Multi-parameter cooperative control dosing method and system for coal gasification settling tank

Abstract

The invention relates to the technical field of coal chemical industry wastewater treatment, discloses a multi-parameter cooperative control dosing method and system for a coal gasification settling tank, and solves the problems that existing manual or single-parameter dosing is low in precision, high in drug consumption, slow in response and difficult in effluent reaching the standard. The method comprises the following steps: monitoring turbidity, hardness, pH and temperature at a water inlet and a water outlet of a settling tank on line, calculating the dosage in a grading manner according to a sequence of hardness control priority, pH regulation second order and turbidity control last order, dynamically correcting the dosage in combination with a PID (Proportion Integration Differentiation) algorithm, and re-executing grading dosage if the effluent does not reach the standard. The method can improve the control precision, reduce the drug consumption, accelerate the response speed, and meet the green development requirements of the coal chemical industry.

Description

Technical Field

[0001] This invention relates to the field of coal chemical wastewater treatment technology, specifically to a multi-parameter coordinated control dosing method and system for coal gasification settling tanks. Background Technology

[0002] Aerospace pulverized coal gasification furnaces are core equipment in the coal chemical industry. The ash water they produce contains a large amount of pulverized coal particles and calcium and magnesium ions, characterized by high turbidity and high hardness. It must be treated in a settling tank before entering the subsequent wastewater treatment system. Existing technologies mostly use manual timed dosing or single-parameter control for dosing, which cannot be precisely adjusted according to real-time changes in water quality. The dosing method is crude and the control precision is low, which not only leads to serious waste of reagents and unstable treatment effects, but also, because it does not consider the interaction between parameters such as turbidity, hardness, and pH, improper dosing sequence can easily cause reagent failure and increase treatment costs. At the same time, the existing control algorithms are not adapted to the characteristics of small particle size and strong colloidal stability of ash water pulverized coal particles, making it difficult to consistently meet the effluent turbidity standards. Hardness control is mostly based on experience in adding reagents, lacking scientific calculation basis. Improper dosage can easily cause subsequent treatment problems or excessive hardness. Moreover, simple feedback control has a long response time and lacks a timely correction mechanism, making it easy for the effluent to fail to meet standards.

[0003] Therefore, how to provide an automated dosing method that can achieve multi-parameter coordination, precise control, rapid response, and stable effluent has become a key problem that urgently needs to be solved by those skilled in the art. Summary of the Invention

[0004] In view of the above problems, the present invention is proposed to provide a multi-parameter coordinated control method for dosing in a coal gasification settling tank to overcome or at least partially solve the above problems.

[0005] To achieve the above objectives, the present invention adopts the following technical solution: S1. Real-time collection of influent water quality parameters and effluent water quality parameters, including turbidity, hardness, and pH value. S2. Based on the collected influent water quality parameters and the chemical reaction influence relationship of the influent water quality parameters, determine the priority order as follows: hardness control as the first priority, pH adjustment as the second priority, and turbidity control as the last priority. S3. In accordance with the aforementioned priority order, administer the hardness control dosing, pH adjustment dosing, and turbidity control dosing in sequence. When performing the dosing operation corresponding to each priority, the dosage of the corresponding agent is calculated based on the current water quality parameters and the dosing is performed, and a preset reaction waiting time is reserved after each dosing. S4. Based on the deviation between the effluent turbidity and the preset turbidity target value, a PID control algorithm is used to dynamically correct the dosage of the turbidity control agent. S5. Monitor the effluent water quality parameters in real time. If the preset water quality standards are not met, return to S3 to re-execute the graded dosing calculation and operation.

[0006] Preferably, in step S3, the hardness control dosing includes: S31. Based on the preset hardness target value, calculate the basic dosage of lime slurry according to the difference between the hardness of the influent and the hardness target value, the treatment volume of the settling tank and the concentration of lime slurry. S32. Introduce a first temperature correction coefficient to adjust the basic dosage to obtain the final lime slurry dosage; S33. Add lime slurry according to the final amount of lime slurry to be added, and wait for the first preset reaction time.

[0007] Preferably, in step S3, the pH adjustment dosing includes: S34. Based on the preset pH target range, calculate the required amount of acid or alkali solution to be added according to the deviation between the pH value of the influent and the pH target range. S35. Based on the treatment volume of the settling tank and the storage concentration of the acid or alkali solution, determine the actual dosage and perform the dosage, then wait for the second preset reaction time.

[0008] Preferably, in step S3, the turbidity control dosing includes: S36. Based on the preset turbidity target value, determine the basic dosage concentration of flocculant according to the influent turbidity value; S37. The base dosage concentration is adjusted by introducing a second temperature correction coefficient and a pH correction coefficient in sequence. The product of the adjusted base dosage concentration and the preset safety factor is the final dosage concentration of the flocculant. S38. Calculate the basic dosage of flocculant and perform dosing based on the final dosage concentration, the amount of water treated in the settling tank, and the storage concentration of flocculant.

[0009] Furthermore, the specific process of dynamically correcting the dosage of turbidity control drugs using a PID control algorithm includes: e(t) = Turcurrent - Turtarget; Where e(t) is the correction bias; Turcurrent is the target turbidity value; Turtarget is the effluent turbidity; K(t)=Kp×e(t)+Ki×∫e(t)dt+Kd×de(t) / dt; Where Kp is the proportional coefficient, Ki is the integral coefficient, and Kd is the differential coefficient; The revised dosage is: Q 修正 =Q 计算 ×K(t) Among them, Q 修正 Q represents the corrected dosage. 计算 This is the base dosage of the flocculant.

[0010] Preferably, the influent water quality parameter collection and effluent water quality parameter collection adopt a matched frequency.

[0011] In addition, the present invention also discloses a multi-parameter collaborative control dosing system for a coal gasification settling tank, used to implement any of the above-mentioned multi-parameter collaborative control dosing methods for a coal gasification settling tank, wherein the system adopts a PLC control system.

[0012] The beneficial effects of the above-described technical solutions provided in the embodiments of the present invention include at least the following: 1. The present invention significantly improves the control precision, ensuring that the turbidity and hardness of the effluent meet the standards. It greatly improves the control effect compared with the traditional single-parameter control method, while significantly reducing the consumption of chemicals, such as flocculants, lime milk, and alkali solutions, thereby reducing the cost of chemicals. 2. The system has a fast response speed and adopts hierarchical time-sequential control, which shortens the response time compared with traditional methods. It can quickly adjust when the water quality fluctuates, avoiding the effluent water quality exceeding the standard. It has good operational stability. Through multi-parameter collaborative control, it avoids the one-sidedness of single-parameter control. Hierarchical dosing avoids mutual interference of chemicals, ensuring the continuous and stable operation of the system. 3. High degree of automation, with automatic monitoring, calculation and dosing throughout the process, requiring no manual intervention, saving labor costs and reducing human error; 4. Highly adaptable, specifically optimized for the characteristics of coal gasification processes, and able to adapt to scenarios with large fluctuations in water quality and high-temperature process water. 5. Significant economic benefits: It can reduce pipe scaling to lower cleaning costs, reduce the load on subsequent sewage treatment, and reduce overall operating costs. 6. Significant environmental benefits: Precise dosing reduces chemical emissions, ensures stable effluent quality, avoids the risk of exceeding environmental standards, and meets the green development requirements of the coal chemical industry. Attached Figure Description

[0013] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.

[0014] Figure 1 This is a flowchart of a multi-parameter coordinated control dosing method for a coal gasification settling tank provided in an embodiment of the present invention; Figure 2 This is a comparison chart of turbidity changes between a multi-parameter coordinated control dosing method for coal gasification settling tank provided in this embodiment of the invention and a traditional method; Figure 3 This is a comparison chart of the hardness variation between a multi-parameter coordinated control dosing method for coal gasification settling tank provided in this embodiment of the invention and a traditional method. Figure 4 This is a comparison chart of pH value changes between a multi-parameter coordinated control dosing method for coal gasification settling tank provided in this embodiment of the invention and a traditional method. Figure 5 This is a schematic diagram of a multi-parameter collaborative control dosing system for a coal gasification settling tank provided in an embodiment of the present invention. Detailed Implementation

[0015] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0016] like Figure 1 As shown, in one embodiment, the present invention includes the following steps: S1. Real-time collection of influent and effluent water quality parameters, including turbidity, hardness, and pH value. S2. Based on the collected influent water quality parameters and the chemical reaction relationship of the influent water quality parameters, the priority order is determined as follows: hardness control is the first priority, pH adjustment is the second priority, and turbidity control is the last priority. S3. In order of priority, administer the hardness control dosing, pH adjustment dosing, and turbidity control dosing in sequence. When performing the dosing operation corresponding to each priority, the dosage of the corresponding agent is calculated based on the current water quality parameters and the dosing is performed, and a preset reaction waiting time is reserved after each dosing. S4. Based on the deviation between the effluent turbidity and the preset turbidity target value, a PID control algorithm is used to dynamically correct the dosage of turbidity control chemicals. S5. Monitor the effluent water quality parameters in real time. If the preset water quality standards are not met, return to S3 to re-execute the graded dosing calculation and operation.

[0017] In one embodiment, hardness control dosing includes: S31. Based on the preset hardness target value, calculate the basic dosage of lime slurry according to the difference between the hardness of the influent and the hardness target value, the treatment volume of the settling tank and the concentration of lime slurry. S32. Introduce a first temperature correction coefficient to adjust the basic dosage to obtain the final lime slurry dosage; S33. Add lime slurry according to the final amount required, and wait for the first preset reaction time. Specifically: When the target hardness > 1100 mg / L, initiate the hardness-controlled dosing operation. Dosing amount calculation: ΔH=H curren tH target Among them, H current H represents the current influent hardness. target The target hardness is 1100 mg / L; Ca(OH) 2理论需求量 =ΔH×0.37mg / L; Where 0.37 is the stoichiometric coefficient, based on the reaction: Ca(OH)₂ + Ca²⁺ + +2HCO3 - →2CaCO3↓+2H2O Ca(OH) 2实际需求量 =Ca(OH) 2理论需求量 / 0.85 Where 0.85 represents the reaction efficiency. Lime slurry dosage = Ca(OH) 2实际需求量 ×Q / (C lime ×1000); Where Q is the water treatment capacity in m³ / h, and C lime The concentration of lime slurry is mg / L; Introducing a first temperature correction factor: K temp =1+(25-T)×0.015, where T is the actual temperature.

[0018] Final dosage = Lime slurry dosage × K temp ; Waiting time after application: 8-10 minutes.

[0019] In one embodiment, step S3, pH adjustment dosing includes: S34. Based on the preset pH target range, calculate the required amount of acid or alkali solution to be added according to the deviation between the pH value of the influent and the pH target range. S35. Based on the treatment capacity of the settling tank and the storage concentration of the acid or alkali solution, determine the actual dosage and execute the dosage, then wait for the second preset reaction time. Specifically: When pH < 7.8 or pH > 8.8, initiate the pH-controlled dosing operation. Dosage calculation: [H + ] current =10^(-pH current ), [H + ] target =10^(-pH target ) Δ[H + ]=[H + ] current -[H + ] target , [OH - ] need =Δ[H + ]×K buffer Where K buffer The buffer coefficient is set to 1.5-2.0.

[0020] C NaOH =[OH - ] need ×40×1000mg / L Where 40 is the molecular weight of NaOH.

[0021] NaOH dosage (L / h) = C NaOH ×Q / (C NaOH_stock ×1000) Among them, C NaOH_stock The storage concentration of NaOH is mg / L.

[0022] Waiting time after application: 3-5 minutes.

[0023] In one embodiment, turbidity control dosing includes: S36. Based on the preset turbidity target value, determine the basic dosage concentration of flocculant according to the influent turbidity value; S37. The second temperature correction coefficient and pH correction coefficient are introduced in sequence to adjust the basic dosage concentration. The product of the adjusted basic dosage concentration and the preset safety factor is the final dosage concentration of the flocculant. S38. Calculate the base dosage of flocculant based on the final dosage concentration, the treated water volume in the settling tank, and the stored concentration of flocculant, and then administer the dosage. Specifically: When turbidity > 20 NTU, initiate the turbidity control dosing operation. Dosing amount calculation: When 20 NTU < turbidity ≤ 30 NTU: C flocculant =5mg / L, where C flocculant This represents the basic concentration of flocculant added; When 30 < turbidity ≤ 100 NTU: C flocculant =5 + (turbidity - 30) × 0.15, where 0.15 represents the turbidity correction factor; When turbidity > 100 NTU: C flocculant =15.5+(turbidity-100)×0.1, where 0.1 represents the turbidity correction factor.

[0024] Based on the determined flocculant dosage concentration C flocculant Introduce a temperature correction factor based on this: K temp =1+(25-T)×0.02 pH correction factor: K pH= 1.0 (pH 7.0-8.5 range) or 1.2 (pH < 7.0 or > 8.5) Final dosage concentration: C final =C flocculant ×K temp ×K pH ×K safety Where C final For the final dosage concentration, C flocculant K represents the basic dosage concentration. temp K represents the temperature correction factor. pH K represents the pH correction factor. safety The safety factor is 1.1-1.2.

[0025] The basic dosage of flocculant (L / h) = C final ×Q / (C stock ×1000) Among them, C stock The concentration of the flocculant is mg / L, and Q is the volume of water to be treated.

[0026] The temperature correction factor mentioned above is calculated based on the difference between the real-time collected temperature and the reference temperature, and is used to compensate for the impact of temperature changes on reaction efficiency.

[0027] In one embodiment, step S4, which involves dynamically correcting the dosage of turbidity control drug using a PID control algorithm, includes the following steps: e(t) = Turcurrent - Turtarget; Where e(t) is the correction bias; Turcurrent is the target turbidity value; Turtarget is the effluent turbidity; K(t)=Kp×e(t)+Ki×∫e(t)dt+Kd×de(t) / dt; Where Kp is the proportional coefficient, Ki is the integral coefficient, and Kd is the differential coefficient; The revised dosage is: Q 修正 =Q 计算 ×K(t) Among them, Q 修正 Q represents the corrected dosage. 计算 This is the base dosage of the flocculant.

[0028] Specifically, Kp = 0.5-1.0 (proportionality coefficient) Ki = 0.01 - 0.05 (integral coefficient) Kd = 0.1 - 0.2 (differential coefficient) When K(t)>1, increase the dosage to reduce turbidity; when K(t)<1, reduce the dosage to prevent overtreatment. This feedback adjustment mechanism can achieve turbidity control within ±2 NTU within ±5 minutes.

[0029] Meanwhile, the collection of influent and effluent water quality parameters adopts a matching frequency to ensure data synchronization and control response timeliness.

[0030] The technical solution of this application will be described in detail below with specific scenarios. In an example of an application under a typical operating condition: Water treatment capacity: Q = 50 m³ / h; Inlet turbidity: 120 NTU; Inlet water hardness: 1500 mg / L CaCO3; Inlet water pH: 7.2; Water temperature: 55℃.

[0031] Control target: Effluent turbidity: ≤20 NTU; Water hardness: ≤1100 mg / L CaCO3; The pH of the effluent is 7.8-8.5.

[0032] Dosing parameters: Lime slurry concentration: 80 g / L (Ca(OH)2 content); NaOH solution concentration: 150 g / L; Polyacrylamide (PAM) concentration: 2000 mg / L; Specific control process: Step 1: Hardness Control Calculation process: ΔH = 1500 - 1100 = 400 mg / L CaCO3 Ca(OH) 2理论需求量 =400×0.37=148 mg / L; Considering a reaction efficiency η = 0.85: Ca(OH) 2实际需求量 =148 / 0.85=174 mg / L; Temperature correction: K temp =1+(25-55)×0.015=0.55; Lime slurry dosage = 174 × 50 / (80000 × 0.55) = 0.198 L / h; Actual dosage setting: 0.20 L / h, wait 8 minutes; Results: Hardness decreased to 1080 mg / L, pH increased to 8.1.

[0033] Step 2: pH Adjustment The current pH is 8.1, and the target pH is 8.0-8.5. Since the pH is within the range, no adjustment is needed, so skip this step.

[0034] Step 3: Turbidity Control Current turbidity: After treatment with lime slurry, the turbidity has been reduced to 85 NTU.

[0035] Calculation process: Because 30 < 85 ≤ 100: C flocculant =5+(85-30)×0.15=13.25 mg / L; Temperature correction: K temp =1+(25-55)×0.02=0.40; pH correction: K pH =1.0 (pH=8.1 within the range of 7.0-8.5); Safety factor: K safety =1.15; Final dosage concentration: C final =13.25×0.40×1.0×1.15=6.1 mg / L; Flocculant dosage = 6.1 × 50 / (2000 × 1000) = 0.153 L / h; Actual dosage setting: 0.15 L / h; Dosing time: Continuous dosing, settling time 20 minutes.

[0036] Processing effect: Effluent turbidity: 18 NTU, meeting the target ≤20 NTU); Water hardness: 1050 mg / L, meeting the target of ≤1100 mg / L; The effluent pH is 8.2, which meets the target of 7.8-8.5.

[0037] In an example of application under high turbidity conditions: Water treatment capacity: Q = 50 m³ / h; Inlet water turbidity: 280 NTU; Inlet water hardness: 1800 mg / L CaCO3; Inlet water pH: 6.8; Water temperature: 45℃.

[0038] Control process: Step 1: Hardness Control ΔH = 1800 - 1100 = 700 mg / L; Ca(OH) 2实际需求量 =700×0.37 / 0.85=305 mg / L; Temperature correction: K temp =1+(25-45)×0.015=0.70; Lime slurry dosage = 305 × 50 / (80000 × 0.70) = 0.272 L / h; Setting: 0.28 L / h; Results: Hardness decreased to 1050 mg / L, pH increased to 7.9.

[0039] Step 2: pH Adjustment pH=7.9, close to the target range, fine-tune: [H + ] current =10^(-7.9)=1.26×10 -8 ; [H + ] target =10^(-8.0)=1.00×10 -8 ; Δ[H + ] = 0.26 × 10 -8 ; [OH - ] need =0.26×10 -8 ×1.8=0.47×10 -8 mol / L; C NaOH=0.47×10 -8 ×40×1000×10 6 =0.19 mg / L; NaOH dosage = 0.19 × 50 / (150000 × 1000) = 0.000063 L / h The dosage is extremely small, with a minimum flow rate of 0.05 L / h, and the dosage is applied intermittently.

[0040] Step 3: Turbidity Control Current turbidity: 220 NTU (high turbidity); Because turbidity > 100: C flocculant =15.5+(220-100)×0.1=27.5 mg / L; Temperature correction: K temp =1+(25-45)×0.02=0.60; pH correction: K pH =1.0; Safety factor: K safety =1.2; C final =27.5×0.60×1.0×1.2=19.8 mg / L; Flocculant dosage = 19.8 × 50 / 2000000 = 0.495 L / h; Setting: 0.50 L / h.

[0041] Processing effect: Effluent turbidity: 19 NTU, meeting discharge standards; Water hardness: 1020 mg / L, meeting discharge standards; The effluent pH is 8.0, which meets the discharge standards.

[0042] This embodiment illustrates that even under abnormally high turbidity and high hardness conditions, the method of the present invention can still accurately calculate the dosage and achieve water quality compliance treatment.

[0043] In an example of a cryogenic application: Operating conditions: Water treatment capacity: Q = 50 m³ / h; Inlet water turbidity: 80 NTU; Inlet water hardness: 1300 mg / L CaCO3; Inlet water pH: 7.5; Water temperature: 15℃ (low temperature in winter).

[0044] Control characteristics: Because the temperature is low (15℃), the chemical reaction rate is slower, and the dosage of the drug needs to be increased.

[0045] Step 1: Hardness Control Ca(OH) 2实际需求量 =200×0.37 / 0.85=87 mg / L; Temperature correction: K temp =1+(25-15)×0.015=1.15; (Increase the dosage by 15% when the temperature is low) Lime slurry dosage = 87 × 50 / (80000 × 1.15) = 0.047 L / h; Setting: 0.05 L / h.

[0046] Step 3: Turbidity Control C flocculant =5 + (80 - 30) × 0.15 = 12.5 mg / L; Temperature correction: K temp =1+(25-15)×0.02=1.20; (Increase the dosage by 20% when the temperature is low) C final =12.5×1.20×1.0×1.15=17.25 mg / L; Flocculant dosage = 0.43 L / h.

[0047] Processing effect: Effluent turbidity: 18 NTU, meeting discharge standards; Water hardness: 1080 mg / L, meeting discharge standards.

[0048] like Figure 2-4 As shown, independent comparison scenarios for three key water quality indicators are clearly defined, and a two-group control design using both traditional methods and the method of this invention is uniformly adopted: Group 1: Comparison of turbidity changes (unit: NTU); Group 2: Comparison of hardness changes (unit: mg / L CaCO3); Group 3: Comparison of pH changes; Meanwhile, all comparisons are plotted on the horizontal axis (covering 0h, 6h, 12h, 18h, and 24h, fully presenting the effect of continuous operation over 24 hours), which can intuitively show the difference in performance between the two methods in long-term operation.

[0049] Regarding turbidity: The turbidity curve of this invention fluctuates slightly around the 20 NTU baseline throughout the entire process, with a very small fluctuation range. The period exceeding 20 NTU is extremely short and the deviation value is small. Most of the time, it can be stably controlled below 20 NTU, which fully meets the baseline requirements. In contrast, the turbidity curve of the traditional method fluctuates violently, frequently crossing the 20 NTU baseline, and the exceedance range is large. Even at key nodes such as 6h and 18h, there are obvious peaks. The long-term compliance rate is far lower than that of the method of this invention, and it cannot stably meet the turbidity baseline. Regarding hardness: the hardness curve of the method of the present invention remains stable below the 1100 mg / L CaCO3 baseline, with a narrow fluctuation range and no exceedance, which fully meets the hardness control target; in contrast, the hardness curve of the traditional method crosses the 1100 mg / L CaCO3 baseline multiple times, and the hardness value is significantly higher than the baseline in some periods, and the exceedance lasts for a long time, indicating that the traditional method has insufficient control precision of hardness. Regarding pH: The pH curve of this invention fluctuates slightly around the reference value of 8, with an extremely narrow fluctuation range and almost no significant deviation, thus accurately maintaining pH stability; in contrast, the pH curve of traditional methods has a wide fluctuation range and frequently deviates from the reference value of 8, failing to meet the requirements for precise pH control.

[0050] Looking at the 24-hour timeline, the three curves (turbidity, hardness, and pH) of the method of this invention showed no significant drift and remained within the baseline range throughout the entire process, demonstrating stable long-term control capabilities. In contrast, the curves of the traditional method showed a drifting trend over time, with the difficulty of achieving the target increasing further in the later stages, reflecting its lack of continuous correction capabilities and unsuitability for long-term continuous operation scenarios.

[0051] In addition, this invention also discloses a multi-parameter coordinated control dosing system for a coal gasification settling tank, used to implement a multi-parameter coordinated control dosing method for a coal gasification settling tank. The system adopts a PLC control system. Specifically: like Figure 5 As shown, the system includes a settling tank, an inlet, and an outlet. Online monitoring equipment (such as turbidity meters, hardness meters, pH meters, and temperature sensors) is deployed at the inlet and outlet to collect influent water quality parameters (turbidity, hardness, pH value, and temperature) and effluent water quality parameters in real time. The system also includes dosing devices (such as lime slurry dosing devices, alkali dosing devices, and flocculant dosing devices), which are connected to the online monitoring equipment through a data acquisition and control system to achieve real-time monitoring of parameters and automatic calculation and adjustment of dosing amounts. This structure reflects a hardware layout for multi-parameter collaborative control, ensuring data synchronization and timely control response.

[0052] The above provides a detailed description of the multi-parameter coordinated control dosing method for a coal gasification settling tank provided by the present invention. Specific examples are used in this embodiment to illustrate the principle and implementation of the present invention. The description of the above embodiments is only for the purpose of helping to understand the method and core idea of ​​the present invention. At the same time, for those skilled in the art, there will be changes in the specific implementation and application scope based on the idea of ​​the present invention. Therefore, the content of this specification should not be construed as a limitation of the present invention.

[0053] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined in these embodiments may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A coal gasification settling tank multi-parameter collaborative control dosing method, characterized in that, The method comprises the following steps: S1, collecting water quality parameters of the influent and effluent in real time, wherein the collection of the water quality parameters of the influent and effluent both comprises turbidity, hardness, and pH value; S2, determining a priority order of hardness control as the primary priority, pH adjustment as the secondary priority, and turbidity control as the tertiary priority based on the collected water quality parameters of the influent and the chemical reaction influence relationship of the water quality parameters of the influent; S3, performing hardness control dosing, pH adjustment dosing, and turbidity control dosing in the priority order; wherein, when performing the dosing operation corresponding to each priority, the dosage of the corresponding medicament is calculated based on the current water quality parameters and is added, and a preset reaction waiting time is reserved after each addition; S4, based on the deviation of the effluent turbidity from a preset turbidity target value, using a PID control algorithm to dynamically correct the dosage of the turbidity control dosing; S5, monitoring the water quality parameters of the effluent in real time, and if the preset water quality standard requirement is not met, returning to S3 to re-perform the calculation and operation of the staged dosing.

2. The multi-parameter collaborative control dosing method for a coal gasification settling tank according to claim 1, characterized in that, In step S3, the hardness control dosing comprises: S31, taking a preset hardness target value as a reference, calculating the basic dosage of lime milk according to the difference between the influent hardness and the hardness target value, the treatment water volume of the settling tank, and the concentration of the lime milk; S32, introducing a first temperature correction coefficient to adjust the basic dosage to obtain the final dosage of the lime milk; S33, adding the lime milk according to the final dosage of the lime milk, and waiting for a first preset reaction time.

3. The multi-parameter collaborative control dosing method for a coal gasification settling tank according to claim 1, characterized in that, In step S3, the pH adjustment dosing comprises: S34, taking a preset pH target interval as a reference, calculating the dosage of the required acid or alkali according to the deviation of the influent pH value from the pH target interval; S35, combining the treatment water volume of the settling tank and the storage concentration of the acid or alkali to determine the actual dosage and perform the addition, and waiting for a second preset reaction time.

4. The multi-parameter collaborative control dosing method for a coal gasification settling tank according to claim 1, characterized in that, In step S3, the turbidity control dosing comprises: S36, taking a preset turbidity target value as a reference, determining the basic dosage concentration of the flocculant according to the influent turbidity value; S37, introducing a second temperature correction coefficient and a pH correction coefficient in sequence to adjust the basic dosage concentration, and the product of the adjusted basic dosage concentration and a preset safety factor is the final dosage concentration of the flocculant; S38, calculating the basic dosage of the flocculant according to the final dosage concentration, the treatment water volume of the settling tank, and the storage concentration of the flocculant, and performing the addition.

5. The multi-parameter collaborative control dosing method for a coal gasification settling tank according to claim 4, characterized in that, In step S4, the specific process of dynamically correcting the dosage of the turbidity control dosing using the PID control algorithm comprises: e(t) = Turcurrent - Turtarget; Wherein, e(t) is the correction deviation; Turcurrent is the turbidity target value; Turtarget is the effluent turbidity; K(t) = Kp × e(t) + Ki × ∫e(t)dt + Kd × de(t) / dt; Wherein, Kp is the proportional coefficient, Ki is the integral coefficient, and Kd is the differential coefficient; The modified dose is: Q 修正 = Q 计算 × K(t) wherein Q 修正 is the corrected dosage; Q 计算 is the base dosage of the flocculant.

6. The multi-parameter coordinated control dosing method for a coal gasification settling tank according to claim 1, characterized in that, The collection of the water quality parameters of the influent and the collection of the water quality parameters of the effluent use matching frequencies.

7. A coal gasification settling tank multi-parameter collaborative control dosing system for implementing the coal gasification settling tank multi-parameter collaborative control dosing method of any one of the preceding claims 1-6, wherein the system adopts a PLC control system.

Images