A process for cyclic water supply with staged depth purification

Abstract

The present application relates to the field of water pollution control and treatment technology, and discloses a hierarchical deep purification process for circulating water supply, comprising: collecting the differential pressure of flow and the fluid conductivity of the two ends of each level of purification area arranged in sequence on line and calculating the process carrying load index; when the index exceeds the preset critical value, the spatial flow direction topology of the flow stream is adjusted, part of the flow entering the first level of purification area is diverted to the inlet of the second level of purification area, the local flow rate is increased to counter the concentration difference polarization boundary layer, the aeration power density of the first level of purification area is simultaneously increased and the dosage ratio of the reagent is decreased, the present application uses the elastic diversion of the flow channel topology, the fluid shear force in situ peels off the organic pollutants on the surface of the filler, effectively alleviates the scaling and blocking of the membrane separation area, and realizes low reagent consumption operation while ensuring the purification efficiency.

Description

Technical Field

[0001] This invention relates to a graded deep purification process for circulating water supply, belonging to the field of water pollution control and treatment technology. Background Technology

[0002] Currently, in industrial circulating water purification systems, the mainstream process uses rigid multi-stage series reaction synergistic separation membrane modules to remove recalcitrant macromolecular organic matter and slightly soluble inorganic hardness mineral ions from the fluid. The interphase mass transfer efficiency of the catalytic medium particles and the filter bed interface within these multi-stage purification channels is highly dependent on the steady-state distribution of the water quality components in the flowing material, and also on the spatial isotropic nature of the flow shear stress. However, when process wastewater discharge causes transient high-load impacts such as macromolecular enrichment and metal ion supersaturation in the water body, the static mass transfer boundary fails locally due to the lack of dynamic channel reconstruction methods. The aggregated organic micelles undergo irreversible physical trapping and layering deep within the pores of the pre-filter medium under the combined effects of flow rate and concentration gradient, causing large-area passivation and blockage of catalytic active sites. At the same time, a concentration polarization boundary layer is induced at the phase interface of the subsequent filtration stage, and the heterogeneous pinning deposition and scaling behavior of inorganic salt crystal nuclei is triggered due to uneven flow rate distribution.

[0003] Rigid hardware configurations are limited in their ability to cope with complex high-load shocks, and the control methods also have shortcomings. For example, Chinese invention patent CN204298151U discloses an alternating magnetic field circulating water treatment scale inhibition device. This device uses a single-phase asynchronous motor to drive the permanent magnet assembly on an aluminum alloy disc to mechanically rotate, creating a constant pulse frequency alternating magnetic field outside the circulating water pipeline to inhibit inorganic salt scaling. This technology relies on a relatively stable material composition and an environment without high concentrations of recalcitrant large-molecule organic matter. In actual process discharges that trigger transient complex high-load shocks, it lacks a feedforward sensing response mechanism based on dynamic flow resistance and state of charge changes. The control method is not compatible with the actual operating conditions. When faced with coupled fouling caused by organic micelle trapping and inorganic salt heterogeneous pinning deposition, it cannot offset the loss of scale inhibition stability due to the concentration polarization boundary layer. Conventional strategies to deal with such impacts include increasing the dosage of reagents or expanding the volume of the conditioning tank. These methods not only introduce the problem of excessive residual reagents and increase the reverse flow resistance of the separation membrane module, but also are constrained by the rigidity of the narrow plant space due to the expansion of the floor space.

[0004] Therefore, the technical problem to be solved by this invention is how to overcome the limitation of interphase mass transfer resistance imbalance in fixed multi-stage series flow channel configuration when dealing with transient high load impact, provide a method for adaptively changing the flow channel topology according to the overflow shear variation within a compact physical configuration, and coordinate with the asymmetric step reshaping of the local mechanical shear energy field power density to eliminate the false step caused by polarization deposition at the mass transfer interface and the backlog of multiphase bubble turbulence. Summary of the Invention

[0005] To address the problems in the background art, the technical solution of the present invention is as follows: A staged deep purification process for circulating water supply, comprising the following steps:

[0006] Step S1: Guide the wastewater through the first-stage purification zone, the second-stage purification zone, and the third-stage purification zone in sequence, and fill each purification zone with porous catalytic material. Collect the differential pressure and fluid conductivity at the inlet and outlet of each purification zone online to construct a shear resistance vector that includes cross-boundary pressure drop variables and conductivity migration variables.

[0007] Step S2: Calculate the process load index based on the differential pressure, fluid conductivity, and transient volumetric flow rate of the main inlet pipe. When the process load index of the first-stage purification zone exceeds the preset safety threshold of 1.35, adjust the spatial flow topology of the flow stream. Divert 65% of the volumetric flow rate that originally entered the first-stage purification zone to the inlet of the second-stage purification zone, so that the local axial velocity inside the second-stage purification zone is maintained between 1.8 m / s and 2.4 m / s, and the remaining 35% of the volumetric flow rate is maintained in the first-stage purification zone to cope with sudden load shocks.

[0008] In step S3, while diverting the flow, the aeration power density at the bottom of the first-stage purification zone is increased from 45W / m³ to a range of 85W / m³ to 120W / m³. Organic pollutants on the surface of the porous catalyst are removed by the shear force of the fluid. At the same time, the molar ratio of the matching reagent added to the first-stage purification zone is reduced by 15%. The purified effluent is then converged at the end of the channel and introduced into the subsequent low-pressure reverse osmosis separation zone.

[0009] Preferably, in step S2, the physical degassing zone connected in parallel to the main flow channel is opened, the differential pressure variance of the total system pressure drop within 5 seconds is periodically measured, and when the differential pressure variance is greater than 0.02 MPa, the fluid flow path is switched, and the material flow rate is distributed between the main flow channel and the physical degassing zone, so that the bubbles in the fluid break under the combined action of the fluid cohesive pressure and the wall fluid shear force, thereby eliminating the bubble backlog interference in the multiphase fluid when the material flow rate is non-uniformly mismatched.

[0010] Preferably, the graded deep purification process maintains a unidirectional series flow state under normal operating conditions, and keeps the flow velocity within each zone stable within a preset range of 0.45m / s.

[0011] Preferably, the following refined steps are included: when the differential pressure at the inlet of the first-stage purification zone jumps from 0.09 MPa to 0.34 MPa within 12 seconds, the spatial flow topology of the flow stream is changed, switching the unidirectional series state to a parallel split state or a partial reflux state, in order to reduce the load on the single-stage zone and alleviate the crystal accumulation caused by the prolonged residence time due to the split.

[0012] Preferably, in step S3, based on the differential pressure at the inlet of the first-stage purification zone and the fluid conductivity, an alternating magnetic field is applied inside the first-stage purification zone, and the duration of the alternating magnetic field is controlled within the range of 30 min to 60 min, so that calcium and magnesium ions in the wastewater medium crystallize into suspended crystal nuclei inside the fluid, thereby blocking the adhesion and scaling of hardness ions on the outer surface of the porous catalyst material.

[0013] Preferably, a low-pressure reverse osmosis separation zone is set at the end of the flow channel in the staged deep purification process. The staged deep purification process also includes the following steps: Step S4, monitor the transmembrane pressure difference in the low-pressure reverse osmosis separation zone, and when the transmembrane pressure difference slides from 0.14MPa to 0.16MPa, start the online chemical cleaning program to stabilize the total organic carbon content of the purified water in the low-pressure reverse osmosis separation zone below 1.43mg / L, and maintain the removal rate of high-valence anions at no less than 96.8%.

[0014] Preferably, in step S4, during the operation of the online chemical cleaning program, a composite mode of alternating intermittent low-concentration acid washing and high-frequency hydraulic rinsing is adopted, and the circulation flow rate of the cleaning solution is controlled to be 0.6 m / s to 0.8 m / s, reducing the system's energy consumption per ton of water purification to no more than 0.39 kWh.

[0015] Preferably, before monitoring in step S1, the following preparatory steps are included: coarse filtration and suspended solids interception of the fluid in the circulating water supply system, controlling the initial turbidity of the wastewater medium entering the graded deep purification process to be lower than 5 NTU, and controlling the initial water temperature to be maintained within the range of 20°C to 35°C.

[0016] Preferably, in step S2, the porous catalyst material is a porous ceramic particle loaded with transition metal oxides, and its micropore size is distributed between 10 nm and 50 nm. The fluid shear force generated after the aeration power density is increased removes organic pollutants on the surface of the porous catalyst material, so as to maintain the exposure of the active sites of the porous catalyst material.

[0017] Compared with the prior art, the beneficial effects of the present invention are:

[0018] 1. In the staged deep purification process of circulating water supply, by connecting a multi-way flow direction switching distribution valve assembly in parallel in the pipeline of the purification zone, when the shear resistance vector constructed by the pressure sensing assembly and the state of charge sensor undergoes a state transition, the feedforward distribution operator dynamically adjusts the volumetric flow rate of the material in each stage, and directly diverts some of the high-load fluid across stages to the inlet of the subsequent purification zone, so that the local axial velocity inside the subsequent stage increases. The shear force of the liquid flow directly flushes the concentration polarization boundary layer at the microscopic interface of the medium pores, avoiding the catalytic site blockage caused by the overload impact of the upstream stage alone. This enables the material flux of each purification space to be non-uniformly mismatched in time and flow path.

[0019] 2. When the pre-reactor is under high load, the main control unit adjusts the driving frequency of the gas-liquid non-uniform contact device at the bottom of the purification zone to increase the power density of the local shear energy field. The gas-liquid disturbance generates bubbles that break down the organic micelles enriched in the pores of the porous catalytic purification medium. At the same time, the auxiliary dosing molar ratio is reduced to increase the collision probability between reactant molecules through mechanical shearing, thereby compensating for the local lack of chemical reactant concentration. While maintaining the deep degradation efficiency, the residual load of the reaction agent is controlled, so that the pre-reactor is in a self-balancing operation state with low drug consumption and high shear cleaning, thus slowing down the organic fouling process on the surface of the separation membrane module.

[0020] 3. When the dissolved solids index at the inlet crosses the edge baseline, the electromagnetic polarization energy field generator mounted on the pipeline receives the trigger command and outputs a high-frequency alternating magnetic field, which directly acts on the flowing wastewater medium to regulate the spatial hydration coordination state of calcium and magnesium ions, reduce the microscopic nucleation activation energy of inorganic salts in the deep pores of the porous catalytic purification medium, and cause heterogeneous supersaturated crystals to spontaneously transform into loosely structured suspended crystal nuclei inside the fluid body. This blocks the heterogeneous adhesion and pinning scaling behavior of hardness ions on the outer surface of the porous medium, alleviates the risk of thermodynamic crystallization caused by the non-uniform extension of local residence time due to diversion scheduling, and maintains the stability of the staged flow section. Attached Figure Description

[0021] Figure 1 This is a flow chart of the load diversion and purification process of the present invention;

[0022] Figure 2 This is a diagram of the multi-zone graded purification process of the present invention.

[0023] The objectives, features, and advantages of this invention will be further explained in conjunction with the embodiments and with reference to the accompanying drawings. Detailed Implementation

[0024] The technical solutions of the embodiments of this application will be clearly described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of this application are within the scope of protection of this application.

[0025] A staged deep purification process for circulating water supply includes the following steps:

[0026] Step S1: Guide the wastewater through the first-stage purification zone, the second-stage purification zone, and the third-stage purification zone in sequence, and fill each purification zone with porous catalytic material. Collect the differential pressure and fluid conductivity at the inlet and outlet of each purification zone online to construct a shear resistance vector that includes cross-boundary pressure drop variables and conductivity migration variables.

[0027] Step S2: Calculate the process load index based on the differential pressure, fluid conductivity, and transient volumetric flow rate of the main inlet pipe. When the process load index of the first-stage purification zone exceeds the preset safety threshold of 1.35, adjust the spatial flow topology of the flow stream. Divert 65% of the volumetric flow rate that originally entered the first-stage purification zone to the inlet of the second-stage purification zone, so that the local axial velocity inside the second-stage purification zone is maintained between 1.8 m / s and 2.4 m / s, and the remaining 35% of the volumetric flow rate is maintained in the first-stage purification zone to cope with sudden load shocks.

[0028] In step S3, while diverting the flow, the aeration power density at the bottom of the first-stage purification zone is increased from 45W / m³ to a range of 85W / m³ to 120W / m³. Organic pollutants on the surface of the porous catalyst are removed by the shear force of the fluid. At the same time, the molar ratio of the matching reagent added to the first-stage purification zone is reduced by 15%. The purified effluent is then converged at the end of the channel and introduced into the subsequent low-pressure reverse osmosis separation zone.

[0029] Preferably, in step S2, the physical degassing zone connected in parallel to the main flow channel is opened, the differential pressure variance of the total system pressure drop within 5 seconds is periodically measured, and when the differential pressure variance is greater than 0.02 MPa, the fluid flow path is switched, and the material flow rate is distributed between the main flow channel and the physical degassing zone, so that the bubbles in the fluid break under the combined action of the fluid cohesive pressure and the wall fluid shear force, thereby eliminating the bubble backlog interference in the multiphase fluid when the material flow rate is non-uniformly mismatched.

[0030] Preferably, the graded deep purification process maintains a unidirectional series flow state under normal operating conditions, and keeps the flow velocity within each zone stable within a preset range of 0.45m / s.

[0031] Preferably, the following refined steps are included: when the differential pressure at the inlet of the first-stage purification zone jumps from 0.09 MPa to 0.34 MPa within 12 seconds, the spatial flow topology of the flow stream is changed, switching the unidirectional series state to a parallel split state or a partial reflux state, in order to reduce the load on the single-stage zone and alleviate the crystal accumulation caused by the prolonged residence time due to the split.

[0032] Preferably, in step S3, based on the differential pressure at the inlet of the first-stage purification zone and the fluid conductivity, an alternating magnetic field is applied inside the first-stage purification zone, and the duration of the alternating magnetic field is controlled within the range of 30 min to 60 min, so that calcium and magnesium ions in the wastewater medium crystallize into suspended crystal nuclei inside the fluid, thereby blocking the adhesion and scaling of hardness ions on the outer surface of the porous catalyst material.

[0033] Preferably, a low-pressure reverse osmosis separation zone is set at the end of the flow channel in the staged deep purification process. The staged deep purification process also includes the following steps: Step S4, monitor the transmembrane pressure difference in the low-pressure reverse osmosis separation zone, and when the transmembrane pressure difference slides from 0.14MPa to 0.16MPa, start the online chemical cleaning program to stabilize the total organic carbon content of the purified water in the low-pressure reverse osmosis separation zone below 1.43mg / L, and maintain the removal rate of high-valence anions at no less than 96.8%.

[0034] Preferably, in step S4, during the operation of the online chemical cleaning program, a composite mode of alternating intermittent low-concentration acid washing and high-frequency hydraulic rinsing is adopted, and the circulation flow rate of the cleaning solution is controlled to be 0.6 m / s to 0.8 m / s, reducing the system's energy consumption per ton of water purification to no more than 0.39 kWh.

[0035] Preferably, before monitoring in step S1, the following preparatory steps are included: coarse filtration and suspended solids interception of the fluid in the circulating water supply system, controlling the initial turbidity of the wastewater medium entering the graded deep purification process to be lower than 5 NTU, and controlling the initial water temperature to be maintained within the range of 20°C to 35°C.

[0036] Preferably, in step S2, the porous catalyst material is a porous ceramic particle loaded with transition metal oxides, and its micropore size is distributed between 10 nm and 50 nm. The fluid shear force generated after the aeration power density is increased removes organic pollutants on the surface of the porous catalyst material, so as to maintain the exposure of the active sites of the porous catalyst material.

[0037] Example 1: During the sewage discharge cycle of a continuously operating circulating water supply system, large-molecule recalcitrant organic matter and high-salt inorganic components exhibit nonlinear, sudden, high-frequency, and violent fluctuations. When transient, high-load aggregates rush into the purification channel, the catalytic sites at the phase interface of the first-stage purification zone face the risk of rapid adsorption and blockage. This causes an unexpected step change in local boundary layer mass transfer resistance and cross-boundary pressure drop. If conventional control methods with rigid series structures are used, high-concentration organic loads will directly penetrate into the surface of the subsequent terminal separation membrane module. Under the effect of concentration polarization, the interface of macromolecular gel and supersaturated inorganic hardness salt crystals will be cross-coupled, thereby assembling a dense and irreversible compacted gel fouling layer on the surface of the low-pressure reverse osmosis membrane unit, causing a decrease in the mass transfer flux of the entire process.

[0038] Pressure sensing components and state-of-charge sensors are installed at the leading and trailing edges of the first, second, and third purification zones to collect the fluid differential pressure and fluid conductivity at both ends of each purification zone online. The main control unit then adjusts the cross-boundary pressure drop variable... With conductivity migration variables and the transient volumetric flow rate of the main inlet pipe Calculate the process transport load index The specific numerical calculation method is entirely executed by the processor's internal logic gates in discrete digital form. The specific calculation path is as follows: the discrete sampled values ​​of the current cycle's cross-boundary pressure drop variable and the discrete sampled values ​​of the conductivity migration variable are multiplied in the multiplication register to obtain an intermediate product scalar representing the combined resistance characteristics. Then, the main control unit calls a divider to divide this intermediate product scalar by the currently collected transient volumetric flow rate of the main inlet pipeline. To completely eliminate the specific residual dimensional faults generated by the composite calculation of pressure drop variables at the 0.001 MPa level, conductivity migration variables at the 1.0 μS / cm level, and volumetric flow rates at the 1 m³ / h level, the processor automatically introduces a standardized normalization conversion constant for product correction after the division operation. This conversion constant is fixed at 1, thereby completely eliminating the composite dimensions and mapping them to uniformly calibrated pure dimensionless values. This gives the final output process load index a definite mathematical boundary and a unified comparison benchmark, allowing direct comparison and judgment with pure scalar values. For process transport load indicators, The pressure difference before and after each purification zone. This refers to ion mobility. The transient volumetric flow rate of the main inlet pipe, indicated by the superscript. Subscripts indicate the regions before and after each purification step. Indicates ion migration, subscript In the inlet main pipeline calculation, the shear resistance vector is constructed as a two-dimensional dynamic feature register array in the hardware cache of the main control unit. This data object is not an abstract concept, but a multi-dimensional data feature vector directly constructed by combining a first numerical dimension component containing the cross-boundary pressure drop variable and a second numerical dimension component containing the conductivity migration variable. Its internal operating mechanism is as follows: the control chip periodically reads the discrete sampled values ​​of the above two independent dimensions and stores them sequentially into two disparate addressing units of a dedicated multiplication register. By performing the coordinate space inner product projection operation of the two-axis data, the two physical components with different dimensions are multiplied together, thereby realizing the transformation of the multi-dimensional feature vector into a single dimensionless standard at the algorithm level. The dimensionality reduction and flattening mapping of quantitative attributes, serving as the multi-data input item for the control algorithm within the main control unit, includes a first component reflecting the cross-boundary pressure drop dimension, which reflects the changes in the system's physical flow resistance, and a second component reflecting the conductivity migration dimension, which reflects the degree of ion enrichment polarization within the fluid. The control chip built into the main control unit periodically reads the discrete sampled values ​​of these two components and algebraically multiplies the values ​​of the first and second components to achieve dimensionality reduction mapping of multi-dimensional feature vectors to a single scalar attribute. The product obtained after multiplication is then divided by the currently collected transient volumetric flow rate value of the main inlet pipeline, allowing online calculation of the process load index characterizing the current overall operational pressure of the system. When the process load index of the first-stage purification zone... When the preset safety threshold of 1.35 is exceeded, the programmable central processing unit inside the main control unit immediately interrupts the conventional unidirectional serial main program loop and instead outputs a high-frequency pulse width modulation current signal with a duty cycle ranging from 45% to 75% to the electric actuator of the electric multi-way diversion regulating valve connected in parallel to the inlet pipeline of the first-stage purification zone. This drives the internal valve core of the electric multi-way diversion regulating valve to produce a precise axial linear displacement, thereby physically changing the hydraulic configuration and fluid flow distribution boundary of the pipeline system. This achieves adaptive elastic switching and topological phase reorganization of the flow path of the overflow material, thus redirecting the untreated material that originally entered the first-stage purification zone. 65% of the fluid volumetric flow rate is directly diverted to the pre-inlet of the second-stage purification zone, controlling the local axial flow velocity within the second-stage purification zone to be between 1.8 m / s and 2.4 m / s. Meanwhile, the remaining 35% of the volumetric flow rate is maintained within the first-stage purification zone to cope with sudden load shocks. The engineering basis for selecting the preset safety threshold value of 1.35 is that when this index is below 1.35, it indicates that the gel layer on the surface of the porous catalyst material has not yet formed a dense flow-blocking structure. If the switching action is triggered too early, it will cause the local axial flow velocity in the first-stage reactor to be too low, resulting in a mass transfer dead zone, which will prevent the effective degradation of macromolecular organic matter due to insufficient contact time.

[0039] When this index exceeds 1.35, it indicates that the adsorption sites on the surface of the porous catalytic material are nearly saturated, and the concentration polarization boundary layer has irreversibly solidified and hardened. At this point, even if a multi-stage flow diversion is initiated, the increased axial flow velocity cannot be used to complete in-situ stripping and cleaning. This can easily cause the transmembrane pressure difference to surge due to the penetration load on the terminal separation membrane module. Therefore, precisely limiting the critical value to 1.35 ensures that the system responds instantly before large-scale passivation and blockage of the catalytic sites, thus locking in the optimal technical window for deep purification and low-drug-consumption self-balancing operation. Before the system is put into online operation, the main control unit collects the absolute value of fluid conductivity through state-of-charge sensors placed at the inlet and outlet of the first, second, and third purification zones. The algebraic difference between the conductivity at the outlet and the conductivity at the inlet of each purification zone is calculated using a differential circuit and defined as a characterizing the wastewater medium. The conductivity migration variable, which reflects the trend of polarization potential change within the catalytic packing bed, is used to perform sliding average noise reduction on this variable by setting a 240-hour sliding sampling window within the processor. The system internally constructs a dual closed-loop interlock control logic for process load indicators caused by long-term slow blockage and for differential pressure step jumps caused by sudden overload. When the differential pressure at the inlet of the first-stage purification zone jumps from 0.09 MPa to 0.34 MPa within 12 seconds, the sudden differential pressure jump signal serves as a feedforward emergency intervention trip command to directly adjust the opening of the multi-way flow direction switching distribution valve assembly. Under normal operating conditions, the process load indicator, which is updated every 2 seconds, serves as the feedback optimization control basis. When this indicator monotonically exceeds the preset safety threshold of 1.35 and is maintained for 5 consecutive sampling cycles, the system triggers a conventional topology conversion program to eliminate dual-head management and high-frequency malfunctions in the control loop caused by monitoring a single type of indicator.

[0040] While the above-mentioned flow diversion and allocation are being carried out, the main control unit adjusts the flow based on the process load indicators. The step scalar, in conjunction with this, increases the aeration power density at the bottom of the first-stage purification zone from 45 W / m³ to a range of 85 W / m³ to 120 W / m³. Utilizing the bubble shear and liquid scouring shear force generated by gas-liquid disturbance, organic pollutants on the surface of the porous catalytic material are in situ stripped and removed. High Reynolds number turbulent scouring directly weakens the interphase mass transfer resistance on the packing surface, providing the flow condition for interphase mass transfer at local interfaces. Simultaneously, the reshaping of aeration energy exposes active sites deep within the multiphase catalytic purification medium layer of the porous structure through gas-liquid shear, which in turn enhances the in-situ stripping efficiency of the local high-speed liquid scouring. This spatial topological flexible diversion and asymmetric step reshaping of the mechanical shear energy field power density... The positive feedback synergy mechanism resolves the conventional contradiction between deep-efficiency degradation and low chemical consumption operation within a compact physical configuration. By increasing the probability of shear collisions to compensate for local deficiencies in chemical reactant concentrations, the molar ratio of the reagents added to the first-stage purification zone can be simultaneously reduced by 15%, controlling the residual load of the reagents. Simultaneously, by altering the spatial boundaries and temporal sequence of the material flux in the flow channel, the long-term excess capacity of subsequent treatment stages is transformed into dynamic compensation for the overload of the upstream unit. This reconstructs the traditional process of relying on increased equipment investment to address local water quality fluctuations into an adaptive flow channel topology phase reorganization based on the transient resistance changes of the fluid itself. This allows for dynamic shaping of the pollution load distribution along the flow path. The purified effluent converges at the end of the flow channel and is then introduced into the subsequent low-pressure reverse osmosis separation zone for final desalination and purification. Because each purification zone directly disrupts the layering and assembly conditions of high-molecular-weight organic matter at the catalytic medium and membrane interface through non-uniform flow bypass and strong turbulent shear stress, subsequent treatment stages and the final low-pressure reverse osmosis membrane module are protected from scaling and compaction damage by high-concentration gel fouling layers. The transmembrane pressure difference exhibits random noise fluctuations consistent with industrial operating conditions between 0.16 MPa and 0.19 MPa. The total organic carbon content in the purified effluent remains stably below 1.43 mg / L, and the removal rate of high-valence anions is no less than 96.8%. The system's energy consumption per ton of water purified is stably controlled below 0.39 kWh. The entire staged deep purification process achieves physicochemical steady state of multi-component impurity synergistic deep purification and low-energy operation of the system under the premise of unchanged physical configuration. This topology reconstruction method, which relies on the change of the fluid medium's own physicochemical resistance as a feedforward response source, is an industrial wastewater purification architecture that deeply combines temporal flow shaping and asymmetric step reshaping of mechanical field energy. Through the non-uniform mismatch of material flux space within the process steps, it replaces the rigid energy dissipation path that relies on physical volume expansion or full saturation of chemicals in traditional water treatment engineering, providing methodological support for long-term intrinsically safe governance under complex industrial closed-loop circulating water reuse conditions.

[0041] Example 2: This example utilizes a physical experimental platform simulating industrial circulating water quality fluctuations to evaluate the reliability and treatment efficiency of a staged deep purification process. This platform includes a first-stage purification zone, a second-stage purification zone, and a third-stage purification zone connected by series pipelines. A low-pressure reverse osmosis membrane separation unit is mounted at the end of the flow channel to simulate a complete industrial recycled water purification path. A differential pressure transmitter for measuring fluid pressure has a measurement range of 0 to 1.0 MPa and a measurement resolution of 0.001 MPa. A conductivity meter for online monitoring and quantification of impurity enrichment has a range of 0 to 100,000 μS / cm and a basic measurement accuracy of 1.0%. Electromagnetic flow meters installed on the main inlet pipeline and branch bypass have a flow measurement range of 0 to 2000 m³ / h, and their data sampling frequency is set to 20 Hz. To verify the process's anti-interference and anti-fluctuation capabilities under field conditions, the experimental group prepared high-concentration... When a sudden combined load of molecularly recalcitrant organic matter and high-salt inorganic components occurs, Gaussian white noise with a signal-to-noise ratio of 20dB is actively superimposed on the front end of the system's electrical sensor data acquisition. An external signal generator introduces 50Hz power frequency electromagnetic interference harmonics to simulate grid fluctuations caused by real variable frequency power equipment, generating a raw measurement signal source with power frequency interference and noise background. During the parameter configuration of the experimental platform, a structured optimization configuration is implemented for the dynamic sampling period of the shear resistance vector of the core control parameter, i.e., the main control unit. The setting of the dynamic sampling period is influenced by two mutually constraining factors: the system's real-time requirement for capturing transient high-load clumps and the processor's high-frequency discrete computing load. The core technical trade-off is to avoid failing to capture the flow resistance step change within 12 seconds due to excessively slow sampling, while preventing processor register overflow and increased energy consumption due to excessively fast sampling. According to the technical design rules, when the monitored cross-boundary pressure drop variable... When the highest characteristic frequency of a signal is under high-frequency pulse disturbance, in order to satisfy the Nyquist sampling theorem and leave more than three times the engineering safety margin to prevent signal aliasing, the dynamic sampling period should approach the lower limit of its calculation window, that is, increase the sampling update frequency. Therefore, under the current typical high load change impact test conditions, the sampling period of the internal clock interrupt of the main control unit is fixed at 2s. This provides a specific engineering example that ensures the capture of transient flow resistance changes while keeping the system calculation load within the safe working window.

[0042] To collaboratively verify the effectiveness, component synergistic effects, and rationality of numerical boundaries of the staged deep purification process within a single experimental framework, the experimental design included a multi-dimensional control system with four independent characteristic comparison combinations. Group 1 was a conventional rigid series control group, which disabled the dispensing function of the multi-channel flow-direction switching distribution valve assembly, ensuring the material flow remained in a fixed multi-stage cascaded series flow state and maintained a fixed reagent dosage ratio. Group 2 was a partially missing control group, which, while retaining the bypass diversion valve, shut down the aeration power density linkage adjustment mechanism at the bottom of the first-stage purification zone, keeping it constant at a standard aeration baseline of 45 W / m³ to isolate and verify the contribution of energy field remodeling. Group 3 was an out-of-range boundary control group, which intentionally included process load indicators stored in the main control unit. The safety threshold is set as an extreme value deviating from the required range, specifically 1.10 below the lower limit and 1.60 above the upper limit, to test the scientific validity of the critical criterion window; the fourth group is the sample group of this invention, which fully operates a complete process scheme including flexible diversion of the flow channel topology and linkage updating of mechanical shear energy field power density. The above four test groups are sequentially applied to an impurity system composed of macromolecular surface-active organic matter and saturated calcium carbonate inorganic salt, and three obvious gradients of pollution severity—low intensity, medium intensity, and high intensity—are constructed by systematically adjusting the initial concentration of total organic carbon in the prepared solution. The corresponding concentration indicators are determined to be 50 mg / L, 150 mg / L, and 300 mg / L, respectively, to objectively evaluate the dynamic response law of the scheme of this invention under different pollutant flux pressures.

[0043] In the verification test conducted on a medium-intensity pollution gradient of 150 mg / L, when the system had been running for 241 hours, a high-load composite agglomerate was instantaneously introduced into the inlet. In the conventional rigid series control group, the pressure transmitter at the front end of the first-stage purification zone showed a rapid increase in pressure within 12 seconds, leading to macromolecular adsorption and blockage on the porous catalyst surface. However, in the operating process of the sample group of this invention, the internal digital low-pressure filter of the main control unit effectively filtered out random fluctuations introduced by power frequency harmonics, allowing the sensor output data to return to the true physical trend. It collected the cross-boundary pressure drop across the first-stage purification zone. The pressure jumps to 0.32 MPa, while the conductivity shifts. The transient volumetric flow rate of the main inlet pipe migrates to 4218 μS / cm. Stabilizing at 1000 m³ / h, the main control unit calculates the process load index in real time based on these clear underlying physical variables and the built-in relational equations. The specific mathematical expression is as follows: ,in, For process transport load indicators, The pressure difference before and after each purification zone. This refers to ion mobility. The transient volumetric flow rate of the main inlet pipe, indicated by the superscript. Subscripts indicate the regions before and after each purification step. Indicates ion migration, subscript This represents the main inlet pipeline; the process load index is calculated by substituting the above discrete data points into the calculation. The value is precisely equal to 1.35. This quantification result accurately triggers the preset phase transition threshold. The main control unit then outputs a valve drive electrical signal to the external actuator, driving the multi-way flow direction switching distribution valve assembly to instantly activate. This allows 65% of the material volume flow rate, i.e., 650 m³ / h, to be directly introduced into the inlet of the second-stage purification zone, rapidly increasing the local axial flow velocity within the second stage from 0.45 m / s to 2.1 m / s. Simultaneously, the frequency converter is linked to progressively reshape the aeration power density at the bottom of the first stage from 45 W / m³ to 105 W / m³. In m³, after adjusting the spatial flow topology of the flow path and initiating the cascading diversion, the dosing system does not use a fixed absolute chemical dosage to address the nonlinear fluctuations in the initial concentration of macromolecular surface-active organic matter in the wastewater medium within the range of 50 mg / L to 300 mg / L. Instead, the variable frequency dosing pump retrieves the discrete gradient adjustment function built into the main control unit's memory, dynamically calculates the current dosage molar ratio baseline value based on the initial total organic carbon content of the influent measured by the online total organic carbon analyzer and the transient volumetric flow rate, and then adjusts this baseline value accordingly. 15% is used as the final dosage of the matching reagent. This locally reduces the concentration of chemical reactants, compensating for the strong turbulent shear stress generated by the increased aeration power density (from 85 W / m³ to 120 W / m³) in step S3, and increases the frequency of local collisions between reactant molecules. Under moderate pollution conditions and with a total organic carbon content of 150 mg / L, the initial molar ratio of the matching degradation reagent is set at 1.2:1. After the cascade diversion is triggered, the molar ratio of the matching reagent is adjusted to 1.02:1, and the effluent is introduced into the subsequent... The total organic carbon content of the purified water after the low-pressure reverse osmosis separation zone is stably maintained below 1.43 mg / L, establishing a monotonic deterministic correlation between the change in chemical dosage and the dynamic fluctuations in water quality load. By demonstrating the evolution of these deterministic intermediate characteristic parameters, the continuity and formal transparency of the internal control chain of the invention are confirmed. Through lateral analysis of multiple sets of control test data and deconstruction of performance inflection points, the scientific necessity of parameter range limitation and the nonlinear technical effect characteristics are clearly presented. In the control group outside the range boundary, when the process carrying load index is... When the preset threshold is lowered to 1.10, the system overreacts to slight fluctuations in flow resistance, causing the valve assembly to prematurely trigger cascading diversion under low load conditions. This results in a reduction in the actual volumetric flow rate through the first-stage purification zone, with the internal local axial velocity dropping to 0.28 m / s. This velocity is lower than the critical turbulent shear rate required by the catalytic packing layer, causing short-circuiting and mass transfer dead zones within the internal fluid, leading to a decrease in mass transfer efficiency and preventing the effective degradation of large organic molecules due to insufficient contact time. Conversely, when the safety threshold is raised to the extreme value of 1.60, data shows that the system exhibits a response hysteresis effect. The first-stage purification zone remains under overload pressure for up to 45 minutes, affecting the surface of the porous catalytic material. The adsorption sites were already fully saturated before the topological triggering of the flow diversion. High-concentration macromolecular impurities accumulated and assembled at the membrane interface, forming an irreversible compacted fouling layer. At this point, even if the bypass flow diversion was activated, the solidified concentration polarization boundary layer could not be removed in situ by liquid flow scouring, causing the transmembrane pressure difference of the terminal separation membrane module to irreversibly soar to over 0.38 MPa. Meanwhile, in the partial missing control group test, although 65% of the material flow was diverted across stages, due to the lack of compensation for the increase in aeration power density, the active sites deep inside the porous packing of the first stage were gradually filled with residual organic gel due to the lack of gas-liquid shear vibration. This confirms that there is an inseparable causal synergy between spatial topological elastic flow diversion and mechanical shear energy field reshaping. In essence, topological splitting provides the flow condition for interphase mass transfer by reducing surface loading, while energy field reshaping, in turn, maintains the long-term unobstructed flow of the splitting channel through efficient stripping. Together, they construct an optimal operating window that simultaneously achieves deep purification and low-drug consumption. The final long-term operational test data realizes a complete logical closed loop from process input to end-product value. Faced with an extreme high-intensity fouling gradient of 300 mg / L, the conventional rigid series control group failed due to the complete inactivation of the first-stage catalytic sites, leading to the direct penetration of large organic molecules into the low-pressure reverse osmosis unit. After 4 hours of operation, it failed because an irreversible, dense gel layer formed on the surface of the low-pressure reverse osmosis membrane unit, and its transmembrane pressure difference decreased sharply. The pressure climbed to 0.46 MPa and the total organic carbon content in the purified water dropped to 5.34 mg / L, while the removal rate of high-valence anions decreased to 72.3%. In contrast, the sample group of this invention, which uses the complete staged deep purification process of this invention, exhibited adaptive adjustment characteristics to multiple pollutant flux gradients. Even under continuous high-intensity load shocks of 300 mg / L, the system completed the spatial dynamic mismatch of the material flux in the flow channels between the first, second, and third purification zones, so that the cumulative rate at the membrane interface was always controlled by the high-flow-rate shear in-situ stripping rate. The surface of the terminal separation membrane module was protected from the scaling and compaction damage of the high-concentration gel layer. The transmembrane pressure difference under long-term stable operation was between 0.16 MPa and 0.The noise fluctuations within the 19 MPa range are consistent with the accuracy observed in real-world engineering settings. Ultimately, the total organic carbon content in the purified water remained stable at 1.41 mg / L, and the removal rate of high-valence anions remained at a high level of 97.1%. Simultaneously, the molar ratio of the added reagents was reduced by 15%, and the energy consumption per ton of water purified was stably controlled within the low-energy consumption range of 0.38 kWh. These objective data fully demonstrate that the method of this invention can achieve physicochemical stability within a single compact system, achieving the goals of deep purification of multi-component impurities and low-reagent, low-energy operation. This confirms the clear engineering feasibility of the technical solution of this invention.

[0044] Example 3: This example combines Figures 1 to 2 A description of a staged deep purification process for circulating water supply, such as... Figure 1 As shown, wastewater sequentially passes through three purification zones. Differential pressure and conductivity are collected to establish a shear resistance vector. Based on the established shear resistance vector, the supercritical value of the carrying capacity index is calculated and the topology is adjusted. Subsequently, the process fluid flow is divided into two paths. One path is diverted to the second purification zone at 65% flow rate, while the other path is maintained at 35% flow rate in the first stage to cope with shocks and to enhance the aeration of the first stage to remove organic pollutants. After treatment by the two process fluids, the reagent dosage ratio is reduced by 15%, and the effluents are merged and finally introduced into the subsequent low-pressure reverse osmosis separation zone.

[0045] like Figure 2 As shown, the pre-treatment preparation includes coarse filtration and suspended solids interception of the system fluid, and guides the wastewater through each purification zone sequentially. Online monitoring includes online acquisition of differential pressure and fluid conductivity, and constructing a shear resistance vector to calculate load indicators. Flexible diversion and allocation adjust the spatial flow topology of the wastewater according to the calculated load indicators. This topology allocation is divided into two independent flow paths. One path diverts 65% of the volumetric flow rate to the second-stage inlet and opens the physical degassing zone of the parallel main flow channel. The other path maintains 35% of the volumetric flow rate in the first-stage zone and increases the aeration power at the bottom of the first-stage purification zone. Then, an alternating magnetic field is applied inside the first-stage purification zone. The terminal desalination and purification process draws the effluent treated by the above paths into the low-pressure reverse osmosis zone at the end, and monitors the transmembrane pressure difference to initiate online chemical cleaning.

[0046] Example 4: During the sewage discharge cycle of the circulating water supply system, when the system faces the disturbance of drastic transient volumetric flow rate changes in the main inlet pipeline, the porous catalyst material layer with an average channel porosity of 0.42 filling the first-stage purification zone will generate local backlog, causing a sudden step change in the cross-boundary pressure drop at both ends of the fluid, deviating from the pattern of impurity accumulation. If a static fixed threshold is directly used to control the multi-way flow direction switching distribution valve assembly, it will cause high-frequency false triggering of valve switching actions, resulting in an increase in the energy consumption of the entire system and the separation membrane assembly in the subsequent low-pressure reverse osmosis separation zone. The increased concentration polarization at the surface necessitates measures to eliminate pressure differential data interference caused by fluctuations in flow flux. Before the water purification system is put into formal operation, a physical experimental platform with a maximum design flow rate of at least 2000 m³ / h and a differential pressure sensor sampling frequency of at least 20 Hz is used to measure the pipeline fluid resistance under clean conditions. Under normal operating conditions where the total influent flow rate gradually increases in increments of 50 m³ / h, a baseline scalar of cross-sectional pressure drop under clean conditions without impurity blockage is collected online. This establishes the transient flow rate of the main influent pipeline. The monotonic correspondence between the initial cross-sectional pressure drop of the clean pipeline and the flow rate is obtained by measuring the initial pressure difference across the fluid under different flow flux gradients to obtain the corresponding transient volumetric flow rate. The pure water dynamic residual resistance component.

[0047] When the process is in continuous online processing, the processor in the main control unit reads the cross-boundary pressure drop variable collected by the differential pressure transmitter. conductivity migration variables collected by conductivity meter Furthermore, a real-time adaptive correction operator based on the residual drag component of pure water dynamics is introduced. Correcting the calculation formula and adaptive correction operator To determine the transient volumetric flow rate of the current main inlet pipe The reciprocal of the aforementioned dynamic residual resistance, retrieved in real time, is used to offset the artificially high pipe friction resistance caused by the increase in volumetric flow rate during flow fluctuations, thus ensuring the calculated process load index is accurate. The mathematical expression for accurately reflecting the mass transfer resistance step caused by pollutant accumulation is as follows: ,in, For process transport load indicators, The pressure difference before and after each purification zone. This refers to ion mobility. The transient volumetric flow rate of the main inlet pipe. As an adaptive correction operator, in actual operation, the real-time retrieval of the adaptive correction operator is achieved through a feature mapping database pre-stored in the main control unit's memory. This database pre-inputs a monotonic correspondence table between multiple sets of transient volumetric flow rate values ​​of the main inlet pipeline and the baseline scalar of the initial cross-boundary pressure drop of the clean pipeline, established under clean hydrodynamic testing, ranging from 0 cubic meters per hour to 2000 cubic meters per hour with equidistant step gradients of 50 cubic meters per hour. When the processor reads the current transient volumetric flow rate value in real time, it retrieves the corresponding pure hydrodynamic residual resistance component online through a linear interpolation algorithm, and calculates the reciprocal of the residual resistance component to define it as the current adaptive correction operator value. This allows for the precise offsetting and elimination of the artificially high pipeline friction resistance term in real time at the software control level.

[0048] After the processor completes the above calculations, the processor's registers register the process load index within a sliding sampling window consisting of five consecutive sampling cycles. To determine the monotonicity trend, the process load index calculated from 5 consecutive sampling points... When all values ​​monotonically exceed the preset safety threshold of 1.35, the main control unit determines that a real overload of fouling has occurred on the packing surface and outputs a drive electrical signal. Based on the internally stored discrete gradient adjustment function, it adjusts the opening increment of the multi-way flow direction switching distribution valve assembly in real time, controlling the diversion ratio of the material volume flow rate originally entering the first-stage purification zone to jump within the range of 50% to 75%, under the current process load index. Under an overload condition of 1.42, the corresponding output diversion ratio is determined to be 65%. The multi-way flow direction switching distribution valve assembly directly diverts 65% of the overflow stream to the inlet of the second-stage purification zone. Since the residual resistance component of the pure water dynamics is offset in real-time during calculation, the multi-way flow direction switching distribution valve assembly operates within the process load index... When the flow rate falls back to within the safe operating window, it stably resets to the conventional cascaded series mode. The entire diversion and reconstruction process has a closed-loop and definite evolution trajectory. The transmembrane pressure difference of the separation membrane modules in the subsequent treatment stages and the terminal low-pressure reverse osmosis separation area does not show any unexpected sudden changes during the entire sewage discharge cycle, and is stably maintained in the range of 0.16MPa to 0.19MPa. The total organic carbon content of the effluent is stably maintained below 1.43mg / L, the removal rate of high-valence anions is greater than or equal to 96.8%, and the energy consumption per ton of water purified by the system is controlled below 0.38kWh.

[0049] Example 5: When the system faces an undesirable application environment with a severe mix of high concentrations of macromolecular surface-active organic matter and saturated hardness salt components, the separation performance of each purification zone may slowly decline over time due to localized mass transfer hindrance caused by the deep layers of the packing material under long-term pressure without flushing. The processor in the main control unit retrieves the continuous historical pressure difference and conductivity variation sequence collected by the sensor according to the preset sliding time window. At this stage, the system introduces the sliding window aging decay operator coefficient to offset the weight interference of historical old data on the current flow resistance change trend. The value of the aging decay operator coefficient is updated and calculated in real time according to the reciprocal of the sliding window length.

[0050] The processor calculates the average flow pressure drop before and after each purification zone within a preset 240-hour operating period. When it detects that the slope of the average flow pressure drop in the first-stage purification zone deviates monotonically from the factory standard baseline by 15%, the main control unit periodically triggers the in-situ local high-pressure air pulse flushing control command without interrupting the hydraulic purification flux. This causes the aeration power density at the bottom of the first-stage purification zone to jump from the normal 45W / m³ to the maximum shear stress impact point of 150W / m³ within a 30-second instantaneous release window. The high Reynolds number shear stress of the gas-liquid turbulence destroys the deep colloidal skeleton of the porous packing that has been adsorbed, causing the deposited pollutants to fall off and be discharged through a low-flow-rate bypass. This maintains the inherent safety and stability of the reactor under long-term operation, and the total organic carbon content in the effluent is stably maintained below 1.43 mg / L.

[0051] It will be apparent to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit or essential characteristics of the present invention.

[0052] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit it. Although the present invention has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can be made to the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.

Claims

1. A staged deep purification process for circulating water supply, characterized in that, Includes the following steps: Step S1: Guide the wastewater through the first-stage purification zone, the second-stage purification zone, and the third-stage purification zone in sequence, and fill each purification zone with porous catalytic material. Collect the differential pressure and fluid conductivity at the inlet and outlet of each purification zone online to construct a shear resistance vector that includes cross-boundary pressure drop variables and conductivity migration variables. Step S2: Calculate the process load index based on the differential pressure, fluid conductivity, and transient volumetric flow rate of the main inlet pipe. When the process load index of the first-stage purification zone exceeds the preset safety threshold of 1.35, adjust the spatial flow topology of the flow stream. Divert 65% of the volumetric flow rate that originally entered the first-stage purification zone to the inlet of the second-stage purification zone, so that the local axial velocity inside the second-stage purification zone is maintained between 1.8 m / s and 2.4 m / s, and the remaining 35% of the volumetric flow rate is maintained in the first-stage purification zone to cope with sudden load shocks. In step S3, while diverting the flow, the aeration power density at the bottom of the first-stage purification zone is increased from 45W / m³ to a range of 85W / m³ to 120W / m³. Organic pollutants on the surface of the porous catalyst are removed by the shear force of the fluid. At the same time, the molar ratio of the matching reagent added to the first-stage purification zone is reduced by 15%. The purified effluent is then converged at the end of the channel and introduced into the subsequent low-pressure reverse osmosis separation zone.

2. The staged deep purification process for circulating water supply according to claim 1, characterized in that, In step S2, the physical degassing zone connected in parallel to the main flow channel is opened, and the differential pressure variance of the total system pressure drop within 5 seconds is periodically measured. When the differential pressure variance is greater than 0.02 MPa, the fluid flow path is switched, and the material flow rate is distributed between the main flow channel and the physical degassing zone. This causes the bubbles in the fluid to burst under the combined action of the fluid cohesive pressure and the wall fluid shear force, thereby eliminating the bubble backlog interference in the multiphase fluid when the material flow rate is non-uniformly mismatched.

3. The staged deep purification process for circulating water supply according to claim 1, characterized in that, The graded deep purification process maintains a unidirectional series flow under normal operating conditions, and keeps the flow velocity within each zone stable within a preset range of 0.45m / s.

4. The graded deep purification process for circulating water supply according to claim 3, characterized in that, The following detailed steps are included: When the differential pressure at the inlet of the first-stage purification zone jumps from 0.09 MPa to 0.34 MPa within 12 seconds, the spatial flow topology of the flow stream is changed, switching the unidirectional series state to a parallel split state or a partial reflux state, in order to reduce the load on the single-stage zone and alleviate the crystal accumulation caused by the extended residence time due to the split.

5. A staged deep purification process for circulating water supply according to claim 1, characterized in that, In step S3, based on the differential pressure at the inlet of the first-stage purification zone and the fluid conductivity, an alternating magnetic field is applied inside the first-stage purification zone, and the duration of the alternating magnetic field is controlled within the range of 30 min to 60 min, so that calcium and magnesium ions in the wastewater medium crystallize into suspended crystal nuclei inside the fluid, thereby blocking the adhesion and scaling of hardness ions on the outer surface of the porous catalyst material.

6. The graded deep purification process for circulating water supply according to claim 1, characterized in that, A low-pressure reverse osmosis separation zone is set at the end of the flow channel in the staged deep purification process. The staged deep purification process also includes the following steps: Step S4, monitor the transmembrane pressure difference in the low-pressure reverse osmosis separation zone. When the transmembrane pressure difference slides from 0.14MPa to 0.16MPa, start the online chemical cleaning program to stabilize the total organic carbon content of the purified water in the low-pressure reverse osmosis separation zone below 1.43mg / L and maintain the removal rate of high-valence anions at no less than 96.8%.

7. A staged deep purification process for circulating water supply according to claim 6, characterized in that, In step S4, during the operation of the online chemical cleaning program, a composite mode of alternating intermittent low-concentration acid washing and high-frequency hydraulic rinsing is adopted, and the circulation flow rate of the cleaning solution is controlled to be 0.6 m / s to 0.8 m / s, reducing the system's energy consumption per ton of water purification to no more than 0.39 kWh.

8. A staged deep purification process for circulating water supply according to claim 1, characterized in that, Before monitoring in step S1, the following preparatory steps are included: coarse filtration and suspended solids interception are performed on the fluid in the circulating water supply system to control the initial turbidity of the wastewater medium entering the graded deep purification process to be lower than 5 NTU, and the initial water temperature is controlled to be maintained within the range of 20°C to 35°C.

9. A staged deep purification process for circulating water supply according to claim 1, characterized in that, In step S2, the porous catalyst material is a porous ceramic particle loaded with transition metal oxides, and its micropore size is distributed between 10 nm and 50 nm. The fluid shear force generated after the aeration power density is increased is used to remove organic pollutants on the surface of the porous catalyst material, so as to maintain the exposure of the active sites of the porous catalyst material.

Images