation parameters solely based on running time, and ensuring that the stage transition reflects the actual formation state of the particles.

[0044] In the above embodiments, preferably, during the particle nucleation stage, the operating time can be 3 to 7 days, dissolved oxygen can be controlled at 0.5 mg / L to 2.0 mg / L, dissolved carbon dioxide can be controlled at 5 mg / L to 15 mg / L without active control, gaseous carbon dioxide is not actively replenished, light intensity is controlled to zero, and operation is carried out under complete darkness, with a light-dark ratio of 0h:24h. The temperature can be controlled at 25℃ to 30℃, pH can be controlled at 6.5 to 7.5, wastewater COD:N:P can be 100:5:1, COD can be 300 mg / L to 1000 mg / L, and organic load can be 0.5 kg COD / (m³). 3 ·d) to 1.5kgCOD / (m 3•d) The hydraulic retention time can be 12h to 24h, and the sludge retention time can be greater than 20d. The MLSS of the aerobic activated sludge inoculated can be 3000mg / L to 5000mg / L. The dominant bacterial community includes nitrifying bacteria, denitrifying bacteria, and extracellular polymeric bacteria. Algae are not inoculated at this stage. The upflow velocity is controlled at 2m / h to 5m / h, the apparent gas velocity can be 0.2cm / s to 0.5cm / s, and the shear force can be 0.1Pa to 0.5Pa. The particle size at this stage is usually less than 0.3mm. The initial floc aggregation and extracellular polymer formation are promoted through low loading and circulation, and small flocs that have not formed stable particles are periodically discharged.

[0045] During the acclimatization and growth phase of bacteria and algae, the operation time was 5 to 10 days, with dissolved oxygen controlled at 2.0 mg / L to 4.0 mg / L, dissolved carbon dioxide at 10 mg / L to 30 mg / L, and gaseous carbon dioxide volume fraction at 1% to 5%. The light intensity was gradually increased to 50 μmol / (m²). 2 ·s) to 200μmol / (m 2 The light-dark ratio was 12h:12h. The temperature was 25℃ to 30℃, the pH was 7.0 to 8.0, the COD:N:P ratio was 100:10:2, the COD was 300mg / L to 600mg / L, and the organic loading was 1.5kgCOD / (m³). 3 ·d) to 3.0 kg COD / (m 3 •d), hydraulic retention time is 8h to 16h, sludge retention time is greater than 25d. MLSS is 4000mg / L to 8000mg / L, and extracellular polymeric substances grow rapidly. Chlorella or Scenedesmus can be inoculated, with an initial OD680 of 0.1 to 0.3; upflow velocity is 5m / h to 10m / h, apparent gas velocity is 0.5cm / s to 1.5cm / s, and shear force is 0.5Pa to 1.5Pa. Particle size can increase to 0.5mm to 3.0mm, and particles with poor settling performance are washed away by the upflow velocity, while particles with a settling velocity greater than 20m / h are retained.

[0046] During the particle screening maturation stage, the operating time is 10 to 20 days, with dissolved oxygen controlled at 4.0 mg / L to 8.0 mg / L, dissolved carbon dioxide at 20 mg / L to 50 mg / L, and gaseous carbon dioxide volume fraction at 5% to 15%. Carbon dioxide-rich flue gas can also be introduced. The light intensity is 300 μmol / (m²). 2 ·s) to 500μmol / (m 2•s), using continuous light or a light-dark ratio of 16h:8h. Temperature: 25℃ to 30℃, pH: 7.5 to 8.5, COD:N:P: 100:(10~15):(1~2), COD: 100mg / L to 400mg / L, organic loading: 2.0kgCOD / (m³) 3 ·d) to 4.0 kg COD / (m 3 •d) The hydraulic retention time is 6 to 10 hours, and the sludge retention time is greater than 30 days. MLSS is 5000 mg / L to 10000 mg / L, microalgae content is 20% to 40%, and OD680 can reach 0.5 to 1.0. Algae mainly reproduce naturally and are not separately inoculated. The upflow velocity is 8 m / h to 15 m / h, the apparent gas velocity is 1.5 cm / s to 3.0 cm / s, and the shear force is 1.0 Pa to 2.5 Pa, avoiding shear force exceeding 5 Pa to prevent significant particle breakage. The particle size is stabilized at 0.8 mm to 2.0 mm, and particles with a settling velocity of 30 m / h to 80 m / h are retained through 10 to 20 minutes of settling screening.

[0047] The basic parameters and methods for regulating the three stages of particle nucleation, bacterial and algal acclimatization and growth, and particle selection and maturation are shown in Table 3 below: Table 3. Basic parameters and methods for three-stage regulation

[0048] In this embodiment, bacterial skeleton formation, microalgae attachment, and particle densification are carried out under conditions that are adapted to their growth patterns, avoiding the use of the same set of parameters throughout the entire startup process.

[0049] In the above implementation, when the proportion of particles with a diameter less than 0.8 mm exceeds 20%, it is determined that the granulation is insufficient. The upward flow rate can be reduced by 10%, and the internal circulation and shear force can be reduced simultaneously. The determination is made again after 12 hours. The upward flow rate should not be lower than 8 m / h.

[0050] When the proportion of particles larger than 2 mm exceeds 20% and MLSS is less than 5 g / L, it indicates that the particles are too large but the total amount of sludge is insufficient. In this case, external circulation separation should not be started. Instead, the upward flow velocity can be increased by 10% to increase internal circulation and shear force. After 12 hours, the situation should be reassessed to break some large particles into medium-sized particles. The upward flow velocity should not exceed 15 m / h.

[0051] Preferably, when the proportion of particles larger than 2 mm exceeds 20% and the concentration of bacterial and algal sludge is greater than 10 g / L, the conditions for collecting mature MBGS particles are met. The central controller 5 activates the external circulation backflow, allowing the external circulation fluid to enter the MBGS particle separation and collection unit 3. Mature large particles are collected using particle size or settling differences, while small and medium-sized particles are returned to the reactor with the separated water. At the same time, the upward flow velocity can be increased by 10% based on the current value. This increase is performed once and the upward flow velocity does not exceed 15 m / h to increase the particle screening intensity and avoid excessively high sludge concentration affecting mass transfer and light transmission.

[0052] When the concentration of bacterial and algal sludge is below 5 g / L, the carbon dioxide flue gas supply and water inflow can be increased by 10% while executing the particle size adjustment logic. The adjustment should be re-evaluated after 4 hours, and the adjustment amount should not exceed 150% of the maximum design capacity of the corresponding equipment. If necessary, an MBGS reinoculation prompt should be output, and the operator can use the harvested bacterial and algal particles for supplementary inoculation.

[0053] When the concentration of bacterial and algal sludge is greater than 10 g / L, and the proportion of particles smaller than 0.8 mm is greater than the proportion of particles larger than 2 mm, it indicates the accumulation of fine particles and flocculent bacterial and algal sludge in the sludge. When SVI5 is greater than 50 mL / g or SVI30 is greater than 80 mL / g, it indicates a decrease in sludge settling performance. When either of these conditions is met, the central controller 5 controls the flocculent bacterial and algal sludge separation and collection unit 2 to switch from the normal state to the enhanced state, while simultaneously enhancing the washing, separation, and collection of fine MBGS particles and flocculent bacterial and algal sludge. When MLSS is greater than 10 g / L and the proportion of fine particles is not greater than the proportion of large particles, external circulation separation and collection of mature particles are the main methods. When the proportion of fine particles is greater than the proportion of large particles, the separation and collection intensity of flocculent bacterial and algal sludge is increased while collecting large particles, and the washing and separation of fine MBGS particles and flocculent bacterial and algal sludge are also increased.

[0054] When the conditions for enhanced harvesting of flocculent bacterial and algal sludge are met, the flocculent bacterial and algal sludge separation and harvesting unit 2 is switched from the normal operation state to the enhanced operation state to improve the separation and harvesting efficiency of flocculent bacterial and algal sludge and enhance the washing and separation of fine MBGS particles and flocculent bacterial and algal sludge.

[0055] During enhanced harvesting, when SVI5 or SVI30 exceeds the corresponding threshold, the circulation and shear intensity can be increased simultaneously, and particle size, sludge concentration, and sludge volume index should be re-collected after 12 hours for secondary assessment. When the sludge concentration is lower than the level required to maintain the granular system, such as below 5 g / L, the central controller 5 can output an MBGS reinoculation prompt, allowing operators to use the harvested algal particles as seed sludge. This manual assistance measure does not change the automatic harvesting control process.

[0056] Specifically, the control logic of the automated control process is shown in Table 4 below: Table 4. Control measures and logic of automated control processes

[0057] In this embodiment, the harvesting path is selected according to the sludge type and particle state, so that mature large particles are output in a directional manner, small and medium particles are retained and cultivated, and fine particles and flocculent bacteria and algae sludge that affect settling performance are removed in a timely manner.

[0058] In the above embodiments, preferably, during the stable operation phase, adjusting the operation based on the reaction condition parameters includes: When dissolved oxygen is greater than 4 mg / L, reduce the air aeration rate and increase the influent flow rate. For example, reduce the air aeration rate by 20% and increase the influent flow rate by 10%, and reassess after 30 minutes to ensure that dissolved oxygen is not lower than 2 mg / L. This adjustment can be made gradually until the air aeration rate is zero or the influent flow rate reaches full capacity. When dissolved oxygen is less than 2 mg / L, increase the carbon dioxide supply and air aeration rate, reduce the influent flow rate, and increase the supplemental lighting intensity. For example, increase the carbon dioxide supply by 20%, increase the air aeration rate by 10%, reduce the influent flow rate by 10%, and increase the supplemental lighting intensity by 10%, ensuring that the supplemental lighting intensity does not exceed 500 μmol / (m²). 2 ·s), and then re-evaluated after 30 minutes.

[0059] When the pH is greater than 8.5, the carbon dioxide supply can be increased by 20% to compensate for carbon dioxide consumption. When the dissolved carbon dioxide concentration is less than 50 μL / L, the carbon dioxide supply can be increased by 20%; when the dissolved carbon dioxide concentration is greater than 70 μL / L, the carbon dioxide supply can be decreased by 15%. After each adjustment, the concentration can be retested after 30 minutes to allow the dissolved carbon dioxide concentration to converge towards the control target of approximately 60 μL / L.

[0060] When the detection value of any light intensity monitor is less than 300 μmol / (m 2 When the sludge concentration and settling performance are determined first to rule out shading caused by excessively high sludge concentration or poor settling performance, the supplementary light power is increased by 20%, and the determination is repeated after 1 hour until both detection values ​​reach the preset range. When either detection value is greater than 500 μmol / (m 2 When the temperature deviates from 25°C to 30°C, the supplementary light power is gradually reduced until both detection values ​​are below the upper limit. The central controller 5 outputs an alarm message and a water inlet temperature adjustment command when the temperature deviates from 25°C to 30°C.

[0061] Specifically, the control logic of the automated control process is shown in Table 5 below: Table 5. Control measures and logic of automated control processes

[0062] In this embodiment, by setting the adjustment range and retest time, the gas supply, water intake, supplemental lighting, and temperature regulation form a gradual convergence process, reducing operational oscillations caused by one-time over-adjustment.

[0063] In the above embodiment, preferably, the upward flow velocity V is determined based on the internal circulation flow rate Q0, satisfying: V = Q0 / S; Q0=Q1+Q2+24×(Q3+Q4+Q5); Where S is the cross-sectional area of ​​the main reaction guide tube 13 of the reactor, Q1 is the influent flow rate, Q2 is the external circulation return flow rate, Q3 is the carbon dioxide gas flow rate, Q4 is the air flow rate, Q5 is the nitrogen replenishment flow rate, and coefficient 24 reflects the thrust gain formed on the water body after the comprehensive gas source is released by gas lift.

[0064] The central controller 5 regulates the upward flow rate V by adjusting at least one of Q1, Q2, Q3, Q4 and Q5.

[0065] Specifically, upon receiving a command to increase the upward flow velocity, the central controller 5 prioritizes adjusting the inlet water, external circulation return, carbon dioxide supply, and air aeration, and calculates the additional push flow required based on the adjusted flow rates. If it is still necessary to increase the upward flow velocity, the nitrogen supply can be increased by 20%, and the calculation will be repeated after 1 hour, with the upward flow velocity not exceeding 15 m / h.

[0066] Upon receiving a command to reduce the upward flow velocity, the nitrogen supply should be reduced first, with each reduction increment being 20%, and a reassessment should be made after 1 hour. When the nitrogen supply is already zero and the upward flow velocity is still higher than the target value, the external circulation return flow, internal circulation, air aeration, and carbon dioxide supply can be reduced sequentially, with the upward flow velocity not lower than 8 m / h.

[0067] When the nitrogen supply is zero and the upward flow velocity is still higher than the target value, the external circulation return, internal circulation, air aeration, and carbon dioxide supply can be reduced by 10% each time until the upward flow velocity reaches the control target. When there are no external circulation, internal circulation, air, or carbon dioxide flow adjustment commands and the upward flow velocity is greater than 9 m / h, the nitrogen supply can be reduced by 20% each time until it is zero, in order to reduce the consumption of air source used only to maintain hydraulic circulation.

[0068] Specifically, the control logic of the automated control process is shown in Table 6 below: Table 6. Control measures and logic of automated control processes

[0069] Furthermore, the system relationships between monitoring indicators, instruments, control commands, and execution devices are shown in Table 7 below: Table 7. Instruments and Interlocking Control Equipment Corresponding to the Indicators

[0070] In this embodiment, hydraulic flow rate and gas propulsion are uniformly converted into upward flow velocity, enabling the central controller 5 to coordinately adjust hydraulic shear and gas-liquid mass transfer conditions according to different flow sources.

[0071] In the above embodiments, preferably, during the stable operation phase, the ratio of the internal circulation return flow to the influent flow is 50% to 500%, the internal circulation return is continuously activated, and the target of the return includes granular sludge in the reactor.

[0072] The ratio of external circulation return flow to influent flow is 50%, and it is normally closed. External circulation return is turned on when the conditions for mature MBGS particle harvesting are met, and turned off when the conditions for mature MBGS particle harvesting are not met. The particles entering the external circulation are separated, with large particles being harvested and medium and small particles being returned.

[0073] When harvesting MBGS pellets, the daily mud discharge rate is 5% / d to 30% / d. The flocculent bacteria and algae sludge separation and collection unit 2 is kept running normally, operating at a separation and collection efficiency of 60% to 70% under normal conditions. When enhanced collection conditions are met, its efficiency is increased to 100%. The effluent discharge ratio can be set to 100%, and the effluent discharge includes compliant effluent as well as fine particles and flocs that enter the flocculent bacteria and algae sludge separation and collection unit 2 with the effluent. When extracellular polymeric substances decrease and the sludge structure becomes loose, the influent load can be reduced to minimize shock and promote particle structure recovery.

[0074] In a specific operational example, suspended solids with a diameter less than 0.2 mm can be discharged by floating or overflowing, particles with a diameter less than 0.5 mm are refluxed for culture, particles with a diameter of 0.5 mm to 1 mm are retained, particles with a diameter of 1 mm to 2 mm are preferentially retained, and particles with a diameter greater than 3 mm are moderately crushed or harvested through enhanced shearing and separation screening. This allows the proportion of particles with a diameter of 0.8 mm to 2.0 mm to be controlled at over 70%, and maintained at approximately 80% under stable conditions.

[0075] During implementation, the following operational targets can also be set: particle settling velocity greater than 20 m / h, SVI5 less than 50 mL / g, SVI30 less than 80 mL / g, settling ratio greater than 85%, MLSS of 5 g / L to 10 g / L, extracellular polymeric substances of 80 mg / g VSS to 150 mg / g VSS, and microalgae content of 15% to 40%. Correspondingly, implementation effects such as COD removal rate greater than 80%, total nitrogen removal rate greater than 60%, total phosphorus removal rate greater than 70%, and carbon dioxide utilization rate greater than 50% can be achieved. These treatment indicators are target values ​​under specific operating conditions and do not constitute a limitation on other implementation methods.

[0076] Specifically, the basic control parameters are set as shown in Table 8 below: Table 8 Basic Control Parameters

[0077] Specifically, the objectives that can be achieved using the above-mentioned control methods are shown in Table 9 below: Table 9 Target effect values ​​of the control methods

[0078] In this implementation, a reasonable particle size structure and sludge concentration are maintained by combining continuous internal circulation, condition-triggered external circulation, and two harvesting intensities, while also ensuring effluent compliance, particle renewal, and recovery of bacterial and algal biomass.

[0079] In the above embodiments, preferably, the central controller 5 integrates a multi-parameter automatic priority control model based on the response surface methodology (RSM). It uses multiple parameters among the influent load, gas-liquid mass transfer conditions, supplemental lighting conditions, and circulation intensity as candidate control parameters, and selects one of the following as the current preset operating index: particle size distribution, sludge concentration, sludge volume index, settling velocity, pollutant removal index, or carbon dioxide utilization index. It then determines the candidate control parameter with the highest impact on the preset operating index as the priority control parameter and outputs the corresponding priority control command.

[0080] The central controller 5 establishes a response relationship between candidate adjustment parameters and preset operating indicators based on historical operating data and real-time operating status. It compares the influence of each candidate adjustment parameter and selects the parameter with the highest influence as the priority adjustment parameter. After outputting the priority control command, it continues to collect operating status parameters and updates the response relationship using the changes in indicators before and after adjustment. Different single indicators can be selected as optimization objects for different operating cycles, thereby continuously improving the control sequence and adjustment measures. When the control objective changes, particle stability, pollutant removal, carbon fixation efficiency, or bacterial and algal biomass yield can be selected as single response indicators, and the corresponding parameters can be optimized sequentially to achieve dynamic coordination of multiple operating objectives.

[0081] In this embodiment, the priority adjustment order can be determined when multiple parameters deviate from the appropriate range at the same time, reducing mutual interference caused by simultaneous changes in water intake, gas supply, supplemental lighting and circulation parameters, and improving the consistency of multi-parameter control decisions.

[0082] The present invention also proposes an automatic sludge collection and operation control system for a dual-source MBGS reactor, characterized in that it includes an MBGS reactor 1, an online monitoring unit 4, a central controller 5, and an operation control execution unit; MBGS reactor 1 may be equipped with a main reaction guide tube 13, a comprehensive gas source distribution component 15, a supplementary lighting component, a water inlet distribution component 16, a reflux cone 17, a qualified water outlet 18, and a circulation separation pipeline to form the reaction space required for water inlet, air stripping circulation, supplementary lighting cultivation, and particle reflux.

[0083] MBGS particle separation and harvesting unit 3 may include a circulating separation pump and separation pipeline 31, a hydraulic screen 32, a separation water storage unit 33, and a particle harvesting unit 34. After the external circulating fluid containing particles enters the hydraulic screen 32, large-diameter mature particles enter the particle harvesting unit 34, while medium and small-diameter particles return to the MBGS reactor 1 with the separation water. Flocculent bacterial and algal sludge separation and harvesting unit 2 may include a water distribution structure 21, a separation reaction zone 22, a dissolved gas release component 23, a flocculent sludge collection unit 24, a sludge scraping component 25, a qualified water discharge component 26, a sludge discharge component 27, and a harvesting agent dosing component 28, used to separate fine MBGS particles and flocculent bacterial and algal sludge.

[0084] The operation regulation execution unit includes a water intake regulation execution unit, a gas-liquid mass transfer regulation execution unit, a supplemental lighting regulation execution unit, a circulation separation regulation execution unit, and a harvesting regulation execution unit. The water intake regulation execution unit may include a water intake pump; the gas-liquid mass transfer regulation execution unit may include a carbon dioxide flow control valve, an air flow control valve, and a nitrogen flow control valve; the supplemental lighting regulation execution unit may include an adjustable power supplemental lighting lamp group 14; the circulation separation regulation execution unit may include a circulation separation pump and corresponding valves; and the harvesting regulation execution unit is connected to the two types of separation harvesting units for control.

[0085] The central controller 5 receives monitoring data from all online instruments, analyzes particle state, sludge concentration, settling performance, and reaction conditions, and outputs adjustment commands to the corresponding execution units. Online particle size analysis results are used to adjust the upward flow velocity and external circulation status; sludge concentration and sludge volume index are used to adjust circulation and harvesting intensity; dissolved oxygen data is used to adjust the gas source, influent, and supplemental lighting; pH and dissolved carbon dioxide data are used to adjust carbon dioxide supply; and dual-point light intensity is used to adjust supplemental lighting power. The harvesting adjustment execution unit selects between mature particle harvesting and enhanced harvesting of flocculent bacterial and algal sludge based on the commands from the central controller 5.

[0086] In this implementation, online sensing, stage identification, operational decision-making, execution adjustment, and dual-source sludge collection are integrated into the same control system. This transforms the complex process of cultivating and collecting algae particles into an automated control process that can be monitored, determined, executed, and corrected by feedback. This improves the consistency of engineering operations and reduces maintenance difficulty.

[0087] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A method for automatic sludge collection and operation control of a dual-source sludge reactor in an MBGS reactor, characterized in that, The MBGS reactor is equipped with a flocculent bacteria and algae sludge separation and harvesting unit for separating and harvesting flocculent bacteria and algae sludge and an MBGS particle separation and harvesting unit for separating and harvesting MBGS particles. The method includes: The operating status parameters of the reactor are collected by the online monitoring unit and sent to the central controller. The operating status parameters include sludge status parameters that characterize the particle size, sludge concentration and settling characteristics of the bacterial and algal sludge, as well as reaction condition parameters that characterize the reaction environment, influent load, gas-liquid mass transfer and circulation status. The central controller identifies whether the reactor is in the particle nucleation stage, the bacterial and algal acclimatization and growth stage, the particle screening and maturation stage, or the stable operation stage based on the sludge state parameters. The central controller, in accordance with the particle nucleation stage, the bacterial and algal acclimatization and growth stage, and the particle screening and maturation stage, controls the operation and regulation execution unit to adjust the influent load, gas-liquid mass transfer conditions, supplemental lighting conditions, and circulation intensity according to the particle cultivation objectives of the corresponding stage, so as to form a bacterial particle skeleton, promote microalgal attachment and growth, and screen mature bacterial-algal symbiotic particles. The operation and regulation execution unit includes an influent regulation execution unit, a gas-liquid mass transfer regulation execution unit, a supplemental lighting regulation execution unit, a circulation separation regulation execution unit, and a harvesting regulation execution unit. During the stable operation phase, the central controller determines whether the mature MBGS particle harvesting conditions or the enhanced harvesting conditions of flocculent bacterial and algal sludge are met based on the sludge state parameters and the reaction condition parameters, and generates corresponding operation adjustment commands. When the conditions for harvesting mature MBGS particles are met, the harvesting regulation execution unit controls the MBGS particle separation and harvesting unit to harvest mature MBGS particles, and controls the circulating separation regulation execution unit to return the separated small and medium-sized MBGS particles to the MBGS reactor. When the conditions for enhanced harvesting of flocculent algae sludge are met, the harvesting adjustment execution unit controls the flocculent algae sludge separation and harvesting unit to switch from the normal operation state to the enhanced operation state, so as to improve the separation and harvesting efficiency of flocculent algae sludge. After executing the operation adjustment command, the operation status parameters continue to be collected, and the central controller updates the reactor operation stage, harvesting conditions and operation adjustment command to form a closed-loop automatic operation control.

2. The method for automatic collection and operation control of dual-source sludge from an MBGS reactor according to claim 1, characterized in that, The online monitoring unit includes a pH and temperature monitor, a first light intensity monitor, a second light intensity monitor, a dissolved oxygen meter, a dissolved carbon dioxide detector, a suspended solids concentration detector, an online particle size analyzer, an online sludge volume index monitor, an influent flow meter, a circulating separation flow meter, a carbon dioxide gas flow meter, an air flow meter, and a nitrogen flow meter. The central controller is connected to the online monitoring unit, the water intake regulation execution unit, the gas-liquid mass transfer regulation execution unit, the supplementary lighting regulation execution unit, the circulation separation regulation execution unit, and the harvesting regulation execution unit, respectively.

3. The method for automatic collection and operation control of dual-source sludge from an MBGS reactor according to claim 1, characterized in that, Identifying reactor operation phases includes: When the proportion of particles with a diameter of 0.2 mm to 0.5 mm is greater than 50%, it is determined that the nucleation of particles is complete, and the process transitions from the particle nucleation stage to the bacterial and algal acclimatization and growth stage. When the proportion of particles with a diameter of 0.5 mm to 3.0 mm is greater than 60% and the particle settling velocity is greater than 20 m / h, it is determined that the domestication and growth of bacteria and algae is completed, and the process transitions from the domestication and growth stage of bacteria and algae to the particle screening and maturity stage. When the proportion of particles with a diameter of 0.8 mm to 2.0 mm is greater than 70%, the particle settling velocity is 30 m / h to 80 m / h, and the concentration of bacterial and algal sludge is 5 g / L to 10 g / L, it is determined that stable bacterial and algal symbiotic particles have been formed and the stable operation stage has been entered.

4. The method for automatic collection and operation control of dual-source sludge in an MBGS reactor according to claim 3, characterized in that, During the particle nucleation stage, dissolved oxygen was controlled at 0.5 mg / L to 2.0 mg / L, light intensity was controlled at zero, and the upflow velocity was controlled at 2 m / h to 5 m / h. During the acclimatization and growth stage of bacteria and algae, dissolved oxygen was controlled at 2.0 mg / L to 4.0 mg / L, and light intensity was gradually increased to 50 μmol / (m²). 2 ·s) to 200μmol / (m 2 •s), the volume fraction of gaseous carbon dioxide is controlled to be 1% to 5%, and the upflow velocity is controlled to be 5 m / h to 10 m / h; During the particle screening and maturation stage, dissolved oxygen was controlled at 4.0 mg / L to 8.0 mg / L, and light intensity was controlled at 300 μmol / (m²). 2 ·s) to 500μmol / (m 2 •s), the volume fraction of gaseous carbon dioxide is controlled to be 5% to 15%, and the upward flow rate is controlled to be 8m / h to 15m / h.

5. The method for automatic collection and operation control of dual-source sludge in an MBGS reactor according to claim 1, characterized in that, The mature MBGS particle harvesting conditions include: particles with a diameter greater than 2 mm account for more than 20%, and the concentration of bacteria and algae sludge is greater than 10 g / L. The enhanced harvesting conditions for the flocculent bacterial and algal sludge include any of the following: The concentration of bacterial and algal sludge is greater than 10 g / L, and the proportion of particles with a diameter of less than 0.8 mm is greater than the proportion of particles with a diameter of greater than 2 mm. Online sludge volume index (SVI5) is greater than 50 mL / g or SVI30 is greater than 80 mL / g; When the mature MBGS particle harvesting conditions are met, the external circulation reflux is activated, and the MBGS particle separation and harvesting unit is controlled to harvest mature MBGS particles, increasing the upward flow velocity by 10%, wherein the upward flow velocity does not exceed 15 m / h. When the enhanced harvesting conditions for flocculent algae sludge are met, the flocculent algae sludge separation and harvesting unit is switched from normal operation to enhanced operation to improve the separation and harvesting efficiency of flocculent algae sludge and enhance the washing and separation of fine MBGS particles and flocculent algae sludge.

6. The method for automatic collection and operation control of dual-source sludge in an MBGS reactor according to claim 2, characterized in that, During the stable operation phase, operational adjustments based on the aforementioned reaction condition parameters include: When dissolved oxygen is greater than 4 mg / L, reduce the air aeration rate and increase the water inflow rate; when dissolved oxygen is less than 2 mg / L, increase the carbon dioxide supply and air aeration rate, reduce the water inflow rate and increase the supplemental lighting intensity. When the pH is greater than 8.5 or the dissolved carbon dioxide concentration is less than 50 μL / L, increase the carbon dioxide supply; when the dissolved carbon dioxide concentration is greater than 70 μL / L, decrease the carbon dioxide supply. When the detection value of the first or second light intensity monitor is less than 300 μmol / (m 2 When ·s), increase the supplementary light power after determining the concentration of bacterial and algal sludge and the sludge settling performance; when either the first light intensity monitor or the second light intensity monitor has a detection value greater than 500 μmol / (m 2 When ·s), reduce the supplementary light power; When the temperature deviates from 25℃ to 30℃, an inlet water temperature adjustment command is output.

7. The method for automatic collection and operation control of dual-source sludge from an MBGS reactor according to claim 1, characterized in that, The upward flow velocity V is determined based on the internal circulation flow rate Q0, satisfying the following: V = Q0 / S; Q0=Q1+Q2+24×(Q3+Q4+Q5); Where S is the cross-sectional area of ​​the main reaction guide tube of the reactor, Q1 is the influent flow rate, Q2 is the external circulation return flow rate, Q3 is the carbon dioxide gas flow rate, Q4 is the air flow rate, Q5 is the nitrogen replenishment flow rate, and 24 is the thrust gain coefficient formed by the gas source. The central controller regulates the upward flow rate V by adjusting at least one of Q1, Q2, Q3, Q4 and Q5.

8. The method for automatic collection and operation control of dual-source sludge in an MBGS reactor according to claim 1, characterized in that, During the stable operation phase, the ratio of internal circulation return flow to influent flow is 50% to 500%, and the internal circulation return is continuously activated. The ratio of external circulation return flow to influent flow is 50%. External circulation return is activated when the mature MBGS pellet harvesting conditions are met and deactivated when the mature MBGS pellet harvesting conditions are not met. When harvesting MBGS pellets, the daily mud discharge rate is 5% / d to 30% / d. The flocculent bacteria and algae sludge separation and collection unit operates with a separation and collection efficiency of 60% to 70% under normal operating conditions, and increases the separation and collection efficiency to 100% under enhanced operating conditions.

9. The method for automatic collection and operation control of dual-source sludge in an MBGS reactor according to claim 1, characterized in that, The central controller integrates a multi-parameter automatic priority control model based on the response surface methodology (RSM). The multi-parameter automatic priority control model is based on the operating state parameters and, according to the response relationship between multiple candidate control parameters and preset operating indicators among the influent load, gas-liquid mass transfer conditions, supplementary lighting conditions, and circulation intensity, determines the candidate control parameter with the highest influence on the preset operating indicators as the priority control parameter and outputs the corresponding priority control command.

10. An automatic sludge collection and operation control system for a dual-source MBGS reactor, characterized in that, It includes an MBGS reactor, an online monitoring unit, a central controller, and an operation regulation and execution unit; The MBGS reactor is equipped with a flocculent bacteria and algae sludge separation and harvesting unit for separating and harvesting flocculent bacteria and algae sludge and an MBGS particle separation and harvesting unit for separating and harvesting MBGS particles. The online monitoring unit is used to collect the operating status parameters of the reactor and send them to the central controller. The operating status parameters include sludge status parameters and reaction condition parameters. The operation adjustment execution unit includes a water intake adjustment execution unit, a gas-liquid mass transfer adjustment execution unit, a supplementary lighting adjustment execution unit, a circulation separation adjustment execution unit, and a harvesting adjustment execution unit; The harvesting adjustment execution unit is connected to the flocculent bacteria and algae sludge separation and harvesting unit and the MBGS particle separation and harvesting unit respectively to adjust the corresponding separation and harvesting operation status. The central controller is connected to the online monitoring unit and the operation adjustment execution unit respectively, and is used to output operation adjustment instructions to the operation adjustment execution unit according to the operation status parameters, and is configured to execute the automatic operation control method according to any one of claims 1 to 9.

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