A complete set of device for waste incineration fly ash electrolysis and resource utilization

Abstract

The present application relates to waste incineration processing technical field, especially to a kind of waste incineration fly ash electrolysis collaborative resource processing complete device, including fly ash water washing pretreatment unit, solid-liquid separation device, electrolysis processing unit, circulating cooling unit, power supply control unit, data acquisition unit, subsequent processing unit and central control unit, central control unit is built-in multi-parameter coupling decision model operation module and weight factor self-adaptive adjustment module, receive temperature, pH value, salt concentration and electrode polarization characteristic value, optimal current density is solved by comprehensive performance evaluation function combined with gradient ascent method iteration, data acquisition unit is also provided with oxidation-reduction potential sensor and total organic carbon analyzer, central control unit is built-in electrolyte aging state evaluation module, aging index is calculated in real time.The present application realizes multi-parameter coupling optimization, weight self-adaptive adjustment and electrolyte full life cycle management, effectively improves electrolysis efficiency and operating stability.

Description

Technical Field

[0001] This invention relates to the field of waste incineration technology, specifically to a complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration via electrolysis. Background Technology

[0002] Waste incineration fly ash contains large amounts of chloride salts, heavy metals, and dioxins, among other harmful substances. Currently, a coupled process of "water washing desalination + electrolytic treatment" is one of the mainstream directions for resource utilization. In this process, the fly ash is washed and filtered to obtain high-salt wastewater rich in chloride ions, which is then fed into an electrolytic cell for electrochemical conversion: in the anode zone, Oxidized It further reacts with water to form hypochlorite (available chlorine), while the oxygen evolution reaction at the anode produces... In the cathode region, water is reduced to produce In the solution Heavy metal ions are electrodeposited as hydroxides or in elemental form under alkaline conditions.

[0003] In the electrolytic process, the setting of power supply parameters directly determines the electrolysis efficiency, temperature control effect, and overall treatment quality. However, due to the complex sources of waste incineration fly ash and the drastic fluctuations in the composition of washing liquid, the optimal values ​​of power supply parameters are not fixed but dynamically shift with the real-time changes of multiple factors such as electrolyte temperature, salt concentration, pH value, electrode surface condition, and electrolyte aging degree. Existing technologies generally have the following shortcomings in determining power supply parameters: (i) The power supply parameters are set based on a single basis and lack multi-dimensional comprehensive perception. In existing electrolysis systems, power supply parameters are typically set to fixed values ​​based on operator experience, or simply adjusted based on temperature alone. However, factors affecting overall electrolysis performance include at least four dimensions: temperature, salt concentration, electrode deposition level, and pH value. Current technology lacks the ability to simultaneously sense data from multiple dimensions and comprehensively calculate optimal power supply parameters, leading to a severe mismatch between power supply parameters and real-time operating conditions. (ii) The weighting factors are static and fixed, lacking adaptive adjustment capabilities. While existing technologies attempt to monitor multiple parameters in the electrolysis process, the weights of each parameter in the decision-making model are typically statically set by operators based on experience, and cannot be adaptively adjusted according to changes in operating conditions. For example, when temperature fluctuations intensify, the system should prioritize temperature control; when pH fluctuations intensify, the system should prioritize pH control. Fixed weighting factors cannot respond to such dynamic changes, resulting in a consistently "one-size-fits-all" control strategy that fails to maintain optimal overall performance across all operational stages. (iii) Lack of online monitoring and assessment of electrolyte aging status As the electrolysis process continues, organic byproducts, impurity ions, and degradation products gradually accumulate in the electrolyte. At the same time, the effective chlorine content and redox activity gradually decline. Electrolyte aging leads to a series of problems such as decreased current efficiency, aggravated side reactions, and accelerated electrode corrosion. However, existing fly ash electrolysis treatment systems lack online monitoring methods for electrolyte aging, making it impossible to quantitatively assess the degree of aging or incorporate the aging status into the calculation and decision-making of power supply parameters. This results in the system still operating with parameters based on "fresh electrolyte" in the later stages of electrolyte operation, causing energy waste and deterioration of treatment effect. Therefore, a complete set of equipment for the co-processing of fly ash from waste incineration by electrolysis is needed to improve the above-mentioned problems. Summary of the Invention

[0004] The purpose of this invention is to provide a complete set of equipment for the co-processing of fly ash from waste incineration by electrolysis, so as to solve the problems mentioned in the background art.

[0005] To achieve the above objectives, the present invention provides the following technical solution: A complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis includes: The fly ash water washing pretreatment unit has a solid-liquid separation device connected to its output end.

[0006] An electrolysis treatment unit has its inlet connected to the liquid phase outlet of the solid-liquid separation device. The electrolysis treatment unit contains an anode assembly, a cathode assembly, and an ion separator disposed between the anode assembly and the cathode assembly.

[0007] The circulating cooling unit has its cooling medium inlet and outlet connected to the heat exchange jacket of the electrolysis processing unit.

[0008] A power supply control unit, electrically connected to the anode assembly and the cathode assembly, is used to apply modulated power supply parameters to the electrolysis processing unit.

[0009] The data acquisition unit includes at least a temperature sensor, a pH sensor, a conductivity sensor, and an electrical signal sampler disposed inside the electrolysis processing unit.

[0010] The subsequent processing unit has its input end connected to the liquid outlet and exhaust port of the electrolysis processing unit, and is used to recycle and harmlessly dispose of the products after electrolysis.

[0011] The central control unit has its signal input terminal connected to the data acquisition module, and its control output terminal connected to the control terminals of the power supply control unit and the circulating cooling unit, respectively.

[0012] The central control unit has a built-in multi-parameter coupled decision model calculation module and a weight factor adaptive adjustment module. The central control unit is configured to: receive real-time electrolyte temperature, pH value, salt concentration characterization value and electrode polarization characterization value fed back by the data acquisition module; input the above data into the multi-parameter coupled decision model calculation module to calculate the target power supply parameters that optimize the overall electrolysis performance; and then output control signals to the power supply control unit to adjust the output current density and cell voltage. At the same time, it synchronously outputs control signals to the circulating cooling unit according to the temperature deviation value to adjust the cooling medium flow rate.

[0013] As a preferred embodiment of the present invention, the multi-parameter coupled decision model computation module is based on a comprehensive performance evaluation function. The comprehensive performance evaluation function is used for optimization calculation. The expression is: in: The theoretical current efficiency coefficient is determined in real time by the central control unit based on the salt concentration characterization value. When the salt concentration is high... A larger value allows the system to pursue higher current efficiency; when the salt concentration is low... The value decreases accordingly; Temperature-related factors; The optimal pH value for the reaction; The change in inter-electrode resistance is calculated from the real-time voltage and current values ​​collected by the electrical signal sampler. This is the initial inter-electrode resistance; and These are the acidity / alkalinity weighting factor and the deposition state weighting factor, respectively.

[0014] As a preferred embodiment of the present invention, the temperature influence factor The expression is: in: The real-time electrolyte temperature is fed back by the temperature sensor. For the optimal reaction temperature, For extreme tolerance temperature, Temperature sensitivity coefficient.

[0015] As a preferred embodiment of the present invention, the central control unit is based on the comprehensive performance evaluation function. The gradient ascent method is used to calculate and output the target current density in real time. : in: The current density at the current moment, The learning step size factor has a value range of 0.05 to 0.1. The perturbation step size ranges from 0.5 to 1.0 A / m. 2 When the comprehensive performance evaluation function The absolute value of the partial derivative with respect to current density is less than the convergence criterion. When the search for the optimal solution has converged, it is determined that the search has been completed.

[0016] Specifically: Apply pressure to both sides of the current working point. The small current disturbance is measured to determine the resulting comprehensive performance evaluation function. The change in the numerical gradient is used to calculate the numerical gradient. Then, along the gradient ascent direction with step size Update the current density, gradually approximating the desired value. Maximum optimal current density value .

[0017] When the comprehensive performance evaluation function The absolute value of the partial derivative with respect to current density is less than the convergence criterion. When the optimization is deemed convergent, the iteration is stopped. Among them, the convergence criterion The range of values ​​is .

[0018] As a preferred embodiment of the present invention, the data acquisition unit further includes an oxidation-reduction potential sensor and a total organic carbon analyzer disposed inside the electrolysis processing unit, and the central control unit has an electrolyte aging status assessment module built in. The aging state assessment module uses the real-time oxidation-reduction potential value fed back by the oxidation-reduction potential sensor. The total organic carbon concentration reported by the total organic carbon analyzer in real time and cumulative electrolysis operating time The electrolyte aging index is calculated according to the following formula. : in: The initial redox potential of fresh electrolyte. The upper limit of the permissible total organic carbon concentration, Design lifespan for the electrolyte. , , This is the aging weighting coefficient. ; The aging index The value range is from 0 to 1. =0 indicates that the electrolyte is in a completely fresh state. =1 indicates that the electrolyte has reached the end of its service life. When the preset aging threshold is exceeded, the central control unit issues a liquid replacement warning signal.

[0019] In a preferred embodiment of the present invention, the weight factor adaptive adjustment module extracts the running state features using a sliding time window, wherein the width of the sliding time window is N=60 sampling points, corresponding to a sampling period. =0.5 seconds, window duration 30 seconds; The weighting factor adaptive adjustment module calculates the temperature fluctuation amplitude in real time. pH fluctuation range and electrode polarization rate : Based on the current status of the above three indicators and the aging index The temperature sensitivity coefficient is updated synchronously using fuzzy logic reasoning rules. pH weighting factor and sedimentation state weighting factor The core logic of the fuzzy inference rule base is as follows: Among them, "high," "medium," and "low" represent the fuzzy membership states of each indicator, divided by pre-set thresholds; big"," middle"," "Small" indicates a significant, medium, or slight increase in the corresponding weight, respectively; "(Regression Benchmark)" indicates that the weights are regressed to the initial benchmark value. .

[0020] The updated weight values ​​are output after being filtered by a first-order low-pass filter to avoid oscillations in control commands caused by frequent changes in weight factors. in, These are the filter coefficients, with values ​​ranging from 0.1 to 0.3. and Using the same smoothing logic, ultimately, the smoothed , , Real-time input into comprehensive performance evaluation function It participates in the calculation.

[0021] As a preferred embodiment of the present invention, the central control unit has a built-in temperature safety threshold comparison module, and the determination logic of the temperature safety threshold comparison module is configured as follows: When the real-time electrolyte temperature exceeds the first safety threshold but is lower than the second safety threshold, the central control unit sends a gradient current reduction command to the power supply control unit and a current increase command to the circulating cooling unit, wherein the first safety threshold is lower than the second safety threshold. When the real-time electrolyte temperature exceeds the second safety threshold, the central control unit sends a step-by-step instruction to the power supply control unit to cut off the power supply branch of the single tank.

[0022] As a preferred embodiment of the present invention, the power supply control unit includes a rectifier module and a pulse width modulation module that are communicatively connected to the central control unit; When the real-time pH value fed back by the pH sensor deviates from the set range, the central control unit fine-tunes the potential distribution ratio between the anode assembly and the cathode assembly through the pulse width modulation module; When the rate of change of the electrode polarization characterization value exceeds a preset range, the central control unit applies a reverse pulse voltage to the anode assembly and the cathode assembly through the pulse width modulation module to suppress the densification growth of deposits on the electrode surface.

[0023] As a preferred embodiment of the present invention, the central control unit has a built-in temperature PID regulation module. This module is independent of the current optimization loop and adjusts the temperature based on the temperature deviation value. Proportional and integral components, output cooling flow correction value : in: This is the proportionality coefficient. The integral coefficient is... The sampling period.

[0024] As a preferred embodiment of the present invention, the subsequent processing module includes: The MVR evaporation and crystallization unit, which is connected to the outlet of the electrolysis treatment unit, is used to concentrate and crystallize the electrolyte to recover industrial salt. A chlorine absorption unit connected to the exhaust port of the electrolysis treatment unit is used to absorb the chlorine-containing gas generated by electrolysis by alkaline spraying to generate hypochlorite byproduct. And a high-temperature melting and solidification unit connected to the solid phase outlet of the solid-liquid separation device, used to melt and vitrify the dechlorinated fly ash to prepare building material aggregate.

[0025] As a preferred embodiment of the present invention, the fly ash water washing pretreatment unit is a three-stage countercurrent water washing system, which includes a slurry conditioning tank, a primary hydrocyclone separator, a secondary concentration washing tank, and a tertiary fine washing tank connected in series. The liquid phase outlet of the tertiary fine washing tank is connected to the solid-liquid separation device. The electrolysis treatment unit is a diaphragm electrolysis cell group, wherein the diaphragm is a cation exchange membrane or a bipolar membrane, and the heat exchange jacket is sleeved on the outer wall of the electrolysis treatment unit. The central control unit is an industrial programmable logic controller or an embedded industrial computer, and its human-machine interface is equipped with a parameter setting module and an abnormal alarm module. The abnormal alarm module is used to issue an audible and visual alarm signal when the real-time electrolyte temperature exceeds the limit threshold or the pH value exceeds the set range.

[0026] Compared with the prior art, the beneficial effects of the present invention are: This invention simultaneously acquires real-time data from four dimensions—temperature, salt concentration, electrode deposition degree, and pH value—through a data acquisition unit. The central control unit incorporates a multi-parameter coupled decision model computation module. Using a comprehensive performance evaluation function as the core decision-making mechanism, it employs a gradient ascent method to iteratively solve for the optimal current density for overall electrolysis performance. The temperature influence factor utilizes a quadratic penalty function design, enabling nonlinear early warning and active suppression when the temperature deviates from the optimal reaction temperature. Real-time monitoring and normalization of inter-electrode resistance changes incorporate the electrode surface deposition state into the quantitative decision-making system for power supply parameters. This upgrades the determination of power supply parameters from traditional single-parameter empirical estimation to multi-dimensional data-driven scientific calculation, ensuring that the system can obtain optimal power supply parameters matching the current electrolyte state under any operating conditions.

[0027] This invention incorporates a weighting factor adaptive adjustment module in the central control unit. This module extracts three operating condition characteristic indicators—temperature fluctuation amplitude, pH fluctuation amplitude, and electrode polarization rate—using a sliding time window. Combined with the electrolyte aging index, it employs fuzzy logic reasoning rules to dynamically update the temperature sensitivity coefficient, pH weighting factor, and deposition state weighting factor in the comprehensive performance evaluation function in real time. This allows the comprehensive performance evaluation function to automatically adjust the priority of each control objective based on real-time operating condition changes, adaptively seeking the optimal balance point under multi-objective conflict conditions. This enhances the system's adaptability to fluctuations in fly ash sources and sudden changes in water quality, ensuring that the electrolysis process maintains optimal comprehensive performance at different operating stages.

[0028] This invention adds a redox potential sensor and a total organic carbon analyzer to the data acquisition unit, and integrates an electrolyte aging status assessment module into the central control unit. By weighted fusion of three dimensions—redox potential drift, total organic carbon accumulation concentration, and operating time—a quantitative calculation formula for the electrolyte aging index is constructed, achieving a leap from qualitative judgment to quantitative assessment of electrolyte aging status. This enables the system to proactively adjust its operating strategy and issue electrolyte replacement warnings based on the aging index, changing the traditional electrolysis system's operation mode of using a single fixed parameter throughout the electrolyte's lifespan. It achieves dynamic management of the entire electrolyte lifecycle, effectively avoiding the decline in operating efficiency and equipment wear caused by electrolyte aging. Attached Figure Description

[0029] Figure 1 This is a schematic diagram of the overall process of the present invention; Figure 2 This is a flowchart of the multi-parameter coupled decision-making and adaptive control process of the central control unit of the present invention. Detailed Implementation

[0030] The technical solutions of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the scope of protection of the present invention.

[0031] To facilitate understanding of the present invention, a more comprehensive description of the invention will be given below with reference to the accompanying drawings, and several embodiments of the invention will be provided. However, the invention can be implemented in many different forms and is not limited to the embodiments described herein. Rather, these embodiments are provided so that the disclosure of the invention will be more thorough and complete.

[0032] Example 1: Please refer to Figure 1-2 This invention provides a complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis, comprising: The fly ash water washing pretreatment unit has a solid-liquid separation device connected to its output end. The fly ash water washing pretreatment unit is a three-stage countercurrent water washing system, which includes a slurry adjustment tank, a first-stage hydrocyclone separator, a second-stage concentration washing tank and a third-stage fine washing tank connected in series. The liquid phase outlet of the third-stage fine washing tank is connected to the solid-liquid separation device.

[0033] The electrolysis treatment unit has its inlet connected to the liquid phase outlet of the solid-liquid separation device. The electrolysis treatment unit has an anode assembly, a cathode assembly, and an ion separator disposed between the anode assembly and the cathode assembly. The electrolysis treatment unit is a diaphragm electrolysis cell group, and the diaphragm is a cation exchange membrane or a bipolar membrane. The outer wall of the electrolysis treatment unit is fitted with a heat exchange jacket.

[0034] The circulating cooling unit has its cooling medium inlet and outlet connected to the heat exchange jacket of the electrolysis treatment unit. The circulating cooling unit includes a cooling tower, a circulating pump, and a variable frequency control valve. The opening degree of the variable frequency control valve and the speed of the circulating pump are both controlled by the central control unit.

[0035] The power supply control unit, electrically connected to the anode and cathode assemblies, is used to apply modulated power supply parameters to the electrolysis unit. The power supply control unit includes a rectifier module and a pulse width modulation module that are communicatively connected to the central control unit.

[0036] The data acquisition unit includes at least a temperature sensor, a pH sensor, a conductivity sensor, and an electrical signal sampler installed inside the electrolysis unit. The conductivity sensor is located on the liquid inlet line of the electrolysis unit, and its detection signal is converted into a salt concentration characterization value by the central control unit. The electrical signal sampler collects the current value I flowing through the electrodes and the voltage value U between the electrodes in real time.

[0037] The subsequent processing unit, whose input end is connected to the liquid outlet and exhaust port of the electrolysis unit, is used for resource recovery and harmless disposal of the products after electrolysis. The subsequent processing module includes: an MVR evaporation and crystallization unit connected to the liquid outlet of the electrolysis unit, used to concentrate and crystallize the electrolyte to recover industrial salt; a chlorine absorption unit connected to the exhaust port of the electrolysis unit, used to absorb the chlorine-containing gas generated by electrolysis through alkaline spraying to generate hypochlorite by-products; and a high-temperature melting and solidification unit connected to the solid phase outlet of the solid-liquid separation device, used to melt and vitrify the dechlorinated fly ash to prepare building material aggregates.

[0038] The central control unit has its signal input terminal connected to the data acquisition module, and its control output terminal connected to the control terminals of the power supply control unit and the circulating cooling unit, respectively. The central control unit is an industrial programmable logic controller or an embedded industrial computer, and its human-machine interface includes a parameter setting module and an alarm module.

[0039] The central control unit has a built-in multi-parameter coupled decision model calculation module and a weight factor adaptive adjustment module. The central control unit is configured to receive real-time electrolyte temperature, pH value, salt concentration characterization value and electrode polarization characterization value fed back by the data acquisition module, input the above data into the multi-parameter coupled decision model calculation module, calculate the target power supply parameters that optimize the overall electrolysis performance, and then output control signals to the power supply control unit to adjust the output current density and cell voltage. At the same time, it synchronously outputs control signals to the circulating cooling unit according to the temperature deviation value to adjust the cooling medium flow rate.

[0040] Furthermore, in this embodiment, the multi-parameter coupled decision model calculation module of the central control unit executes each algorithm in the following order: First, the data acquisition unit collects real-time data in four dimensions at a period of 0.5 seconds; second, the multi-parameter coupled decision model calculation module reads the current weight factors (updated in real time by the weight factor adaptive adjustment module) and substitutes them into the comprehensive performance evaluation function. The calculation is performed; then, the optimal current density is solved iteratively using the gradient ascent method; finally, the updated current density value is output to the power supply control unit for execution. The above algorithm is executed cyclically in each control cycle (0.5 seconds).

[0041] In this embodiment, the multi-parameter coupled decision model computation module is based on the comprehensive performance evaluation function. Perform optimization calculations and comprehensive performance evaluation functions. The expression is: in: The theoretical current efficiency coefficient is determined in real time by the central control unit based on the salt concentration characterization value. When the salt concentration is high... A larger value allows the system to pursue higher current efficiency; when the salt concentration is low... The value decreases accordingly; Temperature-related factors; The optimal pH value for the reaction; The change in inter-electrode resistance is calculated from the real-time voltage and current values ​​collected by the electrical signal sampler. This is the initial inter-electrode resistance; and These are the acidity / alkalinity weighting factor and the deposition state weighting factor, respectively.

[0042] Specifically, the theoretical current efficiency coefficient η is determined as follows: the central control unit has a pre-stored table of the correspondence between salt concentration C and theoretical current efficiency coefficient (this table was obtained through laboratory calibration experiments, using fly ash washing liquid as the electrolyte, at a temperature of 45℃, pH=7.0, and a current density of 150A / m). 2 (Measured under standard conditions). In actual operation, the central control unit performs linear interpolation based on the real-time salt concentration characterization value C fed back by the conductivity sensor to look up the table and output the corresponding η value in real time.

[0043] Furthermore, temperature influence factors The expression is: in: The real-time electrolyte temperature is fed back by the temperature sensor. For the optimal reaction temperature, For extreme tolerance temperature, Temperature sensitivity coefficient.

[0044] Furthermore, the central control unit is based on the comprehensive performance evaluation function. The gradient ascent method is used to calculate and output the target current density in real time. : in: The current density at the current moment, The learning step size factor has a value range of 0.05 to 0.1. The perturbation step size ranges from 0.5 to 1.0 A / m. 2 When the comprehensive performance evaluation function The absolute value of the partial derivative with respect to current density is less than the convergence criterion. When the search for the optimal solution has converged, it is determined that the search has been completed.

[0045] Specifically: Apply pressure to both sides of the current working point. The small current disturbance is measured to determine the resulting comprehensive performance evaluation function. The change in the numerical gradient is used to calculate the numerical gradient. Then, along the gradient ascent direction with step size Update the current density, gradually approximating the desired value. Maximum optimal current density value .

[0046] When the comprehensive performance evaluation function The absolute value of the partial derivative with respect to current density is less than the convergence criterion. When the optimization is deemed convergent, the iteration is stopped. Among them, the convergence criterion The range of values ​​is .

[0047] To verify the effectiveness of the comprehensive performance evaluation function and gradient ascent optimization method in this embodiment, a small-scale laboratory setup (5L effective volume electrolytic cell, 0.02m² electrode area) was used. 2 The electrolyte was fly ash washing liquid from a waste incineration power plant (the salt concentration was adjusted by adding NaCl). Comparative tests were conducted under simulated operating conditions. Real-time data from temperature sensors, pH sensors, conductivity sensors, and electrical signal samplers were recorded during the tests, and calculations were performed according to the above formula. The values ​​and specific test results are as follows: Operating Condition 1: Steady-State Reference Condition Operating parameters: salt concentration .

[0048] Model parameters: .

[0049] Calculation of temperature influence factor: pH penalty: Deposition penalty: Comprehensive performance evaluation function value: Operating Condition 2: High Salt Concentration Condition Operating parameters: salt concentration .

[0050] Calculation of temperature influence factor: pH penalty: Deposition penalty: Comprehensive performance evaluation function value: Operating Condition 3: Temperature deviates from operating condition Operating parameters: , 1. Salt concentration .

[0051] Calculation of temperature influence factor: pH penalty: Deposition penalty: Comprehensive performance evaluation function value: Operating Condition 4: pH deviates from operating condition Operating parameters: , 6.3, Salt concentration .

[0052] Calculation of temperature influence factor: pH penalty: Deposition penalty: Comprehensive performance evaluation function value: The table below shows a comprehensive comparison of the four types of operating conditions: The central control unit has a built-in temperature safety threshold comparison module, and the judgment logic of the temperature safety threshold comparison module is configured as follows: When the real-time electrolyte temperature exceeds the first safety threshold but is lower than the second safety threshold, the central control unit sends a gradient current reduction command to the power supply control unit and a current increase command to the circulating cooling unit. The first safety threshold is lower than the second safety threshold. When the real-time electrolyte temperature exceeds the second safety threshold, the central control unit sends a step-by-step command to the power supply control unit to cut off the power supply branch of the single tank.

[0053] The central control unit has a built-in temperature PID control module, which is independent of the current optimization loop and adjusts the temperature based on the temperature deviation value. Proportional and integral components, output cooling flow correction value : in: This is the proportionality coefficient. The integral coefficient is... The sampling period.

[0054] Example 2: This example describes the electrolyte aging status assessment module and the weight factor adaptive adjustment module based on Example 1.

[0055] The data acquisition unit also includes a redox potential sensor and a total organic carbon analyzer installed inside the electrolysis processing unit, and the central control unit has a built-in electrolyte aging status assessment module. The aging condition assessment module uses real-time oxidation-reduction potential values ​​fed back by the oxidation-reduction potential sensor. The real-time total organic carbon concentration fed back by the total organic carbon analyzer and cumulative electrolysis operating time The electrolyte aging index is calculated according to the following formula. : in: The initial redox potential of fresh electrolyte. The upper limit of the permissible total organic carbon concentration, Design lifespan for the electrolyte. , , This is the aging weighting coefficient. ; Aging Index The value range is from 0 to 1. =0 indicates that the electrolyte is in a completely fresh state. =1 indicates that the electrolyte has reached the end of its service life. When the preset aging threshold is exceeded, the central control unit issues a fluid replacement warning signal.

[0056] Data verification: During the operation of a certain batch, the initial redox potential of the fresh electrolyte was measured. Initial total organic carbon concentration =85 mg / L, electrolyte design life The maximum allowable total organic carbon concentration The aging weighting coefficient is set to The preset aging threshold is 0.85.

[0057] The aging index and related operating parameters at various time points during continuous system operation are recorded as follows: Example of aging index calculation: The system has been running continuously for... Redox potential sensor feedback = Total organic carbon analyzer feedback Substitute into the aging index formula: to 248 hour, = , Aging index: When the aging index approaches the preset aging threshold of 0.85, the abnormal alarm module issues a fluid replacement warning signal.

[0058] Introducing current efficiency comparison data before and after aging assessment: As shown in the table above, without aging assessment, the current efficiency continuously decreased from 91.8% to 68.3% as the operating time increased, a decrease of 23.5 percentage points. However, after aging assessment was introduced, the system adjusted the operating parameters in a timely manner according to the aging index. After 240 hours of operation, the current efficiency was still maintained at 80.5%, and the decrease was controlled within 11.3 percentage points. The introduction of aging assessment extended the effective service life of the electrolyte from about 150 hours to about 230 hours, an extension of 53.3%.

[0059] The weight factor adaptive adjustment module extracts running status features using a sliding time window. The width of the sliding time window is N=60 sampling points, corresponding to the sampling period. =0.5 seconds, window duration 30 seconds; The weight factor adaptive adjustment module calculates the temperature fluctuation amplitude in real time. pH fluctuation range and electrode polarization rate : Based on the current status of the above three indicators and the aging index The temperature sensitivity coefficient is updated synchronously using fuzzy logic reasoning rules. pH weighting factor and sedimentation state weighting factor The core logic of the fuzzy inference rule base is as follows: Among them, "high," "medium," and "low" represent the fuzzy membership states of each indicator, divided by pre-set thresholds; big"," middle"," "Small" indicates a significant, medium, or slight increase in the corresponding weight, respectively; "(Regression Benchmark)" indicates that the weights are regressed to the initial benchmark value. .

[0060] The updated weight values ​​are output after being filtered by a first-order low-pass filter to avoid oscillations in control commands caused by frequent changes in weight factors. in, These are the filter coefficients, with values ​​ranging from 0.1 to 0.3. and Using the same smoothing logic, ultimately, the smoothed , , Real-time input into comprehensive performance evaluation function It participates in the calculation.

[0061] Data verification: Weighted adjustment operation example: In a certain operation window, the temperature data reported by the temperature sensor within 30 seconds is 44.8~47.2℃. Calculate the temperature fluctuation range. The pH sensor reported a pH range of 6.85 to 7.15, which was calculated to be... The rate of change of the inter-electrode resistance R fed back by the electrical signal sampler within 30 seconds is... = aging index .

[0062] The state combinations of the above four indicators are as follows: middle, middle, middle, In the process of matching rule 5 from the fuzzy inference rule base (when all indicators are at a medium level, slightly increase the constraint weight), the fuzzy inference output is: .

[0063] The current weight value is Fuzzy reasoning output , The filter coefficients are taken as follows: After first-order low-pass filtering: The following table shows a comparison of data before and after the introduction of adaptive weight adjustment: The following table compares the effects of adaptive weight adjustment under different operating conditions: As can be seen from the table above, the adaptive weight adjustment has the most significant improvement effect under complex fluctuation conditions, and under comprehensive fluctuation conditions... The value increased by 17.7%, verifying the effectiveness of the fuzzy logic weight adaptive adjustment mechanism.

[0064] Example 3: Based on Examples 1 and 2 above, this example further illustrates the graded protection logic under abnormal operating conditions, reverse pulse cleaning, and long-term operation verification data.

[0065] The power supply control unit includes a rectifier module and a pulse width modulation module that are connected in communication with the central control unit. When the real-time pH value fed back by the pH sensor deviates from the set range, the central control unit fine-tunes the potential distribution ratio between the anode and cathode components through the pulse width modulation module.

[0066] Data verification: During a certain operation, due to the anode chamber Localized decreases in concentration exacerbate oxygen evolution side reactions. (With increased precipitation), the pH value in the anode chamber dropped sharply from 3.2 to 1.8, while the pH value in the cathode chamber rose from 11.5 to 12.8.

[0067] After pH sensor 62 detects an abnormal pH, the central control unit fine-tunes the potential distribution ratio between the anode and cathode through the pulse width modulation module. (1) Do not change the total current density (maintain the current optimization value of 155A / m) 2 ); (2) Reduce the anode pulse duty cycle from 50% to 45% (reduce the anode reaction intensity) and increase the cathode pulse duty cycle from 50% to 55% (increase the cathode reaction intensity); (3) After 5 minutes of fine-tuning, the pH of the anode chamber rose back to 2.5, and the pH of the cathode chamber fell back to 12.0.

[0068] The comparison data of pH fine-tuning effects are shown in the table below: When the rate of change of the electrode polarization characterization value exceeds the preset range, the central control unit applies a reverse pulse voltage to the anode and cathode components through the pulse width modulation module to suppress the densification growth of deposits on the electrode surface.

[0069] Although embodiments of the invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the appended claims and their equivalents.

Claims

1. A complete set of equipment for the co-processing and resource utilization of fly ash from waste incineration by electrolysis, characterized in that, include: The fly ash water washing pretreatment unit has a solid-liquid separation device connected to its output end; An electrolysis treatment unit has its inlet connected to the liquid phase outlet of the solid-liquid separation device. The electrolysis treatment unit has an anode assembly, a cathode assembly, and an ion separator disposed between the anode assembly and the cathode assembly. The circulating cooling unit has its cooling medium inlet and outlet connected to the heat exchange jacket of the electrolysis treatment unit; A power supply control unit, electrically connected to the anode assembly and the cathode assembly, is used to apply modulated power supply parameters to the electrolysis processing unit; The data acquisition unit includes at least a temperature sensor, a pH sensor, a conductivity sensor, and an electrical signal sampler disposed inside the electrolysis processing unit. The subsequent processing unit has its input end connected to the liquid outlet and exhaust port of the electrolysis processing unit, and is used to recycle and harmlessly dispose of the products after electrolysis. The central control unit has its signal input terminal connected to the data acquisition module and its control output terminal connected to the control terminals of the power supply control unit and the circulating cooling unit, respectively. The central control unit has a built-in multi-parameter coupled decision model calculation module and a weight factor adaptive adjustment module. The central control unit is configured to: receive real-time electrolyte temperature, pH value, salt concentration characterization value and electrode polarization characterization value fed back by the data acquisition module; input the above data into the multi-parameter coupled decision model calculation module to calculate the target power supply parameters that optimize the overall electrolysis performance; and then output control signals to the power supply control unit to adjust the output current density and cell voltage. At the same time, it synchronously outputs control signals to the circulating cooling unit according to the temperature deviation value to adjust the cooling medium flow rate.

2. The complete set of equipment for the co-processing and resource utilization of fly ash from waste incineration by electrolysis according to claim 1, characterized in that, The multi-parameter coupled decision model computation module is based on the comprehensive performance evaluation function. The comprehensive performance evaluation function is used for optimization calculation. The expression is: in: The theoretical current efficiency coefficient is determined in real time by the central control unit based on the salt concentration characterization value. Temperature-related factors; The optimal pH value for the reaction; The change in inter-electrode resistance is calculated from the real-time voltage and current values ​​collected by the electrical signal sampler. This is the initial inter-electrode resistance; and These are the acidity / alkalinity weighting factor and the deposition state weighting factor, respectively.

3. The complete set of equipment for the co-processing and resource utilization of fly ash from waste incineration by electrolysis according to claim 2, characterized in that, The temperature influence factor The expression is: in: The real-time electrolyte temperature is fed back by the temperature sensor. For the optimal reaction temperature, For extreme tolerance temperature, Temperature sensitivity coefficient.

4. A complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis according to claim 2, characterized in that, The central control unit is based on the comprehensive performance evaluation function. The gradient ascent method is used to calculate and output the target current density in real time. : in: The current density at the current moment, The learning step size factor has a value range of 0.05 to 0.

1. The perturbation step size ranges from 0.5 to 1.0 A / m. 2 When the comprehensive performance evaluation function The absolute value of the partial derivative with respect to current density is less than the convergence criterion. When the optimization is successful, the convergence criterion is determined. The range of values ​​is .

5. A complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis according to claim 1, characterized in that, The data acquisition unit also includes an oxidation-reduction potential sensor and a total organic carbon analyzer installed inside the electrolysis processing unit, and the central control unit has a built-in electrolyte aging status assessment module. The aging state assessment module uses the real-time oxidation-reduction potential value fed back by the oxidation-reduction potential sensor. The total organic carbon concentration reported by the total organic carbon analyzer in real time and cumulative electrolysis operating time The electrolyte aging index is calculated according to the following formula. : in: The initial redox potential of fresh electrolyte. The upper limit of the permissible total organic carbon concentration, Design lifespan for the electrolyte. , , This is the aging weighting coefficient. ; The aging index The value range is from 0 to 1, when When the preset aging threshold is exceeded, the central control unit issues a liquid replacement warning signal.

6. A complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis according to claim 5, characterized in that, The adaptive adjustment module for weighting factors extracts running status features using a sliding time window. The width of the sliding time window is N=60 sampling points, corresponding to a sampling period. =0.5 seconds, window duration 30 seconds; The weighting factor adaptive adjustment module calculates the temperature fluctuation amplitude in real time. pH fluctuation range and electrode polarization rate : Based on the current status of the above three indicators and the aging index The temperature sensitivity coefficient is updated synchronously using fuzzy logic reasoning rules. pH weighting factor and sedimentation state weighting factor The value of ; The updated weight values ​​are output after being filtered by a first-order low-pass filter: in, These are the filter coefficients, with values ​​ranging from 0.1 to 0.

3. and The same smoothing logic is used.

7. A complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis according to claim 1, characterized in that, The central control unit has a built-in temperature safety threshold comparison module, and the judgment logic of the temperature safety threshold comparison module is configured as follows: When the real-time electrolyte temperature exceeds the first safety threshold but is lower than the second safety threshold, the central control unit sends a gradient current reduction command to the power supply control unit and a current increase command to the circulating cooling unit, wherein the first safety threshold is lower than the second safety threshold. When the real-time electrolyte temperature exceeds the second safety threshold, the central control unit sends a step-by-step instruction to the power supply control unit to cut off the power supply branch of the single tank.

8. A complete set of equipment for the co-processing and resource utilization of fly ash from waste incineration by electrolysis according to claim 1, characterized in that, The power supply control unit includes a rectifier module and a pulse width modulation module that are communicatively connected to the central control unit; When the real-time pH value fed back by the pH sensor deviates from the set range, the central control unit fine-tunes the potential distribution ratio between the anode assembly and the cathode assembly through the pulse width modulation module; When the rate of change of the electrode polarization characterization value exceeds a preset range, the central control unit applies a reverse pulse voltage to the anode assembly and the cathode assembly through the pulse width modulation module to suppress the densification growth of deposits on the electrode surface.

9. A complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis according to claim 1, characterized in that, The subsequent processing module includes: The MVR evaporation and crystallization unit, which is connected to the outlet of the electrolysis treatment unit, is used to concentrate and crystallize the electrolyte to recover industrial salt. A chlorine absorption unit connected to the exhaust port of the electrolysis treatment unit is used to absorb the chlorine-containing gas generated by electrolysis by alkaline spraying to generate hypochlorite byproduct. And a high-temperature melting and solidification unit connected to the solid phase outlet of the solid-liquid separation device, used to melt and vitrify the dechlorinated fly ash to prepare building material aggregate.

10. A complete set of equipment for the co-processing and resource recovery of fly ash from waste incineration by electrolysis according to claim 1, characterized in that, The fly ash water washing pretreatment unit is a three-stage countercurrent water washing system, which includes a slurry conditioning tank, a primary hydrocyclone separator, a secondary concentration washing tank, and a tertiary fine washing tank connected in series. The liquid phase outlet of the tertiary fine washing tank is connected to the solid-liquid separation device. The electrolysis treatment unit is a diaphragm electrolysis cell group, and the diaphragm is a cation exchange membrane or a bipolar membrane. The heat exchange jacket is sleeved on the outer wall of the electrolysis treatment unit. The central control unit also has a temperature PID regulation module. The central control unit is an industrial programmable logic controller or an embedded industrial computer. Its human-machine interface is equipped with a parameter setting module and an abnormal alarm module. The abnormal alarm module is used to issue an audible and visual alarm signal when the real-time electrolyte temperature exceeds the limit threshold or the pH value exceeds the set range.

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