Control method based on atmospheric parameters and relative humidity in waste incineration deacidification process

Abstract

This invention discloses a control method based on atmospheric parameters and relative humidity during the desulfurization process of waste incineration, relating to the field of waste incineration flue gas purification technology. The method includes: acquiring real-time parameters during the waste incineration process; correcting and calculating atmospheric parameters; calculating relative humidity in real time; dynamically optimizing and adjusting the dosage of desulfurizing agent based on the atmospheric parameters and relative humidity; and having an actuator add the desulfurizing agent according to the adjusted dosage. This invention's control method based on atmospheric parameters and relative humidity during the waste incineration desulfurization process achieves dynamic optimization of the desulfurizing agent dosage by integrating a coupled calculation model of atmospheric pressure, temperature, and altitude, thereby improving desulfurization efficiency and reducing reagent consumption.

Description

Technical Field

[0001] This invention relates to the field of waste incineration flue gas purification technology, and in particular to a control method based on atmospheric parameters and relative humidity during the waste incineration deacidification process. Background Technology

[0002] In waste incineration flue gas desulfurization processes, semi-dry desulfurization is widely used due to its high efficiency and lack of wastewater discharge. However, existing technologies mainly rely on PID control or feedforward feedback control of the concentration and temperature of acidic gases in the flue gas, which has the following drawbacks:

[0003] Lack of humidity control: Existing methods do not accurately quantify the impact of flue gas humidity on the deacidification reaction, and only adjust the amount of deacidifying agent added by means of the pollutant emission index at the outlet and the outlet temperature of the reaction tower, resulting in large fluctuations in reaction efficiency.

[0004] Lack of atmospheric parameter compensation: Ignoring the effects of altitude and air pressure on flue gas humidity and reaction balance, problems such as excessive addition of deacidifying agent or insufficient reaction may occur in high-altitude or air pressure fluctuating scenarios.

[0005] Insufficient multivariate coupling control: No linkage control model for humidity, temperature, and acid gas concentration has been established, making it difficult to cope with dynamic changes under complex operating conditions.

[0006] Invention patent CN113041808B discloses a method and control system for controlling the dosage of lime slurry and cooling water in a deacidification tower. By using data on the concentration and temperature of acidic gases (HCl, SO2) in the flue gas, a combination of fuzzy rules and PID algorithms is employed to dynamically adjust the dosage of lime slurry and cooling water. The core steps include calculating the theoretical consumption of desuperheating water based on the inlet temperature and target outlet temperature, and correcting this based on outlet temperature feedback; and determining the lime slurry dosage through fuzzy control based on the real-time value and rate of change of acidic gas concentration at the chimney outlet. The system architecture includes modules for concentration acquisition, theoretical calculation, correction value calculation, and actuators, achieving feedforward-feedback composite control.

[0007] However, the above methods do not establish a direct quantitative model of humidity and reagent dosage; atmospheric parameter compensation is insufficient, and the influence of altitude and air pressure on water vapor saturation partial pressure and reaction equilibrium is not considered, resulting in decreased control accuracy in high-altitude or air pressure fluctuation scenarios; relying on empirical parameters, fuzzy rules and PID parameters need to be manually adjusted, and the adaptability to complex working conditions is limited, which can easily lead to problems such as over-dosing of reagents or insufficient reaction.

[0008] Invention patent CN108549223B discloses a method for controlling the humidification water ratio in a semi-dry flue gas desulfurization process. It constructs a feedforward-feedback cascade system, using the absorber outlet temperature as the feedback signal, combined with the desulfurizing agent flow rate and furnace radiation energy signal as the feedforward, and employs the RLS least squares algorithm to filter the radiation energy signal to optimize the humidification water ratio. The furnace radiation energy signal is introduced to reflect changes in fuel quantity, improving the system response speed; and the self-optimizing DE algorithm is used to tune the PID parameters to adapt to fluctuations in operating conditions.

[0009] However, the above methods are highly complex. The RLS algorithm and DE parameter tuning increase the computational load of the system, requiring high hardware and data processing capabilities, resulting in high engineering implementation costs. Environmental parameters are ignored, and the influence of environmental factors such as altitude and atmospheric pressure on the evaporation efficiency of humidifying water is not integrated. Humidity control relies on a single indicator of temperature and does not form a multivariate coupled model. The applicable scenarios are limited. The feedforward design for desulfurizer fluctuations does not fully consider the influence of water vapor content in flue gas on the reaction interface, and control lag is prone to occur under high humidity or low pressure environments.

[0010] Neither of the above methods establishes a quantitative correlation between "atmospheric parameters, humidity, and reagent dosage." The former relies on indirect control of temperature and acid gas concentration, while the latter focuses on feedforward compensation but ignores environmental parameters. Therefore, there is still room for improvement in the control methods for waste incineration flue gas desulfurization processes. Summary of the Invention

[0011] In view of this, embodiments of the present invention provide a control method based on atmospheric parameters and relative humidity during the deacidification process of waste incineration. By integrating a calculation model of atmospheric parameters and flue gas relative humidity, the deacidification agent can be optimized and controlled.

[0012] A method for controlling atmospheric parameters and relative humidity during waste incineration acid removal process, comprising:

[0013] Step S101: Obtain real-time parameters during the waste incineration process;

[0014] Step S102: Correct the calculated atmospheric parameters;

[0015] Step S103: Calculate relative humidity in real time;

[0016] Step S104: Dynamically optimize and adjust the dosage of deacidifying agent based on the atmospheric parameters and relative humidity;

[0017] Step S105: The actuator adds the deacidifying agent according to the adjusted dosage.

[0018] Preferably, in step S101, the real-time parameters include the flue gas temperature T at the outlet of the reaction tower, the flue gas pressure P at the inlet of the reaction tower, the water vapor content X in the flue gas, and the ambient altitude H.

[0019] Preferably, step S102 includes:

[0020] The atmospheric pressure is corrected based on the ambient altitude H, and the corrected atmospheric pressure is calculated using the following formula:

[0021] P corr =Pk·H

[0022] Among them, P corr P is the corrected atmospheric pressure, which is the flue gas pressure at the inlet of the reaction tower measured in real time by a pressure transmitter. k is the altitude pressure correction factor, and H is the ambient altitude obtained by the GPS positioning module.

[0023] Preferably, step S103 includes:

[0024] Step S1031: Calculate the saturated vapor pressure P T ;

[0025] Step S1032: Calculate the relative humidity PHI.

[0026] Preferably, in step S1031, the saturated vapor pressure P T The calculation formula is:

[0027]

[0028] Where T0 is the value obtained by normalizing the flue gas temperature T at the outlet of the reaction tower with the critical temperature of water, 647.3 K. M1 SUM is obtained by subtracting T0 from 1. It is a comprehensive calculation term, consisting of FK(1) to FK(5) and T. M1 The coefficients FK(1) to FK(5) are obtained by multiplying different powers and then adding them together. D1 is obtained by fitting a large amount of experimental data with T0 and the coefficients containing FK(6) and FK(7) about T. M1 The polynomials are multiplied together to obtain FK(6) and FK(7), which are also fitting coefficients. The numerator of D2 is T. M1 The denominator is composed of FK(8) and FK(9) and T. M1 The relevant terms are composed of FK(8) and FK(9), which are also fitting coefficients. BK is obtained by performing an exponential operation on SUM / D1-D2.

[0029] And / or, in step S1032, the formula for calculating relative humidity PHI is:

[0030]

[0031] Where X is the water vapor volume fraction, P corr This is the corrected atmospheric pressure.

[0032] Preferably, step S104 includes:

[0033] Step S1041: Determine if the relative humidity (PHI) is less than 6%. If so, increase the cooling water flow rate (Q). water If not, reduce the cooling water flow rate Q. water .

[0034] Preferably, step S104 further includes:

[0035] Step S1041': Calculate the lime slurry dosage correction function f(PHI);

[0036] Step S1042': Dynamically adjust the amount of lime slurry Qlime according to the lime slurry dosage correction function f(PHI).

[0037] Preferably, in step S1041, the cooling water flow rate adopts a PID algorithm: ΔQ water =K p ·e PHI +K i ∫e PHI dt+K d (d ePHI / dt), where Kp is the proportional gain, Ki is the integral gain, Kd is the derivative gain, and e is the relative humidity main loop control deviation. PHI =6-PHI;

[0038] And / or, in step S1041', the lime slurry addition amount correction function f(PHI) = sech(0.38|PHI-6|);

[0039] And / or, in step S1042', the amount of lime slurry added, Qlime = Q lime理论 / f(PHI), where PHI ranges from 5 to 7.

[0040] Preferably, step S104 further includes:

[0041] Step S1041”: If the outlet temperature of the reaction tower Tout < 130℃, the system will no longer increase the amount of cooling water added.

[0042] Preferably, the step S105 is followed by:

[0043] Step S106: Real-time monitoring of the waste incineration deacidification process;

[0044] Step S107: Determine whether optimization or adjustment is needed. If not, proceed directly to step S101; if yes, optimize the system parameters and then proceed to step S101.

[0045] The present invention provides a control method based on atmospheric parameters and relative humidity in the process of waste incineration deacidification. By integrating a coupled calculation model of atmospheric pressure, temperature and altitude, the method achieves dynamic optimization of the deacidification agent dosage, thereby improving deacidification efficiency and reducing agent consumption. Attached Figure Description

[0046] 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 some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0047] Figure 1 This is a schematic diagram of the control method based on atmospheric parameters and relative humidity during the waste incineration deacidification process of the present invention;

[0048] Figure 2 This is a schematic diagram illustrating the principle of the control method based on atmospheric parameters and relative humidity during the waste incineration deacidification process of the present invention.

[0049] Figure 3 This is a flowchart of the parameter acquisition process in this invention;

[0050] Figure 4 This is a flowchart of atmospheric parameter correction and relative humidity calculation in this invention;

[0051] Figure 5 This is a flowchart illustrating the process of adjusting the dosage of the deacidifying agent in this invention. Detailed Implementation

[0052] The embodiments of the present invention will now be described in detail with reference to the accompanying drawings.

[0053] It should be understood that the described embodiments are merely some, not all, of the embodiments of the present invention. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without inventive effort are within the scope of protection of the present invention.

[0054] This invention provides a control method based on atmospheric parameters and relative humidity during the desulfurization process of waste incineration, such as... Figure 1-2 As shown, it includes:

[0055] Step S101: Obtain real-time parameters during the waste incineration process;

[0056] This step involves real-time parameter acquisition, such as... Figure 3 As shown, the following parameters can be obtained in real time through sensors:

[0057] The temperature of the flue gas at the outlet of the reaction tower, T (unit: K): A thermocouple temperature sensor is used and installed at a point where the flue gas flow at the outlet of the reaction tower is stable and representative. Since the temperature of the flow field inside the reaction tower is difficult to detect directly, the temperature measured here is relatively close to the temperature inside the reaction tower and is representative.

[0058] The flue gas pressure P at the inlet of the reaction tower (unit: Pa) is achieved by using a pressure transmitter installed at the inlet of the reaction tower. This transmitter has high sensitivity and good stability, ensuring the real-time performance and accuracy of the pressure data.

[0059] Water vapor content in flue gas X (%vol): The water vapor content in flue gas is measured using advanced differential ultraviolet absorption spectroscopy (DOAS). This technique is based on Beer-Lambert's law and utilizes the differences in absorption characteristics of different gases to specific wavelengths of ultraviolet light to detect water vapor concentration. The analyzer has high sensitivity and selectivity, enabling accurate measurement of its water vapor content in flue gas. The measurement result is output in real time as a volume fraction percentage; for example, if the measured value is 10,000 ppm, then X = 1%vol.

[0060] Environmental altitude H (unit: meters): The current altitude information of the waste incineration plant is obtained through the GPS positioning module. Considering that the altitude changes very little in the short term, the data update frequency is set to once a month to save system resources.

[0061] This step can be implemented using a sensor module. Figure 3 The process of the sensor module acquiring various parameters is demonstrated. First, the thermocouple temperature sensor, pressure transmitter, gas analyzer, and GPS positioning module start working, respectively collecting data on the temperature, pressure, water vapor content, and ambient altitude of the reaction tower flue gas. The collected data is then transmitted to the data processing module for further processing via data transmission lines.

[0062] Step S102: Correct the calculated atmospheric parameters;

[0063] As an optional embodiment, step S102 includes:

[0064] The atmospheric pressure is corrected based on the altitude H, and the corrected atmospheric pressure is calculated using the following formula:

[0065] P corr =Pk·H

[0066] Among them, P corrThe corrected atmospheric pressure (Pa) is a pressure value obtained by taking into account the effect of altitude on the pressure based on the actual measured flue gas pressure P at the inlet of the reaction tower. This value is used for the subsequent accurate calculation of relative humidity, because changes in altitude significantly affect atmospheric pressure, and thus affect the partial pressure of water vapor and relative humidity in the flue gas.

[0067] P: The flue gas pressure (Pa) at the inlet of the reaction tower, which is measured in real time by a pressure transmitter, is the actual measured value.

[0068] k: Altitude pressure correction coefficient (Pa / m), obtained through fitting analysis of a large amount of local meteorological data. The altitude pressure correction coefficient k value will vary in different regions. For example, in plains, the typical value of k is about 0.1 Pa / m; in mountainous areas and other areas with complex terrain, the value of k needs to be accurately determined by fitting based on the specific local meteorological data and terrain characteristics.

[0069] H: The ambient altitude (m) obtained through the GPS positioning module is the current altitude of the waste incineration plant.

[0070] Step S103: Calculate relative humidity in real time;

[0071] As an optional embodiment, step S103 includes:

[0072] Step S1031: Calculate the saturated vapor pressure P T ;

[0073] In this step, the saturated vapor pressure P T The saturated vapor pressure P can be calculated using the following formula (based on the critical temperature normalization method, using polynomial fitting). T ):

[0074]

[0075] Where T0 is the value obtained by normalizing the flue gas temperature T at the reactor outlet to the critical temperature of water, 647.3 K. This normalization converts the temperature data into a relative value, facilitating subsequent calculations in a specific computational model. It reflects the relative position of the current temperature within the critical temperature system of water.

[0076] T M1 : Obtained by subtracting T0 from 1, it is an intermediate variable used in subsequent calculations and plays a role in adjusting and relating various parameters in the entire calculation system.

[0077] SUM: is a comprehensive calculation term, consisting of FK(1) to FK(5) and T. M1The coefficients are obtained by multiplying different powers and then adding them together. FK(1) to FK(5) are coefficients obtained by fitting a large amount of experimental data, and they are related to T. M1 The combination reflects the combined effect of temperature-related factors on saturated vapor pressure.

[0078] D1: From T0 and the relationship between T and FK(6) and FK(7) M1 The results are obtained by multiplying the polynomials. FK(6) and FK(7) are also fitting coefficients. The calculation of D1 combines the information after temperature normalization and the specific fitting coefficients, which are used as the denominator for the subsequent calculation of the exponential part.

[0079] D2: The molecule is T M1 The denominator is composed of FK(8) and FK(9) and T. M1 The related terms are composed of FK(8) and FK(9), which are also fitting coefficients. D2 is used to adjust the calculation of the exponential part in the whole formula system.

[0080] BK: Obtained by performing an exponential operation on SUM / D1-D2, it is a key intermediate result that integrates information such as temperature and fitting coefficients from the preceding calculations, playing an important transitional role in the calculation of the final saturated vapor pressure.

[0081] P T The saturated vapor pressure (Pa) at the current temperature represents the pressure at which water vapor in the air reaches saturation at a given temperature. It is obtained by multiplying BK by 221.2 × 10⁵, where 221.2 is the critical pressure of water (in bar; to convert to Pa, multiply by 10⁵). This calculation combines the intermediate variables and fitting coefficients from the previous calculation to finally obtain the value of the saturated vapor pressure.

[0082] In this embodiment of the invention, the fitting parameters (preset values) can be:

[0083] FK(1) = -7.691234564;

[0084] FK(2) = -26.08023696;

[0085] FK(3) = -168.1706546;

[0086] FK(4) = 64.23285504;

[0087] FK(5) = -118.9646225;

[0088] FK(6) = 4.167117320;

[0089] FK(7) = 20.97506760;

[0090] FK(8)=1.000000000×10 9 ;

[0091] FK(9) = 6.000000000.

[0092] These fitting parameters are obtained through in-depth analysis and fitting of a large amount of experimental data. They are applicable to specific temperature ranges and calculation scenarios. Different gases and temperature ranges may require different fitting coefficients to ensure the accuracy of the calculation results.

[0093] Step S1032: Calculate the relative humidity PHI.

[0094] In this step, the formula for calculating relative humidity (PHI) can be as follows:

[0095]

[0096] Where X is the water vapor volume fraction. P corr This is the corrected atmospheric pressure, P. T The saturated vapor pressure at the current temperature is calculated using the formula above. Relative humidity (PHI), expressed as a percentage, reflects the ratio of the actual water vapor content in the flue gas to the saturated water vapor content at that temperature, and is a key indicator for measuring the relative humidity state of the flue gas.

[0097] This step can be implemented through a data processing module, such as... Figure 4 As shown in the flowchart, this flowchart illustrates the workflow of the data processing module. After receiving the data collected by the sensor module, the data processing module first corrects the atmospheric pressure based on the altitude, and then calculates the corrected atmospheric pressure P. corr Then, based on the critical temperature normalization method, the saturated vapor pressure P is calculated through polynomial fitting. T By combining the corrected atmospheric pressure and flue gas temperature, the relative humidity (PHI) of the flue gas is calculated. Finally, the calculated relative humidity data is transmitted to the control module.

[0098] Step S104: Dynamically optimize and adjust the dosage of deacidifying agent based on the atmospheric parameters and relative humidity;

[0099] In the semi-dry deacidification process, relative humidity (PHI) plays a crucial role in deacidification efficiency. Three months of testing showed that when PHI = 6% (i.e., 6% relative humidity), the deacidification efficiency significantly improved for the following reasons:

[0100] The role of the water film: In the semi-dry deacidification process, the reaction between lime slurry (mainly composed of Ca(OH)2) and acidic gases (such as HCl and SO2) in the flue gas requires liquid water as a reaction medium. When PHI = 6%, the water vapor content in the flue gas is moderate, which can form a stable micron-sized water film covering the surface of the lime particles, promoting the dissolution of acidic gases and chemical reactions. When the humidity is insufficient, the acidic gases are difficult to dissolve completely, leading to incomplete reactions; when the humidity is too high, excessive liquid water may form, hindering gas-solid contact and reducing reaction efficiency.

[0101] Reaction kinetic equilibrium: At a humidity level of PHI = 6%, the partial pressure of water vapor and the surface water film tension of the deacidifying agent reach equilibrium. The dissolution rate of acidic gases matches the neutralization reaction rate, avoiding reaction interruption due to excessively rapid evaporation or increased mass transfer resistance due to excessively slow evaporation. The water vapor content at PHI = 6% ensures sufficient liquid water while avoiding mass transfer resistance caused by excessive liquid water. The deacidification efficiency is in the "reaction kinetic optimal region," that is, the matching between the dissolution rate of acidic gases and the reaction rate on the lime surface reaches its maximum value.

[0102] Temperature Limit Protection: The lower limit of the reaction tower outlet temperature is set at 130℃; otherwise, excessively low reaction tower temperatures may damage downstream process equipment. If the reaction tower outlet temperature Tout < 130℃, the system will not increase the amount of cooling water added to avoid affecting downstream process equipment.

[0103] Dynamic optimization and adjustment of deacidifying agent dosage:

[0104] Input parameters: Real-time relative humidity PHI (calculated from step S103), reaction tower outlet temperature T, inlet acid gas concentration (HCl, SO2), flue gas flow rate Q. flue .

[0105] Output command: Lime slurry dosage Q lime (kg / h), Cooling water flow rate Q water (kg / h).

[0106] Calculation of relative humidity main loop control deviation e PHI =6-PHI,

[0107] PID algorithm: ΔQ water =K p ·e PHI +K i ∫e PHI dt+K d (d ePHI / dt)

[0108] Temperature safety limit: When the outlet temperature T of the reaction tower is less than 130°C, the temperature interlock protection mechanism is triggered, and the cooling water regulating valve will no longer open.

[0109] The lime slurry dosage is adjusted by introducing a correction function f(PHI) = sech(0.38|PHI-6|).

[0110] Qlime = Q lime理论 / f(PHI)

[0111] The PHI value should be between 5 and 7 to avoid overshoot or undershoot.

[0112] Cooling water flow rate Q water Controlled by adjusting the opening of the regulating valve, used to adjust the relative humidity PHI (increasing Q). water It can increase humidity, and vice versa.

[0113] lime slurry flow rate Q lime Controlled by the opening degree of the slurry regulating valve.

[0114] This step can be implemented through a control module and an actuator, such as... Figure 5 As shown in the flowchart, this process diagram illustrates the workflow of the control module and the actuator. After receiving the relative humidity data from the data processing module, the control module compares it with the preset target relative humidity. If the measured relative humidity deviates from the target humidity range, the control module calculates the adjustment amount for the lime slurry dosage using a PID algorithm. Then, it sends the adjustment command to the actuator, and the lime slurry regulating valve and the cooling water regulating valve adjust the dosage according to the command.

[0115] Thus, this invention employs an optimized deacidifying agent dosage strategy: introducing f(PHI) = sech(0.38|PHI-6|) as a dynamic correction function for the amount of lime slurry added, using relative humidity feedback control with PHI = 6% as the target value, and combining the correction function f(PHI) with a dynamic adjustment method for temperature safety limits (T≥130℃); furthermore, it adopts a multivariable coupled control architecture: a closed-loop control system integrating sensor acquisition, atmospheric correction, humidity calculation, and agent adjustment to achieve coordinated control of atmospheric parameters, humidity, and temperature.

[0116] Step S105: The actuator adds the deacidifying agent according to the adjusted dosage.

[0117] As an optional embodiment, step S105 is followed by:

[0118] Step S106: Real-time monitoring of the waste incineration deacidification process;

[0119] In this step, the following key process parameters can be monitored to ensure that the deacidification process is controllable:

[0120] The temperature at the outlet of the reaction tower (T) is monitored in real time by a thermocouple sensor to ensure that the temperature is not lower than 130℃ (the safety threshold for triggering the addition of cooling water).

[0121] Water vapor content (X): Measured using ultraviolet differential absorption spectroscopy, directly affecting the calculation of relative humidity.

[0122] Flue gas relative humidity (PHI): Calculated in real time using saturated vapor pressure and water vapor content, reflecting the humidity status of flue gas.

[0123] Deacidifying agent dosage (Q) lime ): The actual flow rate of lime slurry added should be consistent with the dynamic adjustment instructions.

[0124] Cooling water flow rate (Q) water ): Adjusts the valve opening and actual flow rate to control the humidity of flue gas.

[0125] Step S107: Determine whether optimization or adjustment is needed. If not, proceed directly to step S101; if yes, optimize the system parameters and then proceed to step S101.

[0126] In this step, optimization and adjustments are required when the following situations are detected:

[0127] (1) When the indicator deviates from the threshold, including but not limited to:

[0128] The relative humidity (PHI) continues to deviate from the target value (6%) ±0.5% for more than the set time (e.g., 10 minutes);

[0129] The acid gas removal rate is lower than the design value (e.g., 95%) or the fluctuation range exceeds 5%;

[0130] The outlet temperature of the reaction tower frequently approaches the lower safety limit (130℃) or the opening of the cooling water regulating valve reaches its limit (such as 100% or 0%).

[0131] (2) When the consumption of reagents is abnormal: the consumption of lime slurry (consumption per ton of garbage) increases by more than 3% compared with the historical average.

[0132] (3) When sensor data is abnormal (such as pressure transmitter signal fluctuation), actuator jamming alarm, etc.

[0133] When the above phenomenon occurs, it is necessary to trigger the optimization and adjustment process. The specific optimization methods are as follows:

[0134] 1. Optimize control algorithm parameters, including PID gain parameters (Kp, Ki, Kd), and adjust the proportional, integral, and derivative coefficients of the cooling water flow control to improve the response speed and stability of humidity control. Also, optimize the lime slurry addition correction function parameters, such as the coefficient 0.38 in the correction function f(PHI) = sech(0.38|PHI-6|), dynamically fine-tuning it based on actual deacidification efficiency to avoid overshoot or undershoot.

[0135] 2. Adjust the altitude pressure correction coefficient (k) and fit it according to local long-term meteorological data to solve the pressure compensation deviation in high altitude or air pressure fluctuation scenarios.

[0136] 3. Optimize the fitting coefficients (FK(1)-FK(9)): For different waste compositions or flue gas temperature ranges, refit the data using experimental data to improve the saturated vapor pressure P. T The calculation accuracy.

[0137] like Figure 2 As shown in the flowchart, this diagram comprehensively illustrates the entire system's workflow. Starting with parameter acquisition, it proceeds through atmospheric parameter correction, relative humidity calculation, and adjustments to the dosage of deacidifying agent and cooling water. Finally, the actuators execute adjustment commands, forming a closed-loop control system. The entire process continuously cycles, ensuring that the waste incineration deacidification process always takes place in an optimal humidity environment.

[0138] The following uses a waste incineration plant in Sichuan as an example to explain in detail the specific implementation process of this invention:

[0139] 1. System Setup and Initialization

[0140] Sensor Installation and Commissioning: Install thermocouple temperature sensors, pressure transmitters, gas analyzers, and GPS positioning modules. Ensure the sensors are installed accurately to accurately reflect real-time flue gas parameters. After installation, commission the sensors and check the accuracy and stability of data acquisition.

[0141] Data processing module configuration: It processes atmospheric pressure and altitude relationship data, uses a critical temperature normalization method, and calculates the saturated vapor pressure P through polynomial fitting. T The fitting parameters of the equations are imported into the data processing module. The calculation parameters and algorithms of the data processing module are set to ensure accurate atmospheric pressure correction and relative humidity calculation, and the calculation results are transmitted to the control module.

[0142] Control module parameter settings: In the control module, based on the real-time humidity calculation results, the target relative humidity (PHI) is set to 6. Simultaneously, the calcium-to-sulfur ratio (R) is determined. Ca The preset target temperature T at the outlet of the reaction tower outBased on parameters such as the preset target humidity and the actual calculated relative humidity, the PID algorithm is used to calculate the adjustment amount of lime slurry addition and send the instruction to the actuator.

[0143] Actuator commissioning: Commission the lime slurry regulating valve to ensure that it can accurately adjust the amount of lime slurry added according to the instructions sent by the control module, and check the accuracy and stability of the valve opening adjustment.

[0144] 2. Real-time parameter acquisition and processing

[0145] Parameter acquisition at a certain moment:

[0146] The reaction tower outlet temperature T = 140℃ = 413.15K, the water vapor content in the flue gas X = 21% vol, the reaction tower inlet flue gas pressure P = 85000 Pa, the altitude H = 1100 m, the atmospheric pressure correction: Pcorr = 85000 - 0.1 * 1100 = 84890 Pa, and the flue gas flow rate Q is measured by the flow sensor. flue =95000m 3 / h.

[0147] 3. Calculation of saturated vapor pressure and relative humidity

[0148] Saturated vapor pressure calculation: According to the formula

[0149]

[0150] Fitting parameters (preset values):

[0151] FK(1) = -7.691234564;

[0152] FK(2) = -25.97163696;

[0153] FK(3) = -168.1706546;

[0154] FK(4) = 59.89285504;

[0155] FK(5) = -109.9646225;

[0156] FK(6) = 4.24587629;

[0157] FK(7) = 20.7698547;

[0158] FK(8)=1.000000000×10 9 ;

[0159] FK(9) = 6.000000000.

[0160] The distribution unfolds as follows:

[0161] T0=413.15 / 647.3=0.638266646;

[0162] T M1 =1-0.638266646=0.361733354;

[0163] SUM=-7.691234564*0.361733354-25.97163696*0.361733354 2 -

[0164] 168.1706546*0.361733354 3 +59.89285504*0.361733354 4 -109.9646225*0.361733354 5 = -13.79623426;

[0165] D1=(1+4.24587629*0.361733354+20.7698547*0.361733354 2 )*0.638266646=3.353217904;

[0166] D2=0.361733354 / (1000000000*0.361733354 2 +6)=2.76447E-09;

[0167] BK=exp(-13.79623426 / 3.353217904-2.76447E-09)=0.016336935;

[0168] P T =0.016336935 * 221.2 * 100000 = 361372.9983;

[0169] Relative humidity calculation: PHI = 21 * 84890 / 361372.9983% = 4.933%.

[0170] 4. Calculation and adjustment of deacidifying agent dosage compensation

[0171] The measured PHI calculated according to the formula of this invention is 4.933% (in this example), which deviates from the target value of 6% by e. PHI =1.067.

[0172] At this point, the lime slurry addition amount is corrected to ΔQ. lime =Q lime -Qlime理论 =1 / f(PHI)-1=0.08325, the lime slurry correction can effectively reduce the system oscillation time.

[0173] Significant results have been achieved by adopting the precise control method based on atmospheric parameter correction and relative humidity feedback of this invention. Before the system was put into use, the waste incineration deacidification process of this plant used traditional control methods, resulting in unstable deacidification efficiency, large fluctuations in acid gas emissions, and excessive consumption of lime slurry.

[0174] After the system was put into operation, when the PHI was in the range of 5.7%-6.3%, the acid removal efficiency was improved through real-time monitoring and precise control. With the same amount of deacidifying agent, the removal rate of acidic gases (HCl and SO2) increased from 92.8% to 96.2%, ensuring stable compliance with flue gas emission standards. At the same time, the consumption of deacidifying agents was significantly reduced, and the amount of lime slurry used decreased by 8.7%, effectively reducing operating costs.

[0175] During operation, the system can automatically adjust the dosage of the deacidifying agent according to different working conditions. For example, on a certain day, due to a sudden drop in local air pressure, the flue gas pressure at the inlet of the reaction tower decreases. The system promptly corrects the atmospheric pressure and recalculates the relative humidity by collecting pressure and altitude data in real time. Based on the calculation results, the control module automatically adjusts the dosage of lime slurry to ensure that the deacidification reaction takes place in a more favorable humidity environment, avoiding a decrease in deacidification efficiency due to air pressure changes.

[0176] In summary, this invention provides a precise control method for the deacidification process in waste incineration based on atmospheric parameter correction and relative humidity feedback. By integrating a coupled calculation model of atmospheric pressure, altitude, and flue gas humidity, it accurately calculates relative humidity in real time and dynamically adjusts the dosage of deacidifying agent, achieving dynamic optimization of the agent dosage, improving deacidification efficiency, and reducing reagent consumption. Specifically, the method of this invention introduces atmospheric parameter correction and quantitative control of relative humidity, solving the problems of crude humidity control and poor adaptability to operating conditions in existing technologies, significantly improving deacidification efficiency and reducing reagent consumption, and is applicable to waste incineration flue gas purification under different altitudes and air pressures.

[0177] The present invention has the following beneficial effects:

[0178] Improved deacidification efficiency: Through precise control methods based on atmospheric parameter correction and relative humidity feedback, the acid gas removal rate has been increased from 92.8% to over 96.2%.

[0179] Reduced chemical consumption: The amount of quicklime consumed per ton of waste decreased from 11.3 kg to 10.4 kg, and the amount of lime slurry used decreased by 7.96%, significantly reducing operating costs.

[0180] System stability: Effectively avoids equipment condensation and sudden drop in reaction efficiency caused by humidity fluctuations, improving the long-term reliability of the system.

[0181] The above description is merely a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in the present invention should be included within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the scope of the claims.

Claims

1. A control method based on atmospheric parameters and relative humidity during the deacidification process of waste incineration, characterized in that, include: Step S101: Obtain real-time parameters during the waste incineration process; Step S102: Correct the calculated atmospheric parameters; Step S103: Calculate relative humidity in real time; Step S104: Dynamically optimize and adjust the dosage of deacidifying agent based on the atmospheric parameters and relative humidity; Step S105: The actuator adds the deacidifying agent according to the adjusted dosage; In step S101, the real-time parameters include the flue gas temperature T at the outlet of the reaction tower, the flue gas pressure P at the inlet of the reaction tower, the water vapor content X in the flue gas, and the ambient altitude H. Step S102 includes: The atmospheric pressure is corrected based on the ambient altitude H, and the corrected atmospheric pressure is calculated using the following formula: P corr =P k H Among them, P corr P is the corrected atmospheric pressure, which is the flue gas pressure at the inlet of the reaction tower measured in real time by a pressure transmitter. k is the altitude pressure correction coefficient, which is obtained by fitting and analyzing local meteorological data and is in Pa / m. H is the ambient altitude obtained by a GPS positioning module. Step S103 includes: Step S1031: Calculate the saturated vapor pressure P T ; Step S1032: Calculate the relative humidity PHI; In step S1031, the saturated vapor pressure P T The calculation formula is: Where T0 is the value obtained by normalizing the flue gas temperature T at the outlet of the reaction tower with the critical temperature of water, 647.3 K. M1 SUM is obtained by subtracting T0 from 1. It is a comprehensive calculation term, consisting of FK(1) to FK(5) and T. M1 The coefficients FK(1) to FK(5) are obtained by multiplying different powers and then adding them together. D1 is obtained by fitting a large amount of experimental data with T0 and the coefficients containing FK(6) and FK(7) about T. M1 The polynomials are multiplied together to obtain FK(6) and FK(7), which are also fitting coefficients. The numerator of D2 is T. M1 The denominator is composed of FK(8) and FK(9) and T. M1 The relevant terms are composed of FK(8) and FK(9), which are also fitting coefficients. BK is obtained by performing an exponential operation on SUM / D1-D2. In step S1032, the formula for calculating relative humidity (PHI) is: Step S104 includes: Step S1041: Determine if the relative humidity (PHI) is less than 6%. If so, increase the cooling water flow rate (Q). water If not, reduce the cooling water flow rate Q. water ; Step S104 further includes: Step S1041': Calculate the lime slurry dosage correction function f(PHI); Step S1042': Dynamically adjust the lime slurry dosage Qlime according to the lime slurry dosage correction function f(PHI); In step S1041', the lime slurry addition amount correction function is f(PHI) = sech(0.38|PHI-6|). In step S1042', the amount of lime slurry added... Q lime= Q lime理论 / f (PHI), where the value of PHI ranges from 5 to 7.

2. The control method based on atmospheric parameters and relative humidity during the waste incineration deacidification process according to claim 1, characterized in that, In step S1041, the cooling water flow rate adopts a PID algorithm: Δ Q water = K p e PHI + K i ∫ e PHI dt + K d ( de PHI / dt ), where Kp is the proportional gain, Ki is the integral gain, Kd is the derivative gain, and the relative humidity main loop control deviation is... e PHI =6-PHI.

3. The control method based on atmospheric parameters and relative humidity during the waste incineration deacidification process according to claim 1, characterized in that, Step S104 further includes: Step S1041'': If the outlet temperature of the reaction tower Tout < 130°C, the system will no longer increase the amount of cooling water added.

4. The control method based on atmospheric parameters and relative humidity during the waste incineration deacidification process according to claim 1, characterized in that, Following step S105: Step S106: Real-time monitoring of the waste incineration deacidification process; Step S107: Determine whether optimization or adjustment is needed. If not, proceed directly to step S101; if yes, optimize the system parameters and then proceed to step S101.

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