Medicine production wastewater denitrification treatment system

Abstract

The present invention discloses a medicine production wastewater denitrification treatment system, and relates to the technical field of medicine production wastewater treatment, and the system comprises: a raw water pretreatment module, which is composed of a homogeneous regulation unit, a physicochemical purification unit and a biological hydrolysis pretreatment unit, and is used for treating original medicine production wastewater into biochemical friendly water; the core denitrification module consists of a denitrification unit, a nitrification unit and a circulating regulation and control unit and is used for converting the biochemical friendly water into low-nitrogen reaction water; the deep finishing module is composed of a membrane biological reaction unit, a rear denitrification unit and an activated carbon polishing unit, and is used for converting the low-nitrogen reaction water into standard discharge water; and the operation guarantee module is composed of an online monitoring unit, an automatic adding unit, a sludge management unit and an energy efficiency optimization unit, and is used for collecting and integrating water quality and working condition parameters of each treatment position to form a system operation state set. The system is clear in structure, excellent in denitrification effect and suitable for advanced treatment of pharmaceutical wastewater.

Description

Technical Field

[0001] This invention relates to the field of pharmaceutical wastewater treatment technology, and in particular to a pharmaceutical wastewater denitrification treatment system. Background Technology

[0002] With the rapid development of the pharmaceutical industry, the high-concentration, high-salinity, and high-ammonia-nitrogen organic wastewater generated during its production process has become a pressing challenge in industrial wastewater treatment. This type of wastewater is generally characterized by complex composition, toxicity, poor biodegradability, and large fluctuations in treatment load. It contains high concentrations of nitrogenous pollutants such as ammonia nitrogen, nitrates, and organic nitrogen. Direct discharge without effective treatment can easily lead to eutrophication and ecosystem disruption. Therefore, developing efficient and stable denitrification technologies is a crucial direction for achieving the resource recovery and harmless treatment of pharmaceutical wastewater.

[0003] Existing nitrogen removal technologies for pharmaceutical wastewater mainly include physicochemical methods (such as stripping, ion exchange, membrane separation, etc.) and biological methods (such as traditional activated sludge process, SBR, A / O, A...). 2 (e.g., O process). However, in high-salt and highly toxic environments, the activity of functional bacteria in traditional biological methods is easily inhibited, leading to system dysbiosis and fluctuations in treatment efficiency. While physicochemical methods offer rapid removal, they are energy-intensive, costly to operate, and prone to secondary pollution. Furthermore, many current processes lack modular design, relying on manual intervention for system operation and control, making it difficult to adapt to dynamic changes in wastewater quality. Denitrification processes commonly suffer from low carbon source utilization, poor nitrification efficiency, and excessive nitrogen levels in the final effluent.

[0004] To address the aforementioned problems, this invention provides a denitrification treatment system for pharmaceutical production wastewater. It constructs a multi-stage synergistic treatment system with a "module-unit" architecture at its core and multi-level coupled biological denitrification technology as its foundation. This system integrates multiple technologies, including functional bacteria screening and enhancement, biological regulation reactions, membrane separation purification, and end-to-end operational assurance. Through precise coupling and closed-loop control between units, it achieves phased treatment and efficient removal of various nitrogenous elements from wastewater. Summary of the Invention

[0005] To address the above problems, this invention provides a denitrification treatment system for pharmaceutical production wastewater, which solves the problems of poor biodegradability, low nitrogen removal efficiency, and poor system stability in existing technologies.

[0006] To solve the above-mentioned technical problems, the present invention provides the following technical solution: a denitrification treatment system for pharmaceutical production wastewater, comprising the following modules: The raw water pretreatment module consists of a homogenization adjustment unit, a physicochemical purification unit, and a biological hydrolysis pretreatment unit. It is used to sequentially treat raw pharmaceutical production wastewater into flow-equilibrium water, low-suspended liquid phase water, and finally obtain biochemically friendly water. The core denitrification module consists of a denitrification unit, a nitrification unit, and a circulation control unit. It is used to sequentially convert the biochemically friendly water into intermediate ammonia nitrogen-enriched water and nitrate-enriched water and output low-nitrogen reaction water. The deep purification module consists of a membrane bioreactor unit, a post-denitrification unit, and an activated carbon polishing unit. It is used to sequentially convert the low-nitrogen reaction water into a deep clarified liquid, denitrified purified water, and finally obtain compliant discharge water. The operation support module consists of an online monitoring unit, an automatic dosing unit, a sludge management unit, and an energy efficiency optimization unit. It is used to collect and integrate water quality and operating parameters at each treatment location to form a system operation status set. Based on the system operation status set, it generates a quantitative reagent flow, a steady-state structure of sludge concentration, and a dynamic energy consumption feedback flow.

[0007] Furthermore, the homogenization unit, through the coordinated operation of its flow meter, variable frequency pump, stirring system, liquid level monitoring and storage buffer tank, and pH self-adjustment system, treats the original pharmaceutical production wastewater and obtains fluid equilibrium water. In the physicochemical purification unit, based on the real-time turbidity value of the flow equilibrium water collected by the online turbidity meter, the flocculant automatic dosing system adds PAC and PAM to the flow equilibrium water to form a premixed liquid containing primary flocs. Subsequently, the premixed liquid containing primary flocs is sequentially introduced into the high-speed stirring zone and the low-speed stirring zone to obtain mature floc water. Finally, the mature floc water enters the inclined plate sedimentation tank to obtain settled sludge and supernatant. The settled sludge is discharged into the sludge tank for centralized treatment, and the supernatant is used as effluent to obtain low suspended liquid phase water. The biological hydrolysis pretreatment unit, through the synergistic cooperation of its composite salt-tolerant functional bacteria, temperature-controlled heater, dissolved oxygen control device, pH self-adjustment system, and nutrient salt dosing system, treats low-suspension liquid phase water to obtain biochemically friendly water.

[0008] Furthermore, the specific operation of the homogenization and conditioning unit in treating the original pharmaceutical production wastewater is as follows: Based on the influent flow signal fed back by the flow meter, a variable frequency pump is used to dynamically adjust the influent flow of the raw pharmaceutical production wastewater, transforming the unstable raw pharmaceutical production wastewater into raw pharmaceutical production wastewater with a constant flow. Subsequently, the raw pharmaceutical production wastewater with a constant flow is mixed throughout the tank through a stirring system to obtain homogeneous mixed water. Next, a level monitoring and regulation buffer tank is used to buffer and store the homogeneous mixed water for a short period of time, and output buffered mixed water. Finally, an acid or alkali solution is automatically added to the buffered mixed water under closed-loop control of online pH and conductivity sensor data through a pH self-adjustment system, thereby obtaining flow equilibrium water. The specific operations of the biological hydrolysis pretreatment unit for treating low-suspension liquid phase water are as follows: Low-suspension water is introduced into an anoxic reactor. The packing support structure in the anoxic reactor provides an interface for microbial attachment and inoculates a complex salt-tolerant functional bacterial community. This community combines with the low-suspension water to form an initial bacterial attachment solution. Subsequently, the initial bacterial attachment solution is maintained at 30±2℃ by a temperature-controlled heater. Through the coordinated regulation of the dissolved oxygen control device, pH self-adjustment system, and nutrient dosing system in the anoxic reactor, the complex salt-tolerant functional bacterial community secretes hydrolytic enzymes to lyse the large organic molecules in the initial bacterial attachment solution, generating biodegradable small molecules, thus obtaining an intermediate hydrolysate. The intermediate hydrolysate undergoes parameter tuning within 10~30 minutes, resulting in biochemically friendly water.

[0009] Furthermore, in the denitrification unit, biochemically friendly water is introduced into an anoxic reaction tank equipped with high specific surface area elastic packing. The high specific surface area elastic packing provides an attachment interface for denitrifying bacteria. Under the condition that the dissolved oxygen in the anoxic reaction tank is controlled at <0.5mg / L, the biochemically friendly water and the denitrifying bacteria in the anoxic reaction tank form an anoxic mixed solution. Subsequently, based on the real-time signals output by the online NO3⁻-N analyzer and the online COD analyzer, sodium acetate is added to the anoxic mixed solution as an electron donor through a carbon source quantitative addition mechanism, and Acinetobacter haemolyticus X4 strain is inoculated. The anoxic mixed solution with added sodium acetate is intermittently stirred by the stirring system in the anoxic reaction tank, so that the nitrate in the anoxic mixed solution with added sodium acetate is continuously reduced to nitrogen gas and released, ultimately generating intermediate ammonia nitrogen-enriched water. The nitrification unit introduces intermediate ammonia nitrogen-enriched water into a long-flow, multi-section aerobic reactor. The aerobic reactor is equipped with a nitrifying bacteria enhancement layer and uses a staged aeration system to supply oxygen in stages. Under the condition that the dissolved oxygen is controlled at 1.5-2.5 mg / L, the ammonia nitrogen in the intermediate ammonia nitrogen-enriched water is gradually converted into nitrite and then into nitrate. After the reaction is completed, nitrate-enriched water is formed. The circulation control unit, through the feedback algorithm of the PLC controller and the flow ratio controller, sends a portion of the nitrate-enriched water back to the denitrification unit according to the calculated ratio via the return pump group, and uses the remainder as the effluent from the core denitrification module; the PLC controller automatically adjusts the return ratio based on the online NO3⁻-N concentration, flow rate and influent TN data, so that the denitrification carbon source matching and nitrification-denitrification coupling in the denitrification unit remain stable, ultimately forming low-nitrogen reaction water.

[0010] Furthermore, the membrane bioreactor unit, through the synergistic cooperation of its embedded PVDF hollow fiber membrane module, concentration maintenance mechanism, and modified nitrification-denitrification synergistic bacteria community, treats low-nitrogen reaction water and obtains a deeply clarified liquid. The post-denitrification unit, through the synergistic cooperation of its internal anaerobic packing system and slow-release carbon source carrier, treats the deeply clarified liquid and obtains denitrified purified water. The activated carbon polishing unit allows denitrified water to flow from bottom to top through a high specific surface area activated carbon column bed at a flow rate of 5-10 m / h. The activated carbon in the high specific surface area activated carbon column bed achieves dechlorination and deodorization of the denitrified water through its porous surface, as well as adsorption of dissolved organic carbon, color and trace drug components in the denitrified water, ultimately forming compliant discharge water.

[0011] Furthermore, the specific operation of the membrane bioreactor unit in treating low-nitrogen reaction water is as follows: Low-NOx reaction water is introduced into the membrane bioreactor (MBR), and dissolved oxygen is continuously supplied through a microporous aeration device at the bottom of the MBR to stabilize it at 2.0 mg / L, forming the initial mixed liquor in the membrane tank. Subsequently, the initial mixed liquor is subjected to solid-liquid separation using an embedded PVDF hollow fiber membrane module in the MBR, yielding concentrated sludge and primary permeate. The concentrated sludge is returned to the MBR via a concentration maintenance mechanism. Simultaneously, a modified nitrification-denitrification synergistic bacteria community is inoculated into the MBR to remove residual nitrogen from the primary permeate, ultimately obtaining a deeply clarified liquid. The operating flux of the embedded PVDF hollow fiber membrane module is automatically adjusted by an online monitoring system, and backwashing and chemical cleaning are performed according to a set cycle. The specific operation of the post-denitrification unit for treating the deep clarified liquid is as follows: The deeply clarified liquid is introduced into an upflow anaerobic filter. An anaerobic packing system is arranged in the upflow anaerobic filter and filled with a porous inert carrier. At the same time, a slow-release carbon source carrier is added into the upflow anaerobic filter through the anaerobic packing system to form a slow-release carbon source bed. The upflow anaerobic filter is operated in a closed system without aeration. The carbon source in the slow-release carbon source bed consumes the dissolved oxygen in the upflow anaerobic filter to form a low-oxygen reducing environment. Under this environment, the denitrifying bacteria in the upflow anaerobic filter reduce the residual nitrate in the deeply clarified liquid to gaseous nitrogen and escape, thus obtaining denitrified purified water.

[0012] Furthermore, the online monitoring unit deploys multiple types of online sensors at the inlet and outlet of the raw water pretreatment module, the outlet of the core denitrification module, and the outlet and discharge port of the deep finishing module. The real-time data collected by the multiple types of online sensors is converted into standard signals by a data acquisition unit and uploaded to the PLC main control system. The PLC main control system uses a threshold comparison, moving average, and rate of change determination model to generate feedback instructions and output the system operation status set. The automatic dosing unit, controlled by a PLC main control system, gathers various water quality deviations based on the system's operating status and controls a programmable quantitative pump to retrieve denitrifying carbon source, pH-adjusting alkaline solution, and trace nutrients from the reagent storage and preparation system. It then adds these substances according to the needs of each treatment location. Simultaneously, a closed-loop control algorithm corrects the dosage and timing in real time, ensuring the dosing process responds synchronously to load fluctuations caused by influent flow rate and pollutant concentration, thus forming a quantitative reagent flow. The sludge management unit is equipped with SVI monitoring probes and MLSS online sensors in the return channel of the anoxic reaction tank of the core denitrification module, the end of the aerobic reaction tank, and the sludge discharge area of ​​the membrane bioreactor of the deep finishing module. The PLC main control system dynamically calculates the sludge load and target sludge age based on the data monitored by the SVI monitoring probes and MLSS online sensors, and issues sludge discharge and return commands based on the sludge load and target sludge age. Then, according to the sludge discharge and return commands, excess sludge is quantitatively discharged through the sludge discharge pump group, and part of the excess sludge is returned to the anoxic reaction tank by the sludge return device. The remaining excess sludge is sent to the sludge thickening tank for dewatering and discharge, forming a stable sludge concentration structure. The energy efficiency optimization unit is equipped with an energy consumption monitoring system on key energy-consuming equipment. The system collects power data and then sends the collected power data to the energy consumption control system in the PLC main control system. The energy consumption control system then generates control commands and feeds them back to the frequency converters corresponding to each key energy-consuming equipment for execution, thus constructing a dynamic energy consumption feedback flow.

[0013] Compared with the prior art, the present invention has the following beneficial effects: This invention constructs a modular and segmented denitrification system, which achieves gradient reduction and targeted removal of nitrogen in different forms in pharmaceutical production wastewater. Through a step-by-step conversion path of "raw water pretreatment module - core denitrification module - deep refining module", it ensures a reasonable division of treatment logic among various pollutants, enhances the specific treatment capability of each unit for target pollutants, and improves the overall denitrification efficiency and stability of the system, especially under fluctuating influent load conditions, it can still maintain a low nitrogen emission level.

[0014] This invention introduces a functional bacteria enhancement mechanism into the core denitrification module. It employs a composite community of denitrifying and nitrifying bacteria screened from high-salt, high-ammonia-nitrogen environments to construct a multi-species synergistic biological denitrification system under controlled reaction conditions. This effectively overcomes the inhibitory effect of toxic organic matter in pharmaceutical wastewater on traditional bacterial communities. Combined with the anoxic-aerobic-internal circulation reaction structure, the system has a clear nitrogen conversion pathway and a high reaction rate. It can achieve efficient denitrification without adding a large amount of carbon source, reducing operating costs and carbon source dependence.

[0015] This invention employs a linked design of a membrane bioreactor unit and a post-denitrification unit, combined with an activated carbon polishing unit to treat residual pollutants in the water at the end of the process. This achieves multi-dimensional purification of nitrates, recalcitrant organic matter, and odor molecules, ensuring that the effluent fully meets national emission standards in terms of COD, TN, NH4⁺-N, NO3⁻-N, etc., thus filling the gaps in traditional processes for "refined end-of-pipe treatment".

[0016] This invention constructs an operation support module covering the entire process. By deploying multiple types of online sensors at the inlet and outlet of the raw water pretreatment module, the outlet of the core denitrification module, and the outlet and discharge of the deep finishing module, in conjunction with an automatic dosing unit, a sludge management unit, and an energy efficiency optimization unit, it can not only implement precise and dynamic reagent dosing according to the needs of each treatment location in the system, but also realize the management of excess sludge discharge and return, as well as the energy-saving operation of key energy-consuming equipment, ensuring that the effluent water quality continuously meets the standards. Attached Figure Description

[0017] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the embodiments will be briefly introduced below. The following drawings only show some embodiments of the present invention and should not be regarded as a limitation on the scope. For those skilled in the art, other related drawings can be obtained from these drawings without creative effort.

[0018] Figure 1 This is the system architecture diagram of the present invention. Detailed Implementation

[0019] 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 a part of the embodiments of the present invention, not all of them. 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. Therefore, the following detailed description of the embodiments of the present invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but is merely a selection of embodiments of the present invention.

[0020] Please refer to Figure 1 , Figure 1 This is an architecture diagram of a pharmaceutical production wastewater denitrification treatment system provided in an embodiment of the present invention, which includes the following modules: The raw water pretreatment module consists of a homogenization adjustment unit, a physicochemical purification unit, and a biological hydrolysis pretreatment unit. It is used to sequentially treat raw pharmaceutical production wastewater into fluid equilibrium water, low suspended liquid phase water, and finally obtain biochemically friendly water.

[0021] The homogenization unit is used to adjust the flow rate, concentration, and pH of the raw pharmaceutical production wastewater to a stable and controllable state. Specifically, based on the influent flow rate signal fed back by the flow meter, a variable frequency pump is used to dynamically adjust the influent flow rate of the raw pharmaceutical production wastewater, so that the unstable raw pharmaceutical production wastewater is transformed into raw pharmaceutical production wastewater with a constant flow rate. Then, the raw pharmaceutical production wastewater with a constant flow rate is mixed throughout the tank through a stirring system to eliminate concentration stratification and obtain uniform mixed water. Next, a level monitoring and regulation buffer tank is used to buffer and store the uniform mixed water for a short period of time, eliminating instantaneous water volume fluctuations and outputting buffered mixed water. Finally, the pH self-adjustment system automatically adds acid and alkali solutions to the buffered mixed water under closed-loop control of online pH and conductivity sensor data, stabilizing the pH in the range of 7.0 to 8.0 and ensuring that the salinity conditions are not disrupted, thereby obtaining flow equilibrium water.

[0022] The physicochemical purification unit is used to aggregate and separate suspended particles and colloidal pollutants in the fluidized bed equilibrium water, achieving solid-liquid separation. Specifically, based on the real-time turbidity value of the fluidized bed equilibrium water collected by the online turbidity meter, the automatic flocculant dosing system adds PAC and PAM to the fluidized bed equilibrium water to form a premixed liquid containing primary flocs. Subsequently, the premixed liquid containing primary flocs is sequentially introduced into a high-speed stirring zone and a low-speed stirring zone. High-speed stirring promotes the formation of micro-flocculations, while low-speed stirring promotes the growth and stabilization of flocs, resulting in mature floc water. Finally, the mature floc water enters the inclined plate sedimentation tank, where solid-liquid separation is achieved through gravity sedimentation, yielding precipitated sludge and supernatant. The precipitated sludge is discharged into a sludge tank for centralized treatment, while the supernatant is used as effluent, resulting in low-suspension liquid phase water.

[0023] The biological hydrolysis pretreatment unit is used to perform anaerobic hydrolysis of recalcitrant macromolecular organic matter in low-suspension liquid water. Specifically, the low-suspension liquid water is introduced into an anaerobic reaction tank. The packing support structure in the anaerobic reaction tank provides an interface for microbial attachment and is inoculated with a complex salt-tolerant functional bacterial community, which combines with the low-suspension liquid water to form an initial bacterial attachment solution. Subsequently, the initial bacterial attachment solution is maintained at 30±2℃ by a temperature-controlled heater, and the dissolved oxygen in the anaerobic reaction tank is stabilized at 0.5-1.0 mg / L using a dissolved oxygen control device, the pH in the anaerobic reaction tank is controlled at 7.0-7.8 using a pH self-adjustment system, and the COD:N:P in the anaerobic reaction tank is approximately 100:5:1 using a nutrient salt dosing system. As a result, the complex salt-tolerant functional bacterial community secretes hydrolytic enzymes to lyse the macromolecular organic matter in the initial bacterial attachment solution, generating biodegradable small molecules, which is the intermediate hydrolysate. The intermediate hydrolysate undergoes parameter tuning for 10-30 minutes to obtain biochemically friendly water.

[0024] The core denitrification module consists of a denitrification unit, a nitrification unit, and a circulation control unit. It is used to sequentially convert biochemically friendly water into intermediate ammonia nitrogen-enriched water, nitrate-enriched water, and output low-nitrogen reaction water.

[0025] The denitrification unit is used for heterotrophic denitrification treatment of biochemically friendly water. Specifically, the biochemically friendly water is introduced into an anoxic reaction tank equipped with high specific surface area elastic packing. The high specific surface area elastic packing provides an attachment interface for denitrifying bacteria. Under the condition that the dissolved oxygen in the anoxic reaction tank is controlled at <0.5mg / L, the biochemically friendly water and the denitrifying bacteria in the anoxic reaction tank form an anoxic mixed solution. Subsequently, based on the real-time signals output by the online NO3⁻-N analyzer and the online COD analyzer, sodium acetate is added to the anoxic mixed solution as an electron donor through a carbon source quantitative addition mechanism, and Acinetobacter haemolyticus X4 strain is inoculated. Then, the anoxic mixed solution with added sodium acetate is intermittently stirred by the stirring system in the anoxic reaction tank to maintain uniform mixing, so that the nitrate in the anoxic mixed solution with added sodium acetate is continuously reduced to nitrogen gas and released, ultimately generating intermediate ammonia nitrogen-enriched water. The nitrification unit is used for aerobic biological oxidation treatment of intermediate ammonia nitrogen-enriched water. Specifically, the intermediate ammonia nitrogen-enriched water is introduced into a long-flow, multi-section aerobic reactor. The aerobic reactor is equipped with a nitrifying bacteria enhancement layer and uses a staged aeration system to supply oxygen in stages. The oxygen transfer efficiency is improved by a gas-liquid distribution optimization device. Under the condition that the dissolved oxygen is controlled at 1.5-2.5 mg / L, the ammonia nitrogen in the intermediate ammonia nitrogen-enriched water is gradually converted to nitrite and then to nitrate. After the reaction is completed, nitrate-enriched water is formed. The circulation control unit is used to implement diversion and reinjection control of nitrate-enriched water and achieve dynamic balance of influent nitrogen load. Specifically, through the return pump group, under the coordination of the feedback algorithm of the PLC controller and the flow ratio controller, a portion of the nitrate-enriched water is returned to the denitrification unit according to the calculated ratio, and the remaining portion is used as the effluent from the core denitrification module. The PLC controller automatically adjusts the return ratio based on the online NO3⁻-N concentration, flow rate and influent TN data to keep the denitrification carbon source matching and nitrification-denitrification coupling stable, ultimately forming low-nitrogen reaction water.

[0026] The deep finishing module consists of a membrane bioreactor unit, a post-denitrification unit, and an activated carbon polishing unit. It is used to sequentially convert low-nitrogen reaction water into deep clarified liquid, denitrified purified water, and finally obtain compliant discharge water.

[0027] The membrane bioreactor (MBR) unit is used for solid-liquid separation and residual nitrogen removal from low-nitrogen reaction water. Specifically, the low-nitrogen reaction water is introduced into the MBR tank, and dissolved oxygen is continuously supplied through a microporous aeration device at the bottom of the MBR tank to stabilize it at 2.0 mg / L, forming the initial mixed liquor in the membrane tank. Subsequently, an embedded PVDF hollow fiber membrane module is used to perform solid-liquid separation on the initial mixed liquor in the membrane tank, obtaining concentrated sludge and separated primary permeate. The concentrated sludge is returned to the MBR tank through a concentration maintenance mechanism to maintain the biological concentration. At the same time, a modified nitrification-denitrification synergistic bacteria community is inoculated in the MBR tank to remove residual nitrogen from the separated primary permeate, finally obtaining a deeply clarified liquid. The operating flux of the PVDF hollow fiber membrane module is automatically adjusted by an online monitoring system, and backwashing and chemical cleaning are performed according to a set cycle to ensure that the transmembrane pressure difference (TMP) of the PVDF hollow fiber membrane module is ≤0.25 MPa and the flux fluctuation is ≤10%.

[0028] The post-denitrification unit is used to remove residual nitrates from the deep clarified liquid. Specifically, the deep clarified liquid is introduced into an upflow anaerobic filter. An anaerobic packing system is arranged in the upflow anaerobic filter and filled with a porous inert carrier. At the same time, a slow-release carbon source carrier (polyhydroxybutyrate PHB) is added into the upflow anaerobic filter through the anaerobic packing system to form a slow-release carbon source bed. The upflow anaerobic filter is operated in a closed system without aeration. The carbon source in the slow-release carbon source bed consumes the dissolved oxygen in the upflow anaerobic filter to form a low-oxygen reducing environment with DO < 0.2 mg / L and ORP < -100 mV. Under this environment, the denitrifying bacteria in the upflow anaerobic filter reduce the residual nitrates in the deep clarified liquid to gaseous nitrogen and escape, resulting in denitrified purified water.

[0029] The activated carbon polishing unit is used for adsorption and purification of denitrified water. Specifically, the denitrified water flows from bottom to top through a high specific surface area activated carbon column bed at a flow rate of 5-10 m / h. The activated carbon in the high specific surface area activated carbon column bed achieves dechlorination and deodorization of the denitrified water through its porous surface, as well as adsorption of dissolved organic carbon (DOC), color and trace drug components in the denitrified water, ultimately forming compliant discharge water.

[0030] The operation support module consists of an online monitoring unit, an automatic dosing unit, a sludge management unit, and an energy efficiency optimization unit. It is used to collect and integrate water quality and operating parameters at each treatment location to form a system operation status set. Based on the system operation status set, it generates a quantitative reagent flow, a steady-state structure of sludge concentration, and a dynamic energy consumption feedback flow.

[0031] The online monitoring unit is used to collect key water quality and operating parameters in real time during the process of generating compliant effluent and form a system operating status set. Specifically, multiple types of online sensors are deployed at the inlet, outlet, core denitrification module, deep purification module outlet, and discharge outlet of the raw water pretreatment module. These online sensors include COD, NH4+-N, NO3--N, TN, DO, pH, salinity, flow rate, and temperature sensors. Each sensor collects data at a frequency of ≥1 time / minute and converts it into a standard signal by a data acquisition unit. The standard signal is then synchronously uploaded to the PLC main control system. The PLC main control system has a built-in threshold comparison, moving average, and rate of change judgment model to judge the instantaneous value, moving average, and rate of change of each parameter. When any parameter exceeds the preset upper or lower limit or the rate of change exceeds the threshold, the PLC main control system automatically generates a feedback command and outputs the system operating status set.

[0032] The automatic dosing unit is used to accurately and dynamically add chemicals according to the needs of each treatment location. Specifically, the PLC main control system collects various water quality deviations based on the system's operating status and controls the programmable quantitative pump group to retrieve denitrifying carbon source, pH adjusting alkali solution, and trace nutrients from the chemical storage and distribution system. It then adds the denitrifying carbon source, pH adjusting alkali solution, and trace nutrients according to the needs of each treatment location (denitrifying carbon source is added to the anoxic reaction tank, pH adjusting alkali solution is added to the homogenization tank, and nutrients are added to the facultative reaction tank, etc.). At the same time, the dosing amount and timing are corrected in real time through a closed-loop control algorithm, so that the dosing process can respond synchronously to load fluctuations caused by influent flow rate and pollutant concentration, forming a quantitative chemical flow.

[0033] The sludge management unit is used to manage the discharge and recirculation of excess sludge generated in the anoxic reactor, aerobic reactor, and membrane bioreactor. Specifically, SVI monitoring probes and MLSS online sensors are deployed in the recirculation channel of the anoxic reactor in the core denitrification module, at the end of the aerobic reactor, and in the sludge discharge area of ​​the membrane bioreactor in the deep finishing module. The PLC main control system dynamically calculates the sludge load and target sludge age based on the data monitored by the SVI monitoring probes and MLSS online sensors, and issues sludge discharge and recirculation commands based on the sludge load and target sludge age. Then, according to the sludge discharge and recirculation commands, excess sludge is quantitatively discharged through the sludge discharge pump group, and part of the excess sludge is returned to the anoxic reactor by the sludge recirculation device. The remaining excess sludge is sent to the sludge thickening tank for dewatering and discharge, thereby effectively avoiding the problems of sludge bulking and microbial imbalance in the anoxic reactor, aerobic reactor, and membrane bioreactor, and finally forming a stable sludge concentration structure.

[0034] The energy efficiency optimization unit is used to dynamically sense and adjust the energy consumption of key energy-consuming equipment. Specifically, an energy consumption monitoring system is configured on key energy-consuming equipment to collect power data. Key energy-consuming equipment includes blowers in the nitrification unit, reflux pumps in the circulation control unit, stirring systems in the homogenization and denitrification units, and membrane suction pumps in the membrane bioreactor unit. The collected power data is then sent to the energy consumption control system in the PLC main control system. The energy consumption control system optimizes the equipment start-up and shutdown sequence, operating cycle, and variable frequency output frequency based on the treatment capacity, operating period, and water quality compliance requirements. It generates control commands to minimize power and feeds them back to the corresponding frequency converters of each device for execution, realizing peak-valley load adjustment and minimizing output power, thus constructing a dynamic energy consumption feedback flow.

[0035] It should be noted that the entire pharmaceutical production wastewater denitrification treatment system follows a structural path of "raw water pretreatment module - core denitrification module - deep refining module - operation support module," constructing two mutually supportive closed-loop links: the material treatment process and the operation parameter sensing / control process. In the material treatment process, the treatment results of the previous module serve as the direct treatment object of the next module, and the target water form produced by the previous module also serves as the boundary input for the operation conditions of the next module. The operation parameter sensing / control process involves the operation support module collecting parameters in real time at each key node, outputting control commands, and feeding them back to the corresponding execution units, achieving closed-loop regulation of "sensing-decision-execution-re-sensing," ensuring that the system as a whole completes the graded reduction of water quality and ultimately achieves the standard discharge.

[0036] The system operation begins in the raw water pretreatment module. External pharmaceutical production wastewater first enters the homogenization and conditioning unit, where it is balanced by flow rate, stirred and mixed, and pH self-adjusted to obtain fluid equilibrium water. Subsequently, in the physicochemical purification unit, it undergoes flocculation, stirring, and inclined plate sedimentation to obtain low-suspension liquid phase water. Finally, in the biological hydrolysis pretreatment unit, the low-suspension liquid phase water is hydrolyzed and decomposed by a complex salt-tolerant functional bacterial community under facultative anaerobic conditions to form biochemically friendly water with controllability and matching with subsequent denitrification conditions, laying the foundation for subsequent nitrogen bioconversion.

[0037] Biochemically friendly water enters the core denitrification module. Each unit operates continuously in the sequence of "anoxic → aerobic → reflux". In the anoxic environment, the denitrification unit is dominated by denitrifying bacteria such as Acinetobacter haemolyticus X4, which reduce nitrate nitrogen to nitrogen gas and produce intermediate ammonia nitrogen-enriched water. Under the action of staged aeration and nitrifying bacteria enhancement layer, the nitrification unit oxidizes the ammonia nitrogen in the intermediate ammonia nitrogen-enriched water into nitrite and nitrate in sequence, resulting in nitrate-enriched water. The circulation control unit, through proportional reflux and PLC logic regulation, reinjects part of the nitrate-enriched water back into the denitrification unit. The module finally outputs low-nitrogen reaction water, completing the directional removal of nitrogen from soluble form to gaseous form and forming a stable process rhythm.

[0038] The low-nitrogen reaction water enters the deep refining module. The membrane bioreactor unit uses a PVDF hollow fiber membrane to achieve solid-liquid separation and uses a modified nitrification-denitrification synergistic bacterial community to remove residual nitrogen, finally obtaining a deeply clarified liquid. The post-denitrification unit completes terminal denitrification with the support of a slow-release carbon source bed to obtain denitrified purified water. The activated carbon polishing unit performs adsorption purification and sensory improvement on the denitrified purified water, finally forming compliant discharge water.

[0039] The operation support module runs through the entire material treatment path, providing support for data feedback, reagent dosing, sludge control, and energy consumption optimization. The online monitoring unit deploys multiple types of online sensors at the inlet and outlet of the raw water pretreatment module, the outlet of the core denitrification module, the outlet of the deep finishing module, and the discharge outlet. These sensors collect key parameters such as COD, NH4⁺-N, NO3⁻-N, TN, DO, and pH, and output the system operation status set through the PLC main control system. The automatic dosing unit calculates the dosage and timing based on the water quality deviation in the system operation status set, outputting a quantitative reagent flow. The sludge management unit schedules sludge discharge and recirculation based on SVI and MLSS signals to maintain sludge age and microbial balance, forming a steady-state sludge concentration structure. The energy efficiency optimization unit dynamically senses and adjusts the energy consumption of key energy-consuming equipment, constructing a dynamic energy consumption feedback flow.

[0040] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations will be apparent to those skilled in the art. Any modifications, equivalent substitutions, or improvements 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 denitrification treatment system for pharmaceutical production wastewater, characterized in that, Includes the following modules: The raw water pretreatment module consists of a homogenization adjustment unit, a physicochemical purification unit, and a biological hydrolysis pretreatment unit. It is used to sequentially treat raw pharmaceutical production wastewater into flow-equilibrium water, low-suspended liquid phase water, and finally obtain biochemically friendly water. The core denitrification module consists of a denitrification unit, a nitrification unit, and a circulation control unit. It is used to sequentially convert the biochemically friendly water into intermediate ammonia nitrogen-enriched water and nitrate-enriched water and output low-nitrogen reaction water. The deep purification module consists of a membrane bioreactor unit, a post-denitrification unit, and an activated carbon polishing unit. It is used to sequentially convert the low-nitrogen reaction water into a deep clarified liquid, denitrified purified water, and finally obtain compliant discharge water. The operation support module consists of an online monitoring unit, an automatic dosing unit, a sludge management unit, and an energy efficiency optimization unit. It is used to collect and integrate water quality and operating parameters at each treatment location to form a system operation status set. Based on the system operation status set, it generates a quantitative reagent flow, a steady-state structure of sludge concentration, and a dynamic energy consumption feedback flow.

2. The denitrification treatment system for pharmaceutical production wastewater according to claim 1, characterized in that: The homogenization and conditioning unit, through the coordinated operation of its internal flow meter, variable frequency pump, stirring system, liquid level monitoring and storage buffer tank, and pH self-adjustment system, treats the original pharmaceutical production wastewater and obtains fluid equilibrium water. In the physicochemical purification unit, based on the real-time turbidity value of the flow equilibrium water collected by the online turbidity meter, the flocculant automatic dosing system adds PAC and PAM to the flow equilibrium water to form a premixed liquid containing primary flocs. Subsequently, the premixed liquid containing primary flocs is sequentially introduced into the high-speed stirring zone and the low-speed stirring zone to obtain mature floc water. Finally, the mature floc water enters the inclined plate sedimentation tank to obtain settled sludge and supernatant. The settled sludge is discharged into the sludge tank for centralized treatment, and the supernatant is used as effluent to obtain low suspended liquid phase water. The biological hydrolysis pretreatment unit, through the synergistic cooperation of its composite salt-tolerant functional bacteria, temperature-controlled heater, dissolved oxygen control device, pH self-adjustment system, and nutrient salt dosing system, treats low-suspension liquid phase water to obtain biochemically friendly water.

3. The denitrification treatment system for pharmaceutical production wastewater according to claim 2, characterized in that: The specific operation of the homogenization and conditioning unit in treating the raw pharmaceutical production wastewater is as follows: Based on the influent flow signal fed back by the flow meter, a variable frequency pump is used to dynamically adjust the influent flow of the raw pharmaceutical production wastewater, transforming the unstable raw pharmaceutical production wastewater into raw pharmaceutical production wastewater with a constant flow. Subsequently, the raw pharmaceutical production wastewater with a constant flow is mixed throughout the tank through a stirring system to obtain homogeneous mixed water. Next, a level monitoring and regulation buffer tank is used to buffer and store the homogeneous mixed water for a short period of time, and output buffered mixed water. Finally, an acid or alkali solution is automatically added to the buffered mixed water under closed-loop control of online pH and conductivity sensor data through a pH self-adjustment system, thereby obtaining flow equilibrium water. The specific operations of the biological hydrolysis pretreatment unit for treating low-suspension liquid phase water are as follows: Low-suspension water is introduced into an anoxic reactor. The packing support structure in the anoxic reactor provides an interface for microbial attachment and inoculates a complex salt-tolerant functional bacterial community. This community combines with the low-suspension water to form an initial bacterial attachment solution. Subsequently, the initial bacterial attachment solution is maintained at 30±2℃ by a temperature-controlled heater. Through the coordinated regulation of the dissolved oxygen control device, pH self-adjustment system, and nutrient dosing system in the anoxic reactor, the complex salt-tolerant functional bacterial community secretes hydrolytic enzymes to lyse the large organic molecules in the initial bacterial attachment solution, generating biodegradable small molecules, thus obtaining an intermediate hydrolysate. The intermediate hydrolysate undergoes parameter tuning within 10~30 minutes, resulting in biochemically friendly water.

4. The denitrification treatment system for pharmaceutical production wastewater according to claim 1, characterized in that: The denitrification unit introduces bio-friendly water into an anoxic reaction tank equipped with high specific surface area elastic packing. The high specific surface area elastic packing provides an attachment interface for denitrifying bacteria. Under the condition that the dissolved oxygen in the anoxic reaction tank is controlled at <0.5mg / L, the bio-friendly water and the denitrifying bacteria in the anoxic reaction tank form an anoxic mixed solution. Subsequently, based on the real-time signals output by the online NO3⁻-N analyzer and the online COD analyzer, sodium acetate is added to the anoxic mixed solution as an electron donor through a carbon source quantitative addition mechanism, and Acinetobacter haemolyticus X4 strain is inoculated. The anoxic mixed solution with added sodium acetate is intermittently stirred by the stirring system in the anoxic reaction tank, so that the nitrate in the anoxic mixed solution with added sodium acetate is continuously reduced to nitrogen gas and released, ultimately generating intermediate ammonia nitrogen-enriched water. The nitrification unit introduces intermediate ammonia nitrogen-enriched water into a long-flow, multi-section aerobic reactor. The aerobic reactor is equipped with a nitrifying bacteria enhancement layer and uses a staged aeration system to supply oxygen in stages. Under the condition that the dissolved oxygen is controlled at 1.5-2.5 mg / L, the ammonia nitrogen in the intermediate ammonia nitrogen-enriched water is gradually converted into nitrite and then into nitrate. After the reaction is completed, nitrate-enriched water is formed. The circulation control unit, through the feedback algorithm of the PLC controller and the flow ratio controller, sends a portion of the nitrate-enriched water back to the denitrification unit according to the calculated ratio via the return pump group, and uses the remainder as the effluent from the core denitrification module; the PLC controller automatically adjusts the return ratio based on the online NO3⁻-N concentration, flow rate and influent TN data, so that the denitrification carbon source matching and nitrification-denitrification coupling in the denitrification unit remain stable, ultimately forming low-nitrogen reaction water.

5. The denitrification treatment system for pharmaceutical production wastewater according to claim 1, characterized in that: The membrane bioreactor unit, through the synergistic cooperation of its embedded PVDF hollow fiber membrane module, concentration maintenance mechanism and modified nitrification-denitrification synergistic bacteria community, treats low-nitrogen reaction water and obtains a deeply clarified liquid. The post-denitrification unit, through the synergistic cooperation of its internal anaerobic packing system and slow-release carbon source carrier, treats the deeply clarified liquid and obtains denitrified purified water. The activated carbon polishing unit allows denitrified water to flow from bottom to top through a high specific surface area activated carbon column bed at a flow rate of 5-10 m / h. The activated carbon in the high specific surface area activated carbon column bed achieves dechlorination and deodorization of the denitrified water through its porous surface, as well as adsorption of dissolved organic carbon, color and trace drug components in the denitrified water, ultimately forming compliant discharge water.

6. The denitrification treatment system for pharmaceutical production wastewater according to claim 5, characterized in that: The specific operation of the membrane bioreactor unit in treating low-nitrogen reaction water is as follows: Low-NOx reaction water is introduced into the membrane bioreactor (MBR), and dissolved oxygen is continuously supplied through a microporous aeration device at the bottom of the MBR to stabilize it at 2.0 mg / L, forming the initial mixed liquor in the membrane tank. Subsequently, the initial mixed liquor is subjected to solid-liquid separation using an embedded PVDF hollow fiber membrane module in the MBR, yielding concentrated sludge and primary permeate. The concentrated sludge is returned to the MBR via a concentration maintenance mechanism. Simultaneously, a modified nitrification-denitrification synergistic bacteria community is inoculated into the MBR to remove residual nitrogen from the primary permeate, ultimately obtaining a deeply clarified liquid. The operating flux of the embedded PVDF hollow fiber membrane module is automatically adjusted by an online monitoring system, and backwashing and chemical cleaning are performed according to a set cycle. The specific operation of the post-denitrification unit for treating the deep clarified liquid is as follows: The deeply clarified liquid is introduced into an upflow anaerobic filter. An anaerobic packing system is arranged in the upflow anaerobic filter and filled with a porous inert carrier. At the same time, a slow-release carbon source carrier is added into the upflow anaerobic filter through the anaerobic packing system to form a slow-release carbon source bed. The upflow anaerobic filter is operated in a closed system without aeration. The carbon source in the slow-release carbon source bed consumes the dissolved oxygen in the upflow anaerobic filter to form a low-oxygen reducing environment. Under this environment, the denitrifying bacteria in the upflow anaerobic filter reduce the residual nitrate in the deeply clarified liquid to gaseous nitrogen and escape, thus obtaining denitrified purified water.

7. The denitrification treatment system for pharmaceutical production wastewater according to claim 1, characterized in that: The online monitoring unit deploys various types of online sensors at the inlet and outlet of the raw water pretreatment module, the outlet of the core denitrification module, and the outlet and discharge port of the deep finishing module. The real-time data collected by the various types of online sensors is converted into standard signals by a data acquisition unit and uploaded to the PLC main control system. The PLC main control system uses a threshold comparison, moving average, and rate of change determination model to generate feedback instructions and output the system operation status set. The automatic dosing unit, controlled by a PLC main control system, gathers various water quality deviations based on the system's operating status and controls a programmable quantitative pump to retrieve denitrifying carbon source, pH-adjusting alkaline solution, and trace nutrients from the reagent storage and preparation system. It then adds these substances according to the needs of each treatment location. Simultaneously, a closed-loop control algorithm corrects the dosage and timing in real time, ensuring the dosing process responds synchronously to load fluctuations caused by influent flow rate and pollutant concentration, thus forming a quantitative reagent flow. The sludge management unit is equipped with SVI monitoring probes and MLSS online sensors in the return channel of the anoxic reaction tank of the core denitrification module, the end of the aerobic reaction tank, and the sludge discharge area of ​​the membrane bioreactor of the deep finishing module. The PLC main control system dynamically calculates the sludge load and target sludge age based on the data monitored by the SVI monitoring probes and MLSS online sensors, and issues sludge discharge and return commands based on the sludge load and target sludge age. Then, according to the sludge discharge and return commands, excess sludge is quantitatively discharged through the sludge discharge pump group, and part of the excess sludge is returned to the anoxic reaction tank by the sludge return device. The remaining excess sludge is sent to the sludge thickening tank for dewatering and discharge, forming a stable sludge concentration structure. The energy efficiency optimization unit is equipped with an energy consumption monitoring system on key energy-consuming equipment. The system collects power data and then sends the collected power data to the energy consumption control system in the PLC main control system. The energy consumption control system then generates control commands and feeds them back to the frequency converters corresponding to each key energy-consuming equipment for execution, thus constructing a dynamic energy consumption feedback flow.

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