Method for monitoring operation condition of activated carbon adsorption tower

Abstract

The invention relates to the technical field of flue gas purification, and provides a method for monitoring the operation condition of an activated carbon adsorption tower, and the method specifically comprises the following steps: detecting the physicochemical properties of activated carbon and raw flue gas; constructing a tower body structure comprising a feed port, a flue gas purification section, a transition section and a discharge port; collecting activated carbon conveying amount, flue gas flow and pollutant concentration data in real time; calculating the activated carbon temperature of the purification section through a thermodynamic equilibrium equation. According to the method, establishment of a parameter correlation model becomes a breakthrough direction, direct measurement is replaced by indirect calculation, and visual monitoring of the temperature of the purification section is achieved. According to the method, a parameter correlation model is further established, the amount of leaked smoke is judged, and the safety of the system is indirectly judged.

Description

Technical Field

[0001] This invention relates to the field of flue gas purification technology, and to a method for purifying flue gas using an activated carbon adsorption tower, specifically to a method for monitoring the operation of the activated carbon adsorption tower. Background Technology

[0002] In sintering flue gas, we discovered a variety of harmful compound pollutants, including sulfur dioxide (SO2), nitrogen oxides (NOx), hydrogen chloride (HCl), dioxins, and particulate matter. These pollutants contribute significantly to the pollution load of the steel industry, accounting for up to 45% of the total pollution load. This data is based on information from the "Annual Report on Pollutant Emissions from China's Steel Industry." In 2019, to address this serious environmental problem, the Ministry of Ecology and Environment, along with four other ministries, jointly issued new standards for ultra-low emissions from sintering flue gas. According to these standards, the sulfur dioxide (SO2) content in sintering flue gas needs to be controlled below 35 mg / m³, while the nitrogen oxide (NOx) content needs to be reduced to below 50 mg / m³. However, traditional pollution control technologies face considerable challenges and difficulties in achieving these ultra-low emission standards.

[0003] In current technologies, the lateral stratified cross-flow activated carbon flue gas treatment technology (see...) Figure 1 This technology is widely used. (See Adsorption Tower) Figure 2 The activated carbon adsorption tower is divided into three layers: front, middle, and rear. From top to bottom, it consists of a flue gas purification section (flue gas flow channel) and a transition section (non-flue gas flow channel), achieving synergistic purification of multiple pollutants. However, within the flue gas purification section, because the raw flue gas and activated carbon are in continuous contact, it is difficult to accurately measure the temperature of the activated carbon in this section, thus making it impossible to accurately grasp the temperature status of the activated carbon within the flue gas purification section. This results in the inability to adjust the operating parameters of the adsorption tower in a timely manner, thereby affecting the purification effect. Furthermore, if the temperature of the activated carbon in the flue gas purification section is too high, it may cause activated carbon combustion, posing a safety hazard; if the temperature is too low, it will reduce adsorption efficiency and weaken the purification effect. Therefore, real-time monitoring of the activated carbon temperature within the flue gas purification section is particularly crucial. Unfortunately, existing technologies cannot achieve real-time and accurate detection of the activated carbon temperature within the flue gas purification section.

[0004] Furthermore, the current technology suffers from long-term flue gas leakage between the flue gas purification section and the transition section. This leakage causes a localized temperature increase in the activated carbon within the transition section of the activated carbon adsorption tower (ΔT = 20℃ / min), leading to excessively high temperatures of the activated carbon discharged from the tower and increasing the risk of open flame (activated carbon ignition). Additionally, the conveying system experiences condensation (humidity > 10%) due to leaked flue gas, resulting in corrosion (e.g., ...). Figure 3As shown in the figure, this leads to a shortened equipment lifespan. Current technologies cannot detect the amount of flue gas leakage from the flue gas purification section to the transition section in real time and accurately, resulting in an inability to effectively control the temperature of the activated carbon in the transition section, further affecting the stability and safety of equipment operation.

[0005] The patent holder, through in-depth research and innovation, successfully developed a flue gas purification system with an atmosphere protection structure (patent number CN201910971641.4) to address the problem of flue gas leakage. The main design goal of this system is to reduce the amount of flue gas leaking downwards at the source, aiming for a more efficient purification effect. However, in actual production, researchers discovered a significant correlation between the amount of flue gas leaking from the purification section to the transition section and the overall system resistance. This correlation leads to large fluctuations in the leakage amount, making it difficult to adjust and optimize the originally designed atmosphere protection structure in real time, thus affecting the overall system performance and flue gas purification efficiency. Summary of the Invention

[0006] To address the problems existing in the prior art, the purpose of this application is to provide a method for monitoring the operation of an activated carbon adsorption tower, which has the advantage of real-time monitoring of activated carbon temperature. This application proposes a multi-parameter linkage-based activated carbon adsorption tower operation monitoring method, specifically including: detecting the physicochemical properties of activated carbon and raw flue gas; constructing a tower structure including an inlet, a flue gas purification section, a transition section, and a discharge outlet; real-time acquisition of activated carbon delivery rate, flue gas flow rate, and pollutant concentration data; and calculating the activated carbon temperature in the purification section using thermodynamic balance equations. Analysis reveals a thermodynamic correlation between the raw flue gas temperature, exhaust temperature, and activated carbon mass flow rate, while the heat of reaction generated during pollutant adsorption directly affects the temperature distribution. Based on this, establishing a parameter correlation model becomes a breakthrough direction, achieving visualized monitoring of the purification section temperature through indirect calculation instead of direct measurement.

[0007] According to a first embodiment of the present invention, a method for monitoring the operating status of an activated carbon adsorption tower is provided.

[0008] A method for monitoring the operating status of an activated carbon adsorption tower, the method comprising the following steps:

[0009] S1. Detect the physicochemical properties of activated carbon and the physicochemical properties of raw flue gas;

[0010] S2. The activated carbon adsorption tower is divided into an activated carbon inlet, a flue gas purification section, a transition section, and a discharge port from top to bottom. Activated carbon is conveyed into the activated carbon adsorption tower through the inlet. The activated carbon passes through the flue gas purification section and the transition section in sequence inside the activated carbon adsorption tower, and then is discharged from the discharge port of the activated carbon adsorption tower. The raw flue gas is conveyed into the activated carbon adsorption tower, passes through the flue gas purification section of the activated carbon adsorption tower, and is discharged from the exhaust port of the activated carbon adsorption tower after being purified by the flue gas purification section.

[0011] S3. Detect the operating parameters of activated carbon in the activated carbon adsorption tower and the operating parameters of flue gas in the activated carbon adsorption tower;

[0012] S4. Based on the parameters obtained in steps S1 and S3, calculate the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower.

[0013] In this invention, the temperature of the activated carbon in the flue gas purification section of the activated carbon adsorption tower is specifically calculated as follows:

[0014] ...Formula I;

[0015] In Formula I: t3 is the temperature of the activated carbon in the purification section, °C; t1 is the temperature of the raw flue gas, °C; t2 is the temperature of the gas discharged from the flue gas exhaust port of the activated carbon adsorption tower, °C; m1 is the mass of activated carbon in the activated carbon adsorption tower, kg; C p1 Specific heat capacity of sintering flue gas, J / (mol·℃); C p2 ρ is the specific heat capacity of activated carbon, J / (Kg·℃); Vm is the molar volume, taken as 22.4 L / mol; M is the relative molecular mass of SO2, 64 g / mol; H is the heat released by the oxidation of 1 mol SO2 to sulfuric acid, taken as 275000 J / mol; q1 is the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, Nm 3 C0 represents the SO2 concentration in the original flue gas at the flue gas inlet of the adsorption tower, in g / Nm³. 3 C1 represents the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower, in g / Nm³. 3 ; 'a' represents the flue gas adjustment coefficient, in L / Nm³. 3 , with a value of 800-1200; b is the pollutant adjustment coefficient, with a value of 0.9-1.2.

[0016] Preferably, the following parameters are monitored in real time: the temperature of the raw flue gas, the temperature of the gas discharged from the flue gas outlet of the activated carbon adsorption tower, the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the flow rate of the gas discharged from the flue gas outlet of the adsorption tower per unit time, the SO2 concentration in the raw flue gas at the flue gas inlet of the adsorption tower, and the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower. These parameters are then substituted into Equation I to obtain the real-time temperature t of the activated carbon in the flue gas purification section of the activated carbon adsorption tower. 3-实时 .

[0017] As a preferred option, the upper limit of the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower is set to t0. Comparison:

[0018] If t 3-实时 If the value is less than or equal to t0, continue running.

[0019] If t 3-实时 >t0, adjust the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower, or adjust the quality of activated carbon delivered to the activated carbon adsorption tower per unit time, or stop the machine for inspection.

[0020] As a preferred option, if t0 < t 3-实时 ≤f·t0, reduce the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower;

[0021] If t 3-实时 >f·t0, adjust the quality of activated carbon delivered to the activated carbon adsorption tower per unit time or stop the machine for inspection;

[0022] Where f = 1.0-1.4, preferably f = 1.01-1.35, and more preferably f = 1.03-1.30. For example, the values ​​of f are 1.01, 1.02, 1.03, 1.04, 1.05, 1.06, 1.07, 1.08, 1.09, 1.10, 1.11, 1.12, 1.13, 1.14, 1.15, 1.16, 1.17, 1.18, 1.19, 1.20, 1.21, 1.22, 1.23, 1.24, 1.25, 1.26, 1.27, 1.28, 1.29, 1.3, 1.32, 1.35, 1.38, and 1.4.

[0023] In a further optimized technical solution of the present invention, the method further includes the following steps:

[0024] S5. Based on the parameters obtained in steps S1 and S3, calculate the amount of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower.

[0025] In this invention, the specific calculation of the amount of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower is as follows:

[0026] ...Formula II;

[0027] In Formula II, η is the proportion of flue gas leaking from the flue gas purification section to the transition section, %; t3 is the activated carbon temperature in the purification section, °C; t4 is the activated carbon temperature in the transition section, °C; m2 is the mass of activated carbon in the transition section, kg; C p2 q1 is the specific heat capacity of activated carbon, J / (Kg·℃); q1 is the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, Nm³. 3 M is the relative molecular mass of SO2, 64 g / mol; H is the heat released when 1 mol of SO2 is oxidized to sulfuric acid, taken as 275000 J / mol; CO is the SO2 concentration in the original flue gas at the flue gas inlet of the adsorption tower, g / Nm³. 3C1 represents the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower, in g / Nm³. 3 d is the flue gas volume adjustment coefficient, with a value of 0.6-1.5.

[0028] Preferably, the following parameters are monitored in real time: the temperature of the raw flue gas, the temperature of the gas at the exhaust port of the activated carbon adsorption tower, the temperature of the activated carbon in the transition section, the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the mass of activated carbon in the transition section, the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the flow rate of the exhaust gas at the flue gas outlet of the adsorption tower per unit time, the SO2 concentration at the flue gas inlet of the adsorption tower, and the SO2 concentration at the flue gas outlet of the adsorption tower. Substituting these parameters into Equation II, the real-time proportion η of the flue gas leakage from the flue gas purification section to the transition section in the activated carbon adsorption tower is obtained. 实时 .

[0029] As a preferred option, the upper limit of the proportion of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower is set as η0. Comparison:

[0030] If η 实时 If ≤η0, continue running;

[0031] If η 实时 If the value is greater than η0, adjust the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower or shut down the tower for inspection.

[0032] As a preferred option, if η0 < η 实时 ≤g·η0, reduce the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower;

[0033] If η 实时 >g·η0, stop the machine for inspection;

[0034] Wherein: g = 1.0-1.2, preferably g = 1.01-1.15, and more preferably g = 1.02-1.1. For example, the value of g is 1.01, 1.02, 1.03, 1.04, 1.05, 1.06, 1.07, 1.08, 1.09, 1.10, 1.11, 1.12, 1.13, 1.14, 1.15, 1.16, 1.17, 1.18, 1.19, 1.20.

[0035] In this invention, t0 is 100-200℃, preferably 120-180℃, and more preferably 140-160℃. For example, the values ​​of t0 are 100℃, 105℃, 110℃, 115℃, 120℃, 125℃, 130℃, 135℃, 140℃, 145℃, 150℃, 155℃, 160℃, 165℃, 170℃, 175℃, 180℃, 185℃, 190℃, 190℃, and 200℃.

[0036] In this invention, η0 is 0-10%, preferably 0.1%-8%, and more preferably 0.2%-5%. For example, the values ​​of η0 are 0%, 0.1%, 0.2%, 0.3%, 0.4%, 0.5%, 0.6%, 0.7%, 0.8%, 0.9%, 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 6%, 7%, 8%, 9%, and 10%.

[0037] In this invention, if η=0, it means that there is no flue gas leakage from the flue gas purification section to the transition section. If η is negative, it means that there is no flue gas leakage from the flue gas purification section to the transition section, and since the flue gas purification section is connected to the fan, there is a possibility of gas flowing from the transition section into the flue gas purification section, but there is no risk of flue gas leakage.

[0038] In this invention, the physicochemical properties of the activated carbon include its specific heat capacity.

[0039] In this invention, the physical and chemical properties of the raw flue gas include its temperature.

[0040] In this invention, the operating parameters of the activated carbon in the activated carbon adsorption tower include the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the temperature of the activated carbon in the transition section, the mass of the activated carbon in the transition section, and the temperature of the gas discharged from the flue gas exhaust port of the activated carbon adsorption tower.

[0041] In this invention, the operating parameters of the flue gas in the activated carbon adsorption tower include the temperature of the gas discharged at the flue gas exhaust port of the activated carbon adsorption tower, the flow rate of the original flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the flow rate of the gas discharged at the flue gas outlet of the adsorption tower per unit time, the SO2 concentration in the original flue gas at the flue gas inlet of the adsorption tower, and the SO2 concentration in the gas discharged at the flue gas outlet of the adsorption tower.

[0042] In existing technologies, the treatment of sintering flue gas in the steel industry faces the challenge of synergistic purification of multiple pollutants. Traditional activated carbon adsorption towers suffer from a technical bottleneck: the temperature of activated carbon in the flue gas purification section cannot be monitored in real time. Because the flue gas and activated carbon are in continuous contact within the purification section, direct temperature measurement is physically limited, leading to a lag in adjusting operating parameters. Furthermore, interference from the flue gas prevents accurate detection of the activated carbon temperature within the purification section. For example, in a steel plant using lateral stratified cross-flow technology, the activated carbon temperature in the purification section fluctuates by more than 50°C. However, existing detection methods can only obtain discharge port temperature data, failing to reflect the true operating conditions of the purification section, resulting in both the risk of activated carbon combustion and a decrease in adsorption efficiency.

[0043] To address these issues, researchers discovered that the root cause of the temperature anomalies lay in the disruption of the dynamic balance of heat exchange between flue gas and activated carbon. Analysis revealed a thermodynamic correlation between the raw flue gas temperature, exhaust temperature, and activated carbon mass flow rate, with the heat of reaction generated during pollutant adsorption directly influencing the temperature distribution. Based on this, establishing a parameter correlation model became a breakthrough approach, enabling visualized monitoring of the purification section temperature through indirect calculations instead of direct measurements.

[0044] Therefore, this application proposes a multi-parameter linkage-based activated carbon adsorption tower operation monitoring method, specifically including: detecting the physicochemical properties of activated carbon and raw flue gas; constructing a tower structure including an inlet, a flue gas purification section, a transition section, and a discharge outlet; real-time acquisition of data such as activated carbon delivery rate, flue gas flow rate, and pollutant concentration; and calculating the activated carbon temperature in the purification section using thermodynamic balance equations. Using this model, the activated carbon delivery rate and flue gas flow rate are dynamically adjusted to ensure heat exchange balance, effectively reduce temperature fluctuations, improve adsorption efficiency, reduce combustion risks, and achieve precise monitoring and optimized operation.

[0045] Physicochemical property testing refers to the quantitative analysis of thermophysical parameters such as the specific heat capacity of activated carbon and parameters such as flue gas composition. This can be achieved using thermogravimetric analyzers and flue gas analyzers, providing fundamental physical property parameters for thermodynamic calculations. Activated carbon transport process monitoring refers to the dynamic measurement of the mass of activated carbon entering the adsorption tower per unit time, which can be achieved using a loss-in-weight weighing scale to establish material balance equations. Flue gas operating parameter acquisition refers to the simultaneous detection of inlet and outlet flue gas temperature, flow rate, and pollutant concentration, which can be achieved using thermocouple arrays and online monitoring systems to construct energy conservation equations.

[0046] Specifically, during the downward movement of activated carbon, the original flue gas flows through the flue gas purification section from left to right, forming a cross-flow contact. By simultaneously acquiring data on activated carbon mass flow rate, flue gas inlet and outlet temperature difference, and pollutant concentration changes, and combining this with the specific heat capacity parameter of activated carbon, a thermodynamic balance equation is established. When activated carbon adsorbs pollutants such as SO2, the heat released by the chemical reaction is incorporated into the calculation model, and the temperature value of the activated carbon in the flue gas purification section is output in real time through iterative calculations. This temperature value reflects the heat load state under actual operating conditions, providing a direct basis for operation control. This method not only accurately monitors temperature changes but also predicts potential risks, allowing for advance adjustment of operating parameters and ensuring system stability and efficiency. Experimental verification shows that after applying this model, temperature fluctuations are reduced to within 20℃, adsorption efficiency is increased by 15%, effectively avoiding activated carbon combustion accidents and providing reliable technical support for industrial flue gas purification.

[0047] Compared to existing technologies, traditional methods relying on discharge port temperature feedback suffer from significant lag and inaccuracy. This solution, however, achieves indirect real-time calculation of the purification section temperature by constructing multi-parameter simultaneous equations. This method overcomes the limitations of physical detection from a data modeling perspective, improving the timeliness of temperature monitoring while maintaining the existing equipment structure.

[0048] Through the above technical solution, this application effectively solves the temperature blind zone problem in the core reaction zone of the activated carbon adsorption tower, and can promptly identify abnormal temperature fluctuations. When the activated carbon temperature in the flue gas purification section exceeds the safety threshold, the thermal balance can be quickly restored by adjusting the activated carbon dosage or the flue gas flow rate, thus avoiding activated carbon combustion accidents and maintaining stable pollutant adsorption efficiency.

[0049] This application further proposes a specific method for calculating the activated carbon temperature within the flue gas purification section of an activated carbon adsorption tower, which is achieved through Equation I. Here, t3 refers to the real-time temperature of the activated carbon within the flue gas purification section. The average temperature of the activated carbon within this section, calculated by this invention, reflects the heat exchange state when the activated carbon contacts the flue gas. Here, t1 and t2 represent the temperatures at the original flue gas inlet (flue gas inlet of the activated carbon adsorption tower) and the purified flue gas outlet (flue gas discharge outlet of the activated carbon adsorption tower), respectively. These temperatures can be detected using thermocouples or infrared thermometers to establish the heat transfer relationship between the flue gas and the activated carbon. Here, m1 characterizes the mass of activated carbon delivered to the activated carbon adsorption tower per unit time. C p1 C represents the specific heat capacity of the sintering flue gas, and represents an inherent property of the flue gas. p2 ...

[0050] Specifically, during the operation of the activated carbon adsorption tower, heat exchange and adsorption reactions occur between the raw flue gas and the activated carbon in the flue gas purification section. This is achieved by real-time monitoring of the inlet flue gas temperature t1, outlet flue gas temperature t2, activated carbon mass flow rate m1, flue gas flow rate q1, SO2 concentrations C0 and C1, combined with the specific heat capacity C of the sintering flue gas. p1 Specific heat capacity of activated carbon C p2The molar volume Vm, the relative molecular mass M of SO2, the heat H released by the oxidation of 1 mol of SO2 to sulfuric acid, and empirical coefficients a and b are substituted into Equation I to calculate the activated carbon temperature t3 within the purification section. This calculation process comprehensively considers the influence of multiple factors such as flue gas flow, activated carbon transport, and pollutant adsorption reactions on temperature, avoiding the difficulty of directly measuring the activated carbon temperature within the purification section. Through real-time monitoring and dynamic adjustment, the activated carbon temperature is ensured to remain within a safe range, effectively preventing the decrease in adsorption efficiency or the risk of combustion due to abnormal temperature, further improving the stability and reliability of the system. This method not only improves the operational safety of the activated carbon adsorption tower but also optimizes the removal effect of pollutants, achieving a dual improvement in environmental and economic benefits. Through precise temperature control, the system can maintain efficient and stable operation under complex operating conditions.

[0051] Compared to existing technologies, which cannot directly install temperature measuring devices within the flue gas purification section, resulting in a lack of activated carbon temperature monitoring, this solution indirectly obtains the activated carbon temperature within the purification section by establishing a comprehensive calculation model that includes flue gas flow rate, pollutant concentration, and activated carbon heat capacity. This solves the problem of temperature monitoring blind spots caused by structural limitations in traditional technologies.

[0052] Through the above technical solution, this application can calculate the temperature of activated carbon in the flue gas purification section in real time, providing a basis for adjusting the flue gas flow rate or activated carbon delivery amount, thereby avoiding the risk of activated carbon combustion caused by excessively high temperature or the decrease in adsorption efficiency caused by excessively low temperature, and significantly improving the safety and stability of adsorption tower operation.

[0053] This application further proposes to monitor in real time the temperature of the raw flue gas, the temperature of the gas discharged from the flue gas exhaust port of the activated carbon adsorption tower, the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the SO2 concentration in the raw flue gas at the flue gas inlet of the adsorption tower, and the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower. Substituting these values ​​into Equation I, the real-time temperature t of the activated carbon in the flue gas purification section of the activated carbon adsorption tower can be obtained. 3-实时 By monitoring and dynamically adjusting in real time, the activated carbon temperature is kept within the optimal adsorption range, effectively improving pollutant removal efficiency and further enhancing the system's environmental adaptability and operational flexibility.

[0054] Real-time monitoring refers to the continuous acquisition of various parameters through sensors or online monitoring devices, such as using thermocouples to measure temperature, mass flow meters to count activated carbon delivery, and gas analyzers to detect SO2 concentration. This method enables dynamic data updates, providing immediate input for temperature calculations. Equation I is a mathematical model that includes the raw flue gas temperature, exhaust temperature, activated carbon mass flow rate, flue gas flow rate, pollutant concentration, and adjustment coefficients. By substituting real-time monitoring values ​​into this model, the temperature change trend of activated carbon within the flue gas purification section can be dynamically reflected.

[0055] Specifically, during the operation of the activated carbon adsorption tower, the raw flue gas temperature can be obtained through a temperature sensor installed in the flue gas inlet pipe, and the exhaust temperature is monitored through a sensor in the outlet pipe. The activated carbon mass flow rate is recorded by a weighing device in the conveying system, and the flue gas flow rate is statistically analyzed in real time by a flow meter. The SO2 concentration is simultaneously measured by gas analyzers at the inlet and outlet. All parameters are transmitted to the calculation module through a data acquisition system, and iterative calculations are performed according to Equation I to output t. 3-实时 For example, when the flue gas flow rate increases or the SO2 concentration rises, the system automatically updates parameters and recalculates to ensure the timeliness of temperature results. Through this closed-loop control mechanism, the system can quickly respond to changes in operating conditions, automatically adjust the activated carbon delivery rate or flue gas flow rate, maintain stable temperature, optimize adsorption effects, ensure maximum purification efficiency, and simultaneously reduce operating costs and improve overall economic benefits. Furthermore, the system also has a fault warning function; when abnormal data is detected, an alarm mechanism is immediately triggered to remind operators to intervene promptly and prevent accidents.

[0056] Compared to existing technologies, which rely solely on fixed parameters or offline detection data and cannot capture dynamic changes during operation, this solution utilizes periodic manual sampling, resulting in temperature calculations lagging behind actual operating conditions. In contrast, this solution, through real-time data acquisition and model computation, can continuously track activated carbon temperature fluctuations, providing immediate feedback for operational adjustments.

[0057] Through the above technical solution, this application solves the problem that existing technologies cannot monitor the activated carbon temperature in the flue gas purification section in real time. Dynamic monitoring and calculation can promptly detect temperature anomalies and trigger control measures, such as when t... 3-实时 The system automatically reduces flue gas flow when the threshold is exceeded. This effectively avoids the risk of activated carbon combustion due to excessive temperature, while maintaining a suitable temperature range to improve pollutant adsorption efficiency. Furthermore, real-time temperature data can be used to assess equipment operating status and support preventative maintenance.

[0058] This application further proposes setting the upper limit of the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower as t0, and comparing the real-time temperature t0. 3-实时Relationship with t0: If the real-time temperature does not exceed t0, operation continues; if it exceeds t0, control is achieved by adjusting the raw flue gas flow rate, activated carbon delivery rate, or by stopping the machine for inspection. This dynamic control mechanism not only ensures efficient operation of the activated carbon within a safe temperature range but also extends the equipment's lifespan and reduces maintenance frequency.

[0059] The upper limit of activated carbon temperature, t0, refers to a pre-set safe operating temperature threshold, which can be determined through experimental data or historical operating parameters, such as a comprehensive setting based on parameters like the activated carbon ignition point and adsorption efficiency decay temperature. This threshold is used to determine whether the activated carbon is within its safe operating temperature range. Adjusting the raw flue gas flow rate refers to changing the volume of flue gas entering the adsorption tower by adjusting the fan speed or valve opening, for example, by using a frequency converter to control the induced draft fan power. Adjusting the activated carbon delivery rate refers to controlling the amount of activated carbon supplied by changing the screw conveyor speed or the hopper discharge rate, for example, by using a weighing sensor linked with a PLC to achieve closed-loop control.

[0060] Specifically, during operation, the temperature sensor continuously collects the temperature data of the activated carbon in the flue gas purification section and transmits the real-time temperature data. 3-实时 The temperature is compared with a preset threshold t0. When the monitored temperature does not exceed the threshold, the existing operating parameters remain unchanged; when the monitored temperature exceeds the threshold, the control system will automatically trigger an adjustment mechanism, such as prioritizing a reduction in the raw flue gas flow rate to reduce heat load input. If the temperature continues to rise, the activated carbon supply will be further adjusted to change the adsorption reaction rate, or a shutdown procedure will be directly initiated for equipment inspection. This hierarchical control strategy ensures gradual intervention measures are taken when the temperature is abnormal. Through real-time data feedback and dynamic regulation, the system not only improves operational safety but also optimizes energy consumption management, achieving a dual guarantee of high efficiency and safety.

[0061] Compared to existing technologies, which lack real-time temperature monitoring capabilities and cannot promptly detect abnormal activated carbon temperatures, leading to difficulties in adjusting operating parameters when temperatures become too high, this solution addresses this issue by establishing a temperature threshold comparison mechanism and a multi-level control strategy. This enables dynamic monitoring and rapid response to the activated carbon's operating status.

[0062] Through the above technical solution, this application effectively avoids the risk of combustion caused by excessively high activated carbon temperature, while maintaining adsorption efficiency by adjusting operating parameters in a timely manner. The tiered control strategy maximizes continuous equipment operation while ensuring safety, reducing production losses caused by unplanned downtime.

[0063] This application further proposes that during the operation of the activated carbon adsorption tower, when the real-time temperature exceeds the preset upper temperature limit but does not reach the product of the adjustment coefficient and the upper temperature limit, control can be achieved by reducing the raw flue gas flow rate; when the real-time temperature exceeds the product of the adjustment coefficient and the upper temperature limit, intervention can be achieved by adjusting the activated carbon delivery rate or shutting down for inspection. The adjustment coefficient can range from 1.0 to 1.4, preferably from 1.01 to 1.35, and more preferably from 1.03 to 1.30. This coefficient setting is based on extensive experimental data and practical operating experience, ensuring flexibility and reliability under different operating conditions. By precisely controlling the adjustment coefficient, the system can take gentler intervention measures in the early stages of temperature anomalies, avoiding efficiency decline caused by overreaction, thereby maximizing production efficiency and equipment stability while ensuring safety.

[0064] The upper temperature limit refers to the preset critical temperature value for safe operation of activated carbon, which can be determined through experimental data or historical operating parameters, and is used to determine whether the temperature control program needs to be activated. The adjustment coefficient refers to the buffer zone multiple for temperature control, and can be a safety redundancy coefficient under different operating conditions, used to establish a graded response mechanism. Flue gas flow adjustment refers to changing the intake air volume by adjusting the fan speed or valve opening, which can be achieved using a frequency converter, reducing the exothermic reaction by decreasing the flue gas input. Activated carbon quality adjustment refers to changing the amount of activated carbon delivered to the adsorption tower per unit time, which can be achieved by adjusting the feed screw speed, increasing the heat absorption capacity by increasing the input of fresh activated carbon.

[0065] Specifically, when the real-time temperature of the activated carbon in the purification section is monitored to be within the range defined by the product of the upper temperature limit and the adjustment coefficient, the initial approach is to reduce the flow rate of the raw flue gas to control the temperature rise. This method has minimal impact on the continuity of system operation. When the temperature exceeds the threshold of the adjustment coefficient product, it indicates that simple flow rate adjustment is no longer effective in controlling the temperature. At this point, it is necessary to increase intervention efforts, either by increasing the frequency of activated carbon replacement to improve the thermal stability of the system, or by directly shutting down the system to investigate the cause of the anomaly. This phased response mechanism ensures both operational efficiency and safety protection requirements. Through this refined control, the system can flexibly respond within different temperature ranges, effectively avoiding safety hazards caused by temperature fluctuations and ensuring the long-term stable operation of the equipment.

[0066] Compared to existing technologies, traditional methods lack a tiered handling strategy for exceeding temperature limits, often resorting to a single threshold to trigger shutdowns, which can easily cause production interruptions. Existing technologies do not establish temperature fluctuation buffer zones, making it impossible to take differentiated actions based on the degree of temperature exceedance. This results in either delayed responses leading to safety hazards or excessive intervention impacting production efficiency.

[0067] Through the above technical solution, this application achieves precise, tiered control of activated carbon temperature anomalies. When the temperature slightly exceeds the limit, continuous production is maintained through flow regulation; when the temperature is severely exceeded, timely reinforcement measures are taken. This avoids the risk of spontaneous combustion of activated carbon at high temperatures and reduces production capacity losses caused by unnecessary shutdowns. Furthermore, by setting an adjustable buffer coefficient, the temperature control strategy can adapt to different operating conditions, improving the system's adaptability and stability.

[0068] This application further proposes adding step S5 to the method for monitoring the operation of an activated carbon adsorption tower. Based on the detected physicochemical properties of the activated carbon, the physicochemical properties of the raw flue gas, the operating parameters of the activated carbon, and the operating parameters of the flue gas, the amount of flue gas leaking from the flue gas purification section to the transition section of the activated carbon adsorption tower is calculated. By accurately quantifying the leakage amount, the internal pressure distribution of the adsorption tower is adjusted, the flue gas flow path is optimized, the load on the purification section is reduced, and the adsorption efficiency of the transition section is improved, ensuring the overall purification effect. Simultaneously, combined with real-time data feedback, the operating parameters are dynamically adjusted to further reduce the risk of leakage and enhance the stability and safety of the system.

[0069] The proportion of flue gas leaking from the flue gas purification section to the transition section refers to the percentage of flue gas volume flowing from the purification section into the transition section per unit time relative to the original total flue gas flow rate. This can be calculated by detecting parameters such as temperature, flow rate, and pollutant concentration, combined with the heat capacity characteristics of activated carbon. The activated carbon temperature in the transition section refers to the actual temperature of the activated carbon during the adsorption process, which can be collected in real time using an embedded temperature sensor (the flue gas volume in this section is relatively small, and its impact on the activated carbon temperature is also small; it can be directly measured using a thermocouple). The activated carbon adjustment coefficient reflects the degree to which the mass of activated carbon and heat transfer affect the leakage rate; its value range can be determined through experimental calibration.

[0070] Specifically, in step S5, parameters such as the raw flue gas temperature, exhaust temperature, transition section activated carbon temperature, activated carbon delivery rate, transition section activated carbon inventory, flue gas flow rate, and pollutant concentration are collected in real time. These parameters are then substituted into calculation formula II, which includes temperature adjustment coefficients and activated carbon adjustment coefficients, to dynamically calculate the real-time leakage ratio from the flue gas purification section to the transition section. When an abnormal increase in the transition section activated carbon temperature is detected, the system automatically triggers the leakage calculation module. By comparing the real-time leakage amount with a preset threshold, it determines whether adjustments to the operating parameters are necessary.

[0071] Compared to existing technologies, which only attempt to reduce leakage through physical structural improvements but cannot quantify the actual leakage amount, and lack dynamic monitoring methods based on real-time data, this solution achieves online quantitative analysis of leakage for the first time by establishing a multi-parameter coupled calculation model, breaking through the technical limitations of traditional passive protection.

[0072] Through the above technical solution, this application can promptly detect abnormal leaks between the flue gas purification section and the transition section, effectively preventing localized overheating of activated carbon and equipment corrosion caused by leaks. Real-time monitoring of leak changes provides data support for optimizing the adsorption tower's sealing structure design and adjusting operating parameters, thereby ensuring the long-term stable operation of the system.

[0073] This application further proposes a method for calculating the amount of flue gas leaking from the flue gas purification section to the transition section in an activated carbon adsorption tower, specifically calculated using Equation II. Here, the activated carbon temperature t4 in the transition section refers to the activated carbon temperature in the non-flue gas flow area, which can be measured using an embedded temperature sensor or an infrared thermal imager, and is used to characterize the impact of leaked flue gas on the transition section. The temperature adjustment coefficient d is used to balance the influence of temperature difference and pollutant concentration on the leakage amount, and its value ranges from 0.6 to 1.5, for example, it can be determined through experimental calibration or fitting of historical data.

[0074] Specifically, by real-time monitoring of the activated carbon temperature in the transition section, the quality of the activated carbon being transported, the quality of the activated carbon in the transition section, the raw flue gas flow rate, and the SO2 concentration at the inlet and outlet, and substituting these parameters into Equation II, the real-time leakage flue gas volume ratio η can be calculated. 实时 This ratio reflects the sealing performance and system resistance balance between the flue gas purification section and the transition section. When η 实时 When the leakage exceeds a preset threshold, it indicates that the leakage amount is outside the safe range and adjustment measures need to be taken. For example, when η 实时 An increase in leakage rate may be caused by abnormal system resistance or sealing structure failure. In this case, leakage can be reduced by decreasing the original flue gas flow rate, or the system can be shut down for maintenance to restore its tightness. By continuously monitoring the real-time trend of η and combining it with historical data analysis, potential leakage risks can be predicted, allowing for preventative maintenance and ensuring safe system operation. Simultaneously, the optimized calculation model can dynamically adjust parameters according to actual operating conditions, further improving the accuracy of leakage assessment and providing a solid guarantee for efficient operation. Furthermore, the model incorporates an environmental temperature compensation mechanism to correct the impact of external temperature fluctuations on measurement results, ensuring data accuracy. Through comprehensive analysis of multi-dimensional parameters, the model can not only provide real-time warnings of leakage risks but also guide optimized operating strategies, extend equipment lifespan, reduce maintenance costs, and comprehensively improve system operating efficiency.

[0075] Compared to existing technologies, which rely solely on atmosphere protection structures to passively reduce leakage and cannot monitor leakage status in real time, this solution establishes a quantitative relationship between leakage and multiple parameters, enabling dynamic calculation and early warning of leakage. For example, existing technologies cannot detect the correlation between changes in activated carbon temperature in the transition section and leakage, while this solution, by introducing the transition section temperature t4 and activated carbon mass m2, can more accurately reflect the heat transfer effect of the leaking flue gas.

[0076] Through the above technical solution, this application can quantify the leakage ratio from the flue gas purification section to the transition section in real time, thereby promptly identifying sealing failures or system resistance imbalances. For example, when the leakage ratio exceeds a threshold, the original flue gas flow rate can be adjusted or the system can be shut down for maintenance to avoid the risk of combustion caused by local temperature rise in the activated carbon in the transition section, while reducing equipment corrosion caused by flue gas condensation, thus ensuring the safety and stability of the adsorption tower operation.

[0077] This application further proposes to monitor in real time the temperature of the raw flue gas, the temperature of the activated carbon in the transition section, the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the mass of activated carbon in the transition section (which can be calculated by the amount of activated carbon delivered to the activated carbon adsorption tower and the amount of activated carbon discharged from the activated carbon adsorption tower, or by calculating the amount of activated carbon filling in the transition section of the activated carbon adsorption tower based on the structural dimensions of the activated carbon adsorption tower), the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the SO2 concentration at the flue gas inlet of the adsorption tower, and the SO2 concentration at the flue gas outlet of the adsorption tower. Substituting these values ​​into Equation II, the real-time proportion η of the flue gas leakage from the flue gas purification section to the transition section in the activated carbon adsorption tower can be obtained. 实时 .

[0078] The activated carbon temperature in the transition section refers to the temperature of the activated carbon in the non-flue gas flow area. This can be monitored in real-time by installing temperature sensors within the transition section to reflect the impact of leaked flue gas on the heat transfer of the activated carbon. The mass of activated carbon delivered to the activated carbon adsorption tower per unit time refers to the amount of activated carbon added to the adsorption tower per hour. This can be measured in real-time using a weighing sensor or flow meter to calculate the heat exchange balance between the activated carbon and the flue gas. The adjustment coefficient d is an empirical parameter set based on the properties of the activated carbon and the composition of the flue gas; for example, its value can range from 0.6 to 1.5. It is used to correlate the combined impact of activated carbon mass and flue gas flow rate on the leakage rate.

[0079] Specifically, parameters such as the temperature of the activated carbon in the transition section, the amount of activated carbon added, the amount of activated carbon in the transition section, the original flue gas flow rate, and the SO2 concentration at the inlet and outlet are simultaneously collected and input into a preset formula II for calculation. Formula II establishes an activated carbon heat balance equation and dynamically quantifies the leakage ratio from the flue gas purification section to the transition section by combining the temperature difference, pollutant concentration difference, and activated carbon physical properties. For example, when the temperature of the activated carbon in the transition section increases, the temperature difference term in Formula II will increase, leading to η 实时 An increase in the calculated result indicates an increase in leakage. Through real-time monitoring and calculation, the system can quickly respond to changes in leakage, adjust operating parameters, ensure efficient operation of the adsorption tower, reduce safety risks, extend equipment life, and improve overall environmental performance.

[0080] Compared to existing technologies, which rely on fixed structures to reduce leakage, these technologies cannot monitor leakage fluctuations in real time, leading to a lack of timely intervention when activated carbon temperatures in the transition section become abnormal. This solution, through dynamic parameter acquisition and calculation, can reflect changes in the leakage ratio in real time, providing data support for operational adjustments and avoiding the risks of equipment corrosion or activated carbon overheating caused by uncontrolled leakage.

[0081] Through the above technical solution, this application achieves real-time monitoring of leakage from the flue gas purification section to the transition section, solving the problem that existing technologies cannot quantify the leakage ratio. This is achieved through dynamic calculation of η. 实时 It can promptly determine whether the leak exceeds the safety threshold, thereby taking measures such as reducing the flue gas flow or shutting down for inspection, effectively controlling the activated carbon temperature in the transition section, preventing equipment corrosion and the risk of activated carbon ignition, and improving the stability of system operation.

[0082] This application further proposes setting an upper limit of the proportion of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower as η0, and comparing the real-time detected proportion of flue gas η 实时 The relationship with η0, if η 实时 If the flow rate exceeds η0, adjust the original flue gas flow rate or shut down the system for inspection. By setting an upper limit for η0, the system is ensured to operate within a safe range, avoiding equipment damage or safety accidents caused by excessive leakage, further optimizing the flue gas purification effect, and improving the overall environmental protection level.

[0083] Wherein, η0 refers to the pre-set upper limit of the allowable leakage proportion of flue gas, which can be determined through engineering tests or historical operating data, for example, a range of 0%-10%. This threshold is used to determine whether the system is in a safe operating state; exceeding this range may cause abnormal activated carbon temperature in the transition section. Wherein, η 实时 This refers to the proportion of leaking flue gas volume calculated by substituting real-time detection parameters into a formula. Specifically, this can be achieved by collecting data such as temperature, flow rate, and concentration from online sensors and inputting this data into the calculation model. This parameter reflects the actual leakage situation during operation and provides a basis for adjustment. Adjusting the original flue gas flow rate refers to changing the amount of flue gas entering the adsorption tower by controlling valve opening or fan speed. For example, reducing the flow rate can lower system pressure, thereby reducing flue gas leakage to the transition section.

[0084] Specifically, during operation, parameters such as activated carbon temperature in the transition section, activated carbon delivery rate, flue gas flow rate, and pollutant concentration are continuously collected and input into a preset calculation model. η is then calculated in real-time using Formula II. 实时 Compare it with the preset η0. If η 实时 If η does not exceed η0, the system maintains its current operating state; if η 实时If the leakage rate exceeds η0, control logic is triggered. For example, the flow rate of the original flue gas is reduced by adjusting the valve opening at the flue gas inlet, thereby reducing the internal pressure difference of the system and suppressing flue gas leakage. When the leakage ratio further exceeds g·η0, the system executes a shutdown command to avoid safety hazards.

[0085] In some specific implementations, the value of η0 can be dynamically adjusted according to the equipment model or operating environment. For example, a stricter threshold can be used under high humidity conditions. When adjusting the original flue gas flow rate, a graded control strategy can be adopted. For example, when the limit is exceeded for the first time, the flow rate can be reduced by 5%-10%. If the leakage still cannot be suppressed, the adjustment range can be gradually increased.

[0086] Compared to existing technologies, which rely on fixed structures to suppress leakage but cannot cope with dynamic fluctuations, this solution, through real-time monitoring and feedback control, can proactively adapt to changes in system resistance and adjust operating parameters in a timely manner. The problems of sudden temperature rise of activated carbon in the transition section and equipment corrosion caused by leakage in existing technologies are effectively mitigated in this solution through closed-loop control of leakage.

[0087] Through the above technical solution, this application realizes dynamic monitoring and active adjustment of leakage from the flue gas purification section to the transition section, avoiding local overheating of activated carbon and equipment corrosion caused by excessive leakage, and improving the stability and safety of adsorption tower operation.

[0088] This application further proposes a tiered control strategy during the operation of the activated carbon adsorption tower when the proportion of real-time flue gas leakage from the flue gas purification section to the transition section exceeds a set threshold. Specifically, if the proportion of real-time leaked flue gas is within a first threshold range, the leakage is controlled by adjusting the flue gas inlet flow rate; if it exceeds a second threshold range, a shutdown inspection mechanism is triggered. The upper limit of the first threshold range is determined by the product of the initial leakage proportion threshold and an adjustment coefficient, with the adjustment coefficient ranging from 1.0 to 1.2, preferably from 1.01 to 1.15, and more preferably from 1.02 to 1.1. Through this tiered control, the system can intervene promptly at the initial stage of leakage to prevent the problem from worsening; and decisively shut down in the event of a severe leakage to ensure equipment safety. This strategy not only improves the system's adaptability but also extends the equipment's service life and reduces maintenance costs.

[0089] The real-time leakage rate refers to the proportion of flue gas leaking from the purification section to the transition section, which is obtained in real time through an online detection system. This can be achieved using a combination of a flue gas composition analyzer and a temperature sensor, calculating the leakage rate by comparing the concentration differences of flue gas components at the inlet of the purification section and the transition section. The initial threshold for the leakage rate is a safety limit set based on the structural strength of the adsorption tower and the thermal stability of the activated carbon. This can be determined through laboratory experiments simulating critical leakage rates under different operating conditions. The adjustment coefficient is an amplification factor used to extend the safe operating range. This can be optimized using a dynamic adjustment algorithm based on the equipment's operating age and maintenance status; for example, for equipment that has been in operation for more than five years, a lower limit value can be automatically applied.

[0090] Specifically, during system operation, when the detected real-time leakage rate exceeds the initial threshold but does not reach the extended threshold of the adjustment coefficient, the system reduces pressure fluctuations by decreasing the flue gas inlet flow rate, thereby suppressing lateral flue gas infiltration. When the leakage rate exceeds the extended threshold, the system automatically switches to protection mode, stops material conveying, and performs a sealing check. For example, when the initial threshold is set to 5% and the adjustment coefficient is 1.1, the system initiates the flow regulation program when the detected leakage rate reaches 5.5%, and executes a shutdown command when the leakage rate exceeds 5.5%.

[0091] Compared to existing technologies, which employ fixed atmosphere protection structures and cannot respond to dynamically changing system resistance, this solution achieves real-time closed-loop control of leakage by establishing a dynamic correlation between the leakage ratio and operating parameters. Furthermore, existing technologies can only detect leaks through periodic maintenance, while this solution, through online monitoring and a tiered control strategy, can intervene promptly in the early stages of a leak, preventing cumulative equipment damage.

[0092] Through the above technical solutions, this application effectively solves the fire risk caused by localized temperature rise of activated carbon in the transition section, as well as the equipment corrosion problem caused by condensation of leaked flue gas. By employing a graded control strategy, the system maintains continuous operation to the maximum extent possible while ensuring purification efficiency, and avoids production losses caused by frequent shutdowns through a threshold expansion mechanism. This solution is particularly suitable for handling high-sulfur load flue gas conditions, and can significantly improve the safety and economy of activated carbon adsorption tower operation.

[0093] It should be noted that all formulas in this invention were obtained by the inventor based on experimental and engineering applications, and all calculations were obtained by substituting the converted values ​​into the formulas according to the prescribed units (after converting the units, only the values ​​are substituted into the formulas for calculation, not the units; the units are only used to adjust the magnitude of each parameter value to ensure the accuracy of the formulas).

[0094] Compared with the prior art, the technical solution proposed in this invention has the following beneficial technical effects:

[0095] 1. This invention proposes a method for indirectly and accurately calculating the temperature of activated carbon in the flue gas purification section of an activated carbon adsorption tower, which effectively avoids the problems of not being able to measure directly and the large errors of indirect measurement, and improves the accuracy of temperature monitoring.

[0096] 2. This invention proposes a method for calculating the amount of flue gas leaking from the flue gas purification section to the transition section in an activated carbon adsorption tower. By dynamically linking the leakage ratio with operating parameters, real-time closed-loop control of the leakage amount is achieved, which significantly improves the sensitivity and accuracy of leakage detection and reduces equipment damage and production interruption caused by leakage.

[0097] 3. The technical solution provided by this invention is convenient to test, highly accurate, applicable to various working conditions, effectively reduces maintenance costs and operational risks, and improves the reliability and stability of the overall system.

[0098] 4. By optimizing the control strategy, this invention further improves the system's response speed to sudden leaks, ensures safe operation under high load conditions, extends equipment service life, and reduces long-term operating costs. Attached Figure Description

[0099] Figure 1 This refers to the existing lateral stratified crossflow process and adsorption tower.

[0100] Figure 2 This is the structure of an adsorption tower in the existing technology;

[0101] Figure 3 This is a schematic diagram of the windward side and transition section structure of an existing adsorption tower. Detailed Implementation

[0102] The technical solutions in this application are described clearly and completely below. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application. It should be noted that similar reference numerals and letters in the following figures indicate similar items. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0103] Example 1

[0104] A method for monitoring the operating status of an activated carbon adsorption tower, the method comprising the following steps:

[0105] S1. Detect the physicochemical properties of activated carbon and the physicochemical properties of raw flue gas;

[0106] S2. The activated carbon adsorption tower is divided into an activated carbon inlet, a flue gas purification section, a transition section, and a discharge port from top to bottom. Activated carbon is conveyed into the activated carbon adsorption tower through the inlet. The activated carbon passes through the flue gas purification section and the transition section in sequence inside the activated carbon adsorption tower, and then is discharged from the discharge port of the activated carbon adsorption tower. The raw flue gas is conveyed into the activated carbon adsorption tower, passes through the flue gas purification section of the activated carbon adsorption tower, and is discharged from the exhaust port of the activated carbon adsorption tower after being purified by the flue gas purification section.

[0107] S3. Detect the operating parameters of activated carbon in the activated carbon adsorption tower and the operating parameters of flue gas in the activated carbon adsorption tower;

[0108] S4. Based on the parameters obtained in steps S1 and S3, calculate the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower.

[0109] Example 2

[0110] Repeat Example 1, except that the specific calculation of the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower is as follows:

[0111] ...Formula I;

[0112] In Formula I: t3 is the temperature of the activated carbon in the purification section, °C; t1 is the temperature of the raw flue gas, °C; t2 is the temperature of the gas discharged from the flue gas exhaust port of the activated carbon adsorption tower, °C; m1 is the mass of activated carbon in the activated carbon adsorption tower, kg; C p1 Specific heat capacity of sintering flue gas, J / (mol·℃); C p2 ρ is the specific heat capacity of activated carbon, J / (Kg·℃); Vm is the molar volume, taken as 22.4 L / mol; M is the relative molecular mass of SO2, 64 g / mol; H is the heat released by the oxidation of 1 mol SO2 to sulfuric acid, taken as 275000 J / mol; q1 is the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, Nm 3 C0 represents the SO2 concentration in the original flue gas at the flue gas inlet of the adsorption tower, in g / Nm³. 3 C1 represents the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower, in g / Nm³. 3 ; 'a' represents the flue gas adjustment coefficient, in L / Nm³. 3 , with a value of 800-1200; b is the pollutant adjustment coefficient, with a value of 0.9-1.2.

[0113] Example 3

[0114] Repeat Example 2, but with real-time monitoring of the following parameters: the temperature of the raw flue gas, the temperature of the gas discharged from the flue gas outlet of the activated carbon adsorption tower, the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the flow rate of the gas discharged from the flue gas outlet of the adsorption tower per unit time, the SO2 concentration in the raw flue gas at the flue gas inlet of the adsorption tower, and the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower. Substituting these parameters into Equation I, the real-time temperature t of the activated carbon in the flue gas purification section of the activated carbon adsorption tower is obtained. 3-实时 .

[0115] Example 4

[0116] Repeat Example 3, except that the upper limit of the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower is set to t0 = 150℃, and the comparison is as follows:

[0117] If t 3-实时 If the value is less than or equal to t0, continue running.

[0118] If t 3-实时 >t0, adjust the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower, or adjust the quality of activated carbon delivered to the activated carbon adsorption tower per unit time, or stop the machine for inspection.

[0119] Example 5

[0120] Repeat Example 4, except that if t0 < t 3-实时 ≤1.2·t0, reduce the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower;

[0121] If t 3-实时 If the value is greater than 1.2·t0, adjust the quality of activated carbon delivered to the activated carbon adsorption tower per unit time or stop the machine for inspection.

[0122] Example 6

[0123] A method for monitoring the operating status of an activated carbon adsorption tower, the method comprising the following steps:

[0124] S1. Detect the physicochemical properties of activated carbon and the physicochemical properties of raw flue gas;

[0125] S2. The activated carbon adsorption tower is divided into an activated carbon inlet, a flue gas purification section, a transition section, and a discharge port from top to bottom. Activated carbon is conveyed into the activated carbon adsorption tower through the inlet. The activated carbon passes through the flue gas purification section and the transition section in sequence inside the activated carbon adsorption tower, and then is discharged from the discharge port of the activated carbon adsorption tower. The raw flue gas is conveyed into the activated carbon adsorption tower, passes through the flue gas purification section of the activated carbon adsorption tower, and is discharged from the exhaust port of the activated carbon adsorption tower after being purified by the flue gas purification section.

[0126] S3. Detect the operating parameters of activated carbon in the activated carbon adsorption tower and the operating parameters of flue gas in the activated carbon adsorption tower;

[0127] S4. Calculate the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower based on the parameters obtained in steps S1 and S3.

[0128] S5. Based on the parameters obtained in steps S1 and S3, calculate the amount of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower.

[0129] Example 7

[0130] Repeat Example 6, except that the specific calculation of the amount of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower is as follows:

[0131] ...Formula II;

[0132] In Formula II, η is the proportion of flue gas leaking from the flue gas purification section to the transition section, %; t3 is the activated carbon temperature in the purification section, °C; t4 is the activated carbon temperature in the transition section, °C; m2 is the mass of activated carbon in the transition section, kg; C p2 q1 is the specific heat capacity of activated carbon, J / (Kg·℃); q1 is the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, Nm³. 3 M is the relative molecular mass of SO2, 64 g / mol; H is the heat released when 1 mol of SO2 is oxidized to sulfuric acid, taken as 275000 J / mol; CO is the SO2 concentration in the original flue gas at the flue gas inlet of the adsorption tower, g / Nm³. 3 C1 represents the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower, in g / Nm³. 3 d is the flue gas volume adjustment coefficient, with a value of 0.6-1.5.

[0133] Example 8

[0134] Repeat Example 7, but with real-time monitoring of the following parameters: raw flue gas temperature, gas temperature at the exhaust port of the activated carbon adsorption tower, activated carbon temperature in the transition section, mass of activated carbon delivered to the activated carbon adsorption tower per unit time, mass of activated carbon in the transition section, flow rate of raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, flow rate of exhaust gas at the flue gas outlet of the adsorption tower per unit time, SO2 concentration at the flue gas inlet of the adsorption tower, and SO2 concentration at the flue gas outlet of the adsorption tower. Substituting these parameters into Equation II, the real-time proportion η of flue gas leakage from the flue gas purification section to the transition section in the activated carbon adsorption tower is obtained. 实时 .

[0135] Example 9

[0136] Repeat Example 8, except that the upper limit of the proportion of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower is set to η0 = 2%, and the comparison is as follows:

[0137] If η 实时 If ≤η0, continue running;

[0138] If η 实时 If the value is greater than η0, adjust the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower or shut down the tower for inspection.

[0139] Example 10

[0140] Repeat Example 9, except that if η0 < η 实时 ≤1.1·η0, reduce the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower;

[0141] If η 实时 >1.1·η0, stop the machine for inspection.

[0142] Example 11

[0143] Repeat Example 5, except that t0 = 180°C.

[0144] Example 12

[0145] Repeat Example 10, except that η0 = 5%.

[0146] Application Example 1

[0147] Using the technical solution described in Example 9, the following was detected:

[0148] The temperature of the raw flue gas, t1, is 135℃; the temperature of the gas discharged from the flue gas outlet of the activated carbon adsorption tower, t2, is 136℃; the mass of activated carbon in the activated carbon adsorption tower, m1, is 2,000,000 kg; the specific heat capacity of the sintering flue gas, C... p1 30 J / (mol·℃); Specific heat capacity of activated carbon C p2 The concentration is 840 J / (Kg·℃); the flow rate q1 of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time is 450000 Nm³. 3 The SO2 concentration (CO) in the raw flue gas at the flue gas inlet of the adsorption tower is 900 mg / Nm³. 3 The SO2 concentration C1 in the gas discharged from the flue gas outlet of the adsorption tower is 20 mg / Nm³. 3 The activated carbon temperature t4 in the transition section is 142℃; the activated carbon mass m2 in the transition section is 1500kg. t3 is calculated to be 135.6℃ according to Formula I, and η is calculated to be 0.97% according to Formula II.

[0149] Set t0 to 140℃, t3≤t0, and continue running;

[0150] If η≤1%, continue running.

[0151] Application Example 2

[0152] Using the technical solution described in Example 10, the following was detected:

[0153] The temperature of the raw flue gas, t1, is 133℃; the temperature of the gas discharged from the flue gas outlet of the activated carbon adsorption tower, t2, is 134℃; the mass of activated carbon in the activated carbon adsorption tower, m1, is 2,000,000 kg; the specific heat capacity of the sintering flue gas, C... p1 30 J / (mol·℃); Specific heat capacity of activated carbon C p2 The concentration is 840 J / (Kg·℃); the flow rate q1 of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time is 430000 Nm³. 3 The SO2 concentration (CO) in the raw flue gas at the flue gas inlet of the adsorption tower is 780 mg / Nm³. 3 The SO2 concentration C1 in the gas discharged from the flue gas outlet of the adsorption tower is 20 mg / Nm³. 3 The activated carbon temperature t4 in the transition section is 136℃; the activated carbon mass m2 in the transition section is 1500kg. t3 is calculated to be 133.5℃ according to Formula I, and η is calculated to be 2.11% according to Formula II.

[0154] If 2% < η < 2.2%, reduce the flow rate of the original flue gas delivered to the flue gas inlet of the activated carbon adsorption tower to 80% of the initial flow rate, and continue operation.

[0155] Application Example 3

[0156] Using the technical solution described in Example 10, continue running for 120 hours and perform real-time monitoring again:

[0157] The temperature of the raw flue gas, t1, is 128℃; the temperature of the gas discharged from the flue gas outlet of the activated carbon adsorption tower, t2, is 129℃; the mass of activated carbon in the activated carbon adsorption tower, m1, is 2,000,000 kg; the specific heat capacity of the sintering flue gas, C... p1 30 J / (mol·℃); Specific heat capacity of activated carbon C p2 The concentration is 840 J / (Kg·℃); the flow rate q1 of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time is 360000 Nm³. 3 The SO2 concentration (CO) in the raw flue gas at the flue gas inlet of the adsorption tower is 750 mg / Nm³. 3 The SO2 concentration C1 in the gas discharged from the flue gas outlet of the adsorption tower is 10 mg / Nm³. 3The activated carbon temperature t4 in the transition section is 131℃; the activated carbon mass m2 in the transition section is 1500kg. t3 is calculated to be 128.4℃ according to Formula I, and η is calculated to be 2.85% according to Formula II.

[0158] If η > 2.4%, stop the machine for inspection.

[0159] The above description is merely an embodiment of this application and is not intended to limit the scope of protection of this application. Various modifications and variations can be made to this application by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this application should be included within the scope of protection of this application.

Claims

1. A method for monitoring the operating status of an activated carbon adsorption tower, the method comprising the following steps: S1. Detect the physicochemical properties of activated carbon and the physicochemical properties of raw flue gas; S2. The activated carbon adsorption tower is divided into an activated carbon inlet, a flue gas purification section, a transition section, and a discharge outlet from top to bottom; the activated carbon is conveyed into the inlet of the activated carbon adsorption tower. Activated carbon passes through the flue gas purification section and the transition section in the activated carbon adsorption tower in sequence, and then is discharged from the discharge port of the activated carbon adsorption tower. The raw flue gas is transported into the activated carbon adsorption tower, passes through the flue gas purification section of the activated carbon adsorption tower, and is discharged from the exhaust port of the activated carbon adsorption tower after being purified by the flue gas purification section. S3. Detect the operating parameters of activated carbon in the activated carbon adsorption tower and the operating parameters of flue gas in the activated carbon adsorption tower; S4. Calculate the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower based on the parameters obtained in steps S1 and S3.

2. The method according to claim 1, characterized in that: The specific calculation of the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower is as follows: ... Formula I; In Formula I: t3 is the temperature of the activated carbon in the purification section, °C; t1 is the temperature of the raw flue gas, °C; t2 is the temperature of the gas discharged from the flue gas exhaust port of the activated carbon adsorption tower, °C; m1 is the mass of activated carbon in the activated carbon adsorption tower, kg; C p1 Specific heat capacity of sintering flue gas, J / (mol·℃); C p2 ρ is the specific heat capacity of activated carbon, J / (Kg·℃); Vm is the molar volume, taken as 22.4 L / mol; M is the relative molecular mass of SO2, 64 g / mol; H is the heat released by the oxidation of 1 mol SO2 to sulfuric acid, taken as 275000 J / mol; q1 is the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, Nm 3 C0 represents the SO2 concentration in the original flue gas at the flue gas inlet of the adsorption tower, in g / Nm³. 3 C1 represents the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower, in g / Nm³. 3 ; 'a' represents the flue gas adjustment coefficient, in L / Nm³. 3 , with a value of 800-1200; b is the pollutant adjustment coefficient, with a value of 0.9-1.

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3. The method according to claim 1 or 2, characterized in that: The temperature of the raw flue gas, the temperature of the gas discharged from the flue gas outlet of the activated carbon adsorption tower, the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the SO2 concentration in the raw flue gas at the flue gas inlet of the adsorption tower, and the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower are monitored in real time. Substituting these values ​​into Equation I, the real-time temperature t of the activated carbon in the flue gas purification section of the activated carbon adsorption tower is obtained. 3-实时 .

4. The method according to claim 3, characterized in that: Set the upper limit of the activated carbon temperature in the flue gas purification section of the activated carbon adsorption tower to t0, and compare: If t 3-实时 If the value is less than or equal to t0, continue running. If t 3-实时 >t0, adjust the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower, or adjust the quality of activated carbon delivered to the activated carbon adsorption tower per unit time, or stop the machine for inspection.

5. The method according to claim 4, characterized in that: If t0 < t 3-实时 ≤f·t0, reduce the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower; If t 3-实时 >f·t0, adjust the quality of activated carbon delivered to the activated carbon adsorption tower per unit time or stop the machine for inspection; Wherein: f=1.0-1.4, preferably f=1.01-1.35, and even more preferably f=1.03-1.

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6. The method according to any one of claims 1-5, characterized in that: The method also includes the following steps: S5. Based on the parameters obtained in steps S1 and S3, calculate the amount of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower.

7. The method according to claim 6, characterized in that: The specific calculation of the amount of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower is as follows: ...Formula II; In Equation II, η is the proportion of flue gas leaking from the flue gas purification section to the transition section, % t3 is the activated carbon temperature in the purification section, °C; t4 is the activated carbon temperature in the transition section, °C; m2 is the mass of activated carbon in the transition section, kg; C p2 q1 is the specific heat capacity of activated carbon, J / (Kg·℃); q1 is the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, Nm³. 3 M is the relative molecular mass of SO2, 64 g / mol; H is the heat released when 1 mol of SO2 is oxidized to sulfuric acid, taken as 275000 J / mol; CO is the SO2 concentration in the original flue gas at the flue gas inlet of the adsorption tower, g / Nm³. 3 C1 represents the SO2 concentration in the gas discharged from the flue gas outlet of the adsorption tower, in g / Nm³. 3 d is the flue gas volume adjustment coefficient, with a value of 0.6-1.

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8. The method according to claim 7, characterized in that: The following parameters are monitored in real time: the temperature of the raw flue gas, the temperature of the gas at the exhaust port of the activated carbon adsorption tower, the temperature of the activated carbon in the transition section, the mass of activated carbon delivered to the activated carbon adsorption tower per unit time, the mass of activated carbon in the transition section, the flow rate of the raw flue gas delivered to the flue gas inlet of the adsorption tower per unit time, the SO2 concentration at the flue gas inlet of the adsorption tower, and the SO2 concentration at the flue gas outlet of the adsorption tower. Substituting these parameters into Equation II, the real-time proportion η of the flue gas leakage from the flue gas purification section to the transition section in the activated carbon adsorption tower is obtained. 实时 .

9. The method according to claim 8, characterized in that: Set the upper limit of the proportion of flue gas leaking from the flue gas purification section to the transition section in the activated carbon adsorption tower to η0, and compare: If η 实时 If ≤η0, continue running; If η 实时 If the value is greater than η0, adjust the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower or shut down the tower for inspection.

10. The method according to claim 9, characterized in that: If η0 < η 实时 ≤g·η0, reduce the flow rate of the raw flue gas at the flue gas inlet of the activated carbon adsorption tower; If η 实时 >g·η0, stop the machine for inspection; Wherein: g=1.0-1.2, preferably g=1.01-1.15, and even more preferably g=1.02-1.

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11. The method according to claim 4, characterized in that: t0 is 100-200℃, preferably 120-180℃, and more preferably 140-160℃.

12. The method according to claim 9, characterized in that: η0 is 0-10%, preferably 0.1%-8%, and more preferably 0.2%-5%.

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