A High-Efficiency Pneumatic Emulsification Flue Gas Deep Desulfurization Method and System with Multi-Point Feeding

Abstract

This invention discloses a high-efficiency pneumatic emulsification flue gas deep desulfurization method and system with multi-point feeding, relating to the field of flue gas separation technology. The method includes: dividing the flue gas into multiple feeding sections along the height of the desulfurization tower by detecting flue gas load data, and determining the segmented feeding configuration information; determining the high-pressure airflow injection intensity and desulfurizing agent supply amount for each tower section based on the flue gas flow rate; introducing flue gas in segments according to the configuration information, while simultaneously using high-pressure airflow to impact the desulfurizing agent liquid to form droplets, achieving synchronous contact and reaction between the flue gas and the droplets; dynamically adjusting the desulfurizing agent supply distribution ratio by monitoring the residual sulfur dioxide concentration in each tower section to form a concentration decreasing gradient; and finally, discharging the gradient-desulfurized flue gas and desulfurization products from the top and bottom of the tower, respectively. This method achieves segmented and precise flue gas addition and deep desulfurization, exhibiting high desulfurization efficiency.

Description

Technical Field

[0001] This invention relates to the field of flue gas separation technology, specifically to a high-efficiency pneumatic emulsification flue gas deep desulfurization method and system with multi-point feeding. Background Technology

[0002] Flue gas desulfurization (FGD) technology is an important means of controlling air pollution. Existing FGD technologies mainly include spray desulfurization, cyclone desulfurization, and Venturi desulfurization. These technologies typically employ a single-point feed method, introducing the flue gas to be treated from the bottom or middle of the tower, allowing it to undergo a gas-liquid contact reaction with the desulfurizing agent, thereby removing sulfur dioxide from the flue gas.

[0003] With increasingly stringent environmental protection requirements, traditional single-point feed desulfurization technology can no longer meet the demands of deep desulfurization. Single-point feed suffers from problems such as insufficient gas-liquid contact, short reaction time, and low desulfurization efficiency. Furthermore, due to large fluctuations in flue gas load, single-point feed makes it difficult to achieve precise control of the desulfurization process, resulting in low utilization of the desulfurizing agent.

[0004] To improve desulfurization efficiency, various gas-liquid enhanced contact technologies have been developed, such as increasing the packing layer, increasing the liquid-to-gas ratio, and employing multi-stage desulfurization. However, these technologies often lead to increased system resistance and energy consumption, and are difficult to effectively cope with dynamic changes in flue gas load. Especially in large-scale industrial applications, equipment investment and operating costs remain high.

[0005] Existing technologies have also developed some multi-point feed desulfurization schemes, but they generally suffer from problems such as unreasonable feed distribution, poor gas-liquid mixing, and low automation. These schemes lack the ability to accurately identify and dynamically respond to flue gas load characteristics, cannot achieve synergistic optimization of the desulfurization process, and are difficult to guarantee stable deep desulfurization results. Summary of the Invention

[0006] The purpose of this invention is to provide a highly efficient pneumatic emulsification flue gas deep desulfurization method and system with multi-point feeding, aiming to solve at least one of the technical problems existing in the prior art.

[0007] The technical solution of this invention is: a high-efficiency pneumatic emulsification flue gas deep desulfurization method with multi-point feeding, comprising the following steps:

[0008] The flow rate and sulfur dioxide concentration of the flue gas to be treated are detected to obtain flue gas load data;

[0009] Based on the flue gas load data, the flue gas is divided into multiple feeding sections along the height of the desulfurization tower. The flue gas flow rate is allocated to each feeding section and the inlet position is determined to obtain the segmented feeding configuration information.

[0010] Based on the flue gas flow rate of each feeding section in the segmented feeding configuration information, the injection intensity of the high-pressure airflow and the supply of desulfurizing agent liquid in the corresponding tower section are determined, and the atomization control command of each tower section is obtained.

[0011] According to the segmented feeding configuration information, the flue gas is introduced into the desulfurization tower in segments. At the same time, according to the atomization control command, the desulfurizing agent liquid flow is impacted by the high-pressure airflow in each tower segment to form droplets. During the droplet formation process, the flue gas and the droplets are simultaneously contacted and reacted to obtain the reaction intermediate state of each tower segment.

[0012] Monitor the residual sulfur dioxide concentration in the reaction intermediate state, and adjust the distribution ratio of desulfurizing agent supply between adjacent tower sections according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, and obtain flue gas after gradient desulfurization.

[0013] After gradient desulfurization, the flue gas is discharged from the top of the desulfurization tower, and the desulfurization products generated by the reaction are discharged from the bottom of the desulfurization tower.

[0014] Furthermore, based on the flue gas load data, the flue gas is divided into multiple feed sections along the height of the desulfurization tower. Flue gas flow rates are allocated to each feed section, and the inlet locations are determined, resulting in segmented feed configuration information including:

[0015] Obtain the flue gas velocity and sulfur dioxide concentration distribution from the flue gas load data, calculate the pressure loss value at each measurement location of the desulfurization tower, and generate a flue gas flow parameter diagram.

[0016] The flow resistance coefficient and diffusion coefficient of the flue gas in the desulfurization tower are calculated based on the flue gas flow parameter diagram to determine the movement trajectory of the flue gas components and generate flue gas movement characteristic data.

[0017] Based on flue gas motion characteristic data, the gas-liquid mixing coefficient and mass transfer coefficient at different locations in the desulfurization tower are calculated. According to the numerical distribution of the gas-liquid mixing coefficient and mass transfer coefficient, the desulfurization tower is divided into multiple feeding sections along the height direction to determine the feeding section distribution information.

[0018] Based on the distribution information of the feeding section, the position with the optimal mass transfer coefficient value in each feeding section is selected as the feeding port position to form the feeding port position information;

[0019] Calculate the ratio of mass transfer coefficient values ​​for each feeding section, and iteratively calculate the flue gas flow rate based on the ratio of mass transfer coefficient values ​​until the difference in flue gas flow rate between two adjacent iterations is less than the preset flow rate difference threshold, and then determine the flue gas flow rate allocation scheme.

[0020] The information on the distribution of the feeding section, the location of the feeding port, and the flue gas flow distribution scheme are combined to generate segmented feeding configuration information.

[0021] Furthermore, based on flue gas motion characteristic data, the gas-liquid mixing coefficient and mass transfer coefficient at different locations in the desulfurization tower are calculated. According to the numerical distribution of the gas-liquid mixing coefficient and mass transfer coefficient, the desulfurization tower is divided into multiple feed sections along its height. The distribution information of the feed sections includes:

[0022] Based on the flue gas motion characteristic data, the measurement points at different locations of the desulfurization tower are determined, and the gas-liquid relative motion parameters and component transfer parameters at the measurement points are obtained to generate flue gas flow data.

[0023] Calculate the initial gas-liquid mixing coefficient and initial mass transfer coefficient at the measurement point based on flue gas flow data;

[0024] Temperature and pressure parameters are collected at the measurement point. The temperature and pressure parameters are substituted into the initial gas-liquid mixing coefficient and the initial mass transfer coefficient for correction, and the corrected gas-liquid mixing coefficient and mass transfer coefficient are generated.

[0025] Based on the numerical distribution of the corrected gas-liquid mixing coefficient and mass transfer coefficient, a mass transfer performance distribution curve is constructed. The slope change position of the mass transfer performance distribution curve is calculated. According to the slope change position, the desulfurization tower is divided into multiple feed sections along the height direction, and the feed section boundary position is generated.

[0026] Calculate the average values ​​of the gas-liquid mixing coefficient and mass transfer coefficient in multiple feed sections, sort the multiple feed sections according to the average values, and generate the feed section distribution structure.

[0027] The feed section distribution information is generated by combining the feed section boundary location with the feed section distribution structure.

[0028] Furthermore, based on the flue gas flow rate of each feeding section in the segmented feeding configuration information, the injection intensity of the high-pressure airflow and the supply amount of desulfurizing agent in the corresponding tower section are determined, resulting in atomization control commands for each tower section, including:

[0029] Obtain the flue gas flow rate of each feeding section from the segmented feeding configuration information, calculate the flue gas flow velocity of each feeding section, and obtain the flue gas velocity data of each feeding section.

[0030] Based on the flue gas velocity data of each feeding section, the injection intensity of the high-pressure airflow and the effective range of the desulfurizing agent liquid are calculated to obtain the distribution data of the desulfurizing agent liquid.

[0031] Based on the distribution data of the desulfurizing agent liquid, the relationship between the injection intensity of the high-pressure airflow and the supply amount of the desulfurizing agent liquid is calculated to obtain the injection intensity data of the high-pressure airflow.

[0032] Based on the high-pressure airflow injection intensity data and the flue gas flow rate of each feeding section, the minimum supply of desulfurizing agent liquid is calculated, and the desulfurizing agent liquid supply data is obtained.

[0033] Based on the desulfurizing agent supply data, the reaction conversion rate was measured, and the injection intensity of the high-pressure airflow and the supply of the desulfurizing agent were adjusted to obtain the injection intensity and supply ratio data.

[0034] Based on the ratio of injection intensity to supply, the injection intensity of the high-pressure airflow and the supply of desulfurizing agent are set to obtain the atomization control commands for each tower section.

[0035] Furthermore, according to the segmented feeding configuration information, the flue gas is introduced into the desulfurization tower in segments. Simultaneously, according to the atomization control command, the desulfurizing agent liquid flow is impacted by a high-pressure airflow in each tower segment to form droplets. During the droplet formation process, the flue gas and the droplets simultaneously react, resulting in the following reaction intermediate states in each tower segment:

[0036] Obtain the feed inlet location information and flue gas flow distribution scheme from the segmented feed configuration information, introduce the flue gas into the desulfurization tower according to the feed inlet location information, adjust the flue gas flow at the feed inlet according to the flue gas flow distribution scheme, and monitor the flue gas distribution at each feed inlet.

[0037] Based on the monitored flue gas distribution, read the high-pressure airflow injection intensity data and desulfurizing agent liquid supply data from the atomization control command, adjust the injection pressure and injection angle of the high-pressure airflow, and control the supply rate of the desulfurizing agent liquid.

[0038] By adjusting the high-pressure airflow to impact the desulfurizing agent liquid flow, the impact angle and impact position between the high-pressure airflow and the desulfurizing agent liquid flow are controlled, so that the desulfurizing agent liquid flow is atomized into droplets.

[0039] The formed droplets are brought into contact with the introduced flue gas to react. The contact position and contact time between the flue gas and the droplets are adjusted, and the reaction parameters of the flue gas in each tower section are measured, including the sulfur dioxide concentration and the amount of droplets absorbed.

[0040] The removal rate and conversion rate of sulfur dioxide in each tower section are calculated based on the measured reaction parameters. The absorption saturation of droplets in each tower section is determined. The reaction temperature and pressure in each tower section are recorded, and the reaction intermediate state in each tower section is generated.

[0041] Furthermore, the residual sulfur dioxide concentration in the reaction intermediate is monitored, and the distribution ratio of the desulfurizing agent supply between adjacent tower sections is adjusted according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, resulting in the flue gas after gradient desulfurization including:

[0042] Collect the residual sulfur dioxide concentration and gas flow rate in the intermediate state of the reaction, calculate the desulfurization reaction rate and desulfurizing agent conversion efficiency of each tower section, and generate the sulfur dioxide concentration distribution.

[0043] Based on the sulfur dioxide concentration distribution analysis, the residual sulfur dioxide concentration difference between adjacent tower sections is analyzed, the desulfurizing agent consumption and reaction degree of each tower section are calculated, and the concentration change characteristics are obtained.

[0044] Based on the consumption and reaction degree of desulfurizing agent in each tower section, establish the response curve of desulfurizing agent supply and sulfur dioxide residual concentration change, calculate the concentration gradient value and desulfurizing agent demand between adjacent tower sections, and determine the supply adjustment scheme.

[0045] The desulfurizing agent replenishment amount for each tower section is set according to the supply adjustment plan. The desulfurizing agent distribution device is controlled to adjust the supply distribution ratio. The change of sulfur dioxide residual concentration is monitored to obtain sulfur dioxide residual concentration data.

[0046] Calculate the concentration difference between adjacent tower sections based on the residual sulfur dioxide concentration data, adjust the supply ratio of the desulfurizing agent distribution device, control the desulfurizing agent supply rate of each tower section, monitor the sulfur dioxide concentration at the outlet of each tower section, and adjust the desulfurizing agent supply based on the monitored sulfur dioxide concentration until the sulfur dioxide concentration difference between adjacent tower sections meets the preset gradient requirements, thereby obtaining the flue gas after gradient desulfurization.

[0047] Furthermore, the flue gas after gradient desulfurization is discharged from the top of the desulfurization tower, and the desulfurization products generated in the reaction are discharged from the bottom of the desulfurization tower, including:

[0048] The flow characteristics of the flue gas after gradient desulfurization at the top of the desulfurization tower are detected, the flow velocity of the flue gas after gradient desulfurization in the exhaust channel is calculated, the distribution of the flue gas after gradient desulfurization is monitored, and the discharge conditions of the flue gas after gradient desulfurization are determined.

[0049] Based on the determined discharge conditions, the pressure distribution of the flue gas after gradient desulfurization in the exhaust channel is analyzed, the flow field change of the flue gas after gradient desulfurization is calculated, and the treatment scheme of the flue gas after gradient desulfurization is obtained.

[0050] The settling distribution of desulfurization products at the bottom of the desulfurization tower is collected, the distribution location of the desulfurization products is measured, the settling velocity of the desulfurization products is calculated, and the emission requirements of the desulfurization products are determined.

[0051] The treatment scheme for flue gas after gradient desulfurization is matched with the emission requirements of desulfurization products. The operating ratio of exhaust device and emission device is calculated, the opening degree of exhaust device and the rotation speed of emission device are controlled, the discharge amount of flue gas after gradient desulfurization and the discharge amount of desulfurization products are adjusted, and the pressure inside the tower is measured.

[0052] Adjust the operating parameters of the exhaust and emission devices according to the measured pressure inside the tower, control the flue gas after gradient desulfurization to be discharged from the top of the desulfurization tower through the exhaust device, and control the desulfurization products to be discharged from the bottom of the desulfurization tower through the emission device.

[0053] This invention provides a multi-point feeding, high-efficiency pneumatic emulsified flue gas deep desulfurization system, the system comprising:

[0054] The flue gas detection unit is used to detect the flow rate and sulfur dioxide concentration of the flue gas to be treated, and to obtain flue gas load data;

[0055] The feed configuration unit is used to divide the flue gas into multiple feed sections along the height of the desulfurization tower according to the flue gas load data, allocate flue gas flow rate to each feed section and determine the feed inlet position to obtain the segmented feed configuration information.

[0056] The atomization control unit is used to determine the injection intensity of the high-pressure airflow and the supply amount of desulfurizing agent liquid in the corresponding tower section based on the flue gas flow rate of each feed section in the segmented feed configuration information, and to obtain the atomization control command for each tower section.

[0057] The reaction control unit is used to introduce flue gas into the desulfurization tower in stages according to the staged feed configuration information. At the same time, according to the atomization control command, the desulfurizing agent liquid flow is impacted by high pressure airflow in each tower section to form droplets. During the droplet formation process, the flue gas and the droplets are simultaneously contacted and reacted to obtain the reaction intermediate state of each tower section.

[0058] The concentration adjustment unit is used to monitor the residual sulfur dioxide concentration in the reaction intermediate state and adjust the distribution ratio of desulfurizing agent supply between adjacent tower sections according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, and the flue gas after gradient desulfurization is obtained.

[0059] The emission control unit is used to discharge the flue gas after gradient desulfurization from the top of the desulfurization tower and to discharge the desulfurization products generated by the reaction from the bottom of the desulfurization tower.

[0060] One technical solution provided in this embodiment of the invention is an electronic device, including: a memory, a processor, and a computer program stored in the memory and executable on the processor, wherein the processor executes the computer program to implement the steps in any of the aforementioned methods.

[0061] One technical solution provided in this embodiment of the invention is a computer-readable storage medium storing computer program instructions, which, when executed by a processor, implement the steps in any of the aforementioned methods.

[0062] This invention employs dynamic flue gas load detection and segmented feeding to achieve precise distribution and dosing control of flue gas. The gas-liquid contact efficiency is significantly improved through the pneumatic emulsification of the high-pressure airflow and desulfurizing agent liquid. A concentration gradient control strategy is used in each tower section to enhance the mass transfer driving force of the desulfurization process. The synergistic effect of multi-point feeding and pneumatic emulsification ensures full utilization of the desulfurizing agent. It can adaptively adjust according to flue gas load characteristics to maintain a stable desulfurization effect. This reduces system operating resistance, decreases energy consumption, and improves equipment operating efficiency, demonstrating significant engineering application value. Attached Figure Description

[0063] Figure 1 A flowchart of a high-efficiency pneumatic emulsification flue gas deep desulfurization method with multi-point feeding provided in an embodiment of the present invention;

[0064] Figure 2 This is a comparison chart of the droplet size distribution frequency in an embodiment of the present invention.

[0065] Figure 3 This is the dynamic adjustment response curve for abnormal pressure fluctuations inside the tower according to an embodiment of the present invention.

[0066] Figure 4 This is a schematic diagram of a high-efficiency pneumatic emulsification flue gas deep desulfurization system with multi-point feeding, provided in an embodiment of the present invention. Detailed Implementation

[0067] like Figure 1 As shown, Figure 1 This is a flowchart of a multi-point feeding, high-efficiency pneumatic emulsification flue gas deep desulfurization method provided in an embodiment of the present invention. The method includes the following steps:

[0068] The flow rate and sulfur dioxide concentration of the flue gas to be treated are detected to obtain flue gas load data;

[0069] Based on the flue gas load data, the flue gas is divided into multiple feeding sections along the height of the desulfurization tower. The flue gas flow rate is allocated to each feeding section and the inlet position is determined to obtain the segmented feeding configuration information.

[0070] Based on the flue gas flow rate of each feeding section in the segmented feeding configuration information, the injection intensity of the high-pressure airflow and the supply of desulfurizing agent liquid in the corresponding tower section are determined, and the atomization control command of each tower section is obtained.

[0071] According to the segmented feeding configuration information, the flue gas is introduced into the desulfurization tower in segments. At the same time, according to the atomization control command, the desulfurizing agent liquid flow is impacted by the high-pressure airflow in each tower segment to form droplets. During the droplet formation process, the flue gas and the droplets are simultaneously contacted and reacted to obtain the reaction intermediate state of each tower segment.

[0072] Monitor the residual sulfur dioxide concentration in the reaction intermediate state, and adjust the distribution ratio of desulfurizing agent supply between adjacent tower sections according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, and obtain flue gas after gradient desulfurization.

[0073] After gradient desulfurization, the flue gas is discharged from the top of the desulfurization tower, and the desulfurization products generated by the reaction are discharged from the bottom of the desulfurization tower.

[0074] Based on the flue gas load data, the flue gas is divided into multiple feed sections along the height of the desulfurization tower. Flue gas flow rates are allocated to each feed section, and the feed inlet locations are determined. The resulting segmented feed configuration information includes:

[0075] Obtain the flue gas velocity and sulfur dioxide concentration distribution from the flue gas load data, calculate the pressure loss value at each measurement location of the desulfurization tower, and generate a flue gas flow parameter diagram.

[0076] The flow resistance coefficient and diffusion coefficient of the flue gas in the desulfurization tower are calculated based on the flue gas flow parameter diagram to determine the movement trajectory of the flue gas components and generate flue gas movement characteristic data.

[0077] Based on flue gas motion characteristic data, the gas-liquid mixing coefficient and mass transfer coefficient at different locations in the desulfurization tower are calculated. According to the numerical distribution of the gas-liquid mixing coefficient and mass transfer coefficient, the desulfurization tower is divided into multiple feeding sections along the height direction to determine the feeding section distribution information.

[0078] Based on the distribution information of the feeding section, the position with the optimal mass transfer coefficient value in each feeding section is selected as the feeding port position to form the feeding port position information;

[0079] Calculate the ratio of mass transfer coefficient values ​​for each feeding section, and iteratively calculate the flue gas flow rate based on the ratio of mass transfer coefficient values ​​until the difference in flue gas flow rate between two adjacent iterations is less than the preset flow rate difference threshold, and then determine the flue gas flow rate allocation scheme.

[0080] The information on the distribution of the feeding section, the location of the feeding port, and the flue gas flow distribution scheme are combined to generate segmented feeding configuration information.

[0081] In this embodiment, it is necessary to obtain the flow velocity and sulfur dioxide concentration distribution data of the flue gas inside the desulfurization tower as basic parameters. Pressure sensors are installed at measurement points at different heights along the longitudinal direction of the desulfurization tower, and the pressure values ​​at each measurement point are recorded. Taking a certain desulfurization tower as an example, pressure sensors are installed at heights of 3 meters, 7 meters, 11 meters, 15 meters, 19 meters, and 22 meters inside the tower, and the pressure values ​​at the corresponding locations are 2560 Pa, 2480 Pa, 2385 Pa, 2265 Pa, 2155 Pa, and 2080 Pa, respectively. By calculating the pressure difference between adjacent measurement points and combining it with the distance between the measurement points, the pressure loss value of the flue gas in each measurement section is obtained. The pressure difference values ​​between adjacent points are 80 Pa, 95 Pa, 120 Pa, 110 Pa, and 75 Pa, respectively. The pressure loss value is correlated with the flue gas velocity data and sulfur dioxide concentration data measured at the same location to generate a parameter map characterizing the flow state of the flue gas inside the desulfurization tower.

[0082] Using the obtained flue gas flow parameter diagram, the flow resistance coefficient of the flue gas at different heights within the desulfurization tower was calculated. A correlation exists between pressure loss and flow resistance coefficient. Based on fluid mechanics theory, combined with the flue gas velocity and the cross-sectional area of ​​the desulfurization tower, the flow resistance coefficient for each measurement section can be calculated. For the above example, the calculated flow resistance coefficients for each section from bottom to top within the desulfurization tower were 0.68, 0.62, 0.52, 0.48, and 0.42, respectively. Simultaneously, the gradient change of sulfur dioxide concentration at different locations was analyzed, and the diffusion coefficient of flue gas molecules within the desulfurization tower was calculated based on temperature and pressure conditions. The measured temperature inside the tower was 75℃, and under this condition, the calculated flue gas diffusion coefficient ranged from 0.85 × 10⁻⁶. -5 ~1.32×10 -5 m² / s. By combining the flow resistance coefficient and diffusion coefficient, a computational fluid dynamics model is applied to simulate the motion trajectory of flue gas molecules within the desulfurization tower, forming a complete dataset describing the motion characteristics of the flue gas.

[0083] Based on the obtained flue gas motion characteristic data, the gas-liquid mixing coefficient at different heights within the desulfurization tower was calculated. The gas-liquid mixing coefficient reflects the uniformity of mixing between flue gas and desulfurization liquid within the tower, and is calculated by analyzing the interaction between the motion trajectory of flue gas components and the distribution position of the desulfurization liquid. For the above example, the measured gas-liquid mixing coefficients from the bottom to the top of the tower were 0.78, 0.82, 0.76, 0.72, and 0.65, respectively. Simultaneously, the mass transfer coefficient at different heights of the desulfurization tower was calculated. The mass transfer coefficient characterizes the rate of sulfur dioxide transfer from the gas phase to the liquid phase and is a key parameter for evaluating the desulfurization effect. By analyzing the distribution patterns of the gas-liquid mixing coefficient and the mass transfer coefficient along the tower height, locations where significant changes in the mass transfer coefficient occur were identified, and the desulfurization tower was divided into multiple feed sections along the height direction. For a desulfurization tower with a height of 25 meters, the mass transfer coefficient shows significant changes at 4.5 meters, 9.8 meters, 14.2 meters and 20 meters. Based on this, the tower body is divided into four feeding sections with height ranges of 0-4.5 meters, 4.5-9.8 meters, 9.8-14.2 meters and 14.2-25 meters, respectively.

[0084] For each feed section, the location with the optimal mass transfer coefficient was selected as the feed inlet. By analyzing the mass transfer coefficient distribution at all measurement points within each feed section, the point with the highest mass transfer coefficient was determined as the feed inlet location for that section. For regions with a relatively uniform mass transfer coefficient distribution, considering the influence of the gas-liquid mixing coefficient, the location with the best overall performance in terms of both gas-liquid mixing coefficient and mass transfer coefficient was selected as the feed inlet. After detailed analysis and calculation, the optimal feed inlet locations for the four feed sections were determined to be 2.8 meters, 7.2 meters, 12.5 meters, and 17.3 meters from the bottom of the tower, respectively. The mass transfer coefficients at these locations were 3.8 × 10⁻⁶. -3 3.2×10 -3 2.5×10 -3 and 1.9×10 -3 .

[0085] The mass transfer coefficient ratios between each feed section are calculated to provide a basis for flue gas flow distribution. The first feed section with the highest mass transfer coefficient is taken as the baseline section, with a mass transfer coefficient of 3.8 × 10⁻⁶. -3The mass transfer coefficient ratios of other feed sections to the baseline section were calculated, yielding ratios of 0.84, 0.66, and 0.50 for the second, third, and fourth feed sections, respectively. These ratios were used as initial reference values ​​for flue gas flow distribution, and iterative optimization calculations were performed. After each iteration, the mass transfer efficiency of each feed section and the overall desulfurization effect were reassessed based on the adjusted flow distribution. In practical applications, a flow difference threshold of 1% of the total flow was set; that is, when the difference in flue gas flow distribution calculated in two adjacent iterations is less than 1% of the total flow, the convergence condition is considered met, and the final flue gas flow distribution scheme is determined. After five iterations, the final flue gas flow distribution ratios for the four feed sections were determined to be 35%, 28%, 22%, and 15% of the total flow, respectively.

[0086] By integrating the information on the distribution of feeding sections, the location of the feed inlets, and the flue gas flow distribution scheme, a complete segmented feeding configuration is generated. This configuration information details the height range of each feeding section, the exact coordinates of the optimal feed inlet within each section, and the percentage of flue gas flow allocated to each feed inlet. For the example above, the resulting segmented feeding configuration is as follows: the feed inlet location of the first feeding section (0-4.5 meters) is 2.8 meters, with a flue gas flow distribution of 35% of the total flow; the feed inlet location of the second feeding section (4.5-9.8 meters) is 7.2 meters, with a flue gas flow distribution of 28% of the total flow; the feed inlet location of the third feeding section (9.8-14.2 meters) is 12.5 meters, with a flue gas flow distribution of 22% of the total flow; and the feed inlet location of the fourth feeding section (14.2-25 meters) is 17.3 meters, with a flue gas flow distribution of 15% of the total flow. These configuration details serve as control parameters for multi-point feed desulfurization systems, guiding the adjustment and operation of the desulfurization unit.

[0087] In this embodiment, by accurately analyzing the flow characteristics of flue gas within the desulfurization tower, the optimal feed location was precisely determined, avoiding the problem of uneven gas-liquid contact caused by traditional single-point feeding. The multi-point segmented feeding method significantly improves the gas-liquid two-phase contact area and mixing efficiency, and can adjust the feed configuration in real time according to changes in flue gas load, enhancing the effectiveness of the mass transfer process.

[0088] Based on flue gas motion characteristic data, the gas-liquid mixing coefficient and mass transfer coefficient at different locations in the desulfurization tower are calculated. According to the numerical distribution of the gas-liquid mixing coefficient and mass transfer coefficient, the desulfurization tower is divided into multiple feed sections along its height. The distribution information of the feed sections includes:

[0089] Based on the flue gas motion characteristic data, the measurement points at different locations of the desulfurization tower are determined, and the gas-liquid relative motion parameters and component transfer parameters at the measurement points are obtained to generate flue gas flow data.

[0090] Calculate the initial gas-liquid mixing coefficient and initial mass transfer coefficient at the measurement point based on flue gas flow data;

[0091] Temperature and pressure parameters are collected at the measurement point. The temperature and pressure parameters are substituted into the initial gas-liquid mixing coefficient and the initial mass transfer coefficient for correction, and the corrected gas-liquid mixing coefficient and mass transfer coefficient are generated.

[0092] Based on the numerical distribution of the corrected gas-liquid mixing coefficient and mass transfer coefficient, a mass transfer performance distribution curve is constructed. The slope change position of the mass transfer performance distribution curve is calculated. According to the slope change position, the desulfurization tower is divided into multiple feed sections along the height direction, and the feed section boundary position is generated.

[0093] Calculate the average values ​​of the gas-liquid mixing coefficient and mass transfer coefficient in multiple feed sections, sort the multiple feed sections according to the average values, and generate the feed section distribution structure.

[0094] The feed section distribution information is generated by combining the feed section boundary location with the feed section distribution structure.

[0095] The flue gas motion characteristic data includes key parameters such as the trajectory, velocity distribution, and concentration distribution of flue gas within the desulfurization tower. Based on this data, the locations of measurement points within the desulfurization tower are determined, covering the main areas from the inlet to the outlet. In a 25-meter-high desulfurization tower, multiple measurement points can be set along the tower's height, specifically one at each distance from the bottom: 3 meters, 9 meters, 15 meters, and 21 meters. At each measurement point, a gas-liquid relative motion parameter acquisition device and a component transfer parameter acquisition device are installed to obtain parameters such as the relative velocity, relative direction, and sulfur dioxide concentration of the gas and liquid phases. Measurement results show that at 3 meters from the bottom of the tower, the gas-liquid relative velocity is 2.3 m / s, and the sulfur dioxide concentration is 420 mg / m³; at 15 meters from the bottom, the gas-liquid relative velocity decreases to 1.8 m / s, and the sulfur dioxide concentration decreases to 250 mg / m³. These data are combined to form a flue gas flow dataset, providing a basis for subsequent calculations.

[0096] Using the acquired flue gas flow data, the initial gas-liquid mixing coefficient at each measurement point was calculated. The gas-liquid mixing coefficient characterizes the uniformity of mixing between the gas and liquid phases within the desulfurization tower, and its calculation needs to consider factors such as the relative velocity, relative direction, and gas-liquid interface area. For a measurement point with a relative gas-liquid velocity of V and an interface area of ​​A, its initial gas-liquid mixing coefficient can be expressed as a function of the product of V and A. The calculated initial gas-liquid mixing coefficients at 3 meters and 15 meters from the bottom of the tower are 0.76 and 0.68, respectively. Simultaneously, the initial mass transfer coefficient at each measurement point was calculated. The mass transfer coefficient reflects the rate of sulfur dioxide transfer from the gas phase to the liquid phase and is closely related to the gas-liquid contact mode, the relative motion state of the gas and liquid phases, and the component concentration. The mass transfer coefficient calculation considered factors such as the sulfur dioxide diffusion coefficient, the gas-liquid interface area, and the relative motion state of the gas and liquid phases. The calculated initial mass transfer coefficients at 3 meters and 15 meters from the bottom of the tower are 3.8 × 10⁻⁶. -3 and 2.5×10 -3 .

[0097] Temperature and pressure parameters were collected at various measurement points to correct the initial gas-liquid mixing coefficient and initial mass transfer coefficient. Temperature and pressure data were simultaneously collected at each measurement point using temperature and pressure sensors. Measurements showed that the temperature was 75℃ and the pressure was 2560 Pa at 3 meters from the bottom of the column; the temperature was 68℃ and the pressure was 2265 Pa at 15 meters from the bottom of the column. Temperature and pressure both significantly affected the gas-liquid mixing coefficient and the initial mass transfer coefficient. Increased temperature increased the diffusion rate of the gas and liquid phases, improving the mixing effect and mass transfer efficiency; increased pressure increased the solubility of gaseous components in the liquid phase, which was beneficial to the mass transfer process. Based on the measured temperature and pressure parameters, the initial gas-liquid mixing coefficient and the initial mass transfer coefficient were corrected. Temperature correction used the Arrhenius relation, and pressure correction considered the functional relationship between gas solubility and pressure. After correction, the gas-liquid mixing coefficient at 3 meters and 15 meters from the bottom of the column was adjusted to 0.82 and 0.72, respectively, and the mass transfer coefficient was adjusted to 4.2 × 10⁻⁶. -3 and 2.7×10 -3 .

[0098] Based on the corrected values ​​of the gas-liquid mixing coefficient and mass transfer coefficient, mass transfer performance distribution curves were constructed. Using the corrected mass transfer coefficient as the ordinate and the tower height of the measurement points as the abscissa, a curve showing the mass transfer coefficient as a function of tower height was plotted. Similarly, a curve showing the gas-liquid mixing coefficient as a function of tower height was plotted. Numerical analysis was performed on these two curves, calculating the slope at each point and identifying locations where the slope changes significantly. The slope was calculated using the difference quotient method between adjacent measurement points, i.e., the difference in coefficients between two points divided by the distance between the two points. The analysis results showed that the slope of the mass transfer coefficient curve changed significantly at heights of 5.0 m, 10.0 m, 15.0 m, and 20.0 m. Considering the locations of slope changes on both curves, the boundary positions of the feed section were determined at heights of 5.0 m, 10.0 m, 15.0 m, and 20.0 m. Based on this, the desulfurization tower is divided into five feeding sections, with height ranges of 0-5.0 meters, 5.0-10.0 meters, 10.0-15.0 meters, 15.0-20.0 meters, and 20.0-25 meters, respectively.

[0099] The average values ​​of the gas-liquid mixing coefficient and mass transfer coefficient within the five feed sections were calculated. For each feed section, the gas-liquid mixing coefficient and mass transfer coefficient at all measurement points within the section were statistically analyzed, and their arithmetic mean was calculated. The calculation results show that the average gas-liquid mixing coefficients for the five feed sections are 0.80, 0.75, 0.70, 0.65, and 0.60, respectively; the average mass transfer coefficients are 4.0 × 10⁻⁶, 4.0 × 10⁻⁶, and 4.0 × 10⁻⁶, respectively. -3 3.5×10 -3 3.0×10 -3 2.5×10 -3 and 2.0×10 -3Based on the calculated average values, the five feed sections are ranked, with mass transfer efficiency from highest to lowest as follows: Section 1, Section 2, Section 3, Section 4, and Section 5. This ranking reflects the differences in mass transfer capacity among the feed sections, providing a basis for subsequent flue gas distribution. The ranking corresponds to the physical location of the feed sections, forming the feed section distribution structure. Specifically, the first feed section is located at the bottom of the tower (0-5.0 meters), the second feed section is located at the lower part of the tower (5.0-10.0 meters), the third feed section is located in the middle of the tower (10.0-15.0 meters), the fourth feed section is located at the upper part of the tower (15.0-20.0 meters), and the fifth feed section is located at the top of the tower (20.0-25 meters).

[0100] The determined feed section boundary locations are combined with the feed section distribution structure to generate complete feed section distribution information. This information includes the height range of each feed section, the ranking of its mass transfer capacity, and the average mass transfer parameters for each section. The final feed section distribution information is as follows: the first feed section (0-5.0 meters) has the strongest mass transfer capacity, with an average gas-liquid mixing coefficient of 0.80 and an average mass transfer coefficient of 4.0 × 10⁻⁶. -3 The second feed section (5.0-10.0 meters) has the second-highest mass transfer capacity, with an average gas-liquid mixing coefficient of 0.75 and an average mass transfer coefficient of 3.5 × 10⁻³ kg / (m²·s); the third feed section (10.0-15.0 meters) has a moderate mass transfer capacity, with an average gas-liquid mixing coefficient of 0.70 and an average mass transfer coefficient of 3.0 × 10⁻³ kg / (m²·s). -3 The fourth feed section (15.0-20.0 meters) has a relatively weak mass transfer capacity, with an average gas-liquid mixing coefficient of 0.65 and an average mass transfer coefficient of 2.5 × 10⁻⁶. -3 The fifth feeding section (20.0-25 meters) has the weakest mass transfer capacity, with an average gas-liquid mixing coefficient of 0.60 and an average mass transfer coefficient of 2.0 × 10⁻⁶. -3 .

[0101] The multi-point feeding high-efficiency pneumatic emulsification flue gas deep desulfurization method of this invention achieves accurate evaluation and optimized segmentation of the desulfurization tower's mass transfer performance through precise analysis of the flue gas motion characteristics within the tower. It can capture the actual motion state and mass transfer efficiency changes of the gas and liquid phases within the desulfurization tower, avoiding the blindness and inaccuracy of traditional empirical segmentation methods. Feeding sections are divided based on the slope changes of the mass transfer performance curve, ensuring relatively uniform internal mass transfer characteristics in each section, facilitating targeted optimization. The sorted feed section distribution structure intuitively reflects the differences in mass transfer capacity of each section, providing a basis for subsequent feed inlet arrangement and flue gas distribution.

[0102] Based on the flue gas flow rate of each feeding section in the segmented feeding configuration information, the injection intensity of the high-pressure airflow and the supply amount of desulfurizing agent liquid in the corresponding tower section are determined, and the atomization control commands for each tower section are obtained, including:

[0103] Obtain the flue gas flow rate of each feeding section from the segmented feeding configuration information, calculate the flue gas flow velocity of each feeding section, and obtain the flue gas velocity data of each feeding section.

[0104] Based on the flue gas velocity data of each feeding section, the injection intensity of the high-pressure airflow and the effective range of the desulfurizing agent liquid are calculated to obtain the distribution data of the desulfurizing agent liquid.

[0105] Based on the distribution data of the desulfurizing agent liquid, the relationship between the injection intensity of the high-pressure airflow and the supply amount of the desulfurizing agent liquid is calculated to obtain the injection intensity data of the high-pressure airflow.

[0106] Based on the high-pressure airflow injection intensity data and the flue gas flow rate of each feeding section, the minimum supply of desulfurizing agent liquid is calculated, and the desulfurizing agent liquid supply data is obtained.

[0107] Based on the desulfurizing agent supply data, the reaction conversion rate was measured, and the injection intensity of the high-pressure airflow and the supply of the desulfurizing agent were adjusted to obtain the injection intensity and supply ratio data.

[0108] Based on the ratio of injection intensity to supply, the injection intensity of the high-pressure airflow and the supply of desulfurizing agent are set to obtain the atomization control commands for each tower section.

[0109] The flue gas flow rate data for each feed section is extracted from the configuration information. Combined with the geometric parameters of the desulfurization tower, the flue gas velocity in each feed section is calculated. Specifically, the flue gas flow rate for each feed section is divided by the cross-sectional area of ​​that section to obtain the flue gas velocity data for each feed section. Taking a certain desulfurization unit as an example, the desulfurization tower of this unit is divided into four feed sections, with the flue gas flow rates for each section accounting for 35%, 28%, 22%, and 15% of the total flow rate, respectively. The total flue gas flow rate is 30,000 m³ / s. 3 / h, the desulfurization tower has a cross-sectional area of ​​7m³. 2 Based on this, the flue gas velocities of the four feeding sections were calculated to be 4.2 m / s, 3.3 m / s, 2.6 m / s and 1.8 m / s, respectively.

[0110] Based on the calculated flue gas velocity data for each feed section, the interaction characteristics between the high-pressure gas injection and the desulfurizing agent were analyzed. The high-pressure gas injection intensity refers to the mass of gas passing through the nozzle per unit time, and its magnitude directly affects the mixing effect of the gas and liquid phases. The effective range of the desulfurizing agent refers to the spatial range within which the desulfurizing agent can fully contact the flue gas; this range is influenced by both the flue gas velocity and the high-pressure gas injection intensity. Through fluid dynamics analysis, the functional relationship between the high-pressure gas injection intensity and the flue gas velocity was determined, and the effective range of the desulfurizing agent under different injection intensities was calculated. For the four feed sections, when the high-pressure gas injection pressure is 0.6 MPa, the calculated effective ranges of the desulfurizing agent are 0.8 m, 1.0 m, 1.2 m, and 1.5 m, respectively. These data constitute a desulfurizing agent distribution dataset, describing the distribution characteristics of the desulfurizing agent within the desulfurization tower under different operating conditions.

[0111] The distribution data of the desulfurizing agent provides a basis for establishing the correspondence between the high-pressure gas jet intensity and the desulfurizing agent supply. According to the gas-liquid two-phase flow theory, the greater the high-pressure gas jet intensity, the stronger its ability to carry and atomize the desulfurizing agent, but at the same time, the energy consumption is also greater. Therefore, it is necessary to find the optimal ratio between the high-pressure gas jet intensity and the desulfurizing agent supply to achieve efficient desulfurization while reducing energy consumption. By testing the atomization effect under different jet pressures, a correspondence model between the high-pressure gas jet intensity and the desulfurizing agent supply was established. For the four feeding sections, the experiment measured that when the desulfurizing agent supply was 2 L / min, the required high-pressure gas jet pressure was 0.65 MPa for the first feeding section, 0.60 MPa for the second feeding section, 0.55 MPa for the third feeding section, and 0.50 MPa for the fourth feeding section. By changing the desulfurizing agent supply and measuring the corresponding optimal jet pressure, a high-pressure gas jet intensity dataset was formed.

[0112] The high-pressure gas jet intensity data, combined with the flue gas flow rate at each feed section, provides a basis for calculating the minimum supply of desulfurizing agent. The minimum supply of desulfurizing agent refers to the minimum amount of desulfurizing agent required to ensure desulfurization efficiency. Its calculation needs to consider factors such as the sulfur dioxide content in the flue gas, the stoichiometric ratio of the reaction, the reaction efficiency, and the safety margin. Using chemical reaction rate theory, combined with the flue gas flow rate and sulfur dioxide content at each feed section, the theoretically required amount of desulfurizing agent is calculated. Considering reaction efficiency and safety margin factors, the actual supply needs to be appropriately increased based on the theoretical amount. For example, assuming an average sulfur dioxide concentration of 400 mg / m³ in the flue gas. 3 With an effective component concentration of 15% in the desulfurizing agent solution, a reaction efficiency of 85%, and a safety margin coefficient of 1.2, the minimum desulfurizing agent solution supply required for the four feeding sections is calculated to be 4.2 L / min, 3.4 L / min, 2.6 L / min, and 1.8 L / min, respectively.

[0113] Based on the calculated desulfurizing agent supply data, actual operation tests were conducted, and the sulfur dioxide reaction conversion rate was measured. The reaction conversion rate refers to the proportion of sulfur dioxide actually removed from the flue gas by the desulfurizing agent, and is a direct indicator of desulfurization effectiveness. By adjusting the injection intensity of the high-pressure gas flow and the supply of the desulfurizing agent, the operating conditions that achieve the highest reaction conversion rate were found. Specifically, while keeping the desulfurizing agent supply constant, the injection pressure of the high-pressure gas flow was gradually adjusted, and the reaction conversion rate was measured at each pressure. Then, at the optimal injection pressure, the supply of the desulfurizing agent was adjusted, and the reaction conversion rate was measured again. Through this method, the optimal ratio of high-pressure gas flow injection intensity to the desulfurizing agent supply was found. For the above example, the test found that the reaction conversion rate reached the highest value of 92% in the first feeding section when the injection pressure was 0.68 MPa and the desulfurizing agent supply rate was 4.5 L / min; the optimal ratios for the other three feeding sections were 0.62 MPa and 3.6 L / min, 0.58 MPa and 2.8 L / min, and 0.52 MPa and 2.0 L / min, respectively, with corresponding reaction conversion rates of 88%, 85%, and 82%.

[0114] The final configuration of the high-pressure airflow injection intensity and desulfurizing agent supply for each feeding section is determined, generating atomization control commands. These commands include control parameters such as high-pressure airflow injection pressure, injection angle, and desulfurizing agent supply, directly guiding the operation of the desulfurization unit. The final control commands are as follows: First feeding section: high-pressure airflow injection pressure set to 0.68 MPa, injection angle to 60 degrees, desulfurizing agent supply to 4.5 L / min; Second feeding section: high-pressure airflow injection pressure set to 0.62 MPa, injection angle to 65 degrees, desulfurizing agent supply to 3.6 L / min; Third feeding section: high-pressure airflow injection pressure set to 0.58 MPa, injection angle to 70 degrees, desulfurizing agent supply to 2.8 L / min; Fourth feeding section: high-pressure airflow injection pressure set to 0.52 MPa, injection angle to 75 degrees, desulfurizing agent supply to 2.0 L / min. These control commands are sent to each actuator via an automatic control device, achieving precise control of the desulfurization process.

[0115] like Figure 2The figure shows a comparison of the droplet size distribution frequency in this embodiment. As can be seen from the figure, the curve of this technical solution exhibits a clear "leftward shift of the peak," with the peak appearing at 50 μm and a narrow distribution range (concentrated between 30-70 μm). This is due to the high-pressure airflow injection intensity calculated based on the flue gas velocity (e.g., up to 0.68 MPa in the first feed section). The high-pressure airflow provides strong shear force, breaking the desulfurizing agent liquid into finer particles. In contrast, the peak value of the curve in the prior art is located in the 90-110 μm range and has a wide distribution, indicating that it produces larger and less uniform droplet diameters.

[0116] The multi-point feeding high-efficiency pneumatic emulsification flue gas deep desulfurization method of this invention achieves precise control and optimized operation of the desulfurization process. Through a segmented control strategy based on flue gas flow rate, differentiated atomization treatment is implemented for the flue gas characteristics of different feeding sections, significantly improving the utilization efficiency of the desulfurizing agent. The precise ratio of high-pressure airflow injection intensity to the desulfurizing agent supply ensures sufficient mixing and contact between the gas and liquid phases, enhancing the mass transfer process and improving the conversion rate of the desulfurization reaction. The control parameters can be dynamically adjusted according to actual operating conditions, reducing operating costs and energy consumption while improving desulfurization efficiency and reducing wastewater discharge by decreasing the amount of desulfurizing agent used.

[0117] According to the segmented feeding configuration information, the flue gas is introduced into the desulfurization tower in segments. Simultaneously, according to the atomization control command, the desulfurizing agent liquid flow is impacted by a high-pressure airflow in each tower segment to form droplets. During the droplet formation process, the flue gas and the droplets simultaneously react, resulting in the following reaction intermediate states in each tower segment:

[0118] Obtain the feed inlet location information and flue gas flow distribution scheme from the segmented feed configuration information, introduce the flue gas into the desulfurization tower according to the feed inlet location information, adjust the flue gas flow at the feed inlet according to the flue gas flow distribution scheme, and monitor the flue gas distribution at each feed inlet.

[0119] Based on the monitored flue gas distribution, read the high-pressure airflow injection intensity data and desulfurizing agent liquid supply data from the atomization control command, adjust the injection pressure and injection angle of the high-pressure airflow, and control the supply rate of the desulfurizing agent liquid.

[0120] By adjusting the high-pressure airflow to impact the desulfurizing agent liquid flow, the impact angle and impact position between the high-pressure airflow and the desulfurizing agent liquid flow are controlled, so that the desulfurizing agent liquid flow is atomized into droplets.

[0121] The formed droplets are brought into contact with the introduced flue gas to react. The contact position and contact time between the flue gas and the droplets are adjusted, and the reaction parameters of the flue gas in each tower section are measured, including the sulfur dioxide concentration and the amount of droplets absorbed.

[0122] The removal rate and conversion rate of sulfur dioxide in each tower section are calculated based on the measured reaction parameters. The absorption saturation of droplets in each tower section is determined. The reaction temperature and pressure in each tower section are recorded, and the reaction intermediate state in each tower section is generated.

[0123] The feed inlet location information clearly defines the specific location of the flue gas inlet on the desulfurization tower, while the flue gas flow distribution scheme specifies the proportion of flue gas introduced through each feed inlet. In a certain desulfurization unit, the desulfurization tower is 25 meters high and divided into four feed sections. The feed inlets are located at distances of 2.8 meters, 7.2 meters, 12.5 meters, and 17.3 meters from the bottom of the tower, respectively, with the flue gas flow rates accounting for 35%, 28%, 22%, and 15% of the total flow rate. The total flue gas flow rate is 30,000 m³ / h. 3 Based on this, the flue gas flow rates at the four feed inlets are calculated to be 10500 m³ / h. 3 / h、8400m 3 / h、6600m 3 / h and 4500m 3 / h. Install flow regulating valves at each feed inlet to control the amount of flue gas entering each inlet by adjusting the valve opening. At the same time, install flow meters at each feed inlet to monitor the flue gas flow rate in real time, ensuring that it is consistent with the set value and the deviation is controlled within ±3%.

[0124] Based on the monitored flue gas distribution, relevant parameters from the atomization control command are read. The atomization control command includes high-pressure gas injection intensity data and desulfurizing agent supply data, which are directly related to the flue gas flow rate of each feeding section. The high-pressure gas injection intensity is determined by both injection pressure and injection angle. In the example above, the high-pressure gas injection pressures for the four feeding sections are set to 0.68 MPa, 0.62 MPa, 0.58 MPa, and 0.52 MPa, respectively, with injection angles of 60 degrees, 65 degrees, 70 degrees, and 75 degrees. The desulfurizing agent supply data specifies the supply rate for each feeding section, with supply rates of 4.5 L / min, 3.6 L / min, 2.8 L / min, and 2.0 L / min for the four feeding sections. The injection pressure is controlled by a high-pressure gas regulating valve, the injection angle by a nozzle angle adjusting device, and the supply rate by a desulfurizing agent metering pump to ensure that all parameters meet the requirements of the atomization control command.

[0125] The regulated high-pressure airflow is injected through a specially designed nozzle, creating a specific impact relationship with the desulfurizing agent liquid flow, atomizing the desulfurizing agent liquid into droplets. The impact angle and impact position between the high-pressure airflow and the desulfurizing agent liquid flow are key parameters affecting the atomization effect. The impact angle determines the direction of the airflow's impact force on the liquid flow, while the impact position affects the liquid flow's fragmentation mode. For the first feeding section, the impact angle between the high-pressure airflow and the desulfurizing agent liquid flow is set to 60 degrees, with the impact position located 5 mm below the liquid flow outlet; for the second feeding section, the impact angle is 65 degrees, with the impact position located 6 mm below the liquid flow outlet; for the third feeding section, the impact angle is 70 degrees, with the impact position located 7 mm below the liquid flow outlet; and for the fourth feeding section, the impact angle is 75 degrees, with the impact position located 8 mm below the liquid flow outlet. By precisely controlling these parameters, the desulfurizing agent liquid flow forms a cluster of droplets with uniform particle size distribution under the impact of the high-pressure airflow. The droplet size distribution measurement results show that the average droplet sizes formed in the four feeding sections are 50 μm, 60 μm, 70 μm and 80 μm, respectively, and the droplet size distribution uniformity coefficients are 0.85, 0.82, 0.78 and 0.75, respectively.

[0126] The atomized droplets react with the introduced flue gas within the desulfurization tower. The contact position and contact time between the flue gas and the droplets are crucial factors affecting the reaction efficiency. The contact position should be close to the feed inlet to fully utilize the freshly formed droplets; the contact time must ensure sufficient reaction time. The contact positions between the flue gas and droplets in the four feed sections are set at 50mm, 60mm, 70mm, and 80mm below their respective feed inlets, guided by specially designed flow guide devices. The contact time between the flue gas and droplets is controlled by adjusting the residence time of the flue gas within the tower; the residence times for the four feed sections are set to 2.5 seconds, 3.0 seconds, 3.5 seconds, and 4.0 seconds, respectively. Gas composition analyzers and droplet sampling devices are installed in each tower section to measure the sulfur dioxide concentration in the flue gas and the amount of droplets absorbed in real time. Measurement results show that the sulfur dioxide concentration in the flue gas at the inlet of all four feed sections is 400 mg / m³. 3 The concentration at the outlet decreased to 36 mg / m³. 3 48mg / m 3 60mg / m 3 and 72mg / m 3 The corresponding droplet absorption amounts were 1.8 mg / mL, 1.5 mg / mL, 1.2 mg / mL and 0.9 mg / mL, respectively.

[0127] Based on the measured reaction parameters, reaction efficiency indicators for each tower section were calculated, and intermediate reaction data were generated. Sulfur dioxide removal rate is a direct indicator of desulfurization efficiency, calculated as the inlet concentration minus the outlet concentration, then divided by the inlet concentration. The sulfur dioxide removal rates for the four feed sections were 91%, 88%, 85%, and 82%, respectively. Conversion rate reflects the degree of reaction completion, calculated as the actual reaction amount divided by the theoretical reaction amount. The conversion rates for the four feed sections were 95%, 92%, 88%, and 85%, respectively. Droplet absorption saturation characterizes the utilization of droplet absorption capacity, calculated as the actual absorption amount divided by the theoretical maximum absorption amount. The results showed that the droplet absorption saturation for the four feed sections were 75%, 70%, 65%, and 60%, respectively. Simultaneously, the reaction temperature and pressure within each feed section were recorded. The reaction temperature in the first feed section was 78℃, and the pressure was 2650 Pa; the reaction temperature in the second feed section was 75℃, and the pressure was 2450 Pa; the reaction temperature in the third feed section was 72℃, and the pressure was 2350 Pa; and the reaction temperature in the fourth feed section was 68℃, and the pressure was 2250 Pa. These data collectively constitute the reaction intermediate states of each feed section, providing a basis for subsequent process optimization.

[0128] This invention presents a multi-point feeding, high-efficiency pneumatic emulsification method for deep flue gas desulfurization. By combining segmented feeding with pneumatic emulsification technology, it achieves highly efficient operation of the deep flue gas desulfurization process. The desulfurization tower is divided into multiple feeding sections along its height. Based on the differences in mass transfer characteristics of each section, a targeted flue gas distribution strategy is adopted, avoiding the uneven gas-liquid contact problem caused by traditional single-point feeding. The pneumatic emulsification technology, which uses high-pressure airflow to impact the desulfurizing agent liquid flow, forms micro-droplets of the desulfurizing agent liquid, increasing the gas-liquid contact area and enhancing the mass transfer process. The droplet formation process occurs synchronously with the flue gas contact reaction, fully utilizing the high activity of the newly formed droplet surface, thereby improving the reaction rate and conversion rate. By monitoring the reaction parameters in each tower section in real time and generating intermediate reaction data, a basis is provided for the dynamic adjustment and optimization of the desulfurization process.

[0129] The residual sulfur dioxide concentration in the reaction intermediate is monitored, and the distribution ratio of the desulfurizing agent supply between adjacent tower sections is adjusted according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, resulting in the flue gas after gradient desulfurization, which includes:

[0130] Collect the residual sulfur dioxide concentration and gas flow rate in the intermediate state of the reaction, calculate the desulfurization reaction rate and desulfurizing agent conversion efficiency of each tower section, and generate the sulfur dioxide concentration distribution.

[0131] Based on the sulfur dioxide concentration distribution analysis, the residual sulfur dioxide concentration difference between adjacent tower sections is analyzed, the desulfurizing agent consumption and reaction degree of each tower section are calculated, and the concentration change characteristics are obtained.

[0132] Based on the consumption and reaction degree of desulfurizing agent in each tower section, establish the response curve of desulfurizing agent supply and sulfur dioxide residual concentration change, calculate the concentration gradient value and desulfurizing agent demand between adjacent tower sections, and determine the supply adjustment scheme.

[0133] The desulfurizing agent replenishment amount for each tower section is set according to the supply adjustment plan. The desulfurizing agent distribution device is controlled to adjust the supply distribution ratio. The change of sulfur dioxide residual concentration is monitored to obtain sulfur dioxide residual concentration data.

[0134] Calculate the concentration difference between adjacent tower sections based on the residual sulfur dioxide concentration data, adjust the supply ratio of the desulfurizing agent distribution device, control the desulfurizing agent supply rate of each tower section, monitor the sulfur dioxide concentration at the outlet of each tower section, and adjust the desulfurizing agent supply based on the monitored sulfur dioxide concentration until the sulfur dioxide concentration difference between adjacent tower sections meets the preset gradient requirements, thereby obtaining the flue gas after gradient desulfurization.

[0135] The intermediate reaction data includes key parameters such as residual sulfur dioxide concentration and gas flow rate in each tower section, and these data need to be collected for subsequent analysis and adjustment. A gas composition analyzer and flow rate measuring device are installed at the outlet of each tower section of the desulfurization tower to collect real-time data on residual sulfur dioxide concentration and gas flow rate. Under initial operating conditions, the residual sulfur dioxide concentration at the outlet of each tower section is 36 mg / m³. 3 48mg / m 3 60mg / m 3 and 72mg / m 3 The corresponding gas flow velocities were 4.0 m / s, 3.1 m / s, 2.4 m / s, and 1.7 m / s, respectively. The desulfurization reaction rate for each tower section was calculated based on the collected data, using the method of dividing the amount of sulfur dioxide removed per unit time by the tower section volume. The desulfurization reaction rates for the four tower sections were 0.065 kg / (m³). 3 ·h), 0.055kg / (m 3 ·h), 0.042kg / (m 3 ·h) and 0.030kg / (m 3 (h). Simultaneously, the desulfurizing agent conversion efficiency, i.e., the ratio of the actual amount of sulfur dioxide removed to the theoretically calculated amount, was calculated. The desulfurizing agent conversion efficiencies for the four tower sections were 92%, 88%, 82%, and 76%, respectively. These data constituted a sulfur dioxide concentration distribution map, visually reflecting the desulfurization status of each tower section.

[0136] Based on the sulfur dioxide concentration distribution map, the residual sulfur dioxide concentration differences between adjacent tower sections were analyzed. These differences reflect the concentration gradient changes during the desulfurization process. The calculation method for the residual sulfur dioxide concentration difference between adjacent tower sections is the downstream tower section outlet concentration minus the upstream tower section outlet concentration. In this embodiment, the difference between the first and second tower sections is 12 mg / m³. 3The difference between the second and third tower sections was 12 mg / m³. 3 The difference between the third and fourth tower sections was 12 mg / m³. 3 The desulfurizing agent consumption for each tower section was calculated, i.e., the amount of desulfurizing agent used to remove sulfur dioxide per unit time. The desulfurizing agent consumption for the four tower sections was 3.2 L / min, 2.6 L / min, 2.0 L / min, and 1.4 L / min, respectively. The reaction degree of each tower section was analyzed, including indicators such as reaction rate, reaction depth, and reaction completion. The reaction depth is expressed as the difference between the inlet sulfur dioxide concentration and the outlet concentration. The reaction depth of the four tower sections was 364 mg / m³. 3 352mg / m 3 340mg / m 3 and 328mg / m 3 By analyzing these data, we can obtain the concentration change characteristics of the desulfurization process, providing a basis for subsequent adjustments.

[0137] Based on the data on desulfurizer consumption and reaction rate in each tower section, response curves were established for the relationship between desulfurizer supply rate and residual sulfur dioxide concentration. The response curves describe the degree of influence and response rate of changes in desulfurizer supply rate on residual sulfur dioxide concentration. The response curves were obtained by testing changes in residual sulfur dioxide concentration under different desulfurizer supply rates. For the first tower section, when the desulfurizer supply rate increased from 3.2 L / min to 3.5 L / min, the residual sulfur dioxide concentration increased from 36 mg / m³ to... 3 Reduced to 32 mg / m 3 When the desulfurizing agent supply rate decreased from 3.2 L / min to 2.9 L / min, the residual sulfur dioxide concentration decreased from 36 mg / m³. 3 Increased to 40 mg / m 3 Similarly, the response curve data for the other three tower sections were obtained. Based on the response curves, the concentration gradient values ​​between adjacent tower sections and the desulfurizing agent demand were calculated to determine a reasonable supply adjustment scheme. In the adjustment scheme, to ensure a uniform decreasing gradient of sulfur dioxide concentration at the outlet of each tower section, the target was set at a concentration difference of 15 mg / m³ between adjacent tower sections. 3 The desulfurizing agent supply rates for the four tower sections were adjusted to 3.5 L / min, 2.8 L / min, 2.1 L / min, and 1.5 L / min, respectively.

[0138] According to the established supply adjustment plan, the desulfurizer replenishment amount for each tower section is set. The supply distribution ratio is adjusted through the desulfurizer distribution device to achieve precise control of the desulfurizer supply to each tower section. The desulfurizer distribution device includes a multi-channel flow control valve and a flow metering system, which can automatically adjust the desulfurizer flow rate of each channel according to the set value.

[0139] The adjusted desulfurizing agent supply ratio is 35.4%:28.3%:21.2%:15.1%. The desulfurizing agent distribution device is started, and desulfurizing agent is supplied according to the new ratio. The changes in residual sulfur dioxide concentration are monitored in real time using a gas composition analyzer. Monitoring data shows that the residual sulfur dioxide concentration at the outlet of the four tower sections has changed to 30 mg / m³ after the adjustment. 3 45mg / m 3 60mg / m 3 and 75mg / m 3 The concentration difference between adjacent tower sections was 15 mg / m³. 3 15mg / m 3 and 15mg / m 3 The data meet the set gradient requirements. These data constitute the adjusted sulfur dioxide residual concentration dataset, providing a basis for further optimization.

[0140] Based on the monitored residual sulfur dioxide concentration data, the concentration difference between adjacent tower sections is calculated to evaluate the effectiveness of the current desulfurizing agent distribution scheme. If the concentration difference between adjacent tower sections does not meet the preset gradient requirement, the replenishment ratio of the desulfurizing agent distribution device needs to be further adjusted. The adjustment method is to determine the amount of desulfurizing agent to be increased or decreased based on the deviation between the current concentration difference and the target difference, according to the response curve. Assume that monitoring shows a concentration difference of 13 mg / m³ between the first and second tower sections. 3 15 mg / m³ lower than the target value 3 The desulfurizing agent supply needs to be reduced in the first tower section or increased in the second tower section. According to the response curve, reducing the desulfurizing agent supply in the first tower section by 0.2 L / min or increasing it in the second tower section by 0.3 L / min will increase the concentration difference by 2 mg / m³ to reach the target value. Considering the overall desulfurization effect, the option of increasing the desulfurizing agent supply in the second tower section is selected, adjusting it from 2.8 L / min to 3.1 L / min. After adjustment, the sulfur dioxide concentration at the outlet of each tower section is re-monitored. If the sulfur dioxide concentration difference between adjacent tower sections meets the preset gradient requirement, the final desulfurizing agent distribution scheme can be determined; otherwise, adjustments continue until the requirement is met.

[0141] The final determined desulfurization agent supply rates for the four tower sections are 3.5 L / min, 3.1 L / min, 2.3 L / min, and 1.6 L / min, corresponding to outlet sulfur dioxide concentrations of 30 mg / m³. 3 45mg / m 3 60mg / m 3 and 75mg / m 3 The concentration difference between adjacent tower sections was 15 mg / m³. 3 This creates a uniform decreasing gradient, resulting in flue gas after gradient desulfurization.

[0142] This invention presents a multi-point feeding, high-efficiency pneumatic emulsification flue gas deep desulfurization method. Through precise monitoring of the residual sulfur dioxide concentration in each tower section and dynamic adjustment of the desulfurizer supply, it achieves gradient-decreasing control of the sulfur dioxide concentration in the flue gas along the tower height. Based on the actual desulfurization status of each tower section, the distribution and use of the desulfurizer are optimized, avoiding the problem of excessive or insufficient desulfurizer in some sections and improving the desulfurizer utilization efficiency. The gradient-decreasing concentration distribution ensures that the desulfurization process proceeds uniformly along the tower height, avoiding the inhibitory effect of high-concentration areas on the reaction rate in traditional methods, improving the overall reaction kinetic efficiency, and automatically adjusting the desulfurizer distribution strategy according to changes in inlet flue gas conditions to maintain a stable desulfurization effect.

[0143] The flue gas after gradient desulfurization is discharged from the top of the desulfurization tower, and the desulfurization products generated by the reaction are discharged from the bottom of the desulfurization tower, including:

[0144] The flow characteristics of the flue gas after gradient desulfurization at the top of the desulfurization tower are detected, the flow velocity of the flue gas after gradient desulfurization in the exhaust channel is calculated, the distribution of the flue gas after gradient desulfurization is monitored, and the discharge conditions of the flue gas after gradient desulfurization are determined.

[0145] Based on the determined discharge conditions, the pressure distribution of the flue gas after gradient desulfurization in the exhaust channel is analyzed, the flow field change of the flue gas after gradient desulfurization is calculated, and the treatment scheme of the flue gas after gradient desulfurization is obtained.

[0146] The settling distribution of desulfurization products at the bottom of the desulfurization tower is collected, the distribution location of the desulfurization products is measured, the settling velocity of the desulfurization products is calculated, and the emission requirements of the desulfurization products are determined.

[0147] The treatment scheme for flue gas after gradient desulfurization is matched with the emission requirements of desulfurization products. The operating ratio of exhaust device and emission device is calculated, the opening degree of exhaust device and the rotation speed of emission device are controlled, the discharge amount of flue gas after gradient desulfurization and the discharge amount of desulfurization products are adjusted, and the pressure inside the tower is measured.

[0148] Adjust the operating parameters of the exhaust and emission devices according to the measured pressure inside the tower, control the flue gas after gradient desulfurization to be discharged from the top of the desulfurization tower through the exhaust device, and control the desulfurization products to be discharged from the bottom of the desulfurization tower through the emission device.

[0149] The flow characteristics of the flue gas after gradient desulfurization at the top of the desulfurization tower are key parameters for determining exhaust conditions. These flow characteristics include flue gas velocity, temperature, pressure, humidity, and gas composition, which need to be obtained through sensor detection. Velocity sensors, temperature sensors, and pressure sensors are installed at the top of the desulfurization tower to monitor the flow state of the flue gas after gradient desulfurization in real time. For a multi-point feed high-efficiency pneumatic emulsification desulfurization unit, the measured flue gas velocity at the top of the tower was 1.5 m / s, the temperature was 62℃, the pressure was 2050 Pa, and the humidity was 85%. A multi-point velocity measuring device was installed in the exhaust channel, measuring the flue gas velocity at the inlet of the exhaust channel as 1.5 m / s, the velocity in the middle of the channel as 2.2 m / s, and the velocity at the outlet of the channel as 3.0 m / s. The increase in velocity is due to the decrease in the cross-sectional area of ​​the channel. Simultaneously, the composition distribution of the flue gas at the top of the tower was monitored using a flue gas analyzer, and the measured residual sulfur dioxide concentration was 30 mg / m³, the oxygen content was 6.5%, and the water vapor content was 12%. Based on these monitoring data, the discharge conditions for flue gas after gradient desulfurization were determined as follows: the exhaust temperature should not be lower than 60℃ to prevent water vapor condensation; the exhaust pressure should be controlled at 2000-2100Pa to maintain appropriate system pressure; and the exhaust velocity should be controlled at 2.8-3.2m / s to ensure stable emissions.

[0150] Based on the defined discharge conditions, the pressure distribution of the flue gas after gradient desulfurization in the exhaust channel was analyzed. Pressure sensors were installed at the inlet, middle, and outlet of the exhaust channel, and the measured pressures at these three locations were 2050 Pa, 1980 Pa, and 1920 Pa, respectively, showing a gradual decreasing trend along the exhaust direction, which is consistent with the principles of fluid mechanics. Using computational fluid dynamics, a flue gas flow field model was established within the exhaust channel, and the flow field changes under different operating conditions were calculated. The calculation results show that when the exhaust valve opening is 60%, a stable laminar flow state is formed in the channel with a uniform velocity distribution; when the opening increases to 80%, the flow velocity in the channel increases, but the laminar flow state is still maintained; when the opening reaches 90% or more, local turbulence appears at the bends of the channel, which may lead to flow instability. Based on the flow field analysis results, the optimal exhaust scheme was determined: the exhaust valve opening is set to 75%, at which point a stable flow field is formed in the exhaust channel, the outlet flue gas velocity is 3.0 m / s, and the pressure is 1920 Pa, which meets the exhaust requirements.

[0151] The settling distribution of desulfurization products at the bottom of the desulfurization tower is a fundamental parameter for determining emission requirements. Level and concentration sensors were installed at the bottom of the tower to monitor the accumulation of desulfurization products. Measurements showed that the products were mainly distributed within a 0-0.5 meter height range at the bottom of the tower, exhibiting a stratified structure with lower concentrations at the top and higher concentrations at the bottom. The concentration of desulfurization products was 25% at 0.1 meters, 18% at 0.3 meters, and 12% at 0.5 meters. Particle image velocimetry (PEV) was used to measure the settling velocity of desulfurization product particles of different sizes. The results showed that the settling velocity of particles with a diameter of 50 μm was 0.6 mm / s, that of particles with a diameter of 100 μm was 1.2 mm / s, and that of particles with a diameter of 150 μm was 1.8 mm / s. Based on the settling velocity and concentration distribution, the emission requirements for desulfurization products are determined as follows: the emission outlet is located at the lowest point of the tower to collect high-concentration desulfurization products settling down; the emission rate is controlled at 12 L / min to match the generation rate of desulfurization products; and the emission concentration is controlled at 20-25% to ensure the resource utilization value of desulfurization products.

[0152] The treatment scheme for the flue gas after gradient desulfurization was matched with the emission requirements of the desulfurization products, and the operating ratio of the exhaust and emission devices was calculated. The operation of the exhaust and emission devices should be coordinated to maintain pressure and material balance within the desulfurization tower. Calculations show that when the flue gas discharge rate is 30,000 m³ / h, the corresponding desulfurization product emission rate should be 720 L / h, or 12 L / min, with a ratio of 41667:1. Based on this ratio, the opening degree of the exhaust device and the rotation speed of the emission device were controlled. Specifically, the exhaust valve opening degree was set to 75%, and the emission pump speed was set to 1450 r / min, achieving a flue gas discharge rate of 30,000 m³ / h and a desulfurization product emission rate of 12 L / min. Pressure sensors installed at different heights within the desulfurization tower monitored the pressure distribution within the tower. The measured pressure at the bottom of the tower was 2650 Pa, the pressure in the middle of the tower was 2350 Pa, and the pressure at the top of the tower was 2050 Pa. The pressure distribution was reasonable and met the design requirements.

[0153] Based on the measured pressure data inside the tower, the operating parameters of the exhaust and emission devices are adjusted to optimize the exhaust emission process. When the measurement shows that the pressure inside the tower is too high, exceeding the set range, the opening of the exhaust valve is increased or the speed of the emission pump is decreased; when the pressure inside the tower is too low, the opening of the exhaust valve is decreased or the speed of the emission pump is increased. In the above example, if the pressure at the top of the tower is detected to rise to 2150 Pa, exceeding the set upper limit of 2100 Pa, the opening of the exhaust valve should be adjusted from 75% to 78% to reduce the pressure back to the normal range; if the pressure at the bottom of the tower drops to 2550 Pa, below the normal value of 2650 Pa, the speed of the emission pump should be reduced from 1450 r / min to 1400 r / min to slow down the emission rate and restore the pressure to normal. Through this real-time adjustment mechanism, the flue gas after gradient desulfurization is controlled to be stably discharged from the top of the desulfurization tower through the exhaust device, while the desulfurization products are controlled to be uniformly discharged from the bottom of the desulfurization tower through the emission device, maintaining the stable operation of the desulfurization system. In actual operation, the adjustment range of the exhaust device is 60-85% of the valve opening, and the adjustment range of the discharge device is 1300-1600 r / min of the pump speed. Fine adjustment is made within this range to ensure that the system operating parameters are always in the best state.

[0154] like Figure 3 As shown, the dynamic adjustment response curve for abnormal pressure fluctuations within the tower in this embodiment is illustrated, with the horizontal axis representing time and the vertical axis representing the tower top pressure. At t=20s, the simulated tower top pressure increased to 2150Pa due to disturbance, exceeding the set upper limit of 2100Pa. At this point, this technical solution immediately triggered the adjustment mechanism, fine-tuning the exhaust valve opening from 75% to 78%. Thanks to precise proportioning calculations, the pressure quickly dropped back at t=40s and stabilized at a normal value of 2050Pa at t=50s. In contrast, conventional PID feedback control or manual adjustment resulted in a delayed response and inappropriate adjustment amplitude, causing the pressure to hover around 2200Pa or produce overshoot oscillations, significantly prolonging the recovery time. This demonstrates the effectiveness of the pressure feedback-based coordinated control strategy for the exhaust and emission devices, ensuring rapid steady-state recovery of the system.

[0155] This invention presents a multi-point feeding, high-efficiency pneumatic emulsification flue gas deep desulfurization method. Through precise control of the flue gas discharge and desulfurization product emission processes after gradient desulfurization, it achieves dynamic adjustment of the material and pressure balance of the desulfurization system. Based on real-time monitoring of flow characteristics, pressure distribution, and sedimentation distribution data, a coordinated control mechanism for exhaust and emission is established. By maintaining a reasonable pressure gradient within the tower, it ensures orderly flow of flue gas within the tower while preventing equipment damage risks caused by excessive local pressure. The precisely controlled emission process ensures appropriate desulfurization product concentrations, facilitating subsequent resource utilization and reducing the burden of waste treatment.

[0156] Figure 4This is a schematic diagram of a multi-point feeding, high-efficiency pneumatic emulsification flue gas deep desulfurization system provided in an embodiment of the present invention. The system includes:

[0157] The flue gas detection unit is used to detect the flow rate and sulfur dioxide concentration of the flue gas to be treated, and to obtain flue gas load data;

[0158] The feed configuration unit is used to divide the flue gas into multiple feed sections along the height of the desulfurization tower according to the flue gas load data, allocate flue gas flow rate to each feed section and determine the feed inlet position to obtain the segmented feed configuration information.

[0159] The atomization control unit is used to determine the injection intensity of the high-pressure airflow and the supply amount of desulfurizing agent liquid in the corresponding tower section based on the flue gas flow rate of each feed section in the segmented feed configuration information, and to obtain the atomization control command for each tower section.

[0160] The reaction control unit is used to introduce flue gas into the desulfurization tower in stages according to the staged feed configuration information. At the same time, according to the atomization control command, the desulfurizing agent liquid flow is impacted by high pressure airflow in each tower section to form droplets. During the droplet formation process, the flue gas and the droplets are simultaneously contacted and reacted to obtain the reaction intermediate state of each tower section.

[0161] The concentration adjustment unit is used to monitor the residual sulfur dioxide concentration in the reaction intermediate state and adjust the distribution ratio of desulfurizing agent supply between adjacent tower sections according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, and the flue gas after gradient desulfurization is obtained.

[0162] The emission control unit is used to discharge the flue gas after gradient desulfurization from the top of the desulfurization tower and to discharge the desulfurization products generated by the reaction from the bottom of the desulfurization tower.

[0163] One technical solution provided in this embodiment of the invention is an electronic device, including: a memory, a processor, and a computer program stored in the memory and executable on the processor, wherein the processor executes the computer program to implement the steps in any of the aforementioned methods.

[0164] One technical solution provided in this embodiment of the invention is a computer-readable storage medium storing a computer program, wherein the processor executes the computer program to implement the steps in any of the aforementioned methods.

[0165] The specific embodiments described above are preferred embodiments of the present invention and are not intended to limit the specific scope of the present invention. The scope of the present invention includes, but is not limited to, these specific embodiments. All equivalent changes made in accordance with the shape and structure of the present invention are within the protection scope of the present invention.

Claims

1. A high-efficiency pneumatic emulsification flue gas deep desulfurization method with multi-point feeding, characterized in that, Includes the following steps: The flow rate and sulfur dioxide concentration of the flue gas to be treated are detected to obtain flue gas load data; Based on the flue gas load data, the flue gas is divided into multiple feeding sections along the height of the desulfurization tower. The flue gas flow rate is allocated to each feeding section and the inlet position is determined to obtain the segmented feeding configuration information. Based on the flue gas flow rate of each feeding section in the segmented feeding configuration information, the injection intensity of the high-pressure airflow and the supply of desulfurizing agent liquid in the corresponding tower section are determined, and the atomization control command of each tower section is obtained. According to the segmented feeding configuration information, the flue gas is introduced into the desulfurization tower in segments. At the same time, according to the atomization control command, the desulfurizing agent liquid flow is impacted by the high-pressure airflow in each tower segment to form droplets. During the droplet formation process, the flue gas and the droplets are simultaneously contacted and reacted to obtain the reaction intermediate state of each tower segment. Monitor the residual sulfur dioxide concentration in the reaction intermediate state, and adjust the distribution ratio of desulfurizing agent supply between adjacent tower sections according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, and obtain flue gas after gradient desulfurization. The flue gas after gradient desulfurization is discharged from the top of the desulfurization tower, and the desulfurization products generated by the reaction are discharged from the bottom of the desulfurization tower. Based on the flue gas load data, the flue gas is divided into multiple feed sections along the height of the desulfurization tower. Flue gas flow rates are allocated to each feed section, and the feed inlet locations are determined. The resulting segmented feed configuration information includes: Obtain the flue gas velocity and sulfur dioxide concentration distribution from the flue gas load data, calculate the pressure loss value at each measurement location of the desulfurization tower, and generate a flue gas flow parameter diagram. The flow resistance coefficient and diffusion coefficient of the flue gas in the desulfurization tower are calculated based on the flue gas flow parameter diagram to determine the movement trajectory of the flue gas components and generate flue gas movement characteristic data. Based on flue gas motion characteristic data, the gas-liquid mixing coefficient and mass transfer coefficient at different locations in the desulfurization tower are calculated. According to the numerical distribution of the gas-liquid mixing coefficient and mass transfer coefficient, the desulfurization tower is divided into multiple feeding sections along the height direction to determine the feeding section distribution information. Based on the distribution information of the feeding section, the position with the optimal mass transfer coefficient value in each feeding section is selected as the feeding port position to form the feeding port position information; Calculate the ratio of mass transfer coefficient values ​​for each feeding section, and iteratively calculate the flue gas flow rate based on the ratio of mass transfer coefficient values ​​until the difference in flue gas flow rate between two adjacent iterations is less than the preset flow rate difference threshold, and then determine the flue gas flow rate allocation scheme. The information on the distribution of the feeding section, the location of the feeding port, and the flue gas flow distribution scheme are combined to generate segmented feeding configuration information.

2. The method according to claim 1, characterized in that, Based on flue gas motion characteristic data, the gas-liquid mixing coefficient and mass transfer coefficient at different locations in the desulfurization tower are calculated. According to the numerical distribution of the gas-liquid mixing coefficient and mass transfer coefficient, the desulfurization tower is divided into multiple feed sections along its height. The distribution information of the feed sections includes: Based on the flue gas motion characteristic data, the measurement points at different locations of the desulfurization tower are determined, and the gas-liquid relative motion parameters and component transfer parameters at the measurement points are obtained to generate flue gas flow data. Calculate the initial gas-liquid mixing coefficient and initial mass transfer coefficient at the measurement point based on flue gas flow data; Temperature and pressure parameters are collected at the measurement point. The temperature and pressure parameters are substituted into the initial gas-liquid mixing coefficient and the initial mass transfer coefficient for correction, and the corrected gas-liquid mixing coefficient and mass transfer coefficient are generated. Based on the numerical distribution of the corrected gas-liquid mixing coefficient and mass transfer coefficient, a mass transfer performance distribution curve is constructed. The location of the slope change of the mass transfer performance distribution curve is calculated. According to the location of the slope change, the desulfurization tower is divided into multiple feed sections along the height direction, and the feed section boundary positions are generated. Calculate the average values ​​of the gas-liquid mixing coefficient and mass transfer coefficient in multiple feed sections, sort the multiple feed sections according to the average values, and generate the feed section distribution structure. The feed section distribution information is generated by combining the feed section boundary location with the feed section distribution structure.

3. The method according to claim 1, characterized in that, Based on the flue gas flow rate of each feeding section in the segmented feeding configuration information, the injection intensity of the high-pressure airflow and the supply amount of desulfurizing agent liquid in the corresponding tower section are determined, and the atomization control commands for each tower section are obtained, including: Obtain the flue gas flow rate of each feeding section from the segmented feeding configuration information, calculate the flue gas flow velocity of each feeding section, and obtain the flue gas velocity data of each feeding section. Based on the flue gas velocity data of each feeding section, the injection intensity of the high-pressure airflow and the effective range of the desulfurizing agent liquid are calculated to obtain the distribution data of the desulfurizing agent liquid. Based on the distribution data of the desulfurizing agent liquid, the relationship between the injection intensity of the high-pressure airflow and the supply amount of the desulfurizing agent liquid is calculated to obtain the injection intensity data of the high-pressure airflow. Based on the high-pressure airflow injection intensity data and the flue gas flow rate of each feeding section, the minimum supply of desulfurizing agent liquid is calculated, and the desulfurizing agent liquid supply data is obtained. Based on the desulfurizing agent supply data, the reaction conversion rate was measured, and the injection intensity of the high-pressure airflow and the supply of the desulfurizing agent were adjusted to obtain the injection intensity and supply ratio data. Based on the ratio of injection intensity to supply, the injection intensity of the high-pressure airflow and the supply of desulfurizing agent are set to obtain the atomization control commands for each tower section.

4. The method according to claim 1, characterized in that, According to the segmented feeding configuration information, the flue gas is introduced into the desulfurization tower in segments. Simultaneously, according to the atomization control command, the desulfurizing agent liquid flow is impacted by a high-pressure airflow in each tower segment to form droplets. During the droplet formation process, the flue gas and the droplets simultaneously react, resulting in the following reaction intermediate states in each tower segment: Obtain the feed inlet location information and flue gas flow distribution scheme from the segmented feed configuration information, introduce the flue gas into the desulfurization tower according to the feed inlet location information, adjust the flue gas flow at the feed inlet according to the flue gas flow distribution scheme, and monitor the flue gas distribution at each feed inlet. Based on the monitored flue gas distribution, read the high-pressure airflow injection intensity data and desulfurizing agent liquid supply data from the atomization control command, adjust the injection pressure and injection angle of the high-pressure airflow, and control the supply rate of the desulfurizing agent liquid. By adjusting the high-pressure airflow to impact the desulfurizing agent liquid flow, the impact angle and impact position between the high-pressure airflow and the desulfurizing agent liquid flow are controlled, so that the desulfurizing agent liquid flow is atomized into droplets. The formed droplets are brought into contact with the introduced flue gas to react. The contact position and contact time between the flue gas and the droplets are adjusted, and the reaction parameters of the flue gas in each tower section are measured, including the sulfur dioxide concentration and the amount of droplets absorbed. The removal rate and conversion rate of sulfur dioxide in each tower section are calculated based on the measured reaction parameters. The absorption saturation of droplets in each tower section is determined. The reaction temperature and pressure in each tower section are recorded, and the reaction intermediate state in each tower section is generated.

5. The method according to claim 1, characterized in that, The residual sulfur dioxide concentration in the reaction intermediate is monitored, and the distribution ratio of the desulfurizing agent supply between adjacent tower sections is adjusted according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, resulting in the flue gas after gradient desulfurization, which includes: Collect the residual sulfur dioxide concentration and gas flow rate in the intermediate state of the reaction, calculate the desulfurization reaction rate and desulfurizing agent conversion efficiency of each tower section, and generate the sulfur dioxide concentration distribution. Based on the sulfur dioxide concentration distribution analysis, the residual sulfur dioxide concentration difference between adjacent tower sections is analyzed, the desulfurizing agent consumption and reaction degree of each tower section are calculated, and the concentration change characteristics are obtained. Based on the consumption and reaction degree of desulfurizing agent in each tower section, establish the response curve of desulfurizing agent supply and sulfur dioxide residual concentration change, calculate the concentration gradient value and desulfurizing agent demand between adjacent tower sections, and determine the supply adjustment scheme. The desulfurizing agent replenishment amount for each tower section is set according to the supply adjustment plan. The desulfurizing agent distribution device is controlled to adjust the supply distribution ratio. The change of sulfur dioxide residual concentration is monitored to obtain sulfur dioxide residual concentration data. Calculate the concentration difference between adjacent tower sections based on the residual sulfur dioxide concentration data, adjust the supply ratio of the desulfurizing agent distribution device, control the desulfurizing agent supply rate of each tower section, monitor the sulfur dioxide concentration at the outlet of each tower section, and adjust the desulfurizing agent supply based on the monitored sulfur dioxide concentration until the sulfur dioxide concentration difference between adjacent tower sections meets the preset gradient requirements, thereby obtaining the flue gas after gradient desulfurization.

6. The method according to claim 1, characterized in that, The flue gas after gradient desulfurization is discharged from the top of the desulfurization tower, and the desulfurization products generated by the reaction are discharged from the bottom of the desulfurization tower, including: The flow characteristics of the flue gas after gradient desulfurization at the top of the desulfurization tower are detected, the flow velocity of the flue gas after gradient desulfurization in the exhaust channel is calculated, the distribution of the flue gas after gradient desulfurization is monitored, and the discharge conditions of the flue gas after gradient desulfurization are determined. Based on the determined discharge conditions, the pressure distribution of the flue gas after gradient desulfurization in the exhaust channel is analyzed, the flow field change of the flue gas after gradient desulfurization is calculated, and the treatment scheme of the flue gas after gradient desulfurization is obtained. The settling distribution of desulfurization products at the bottom of the desulfurization tower is collected, the distribution location of the desulfurization products is measured, the settling velocity of the desulfurization products is calculated, and the emission requirements of the desulfurization products are determined. The treatment scheme for flue gas after gradient desulfurization is matched with the emission requirements of desulfurization products. The operating ratio of exhaust device and emission device is calculated, the opening degree of exhaust device and the rotation speed of emission device are controlled, the discharge amount of flue gas after gradient desulfurization and the discharge amount of desulfurization products are adjusted, and the pressure inside the tower is measured. Adjust the operating parameters of the exhaust and emission devices according to the measured pressure inside the tower, control the flue gas after gradient desulfurization to be discharged from the top of the desulfurization tower through the exhaust device, and control the desulfurization products to be discharged from the bottom of the desulfurization tower through the emission device.

7. A multi-point feeding high-efficiency pneumatic emulsified flue gas deep desulfurization system, used to implement the method described in any one of claims 1-6, characterized in that, The system includes: The flue gas detection unit is used to detect the flow rate and sulfur dioxide concentration of the flue gas to be treated, and to obtain flue gas load data; The feed configuration unit is used to divide the flue gas into multiple feed sections along the height of the desulfurization tower according to the flue gas load data, allocate flue gas flow rate to each feed section and determine the feed inlet position to obtain the segmented feed configuration information. The atomization control unit is used to determine the injection intensity of the high-pressure airflow and the supply amount of desulfurizing agent liquid in the corresponding tower section based on the flue gas flow rate of each feed section in the segmented feed configuration information, and to obtain the atomization control command for each tower section. The reaction control unit is used to introduce flue gas into the desulfurization tower in stages according to the staged feed configuration information. At the same time, according to the atomization control command, the desulfurizing agent liquid flow is impacted by high pressure airflow in each tower section to form droplets. During the droplet formation process, the flue gas and the droplets are simultaneously contacted and reacted to obtain the reaction intermediate state of each tower section. The concentration adjustment unit is used to monitor the residual sulfur dioxide concentration in the reaction intermediate state and adjust the distribution ratio of desulfurizing agent supply between adjacent tower sections according to the difference in residual sulfur dioxide concentration in each tower section, so that the sulfur dioxide concentration at the outlet of each tower section forms a decreasing gradient, and the flue gas after gradient desulfurization is obtained. The emission control unit is used to discharge the flue gas after gradient desulfurization from the top of the desulfurization tower and to discharge the desulfurization products generated by the reaction from the bottom of the desulfurization tower.

8. An electronic device, characterized in that, include: A memory, a processor, and a computer program stored in the memory and executable on the processor, wherein the processor, when executing the computer program, implements the steps of the method as described in any one of claims 1 to 6.

9. A computer-readable storage medium, characterized in that, The computer-readable storage medium stores computer program instructions that, when executed by a processor, implement the steps of the method as described in any one of claims 1 to 6.

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