Method and system for co-processing multiple pollutants in sintering flue gas

Abstract

The invention provides a sintering flue gas multi-pollutant cooperative treatment method and system, and belongs to the technical field of environmental engineering. The sintering flue gas multi-pollutant cooperative treatment method comprises the steps that sintering flue gas is subjected to desulfurization and dust removal treatment and then is treated through a multifunctional catalytic bed layer, and the multifunctional catalytic bed layer at least comprises a CO-NOx catalytic bed layer and is used for conducting oxidation reduction treatment on CO-NOx in the sintering flue gas; in the treatment process, NOx is subjected to catalytic reduction reaction by CO to generate N2 and CO2 through a high-energy particle action mechanism; and the treated sintering flue gas is discharged after reaching the standard. The problems that a heat exchange device needs to be used for reheating, and energy consumption is large are solved; and heavy metal oxidation and dioxin oxidative degradation in the sintering flue gas can be realized, and catalyst deactivation caused by the fact that alkali metal and chlorobenzene are attached to the surface of the catalyst is avoided.

Description

Technical Field

[0001] The present invention relates to the field of environmental engineering technology, and in particular to a method and system for collaboratively treating multiple pollutants in sintering flue gas. Background Art

[0002] Sintering flue gas is the most polluting waste gas in the steel industry, and reducing CO emissions in sintering flue gas is the top priority of governance. At present, the method for removing CO from sintering flue gas in the existing technology is mainly to heat the sintering flue gas after dust removal through a hot blast furnace, heat the flue gas to 1000-1400°C, and blow the heated flue gas into the blast furnace through the blast furnace tuyere to replace air for ironmaking production. This method combines the sintering flue gas with the ironmaking hot blast furnace, but the thermal system of the blast furnace hot blast furnace is strict, and the sintering flue gas itself fluctuates greatly, and the amount of sintering flue gas is large, far exceeding the demand for blast furnace hot blast furnace flue gas. In actual use, the excess sintering flue gas still needs to be purified. And the NO in the sintering flue gas x The use of low-temperature SCR denitrification technology is simple to operate, but due to the large temperature fluctuations of sintering flue gas, hot air furnaces are usually required for supplementary heating, which consumes a lot of energy and has high working costs. x Collaborative emission reduction is of great significance.

[0003] To address the above-mentioned issues, patent document CN212236736U provides a device for the combined removal of CO and NOx from sintering flue gas. The device is equipped with a flue, a heating system, a CO catalytic reaction system, an ammonia injection system, a low-temperature SCR denitrification reaction system, and a rotary heat exchanger. The heat generated by the catalytic oxidation of CO in the sintering flue gas to CO2 in the CO removal reactor is used to provide thermal energy for the subsequent denitrification of the low-temperature SCR denitrification reaction system. Finally, a rotary heat exchanger is provided to transfer the heat contained in the clean flue gas after the removal of CO and NOx to the inlet of the heating system through the rotary heat exchanger. The drawbacks of this patent are that the overall device structure is complex, the floor space is large, and the engineering cost is high. The flue gas after desulfurization needs to be supplemented with heat from a hot blast furnace, which consumes a lot of energy. The CO catalyst faces the problem of alkali metal poisoning, resulting in poor CO removal. In addition, the rotary heat exchange method used in the device results in a certain amount of heat loss.

[0004] Patent document No. CN113797753A provides a method for simultaneously removing CO and NO from sintering flue gas. xThe system can make full use of the heat released by CO oxidation, reduce the energy consumption of the system, and simplify the reaction device by utilizing the turbulence effect of catalysts with different morphologies. The flue gas is heated by the heat exchange device, and the heated flue gas enters the multifunctional oxidation layer, where the CO oxidation heat is released to increase the flue gas temperature, promoting the oxidation of NO in the flue gas to NO2. At the same time, by adjusting the thickness and inclination angle of the multifunctional oxidation layer, the gas concentration and flow rate are made more balanced; after passing through the multifunctional oxidation layer, the flue gas enters the SCR catalyst layer for denitrification reaction; the flue gas after denitrification is recovered through the heat exchange device for waste heat recovery and then discharged cleanly. CO and NO x The graded treatment involves oxidation and reduction processes, which place stringent demands on the flue gas composition. Furthermore, the flue gas requires heat exchangers to raise its temperature, resulting in high energy consumption and a complex process.

[0005] In view of this, the inventors, based on many years of experience in production design in this field and related fields, have designed a method and system for the coordinated treatment of multiple pollutants in sintering flue gas after repeated experiments, in order to solve the problems existing in the prior art. Summary of the Invention

[0006] The purpose of the present invention is to provide a method and system for the coordinated treatment of multiple pollutants in sintering flue gas, which can achieve the goal of reducing CO and NO x At the same time, it can remove and reduce the harsh demands of working conditions on the process.

[0007] In order to achieve the above-mentioned purpose, the present invention proposes a method for the coordinated treatment of multiple pollutants in sintering flue gas, wherein the sintering flue gas is subjected to desulfurization and dust removal treatment and then treated by a multifunctional catalytic bed, which includes at least one layer of CO-NO x Catalytic bed, used for CO-NO x Redox treatment: During the treatment process, CO is used to reduce NO x The catalytic reduction reaction generates N2 and CO2; the treated sintering flue gas meets emission standards.

[0008] The present invention also proposes a system for the coordinated treatment of multiple pollutants in sintering flue gas, wherein the system for the coordinated treatment of multiple pollutants in sintering flue gas comprises a flue and a multifunctional catalytic bed connected to the flue, the multifunctional catalytic bed comprising at least one layer of CO-NO x Catalytic bed, CO-NO x The catalytic bed is used to remove CO-NO in sintering flue gas. x The system for the coordinated treatment of multiple pollutants in sintering flue gas also includes a high-energy particle emission device and an emission outlet. The high-energy particle emission device generates active substances O through discharge. - or OH- and injected into CO-NO xThe catalytic bed layer has an emission outlet connected to the multifunctional catalytic bed layer and is used to emit the treated sintering flue gas.

[0009] Compared with the prior art, the present invention has the following characteristics and advantages:

[0010] The present invention proposes a method and system for the coordinated treatment of multiple pollutants in sintering flue gas, which can achieve the goal of reducing carbon monoxide and NO x At the same time, it removes NO from flue gas, reducing the harsh requirements of working conditions on the process. The present invention uses CO as a reducing agent to catalyze the reduction of NO in flue gas. x , which can reduce the cost of using reducing agents and achieve the purpose of "treating waste with waste"; the present invention uses the active substances generated by discharge to treat NO in flue gas x The bond with CO is broken, reducing the activation energy of the reaction. This solves the problem of requiring reheating with a heat exchanger, which consumes a lot of energy. The present invention can achieve the oxidation of heavy metals and the oxidative degradation of dioxins in sintering flue gas, avoiding the deactivation of the catalyst caused by the adhesion of alkali metals and chlorobenzene to the catalyst surface.

[0011] This invention proposes a method and system for the coordinated treatment of multiple pollutants in sintering flue gas. This system uses a jet of high-energy particles to regenerate the catalyst in situ. Furthermore, by regenerating the catalyst on the catalytic bed, the invention improves the removal rate of surface deposits and the recovery rate of catalyst activity, thereby extending the catalyst's service life. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] The drawings described herein are for illustrative purposes only and are not intended to limit the scope of the present invention in any way. In addition, the shapes and proportional dimensions of the various components in the drawings are merely illustrative and are used to help understand the present invention, and are not intended to specifically limit the shapes and proportional dimensions of the various components of the present invention. Those skilled in the art can select various possible shapes and proportional dimensions to implement the present invention according to specific circumstances under the guidance of the present invention.

[0013] Figure 1 A schematic diagram of a method for collaboratively treating multiple pollutants in sintering flue gas according to the present invention;

[0014] Figure 2 A schematic diagram of another method for collaboratively treating multiple pollutants in sintering flue gas according to the present invention;

[0015] Figure 3 Schematic diagram of the multifunctional catalytic treatment method of the present invention;

[0016] Figure 4 Schematic diagram of the system for co-processing multiple pollutants in sintering flue gas according to the present invention;

[0017] Figure 5 Schematic diagram of the jet generator of the present invention.

[0018] Description of Reference Numerals

[0019] 100. System for the coordinated treatment of multiple pollutants in sintering flue gas; 10. Flue;

[0020] 20. Multifunctional catalytic bed; 30. Jet generator;

[0021] 40. Power supply; 50. Fan

[0022] 60. Homogenizing mechanism; 70. Thermal energy conversion device. DETAILED DESCRIPTION

[0023] The details of the present invention can be more clearly understood by referring to the accompanying drawings and the description of the specific embodiments of the present invention. However, the specific embodiments of the present invention described herein are only for the purpose of explaining the present invention and are not to be construed as limiting the present invention in any way. Based on the teachings of the present invention, a skilled person can conceive of any possible variations based on the present invention, and such variations should be considered to fall within the scope of the present invention.

[0024] like Figures 1 to 3 As shown, the present invention proposes a method for the coordinated treatment of multiple pollutants in sintering flue gas, wherein the sintering flue gas is treated by desulfurization and dust removal, and then treated by a multifunctional catalytic bed 20, which includes at least one layer of CO-NO x Catalytic bed for CO-NO x Redox treatment: During the treatment process, CO is used to reduce NO x The catalytic reduction reaction generates N2 and CO2; the treated sintering flue gas meets emission standards.

[0025] The method for co-processing multiple pollutants in sintering flue gas proposed by the present invention is to introduce the sintering flue gas containing CO-NO into the flue gas after desulfurization and dust removal. x The multifunctional catalytic bed 20 of the catalytic bed uses CO in the flue gas as a reducing agent to catalytically reduce NO under the action of high-energy particles. x Generate N2 and CO2, realize CO and NO x The simultaneous and efficient removal of CO and NO in the treated flue gas reduces the dependence on external reducing agents (such as ammonia), while reducing the reaction activation energy demand and avoiding the energy consumption of additional heating in traditional processes. x The concentration was reduced to ≤300 mg / m 3 and ≤40 mg / m 3 The following meets the ultra-low emission requirements of the steel industry.

[0026] The present invention proposes a system 100 for co-processing multiple pollutants in sintering flue gas, wherein Figure 4 、 Figure 5 As shown, the system 100 for co-processing multiple pollutants in sintering flue gas includes a flue 10 and a multifunctional catalytic bed 20 connected to the flue 10. The multifunctional catalytic bed 20 includes at least one layer of CO-NO x Catalytic bed, CO-NO x The catalytic bed is used to remove CO-NO in sintering flue gas. x The system 100 for the coordinated treatment of multiple pollutants in sintering flue gas further comprises a high-energy particle emission device and an emission outlet. The high-energy particle emission device generates active substances (such as O - or OH- or other free radicals) and injected into CO-NO x The catalytic bed layer has an emission outlet connected to the multifunctional catalytic bed layer 20 and is used to emit the treated sintering flue gas.

[0027] The system 100 for coordinating the treatment of multiple pollutants in sintering flue gas proposed by the present invention uses the active material O generated by the high-energy particle emission device. - , OH- or free radicals, directly acting on CO-NO x Catalytic bed, activation of CO and NO x The catalytic reduction reaction of CO and NO can be achieved at low temperature (100-140℃) without relying on external heat source or ammonia injection process. x The efficient synergistic removal of CO and NO in the treated sintering flue gas can reduce the energy consumption and operation risk of the system. x The concentration was reduced to ≤300 mg / m 3 and ≤40 mg / m 3 Below, the emission standards are met directly through the emission outlet to meet the ultra-low emission requirements of the steel industry.

[0028] In an optional embodiment of the present invention, the multifunctional catalytic bed 20 also includes an alkali metal adsorption layer for adsorbing heavy metals in the flue gas. The alkali metal adsorption layer has a filling height of 200-500 mm. In the process flow, after passing through the homogenization mechanism 60, the flue gas first enters the multifunctional catalyst bed. The alkali metal adsorption layer can remove more than 90% of alkali metals such as K and Na. The alkali metal adsorption layer is filled with materials such as γ-Al2O3 particles, molecular sieves, and activated carbon (particle size 3-5 mm). Its filling height is set within the range of 200-500 mm, which can ensure effective adsorption of alkali metals in the flue gas.

[0029] In an optional example of this embodiment, the alkali metal adsorption layer is filled with the adsorbent γ-Al2O3, with particles of 3–5 mm in size; or molecular sieve or activated carbon. The alkali metal adsorption layer uses γ-Al2O3 particles with a particle size of 3–5 mm and a filling height of 500 mm, capable of removing over 90% of alkali metals such as K and Na. The alkali metal adsorption layer is located within the multifunctional catalyst bed. After the sintering flue gas passes through the homogenization mechanism 60, it first enters this adsorption layer. The large surface area and strong adsorption properties of the γ-Al2O3 particles, molecular sieve, or activated carbon effectively adsorb the alkali metals in the flue gas. The high porosity and abundant active adsorption sites on the surface of γ-Al2O3 particles enable selective adsorption of alkali metals. Molecular sieve and activated carbon, with their regular pore structure and well-developed pore system, respectively, have excellent alkali metal capture capabilities. By selecting these adsorbents and controlling the particle size to 3–5 mm, adsorption efficiency is guaranteed while bed resistance is reduced, ensuring uniform flue gas flow through the adsorption layer.

[0030] In an optional embodiment of the present invention, the multifunctional catalytic bed 20 also includes a dioxin oxidation layer, comprising a honeycomb ceramic catalyst layer composed of V2O5-WO3 / TiO2 molecules and transition metals. The honeycomb ceramic catalyst layer has a thickness of 200-400 mm and a pore density of 200-400 cpsi. By optimizing the pore density and thickness parameters, such as a pore density of 300 cpsi and a thickness of 300 mm in the embodiment, this layer can efficiently oxidize and degrade dioxins (PCDD / Fs) in sintering flue gas at a low temperature of 120°C, with a degradation rate of ≥85%. The honeycomb ceramic structure increases the gas-solid contact area. The coordinated design of pore density and thickness ensures airflow while extending the reaction residence time. The introduction of transition metals further enhances oxidation activity, thereby achieving deep dioxin purification with low energy consumption.

[0031] In an optional example of this embodiment, the transition metal used in the honeycomb ceramic catalyst layer is a combination of one or more of Pb, Cu, Fe, Mn, Ce, Zr, and Nb. This combination design can flexibly adjust the type and ratio of transition metals (for example, combinations of Pb-Ce, Fe-Mn, or Cu-Zr) according to different flue gas components, utilizing the synergistic effect between metals to enhance the oxidative degradation ability of dioxins. For example, in Example 1, a honeycomb ceramic catalyst using a single or composite transition metal has a PCDD / Fs degradation rate of ≥85% at 120°C. The coordinated control of its pore density and thickness (200-400 cpsi, 200-400 mm) ensures that the highly active sites are exposed and fully contacted with the reaction gas, thereby achieving efficient dioxin removal under low temperature conditions while avoiding the problem of catalyst deactivation caused by local overheating or carbon deposition.

[0032] In an optional embodiment of the present invention, the CO-NOx catalytic bed layer comprises a honeycomb ceramic molecular sieve composed of a catalyst and a transition metal, the honeycomb ceramic molecular sieve pore density is set to 200-600 cpsi, and the filling height is 200-800 mm. The catalytic bed layer is formed by selecting a honeycomb ceramic molecular sieve with a specific pore density and filling height, so that the catalyst is fully in contact with the flue gas, ensuring good mass transfer and reaction effects, and can effectively improve the conversion rate of CO and NOx. As in Example 1, the pore density is 400 cpsi, the filling height is 800 mm, and the air velocity is controlled at 2000-5000 h -1 , CO and NO are achieved at 120-130℃ x The efficient catalytic reduction of CO and NO x The removal rates were 96% and 92% respectively.

[0033] In an alternative example of this embodiment, CO-NO x The catalyst bed is V2O5-MoO3, and the active components of the catalyst molecules account for 5-20%. Highly dispersed active sites are formed by loading on the molecular sieve honeycomb ceramic matrix. This ratio range can balance the catalytic activity and stability. When the active component accounts for too low a proportion (such as 5%), the catalytic activity is insufficient, and when the proportion is too high (such as 20%), it is easy to cause the active components to agglomerate and deactivate. For example, when the active component accounts for 12% in Example 1, at 120-130°C and an air velocity of 3000h -1 Under these conditions, CO and NO x The removal rates of V2O5 and MoO3 were 96% and 92%, respectively. By optimizing the ratio of active ingredients, the synergistic effect of V2O5 and MoO3 enhances the reduction ability of CO to NOx while avoiding performance degradation caused by local reaction overheating or sintering of the catalyst.

[0034] In an alternative example of this embodiment, CO-NO x The catalytic bed layer contains transition metals, which are one or more of Pb, Cu, Fe, Mn, Ce, Zr, and Nb. Under the action of transition metals, the activity and selectivity of the catalyst are effectively improved, thereby enhancing the reduction effect of NOx and achieving efficient CO-NOx catalytic reduction reaction. The addition of transition metals optimizes the electronic structure and surface properties of the catalyst, promoting the reduction of CO and NOx. x Adsorption and reaction on the catalyst surface increase the reaction rate and conversion rate.

[0035] In an optional example of this embodiment, when the CO concentration in the flue gas is ≤2000 mg / m 3When the CO-NOx catalyst bed uses FeMn / US-SSY molecular catalyst, the active component accounts for 8%. As in Example 2, for low CO concentration scenarios, when the CO concentration in the flue gas is insufficient, it is necessary to add a reducing agent. x An H2 injection device is added before the catalytic bed, and FeMn / US-SSY catalyst is used, with an active component ratio of 8%, which is suitable for the H2 reduction path. By using FeMn / US-SSY molecular catalyst, combined with the H2 reduction path at low CO concentration, it can effectively improve NO x The removal rate enables the system to maintain good treatment effect under low CO concentration conditions, enhancing the adaptability and flexibility of the system.

[0036] In an alternative example, CO-NO x H2 or CH4 is injected before the catalytic bed as a supplemental reducing agent. By dynamically adjusting the reducing agent injection rate to match the reaction conditions, the system effectively avoids the decline in NOx removal efficiency caused by insufficient CO, enhances the system's adaptability to fluctuating flue gas components, and ensures that ultra-low emission requirements can still be met stably in low CO concentration scenarios.

[0037] In an optional example, the concentration of H2 in the reducing agent is 1-3%, and H2 and NO x Molar ratio 1.2:1; CH4 concentration 1-3%, CH4 and NO x Molar ratio 1.2:1; through precise concentration and molar ratio control, it can ensure that when the CO concentration in the flue gas is insufficient, the supplementary reducing agent can efficiently participate in the reduction reaction, synergistically act with CO, and fully reduce NO x , thereby increasing NO x The removal efficiency is high, ensuring that the system can achieve good treatment effects under different working conditions.

[0038] In an optional embodiment of the present invention, the mechanism of action of high-energy particles is the active material O generated by discharge. - Or OH- or free radicals react with CO and NOx to break bonds, reducing the activation energy. As in Example 1, when a voltage of 25-35kV, a jet velocity of 10-15m / s and a pulse frequency of 1kHz are used, the concentration of active substances is significantly increased, and CO and NO can be triggered without additional heating at 120-130°C. x The catalytic reduction reaction achieved removal rates of 96% and 92%, respectively. This mechanism reduces activation energy by approximately 40%, achieving low-temperature, high-efficiency reactions while also reducing energy consumption associated with high-temperature heating in traditional processes by 38%, ensuring the system consistently meets emission standards at low operating costs.

[0039] In an optional example of this embodiment, the high-energy particle action mechanism uses a point power source 40 to apply voltage to the jet generator 30, and through the action of the fan 50, the high-energy particles are sprayed onto the catalyst surface to produce a catalytic reduction reaction with the flue gas; the discharge range of the point power source 40 is 0-35kV, the jet velocity is 10-25m / s, and the pulse frequency is 0-2kHz. In Example 1, when a voltage of 25-35kV, a jet velocity of 10-15m / s and a pulse frequency of 1kHz are used, the active material (O - , OH- or free radicals) is significantly improved, triggering CO and NO at 120-130 ° C x The catalytic reduction reaction (removal rates reached 96% and 92%, respectively). This mechanism ensures that high-energy particles evenly cover the catalyst surface and fully participate in the reaction through the coordinated regulation of jet velocity and voltage. The optimization of pulse frequency further reduces energy loss, ultimately achieving low-temperature and high-efficiency catalytic reduction at low energy consumption (energy consumption is reduced by 38%).

[0040] In an optional embodiment of the present invention, the supplementary chemical reaction in the catalytic reduction reaction equation is:

[0041]

[0042] In this catalytic reduction reaction equation, under the action of high-energy particles, CO and NO x In CO-NO x A reaction occurs in the catalytic bed. Through this chemical reaction, CO acts as a reducing agent to reduce NO x It is reduced to N2 and oxidized to CO2, achieving efficient CO-NO x Catalytic reduction effectively reduces CO and NO in sintering flue gas x concentration.

[0043] In an optional embodiment of the present invention, the catalytic reduction reaction temperature is maintained at 100-140°C, and the space velocity is controlled at 2000-5000h -1 , residence time 2s.

[0044] In an optional example of this embodiment, the catalytic reduction reaction temperature is optimally maintained at 120-130°C, and the space velocity is controlled at 3000h -1 .

[0045] Specifically, in Example 1, the catalytic reduction reaction temperature is strictly controlled in the range of 100-140°C, preferably 120-130°C, and the space velocity is adjusted to the range of 2000-5000h -1 , preferably 2500-3500h -1And ensure that the residence time of the flue gas in the catalytic bed is 2 seconds. In the embodiment, at 120-130 ° C and a space velocity of 3000h -1 Under these conditions, CO and NO x The removal rates reached 96% and 92%, respectively. This temperature range balances reaction kinetics with energy consumption requirements, avoiding catalyst sintering caused by high temperatures or insufficient reaction efficiency at low temperatures. The coordinated control of space velocity and residence time optimizes gas-solid contact efficiency, ensuring that reactants fully react on the catalyst surface.

[0046] In an optional embodiment of the present invention, the high-energy particle action mechanism can also utilize an in-situ regeneration mechanism to regenerate the catalyst in situ after the catalytic reduction reaction. The high-energy particle action mechanism regenerates the catalyst in situ after the catalytic reduction reaction through an in-situ regeneration mechanism, specifically including alternately introducing high-oxygen gas, O2 concentration ≥30%, and reducing gas, H2 concentration 3-5%, at a jet velocity of 15-20m / s, and a voltage of 30-40kV, spraying the catalyst surface, continuously cleaning for 2 hours and cycling twice. When using this process, the catalyst surface attachments, such as Cl - , alkali metal salts, with a removal rate of ≥98% and an activity recovery rate of ≥97%. This regeneration mechanism effectively decomposes and removes contaminants on the catalyst surface through an alternating oxidation-reduction cleaning strategy, avoiding deactivation caused by alkali metal poisoning or carbon deposition. Simultaneously, the coordinated optimization of jet velocity and voltage reduces regeneration energy consumption, with unit energy consumption reduced by 12%, ensuring long-term stable operation of the catalyst without the need for frequent replacement.

[0047] In an optional example of this embodiment, the catalyst in situ method is: start the jet generator 30 once every preset time, alternately use high-oxygen gas and reducing gas H2 as gas sources, spray high-energy particles at a preset speed, repeatedly clean for a preset cleaning time, and cycle a preset number of times to remove deposits on the catalyst surface.

[0048] Through this regeneration process, Cl attached to the catalyst surface - Contaminants such as alkali metal salts are removed through physical flushing and chemical oxidation / reduction, achieving a removal rate of ≥95% and restoring catalyst activity to over 95% of its initial state. This periodic regeneration strategy, by matching fixed time intervals with parameters, ensures long-term, stable operation of the catalyst while avoiding the additional energy consumption and equipment loss caused by frequent regeneration, ultimately significantly extending catalyst life.

[0049] In an optional example, the preset time is preferably 24 hours, the preset speed is preferably 12 m / s, the preset cleaning time is preferably 2 hours, and the preset number of times is preferably 2 times.

[0050] In an optional embodiment of the present invention, the temperature range of the flue gas entering the multifunctional catalytic bed 20 for catalytic treatment is controlled at 90-140°C, wherein the optimal temperature is 120-130°C, to ensure that the catalytic reaction proceeds within the optimal temperature window. In Example 1, the flue gas is heated from 90°C to 120°C after desulfurization and dust removal, and maintained at 120-130°C in the catalytic bed. CO and NO x The removal rates reached 96% and 92%, respectively. This temperature control strategy matches the catalyst's active temperature range (120-130°C) to avoid insufficient reaction efficiency caused by low temperatures (<90°C) or catalyst sintering caused by high temperatures (>140°C). At the same time, the introduction of a heating device ensures stable operation of the system under low-temperature flue gas conditions, ensuring that the pollutant removal effect meets ultra-low emission requirements.

[0051] In an optional embodiment of the present invention, before the flue gas enters the multifunctional catalytic bed 20, the flue gas is homogenized and subjected to primary purification treatment. The flue gas flow rate is adjusted to 0.8m / s by the homogenization mechanism 60, and the flue gas enters and passes through the multifunctional catalyst layer evenly. This homogenization design eliminates the dead zone of flue gas flow by accurately matching the porosity and flow rate, ensuring full contact between the pollutants and the catalyst surface; in the primary purification stage, the evenly distributed flue gas is adsorbed by the alkali metal adsorption layer (γ-Al2O3 particles, particle size 3-5mm) to remove more than 90% of alkali metals such as K and Na, reducing the risk of downstream catalyst poisoning. After adopting this homogenization and primary purification process in the embodiment, the pressure difference of the catalytic bed is stable, the reaction efficiency is improved by 15%, and the stability of the system operation is significantly enhanced.

[0052] In an optional embodiment of the present invention, the flue gas is pretreated before entering the multifunctional catalytic bed 20; this pretreatment adopts conventional technical means to perform desulfurization and dust removal, including limestone-gypsum desulfurization to remove SO x Pollutants, and dry dust removal (bag dust collector) removes particulate matter (such as PM) in the flue gas, so that the sulfide and dust content in the flue gas meets the requirements of the catalytic reaction, so as to reduce the risk of poisoning and clogging of the catalyst by sulfide and dust in the flue gas.

[0053] In an optional embodiment of the present invention, before the flue gas is discharged, the waste heat generated in the reduction reaction in the flue gas is recovered and the flue gas discharge temperature is controlled below 100°C. In Example 1, when a shell and tube heat exchanger is used, the waste heat recovery efficiency is ≥65%, the outlet temperature is stably controlled at 100°C, and the CO and NO in the flue gas are purified. x The concentration was reduced to ≤300 mg / m 3 and ≤40 mg / m 3The waste heat recovery design reduces the total energy consumption of the system by recycling heat energy, while avoiding energy waste caused by direct emission of high-temperature flue gas.

[0054] In an optional example of this embodiment, the heat energy conversion device 70 of the flue gas exhaust converts the waste heat in the flue gas to the flue duct 10 at the flue gas inlet, heating the inlet flue gas. This design reduces external heating energy consumption by recycling heat energy and lowers the exhaust gas temperature to below 100°C, significantly improving the system's energy efficiency and economic efficiency while meeting ultra-low emission requirements.

[0055] In an optional example of this embodiment, the coordinated treatment of multiple pollutants in flue gas adopts the following steps:

[0056] S1, flue gas pretreatment: desulfurization and dust removal;

[0057] S2, homogenization and primary purification;

[0058] S3, multifunctional catalytic treatment;

[0059] S3.1, alkali metal adsorption treatment, removing more than 90% of alkali metals;

[0060] S3.2, dioxin oxidation treatment, oxidative degradation of PCDD / Fs, degradation rate ≥ 85%;

[0061] S3.3, CO-NOx catalytic reduction reaction treatment, injection of high-energy particles;

[0062] S4, smoke emission;

[0063] S5, flue gas waste heat recovery (S4 and S5 can be carried out simultaneously);

[0064] S6, in-situ regeneration of the catalyst.

[0065] First, S1 flue gas pretreatment is performed, including desulfurization (limestone-gypsum method) and dry dust removal (bag filter), which removes most pollutants from the flue gas and reduces the burden of subsequent treatment. Next, S2 homogenization and primary purification are carried out, using a porous plate flow equalizer to evenly distribute the flue gas. This is followed by the S3 multifunctional catalytic treatment stage, which includes S3.1 alkali metal adsorption treatment, using adsorbents such as γ-Al2O3 particles to remove over 90% of alkali metals; S3.2 dioxin oxidation treatment, using catalysts such as V2O5-WO3 / TiO2 to oxidatively degrade PCDD / Fs, with a degradation rate of ≥85%; and S3.3 CO-NOx catalytic reduction reaction treatment, using high-energy particles to promote the reaction of CO and NOx to produce N2 and CO2. This is followed by S4 flue gas emission, while S5 flue gas waste heat recovery is simultaneously implemented, using a heat exchanger to recycle the recovered heat and control the exhaust temperature below 100°C. S4 and S5 can be performed simultaneously. Finally, the S6 catalyst undergoes in-situ regeneration. Every 24 hours, the jet generator 30 is activated, alternating between high-oxygen and reducing H2 gases, spraying high-energy particles to remove deposits from the catalyst surface. Regeneration efficiency is ≥95%. This series of steps works in tandem to efficiently treat multiple pollutants in the sintering flue gas, reducing energy consumption, emissions, extending the catalyst's service life, and ensuring long-term, stable operation of the system.

[0066] In an optional example of this embodiment, the coordinated treatment of multiple pollutants in flue gas adopts the following steps:

[0067] S1, flue gas pretreatment:

[0068] S1.1, desulfurization and dust removal;

[0069] S1.2, injection of reducing agent;

[0070] S2, homogenization and primary purification;

[0071] S3, multifunctional catalytic treatment;

[0072] S3.1, alkali metal adsorption treatment, removing more than 90% of alkali metals;

[0073] S3.2, dioxin oxidation treatment, oxidative degradation of PCDD / Fs, degradation rate ≥ 85%;

[0074] S3.3, CO-NO x Catalytic reduction reaction treatment, shooting in high-energy particles;

[0075] S4, smoke emission;

[0076] S5, flue gas waste heat recovery (S4 and S5 can be carried out simultaneously);

[0077] S6, in-situ regeneration of the catalyst.

[0078] Specifically, the collaborative treatment of multiple pollutants in flue gas proposed by the present invention adopts the following steps: S1 flue gas pretreatment: S1.1 desulfurization and dust removal operations are performed on the sintering flue gas to remove most of the pollutants in the flue gas and reduce the burden of subsequent treatment; S1.2 When the CO concentration in the flue gas is insufficient, a reducing agent is injected, such as in the CO-NO x A H2 injection device is added before the catalytic bed, and FeMn / US-SSY catalyst is used to adapt to the H2 reduction path to ensure that NO can be effectively reduced even at low CO concentrations. x , improve the adaptability of the system. S2 Homogenization and primary purification: Use a porous plate flow equalizer to evenly distribute the flue gas to ensure that the flue gas enters the subsequent treatment unit evenly. S3 Multifunctional catalytic treatment: S3.1 Alkali metal adsorption treatment, using adsorbents such as γ-Al2O3 particles to remove more than 90% of alkali metals and protect subsequent catalysts; S3.2 Dioxin oxidation treatment, using V2O5-WO3 / TiO2 and other catalysts to oxidize and degrade PCDD / Fs, with a degradation rate of ≥85%; S3.3 CO-NO x Catalytic reduction reaction treatment, through the action of high-energy particles, promotes the reaction of CO and NOx to produce N2 and CO2. S4 Flue gas emission: The treated flue gas meets the emission standards. S5 Flue gas waste heat recovery: The waste heat in the flue gas is recovered by the heat exchanger, and the heat is recycled to improve energy efficiency and reduce energy consumption. S4 and S5 can be carried out simultaneously. S6 Catalyst in-situ regeneration treatment: The jet generator 30 is started once every 24 hours, and high-oxygen gas and reducing gas H2 are used alternately as the gas source to spray high-energy particles to remove attachments on the catalyst surface. The regeneration efficiency is ≥95%, extending the service life of the catalyst. This series of steps work together to achieve efficient and coordinated treatment of multiple pollutants in sintering flue gas, reduce energy consumption, reduce emissions, and ensure long-term stable operation of the system.

[0079] In another optional embodiment of the present invention, the sintering flue gas enters the flue 10 of the system; the multifunctional catalytic bed 20 is processed, and the multifunctional catalytic bed 20 includes at least one layer of CO-NO x Catalytic bed, used for the oxidation and reduction of CO-NOx in the gas; at least includes a high-energy particle emission device for CO to NO x The catalytic reduction reaction generates N2 and CO2; including the sintering flue gas emission outlet. x The catalytic bed layer uses a catalyst composed of V2O5-MoO3 loaded on a molecular sieve honeycomb ceramic matrix, with an active component ratio of 5-20%, a pore density of 200-600 cpsi, and a filling height of 200-800 mm. The high-energy particle emission device sprays O into the catalytic bed layer by applying a voltage of 25-35 kV and a jet velocity of 10-15 m / s. - , OH- or other free radicals and other active substances, promoting the reaction of CO and NOx A catalytic reduction reaction occurs to generate N2 and CO2.

[0080] In another optional embodiment of the present invention, the multifunctional catalytic bed 20 also includes an alkali metal adsorption layer for adsorbing heavy metals from the flue gas. The alkali metal adsorption layer has a fill height of 200-500 mm and is composed of γ-Al2O3 particles, molecular sieves, and activated carbon, with a particle size of 3-5 mm. This adsorption layer homogenizes the flue gas, efficiently adsorbing alkali metal ions such as K and Na in the flue gas, with a removal rate of ≥90%. The optimized fill height balances adsorption efficiency and system pressure drop, ensuring uniform distribution of the flue gas to the downstream catalytic bed.

[0081] In one optional example of this embodiment, the alkali metal adsorption layer is filled with γ-Al2O3 particles, molecular sieves, and activated carbon, with particle sizes of 3–5 mm. The transition metals include at least one of Pb, Cu, Fe, Mn, Ce, Zr, and Nb. The γ-Al2O3 particles, due to their surface area and strong adsorption properties, effectively adsorb alkali and heavy metals from flue gas. The molecular sieves, with their unique pore structure, effectively screen and adsorb alkali metals. The activated carbon, with its developed pore structure and surface activity, further enhances its capture capacity for alkali and heavy metals. This combination of fillings enables the alkali metal adsorption layer to efficiently remove alkali metals from flue gas, with a removal rate exceeding 90%, effectively preventing alkali metal poisoning of subsequent catalysts.

[0082] In an optional example of this embodiment, the multifunctional catalytic bed 20 also includes a dioxin oxidation layer, comprising a honeycomb ceramic catalyst layer composed of V2O5-WO3 / TiO2 molecules and transition metals. The honeycomb ceramic catalyst layer has a thickness of 200-400 mm and a pore density of 200-400 cpsi. The transition metal employed in the honeycomb ceramic catalyst layer includes at least one of Pb, Cu, Fe, Mn, Ce, Zr, and Nb. The oxidative activity of the transition metals combined with the high specific surface area of ​​the honeycomb ceramics achieves efficient degradation of PCDD / Fs (degradation rate ≥ 85%) at a low temperature of 120°C. The coordinated design of pore density and thickness (200-400 cpsi, 200-400 mm) ensures smooth airflow while extending reaction residence time. The introduction of transition metals enhances the directional oxidation of dioxins, preventing catalyst deactivation due to carbon deposition of chlorobenzene byproducts, ultimately achieving deep dioxin purification with low energy consumption.

[0083] In an optional example of this embodiment, the multifunctional catalytic bed 20 also includes a CO-NOx catalytic bed, a honeycomb ceramic molecular sieve composed of a catalyst and a transition metal, the honeycomb ceramic molecular sieve has a pore density of 200-600 cpsi, and a filling height of 200-800 mm; the CO-NOx catalytic bed, the catalyst is V2O5-MoO3, and the active components of the catalyst molecules account for 5-20%; the CO-NOx catalytic bed, the transition metal includes at least any one of Pb, Cu, Fe, Mn, Ce, Zr, and Nb.

[0084] Specifically, taking Example 1 as an example, the active ingredient ratio is strictly controlled at 12%, and at least one transition metal selected from Pb, Cu, Fe, Mn, Ce, Zr, and Nb is compounded as an active component; the pore density of the honeycomb ceramic molecular sieve is 400 cpsi, and the filling height is 800 mm. The catalytic bed is designed with a high pore density of 200-600 cpsi and a filling height of 200-800 mm for the honeycomb ceramic. At 120-130°C and a space velocity of 3000 h -1 Under these conditions, CO and NO x The removal rates of CO and NO were 96% and 92% respectively. The introduction of transition metals enhances the removal of CO to NO through electronic synergy. x The reduction ability of CO and NO is improved by optimizing the proportion of active ingredients (5-20%), which balances the catalytic activity and stability, avoids the agglomeration and deactivation of active components, and finally realizes the conversion of CO and NO under low temperature conditions. x Efficient collaborative purification.

[0085] In an alternative example of this embodiment, CO-NO x The catalytic bed uses FeMn / US-SSY catalyst, with active components accounting for 8%; in CO-NO x The catalytic bed is equipped with an injection device to supplement the reducing agent H2; the concentration of H2 in the reducing agent is 1-3%. x The molar ratio is 1.2:1. The catalyst adapts to the H2 reduction path through the synergistic effect of Fe and Mn, and is heated to 110 ° C and a space velocity of 2500 h -1 Under these conditions, CO and NO x The removal rates of H2 and H2+ were increased to 85% and 88%, respectively. Precise control of H2 concentration and molar ratio ensures that active sites fully participate in the reaction, avoiding efficiency fluctuations caused by excessive or insufficient reducing agent.

[0086] In an optional example of this embodiment, the high-energy particle action emission device includes at least a point power source 40 and a jet generator 30; the discharge range of the point power source 40 is 0-35kV, the jet velocity is 10-25m / s, and the pulse frequency is 0-2kHz. When a voltage of 25-35kV, a jet velocity of 10-15m / s, and a pulse frequency of 1kHz are used, the active material O- The generation efficiency of OH- or free radicals is significantly improved, triggering the catalytic reduction reaction of CO and NOx at 120-130°C, with removal rates reaching 96% and 92%, respectively. Through the coordinated control of voltage, jet velocity, and pulse frequency, high-energy particles are ensured to evenly cover the active sites of the catalyst and fully participate in the reaction.

[0087] In an optional example of this embodiment, a homogenizing device is provided above the multifunctional catalytic bed 20 to adjust the flue gas flow rate to 0.8m. By adjusting the pore distribution, the flue gas flow rate is precisely controlled to 0.8m / s to ensure that the flue gas passes evenly through the alkali metal adsorption layer and the subsequent catalytic bed. In a specific implementation, the homogenizing device stabilizes the flue gas flow rate at 0.8m / s, improves the flue gas distribution uniformity by 30%, eliminates the problem of uneven catalyst surface reaction caused by excessively high or low local flow rates, and controls the pressure drop within the design range of ≤50Pa. This homogenizing design provides stable gas-solid contact conditions for subsequent catalytic reactions by optimizing the matching of flow rate and porosity, significantly improving CO-NO x Catalytic reduction efficiency (removal rate increased by 15%) and system operation stability.

[0088] In an alternative embodiment of this embodiment, a heat conversion device 70 is installed in the flue 10 before the sintering flue gas reaches the standard exhaust outlet. This device 70 is a shell-and-tube heat exchanger or a plate heat exchanger for waste heat recovery. This design reduces external energy consumption by recycling heat, ensuring that the exhaust temperature meets environmental standards while improving the overall energy efficiency of the system.

[0089] The present invention also proposes that the catalyst regeneration is triggered based on the pressure of the multifunctional catalytic bed and the monitoring data of the catalyst; a high-energy particle emission mechanism is used to inject a regeneration combination gas into the catalyst bed; the regeneration combination gas will undergo an oxidation-reduction reaction through the in-situ regenerated catalyst to achieve a cleaning treatment of the catalyst surface. Specifically, the catalyst regeneration is dynamically triggered based on the pressure difference sensor data of the multifunctional catalytic bed 20 and the monitoring results of the catalyst surface attachment by the infrared spectrometer. During regeneration, the high-energy particle emission device sprays the regeneration combination gas (high-oxygen gas O2 ≥ 30% and reducing gas H2 3-5%, alternately injected in a volume ratio of 1:1) into the catalytic bed at a jet velocity of 15-20m / s and a voltage of 30-40kV, and decomposes the Cl deposited on the catalyst surface through the oxidation-reduction alternating reaction. - , alkali metal salts and carbon deposits. In the embodiment, when the pressure difference increases by 20% or more than the initial value, -When the concentration is ≥50ppm, the system automatically initiates the regeneration process and continues cleaning until the deposit removal rate is ≥98% and the catalyst activity recovery rate is ≥97%. This regeneration mechanism, through real-time data feedback and adaptive parameter adjustment, ensures efficient catalyst regeneration while reducing the regeneration frequency (dynamic cycle 18-30 hours), reducing energy consumption by 20%, and achieving long-term stable operation of the catalytic system.

[0090] In another optional embodiment of the present invention, the regenerated catalyst bed is composed of catalyst-V2O5-MoO3 / honeycomb ceramic; the active component of the catalyst accounts for 10-15%; the honeycomb ceramic pore density is 400-600 cpsi. Taking Example 3 as an example, the regenerated catalyst bed is composed of V2O5-MoO3 loaded on a honeycomb ceramic matrix, the active component ratio is precisely controlled to be 10-15%, and the honeycomb ceramic pore density is 400-600 cpsi. When the active component ratio is 12% and the pore density is 500 cpsi in the embodiment, the catalyst surface attachments (such as Cl - , alkali metal salts) removal rate ≥ 98%, activity recovery rate ≥ 97%. The optimization of the proportion of active ingredients (10-15%) avoids agglomeration and deactivation by balancing the density and dispersion of active sites; the high specific surface area design of the honeycomb ceramic pore density (400-600 cpsi) ensures full contact between the regeneration gas (high oxygen and reducing gas) and the catalyst, and the synergistic effect of the jet velocity and voltage (15-20m / s, 30-40kV) further enhances the cleaning effect. This regenerated catalyst bed structure significantly extends the service life of the catalyst to 1.5 times that of the original process, while reducing regeneration energy consumption by 12%, ensuring long-term efficient and stable operation of the system.

[0091] In another optional embodiment of the present invention, the regeneration gas combination consists of a high-oxygen gas O2 concentration ≥ 30% and a reducing gas H2 concentration 3-5%; the high-oxygen gas O2 and the reducing gas H2 are injected alternately; the gas ratio is 1:1. In a specific implementation, the high-oxygen gas (O2 ≥ 30%) is used to oxidize and decompose organic matter and inorganic salts on the catalyst surface, and then switched to reducing gas (H2 3-5%) to remove residual metal oxides, and the alternating cycle is repeated 2 times, each lasting 1 hour. This gas ratio and alternating injection strategy, through the synergistic effect of oxidation-reduction, can remove the attached substances (such as Cl - , alkali metal salts) removal rate ≥ 98%, and activity recovery rate ≥ 97%. The precise ratio of high oxygen to reducing gas (1:1) avoids secondary pollution or energy waste caused by excessive use of either gas, while also adapting to the removal needs of different pollutant components, ultimately achieving efficient catalyst regeneration and long-term stable system operation.

[0092] In another optional embodiment of the present invention, the high-energy particle emission mechanism, the jet parameters are: jet velocity 15-20m / s, pulse frequency 1.5-2.5kHz, voltage range 30-40kV. By optimizing the jet velocity, pulse frequency and voltage range, it is possible to more effectively remove the attachments on the catalyst surface, improve the regeneration efficiency and activity recovery rate of the catalyst. Taking Example 3 as an example, by this parameter combination (such as jet velocity 18m / s, pulse frequency 2kHz, voltage 35kV), high-energy particles (0 - , OH- or free radicals) are significantly improved in terms of generation density and distribution uniformity, and the Cl attached to the catalyst surface - The removal rate of pollutants such as alkali metal salts is ≥98%. The optimization of pulse frequency (1.5-2.5kHz) reduces energy loss through intermittent discharge. The coordinated regulation of jet velocity and voltage (15-20m / s, 30-40kV) ensures that the active material fully covers the catalyst surface, ultimately achieving a catalyst activity recovery rate of ≥97%, reducing regeneration energy consumption by 12%, and extending the catalyst service life to 1.5 times that of the original process.

[0093] In another optional embodiment of the present invention, the regeneration triggering condition is that the pressure difference sensor of the multifunctional catalytic bed 20 detects an increase in the bed pressure difference or the infrared spectrometer recognizes Cl - When the pressure difference is abnormal or Cl - After accumulation-triggered regeneration, alternating high-oxygen and reducing gas cleaning (O2 ≥ 30%, H2 3-5%) achieves a deposit removal rate of ≥ 98% and a catalyst activity recovery rate of ≥ 97%. This triggering mechanism dynamically controls regeneration timing through real-time data feedback, avoiding the resource waste or lag issues associated with fixed-cycle regeneration. It also precisely matches the catalyst's actual contamination status, reducing unnecessary regenerations (by 15%). This ensures efficient catalyst regeneration while extending its service life (from 8,000 hours to 12,000 hours) and reducing regeneration energy consumption by 20%.

[0094] In an optional example of this embodiment, the catalyst bed pressure difference and the catalyst bed pressure difference are monitored in real time by an intelligent monitoring system; the catalyst regeneration cycle is dynamically adjusted based on the monitoring data obtained. The intelligent monitoring system monitors the catalyst bed pressure difference in real time through a pressure difference sensor and analyzes the Cl content on the catalyst surface through an infrared spectrometer. - 、alkali metal salts and other attachments, dynamically adjust the regeneration cycle. When the pressure difference rises more than 20% of the initial value or Cl - When the concentration is ≥50ppm, the system automatically triggers the regeneration program; if there is no abnormal data, the regeneration interval is dynamically extended to 30 hours.

[0095] In an optional example, the regeneration trigger is when the pressure difference sensor detects an increase in the bed pressure difference or the infrared spectrometer identifies Cl - When alkali metal salts accumulate, the system automatically initiates the regeneration process. This trigger mechanism monitors the operating status of the multifunctional catalytic bed 20 in real time, responding promptly to the contamination of the catalyst surface and ensuring timely regeneration when needed.

[0096] In another optional embodiment of the present invention, the regeneration method adopts the following steps:

[0097] S1: Regeneration trigger:

[0098] S2: The first stage (oxidation cleaning): high-oxygen gas (O2 concentration 30%) is introduced with a jet velocity of 18 m / s and a voltage of 35 kV for 1 hour to oxidize and decompose organic matter and some inorganic salts.

[0099] S3: Second stage (reduction cleaning): switch to H2 (concentration 5%) and N2 mixed gas, jet speed 15m / s, voltage 30kV, last for 1 hour, reduction and removal of residual metal oxides.

[0100] S4. Regeneration process monitoring: Real-time monitoring of pressure difference changes and infrared spectrum data. If the removal rate of attachments does not reach 90%, the regeneration time will be automatically extended (by 0.5 hours each time, up to 2 times).

[0101] S5. Regeneration is completed and operation is resumed. The pressure difference is restored to within ±5% of the initial value. The system switches to normal processing mode and records the regeneration data for subsequent optimization.

[0102] The catalyst regeneration method proposed in the present invention adopts the following steps: S1 regeneration trigger: when the pressure difference sensor detects that the bed pressure difference increases or the infrared spectrometer identifies Cl - , when alkali metal salts accumulate, the system automatically starts the regeneration program. S2 The first stage (oxidation cleaning): introduce high-oxygen gas (O2 concentration 30%), the jet speed is 18m / s, the voltage is 35kV, and it lasts for 1 hour to oxidize and decompose organic matter and some inorganic salts. S3 The second stage (reduction cleaning): switch to a mixture of H2 (concentration 5%) and N2, the jet speed is 15m / s, the voltage is 30kV, and it lasts for 1 hour to reduce and remove residual metal oxides. S4 Regeneration process monitoring: real-time monitoring of pressure difference changes and infrared spectrum data. If the attachment removal rate does not reach 90%, the regeneration time will be automatically extended (0.5 hours each time, up to 2 times). S5 Regeneration completion and resumption of operation: When the pressure difference returns to within ±5% of the initial value, the system switches to normal processing mode and records the regeneration data for subsequent optimization.

[0103] In one optional example, the regeneration process is monitored in real time; pressure differential changes and infrared spectral data are monitored in real time. If the deposit removal rate does not reach 90%, the regeneration time is automatically extended by 0.5 hours each time, up to a maximum of two times. A pressure differential sensor is used to monitor the pressure differential changes of the multifunctional catalytic bed 20, and an infrared spectrometer is used to analyze the composition of deposits on the catalyst surface in real time. During the regeneration process, if the monitoring data shows that the deposit removal rate does not reach 90%, the system will automatically extend the regeneration time by 0.5 hours each time, up to a maximum of two times. This real-time monitoring and automatic adjustment mechanism ensures that deposits such as organic matter and inorganic salts on the catalyst surface are fully removed, thereby restoring the catalyst's activity and performance.

[0104] In another optional embodiment of the present invention, an intelligent monitoring system, a catalyst bed, an intelligent monitoring system, and a high-energy particle emission device are included. The intelligent monitoring system monitors the bed pressure difference in real time through a pressure difference sensor, and analyzes the Cl on the catalyst surface through an infrared spectrometer. - , alkali metal salt concentration, dynamic trigger regeneration program (pressure difference increases ≥ 20% or Cl - ≥50ppm automatically starts); the catalyst bed consists of a CO-NOx catalytic bed (V2O5-MoO3 / honeycomb ceramic, active ingredient 12%) and an alkali metal adsorption layer (γ-Al2O3 particles, filling height 500mm), which respectively achieve CO-NO x Synergistic removal (efficiency ≥ 92%) and heavy metal adsorption (efficiency ≥ 90%); high-energy particle emission device sprays active substances (O - , OH- or free radicals), reducing the activation energy of the reaction. In the embodiment, the system is at 120-130 ° C and a space velocity of 3000h -1 Under these conditions, the CO and NOx removal rates reached 96% and 92% respectively, the regeneration energy consumption was reduced by 20%, and the catalyst life was extended to 12,000 hours, achieving low-temperature and high-efficiency coordinated purification and intelligent operation and maintenance.

[0105] In an optional example of this embodiment, the intelligent monitoring system, monitoring the pressure difference change of the multifunctional catalytic bed 20, is composed of a pressure difference sensor, a real-time analysis of the composition of the attached matter on the catalyst surface, and an infrared spectrometer. The pressure difference sensor monitors the pressure difference change of the multifunctional catalytic bed 20 in real time, and the infrared spectrometer dynamically detects the Cl on the catalyst surface through spectral analysis technology. - 、Alkali metal salts and other attachments. When the pressure difference exceeds 20% of the initial value or Cl - When the concentration is ≥50ppm, the system automatically triggers the regeneration process. In the embodiment, the monitoring system makes the regeneration trigger accurately match the actual pollution state of the catalyst, reducing the regeneration frequency by 15% and the catalyst activity recovery rate by ≥97%.

[0106] In one optional example of this embodiment, the regeneration catalyst bed is constructed using a V2O5-MoO3 catalyst / honeycomb ceramic; the active component accounts for 10-15% of the catalyst; and the honeycomb ceramic has a pore density of 400-600 cpsi. Through optimized dispersion of the active component and the high specific surface area of ​​the honeycomb ceramic (pore density of 400-600 cpsi), sufficient contact between the high-oxygen / reducing gas and the catalyst is ensured during the regeneration process, achieving a deposit removal rate of ≥98% and an activity recovery rate of ≥97%, extending the catalyst life by 1.5 times that of the original process.

[0107] In an optional example of this embodiment, the high-energy particle emission device is composed of a point power source 40 and a jet generator 30. The point power source 40 provides a discharge voltage of 0-35kV, and the jet generator 30 is driven by a fan 50 to emit high-energy particles (O - , OH-, or free radicals) are sprayed onto the catalyst surface. In the examples, using a voltage of 25-35 kV and a jet velocity of 10-15 m / s significantly improved the efficiency of active material generation, achieving CO and NOx removal rates of 96% and 92%, respectively, at 120-130°C. This also reduces the activation energy required for the reaction and reduces external heating energy consumption by 38%.

[0108] The specific implementation process of the present invention is now described in detail with reference to the embodiments:

[0109] Example 1: Typical sintering flue gas treatment scenario

[0110] 1. Device configuration and parameters:

[0111] Flue gas conditions: initial temperature: 90°C;

[0112] Pollutant concentration: CO 8000mg / m 3 , NOx 400mg / m 3 , contains trace amounts of heavy metals (such as Pb, Zn) and dioxins (PCDD / Fs).

[0113] Heating device: Shell and tube heat exchanger, heating the flue gas to 120℃.

[0114] Homogenizing mechanism: It uses a porous plate flow equalizer with a porosity of 40% to ensure that the flue gas is evenly distributed to the catalytic bed.

[0115] Multifunctional catalyst bed: alkali metal adsorption layer: γ-Al2O3 particles (particle size 3–5 mm), filling height 500 mm.

[0116] Dioxin oxidation layer: V2O5-WO3 / TiO2 honeycomb ceramic catalyst (pore density 300 cpsi), thickness 300 mm.

[0117] CO-NOx catalytic bed: Catalyst: V2O5-MoO3 / honeycomb ceramic (active ingredient accounts for 12%), pore density 400 cpsi, filling height 800 mm.

[0118] High-energy particle generator: voltage range: 25–35 kV, jet velocity: 10–15 m / s, pulse frequency 1 kHz.

[0119] Heat exchanger waste heat recovery efficiency: ≥65%.

[0120] 2. Process

[0121] Flue gas pretreatment: After desulfurization (limestone-gypsum method) and dry dust removal (bag filter), the flue gas enters the heat exchanger and is heated to 120°C.

[0122] Homogenization and primary purification: The homogenization mechanism 60 adjusts the flue gas flow rate to 0.8 m / s so that the flue gas flows evenly through the multifunctional catalyst bed.

[0123] The alkali metal adsorption layer removes more than 90% of alkali metals such as K and Na; the dioxin oxidation layer oxidizes and degrades PCDD / Fs at 120°C (degradation rate ≥85%).

[0124] CO-NOx catalytic reduction: Flue gas enters the CO-NOx catalytic bed, and under the action of high-energy particles (30kV), CO reacts with NOx:

[0125]

[0126] The reaction temperature was maintained at 120–130°C and the space velocity was controlled at 3000 h -1 , residence time 2s.

[0127] Waste heat recovery and emission: After the reaction, the flue gas is recycled through the heat exchanger (the outlet temperature is reduced to 100°C), and the CO concentration in the purified flue gas is ≤300mg / m 3 , NOx concentration ≤ 40mg / m 3 , and meet emission standards.

[0128] Catalyst in-situ regeneration: Start the jet generator 30 times every 24 hours, spray high-energy particles at a speed of 12m / s to remove the deposits on the catalyst surface (such as Cl - , alkali metal salts), regeneration efficiency ≥95%.

[0129] Implementation effect:

[0130] Pollutant removal rates: CO 96%, NOx 92%, dioxin 88%. Energy consumption comparison: Compared with traditional SCR processes, heating energy consumption is reduced by 38% and total operating costs are reduced by 25%.

[0131] Parameter range summary:

[0132] Heating temperature: 100–140°C (preferably 120–130°C).

[0133] Energetic particle voltage: 10–50 kV (typically 25–35 kV).

[0134] Jet velocity: 5–20 m / s (typical 10–15 m / s).

[0135] The proportion of active ingredients in the catalyst: 5–15% (such as V2O5-MoO3 is 10–12%).

[0136] Airspeed range: 2000–5000 h -1 (Preferably 2500–3500h -1 ).

[0137] Example 2: Application of Supplementary Reductant in Low CO Concentration Scenario

[0138] 1. Special working conditions:

[0139] The CO concentration in the flue gas is insufficient (≤2000mg / m 3 ), reducing agent needs to be added.

[0140] 2. Improvement plan:

[0141] Reductant injection: Add a H2 injection device (H2 concentration 1–3%) in front of the CO-NOx catalyst bed.

[0142] Catalytic bed adjustment: FeMn / US-SSY catalyst (active ingredient proportion 8%) is used to adapt to the H2 reduction path.

[0143] 3. Process parameters:

[0144] Reaction temperature: 110°C, space velocity 2500h -1 , the molar ratio of H2 to NOx is 1.2:1.

[0145] 4. Implementation effect:

[0146] The NOx removal rate still reached 88%, the CO removal rate increased to 85%, and the system adaptability was significantly enhanced.

[0147] Example 3: Catalyst regeneration process

[0148] 1. Device configuration and parameters:

[0149] Regeneration process optimization conditions:

[0150] Catalyst type: V2O5-MoO3 / honeycomb ceramic (active ingredient accounts for 10-15%), pore density 400-600 cpsi.

[0151] Regeneration gas combination: high-oxygen gas (O2 concentration ≥ 30%) and reducing gas (H2 concentration 3-5%), injected alternately, ratio 1:1 (volume ratio).

[0152] Jet parameter optimization: jet velocity increased to 15-20m / s, pulse frequency adjusted to 1.5-2.5kHz, and voltage range extended to 30-40kV.

[0153] Intelligent monitoring system: Add a pressure difference sensor (to monitor the pressure difference changes of the catalyst bed) and an infrared spectrometer (to analyze the composition of the catalyst surface attachments in real time).

[0154] Regeneration cycle adjustment:

[0155] Dynamic regeneration strategy: Based on the pressure difference sensor data (regeneration is triggered when the pressure difference exceeds 20% of the initial value) and pollutant concentration feedback, the regeneration interval is adjusted to 18-30 hours (not fixed 24 hours).

[0156] 2. Process

[0157] Regeneration trigger: When the pressure difference sensor detects an increase in the bed pressure difference or the infrared spectrometer identifies Cl - , when alkali metal salts accumulate, the system automatically starts the regeneration program.

[0158] Regeneration gas injection:

[0159] The first stage (oxidation cleaning): introduce high-oxygen gas (O2 concentration 30%), with a jet speed of 18m / s and a voltage of 35kV for 1 hour to oxidize and decompose organic matter and some inorganic salts.

[0160] The second stage (reduction cleaning): switch to a mixture of H2 (concentration 5%) and N2, with a jet speed of 15m / s and a voltage of 30kV for 1 hour to reduce and remove residual metal oxides.

[0161] Regeneration process monitoring:

[0162] Real-time monitoring of pressure difference changes and infrared spectrum data. If the removal rate of deposits does not reach 90%, the regeneration time will be automatically extended (by 0.5 hours each time, up to 2 times).

[0163] Regeneration completed and resumed operation:

[0164] When the pressure difference returns to within ±5% of the initial value, the system switches to normal processing mode and records the regeneration data for subsequent optimization.

[0165] 3. Implementation Effect

[0166] Improved regeneration efficiency:

[0167] The removal rate of deposits on the catalyst surface is ≥98% (the original process is 95%), and the residual amount of alkali metal salt is <0.5 mg / g.

[0168] The catalyst activity recovery rate is ≥97%, and the service life is extended to 1.5 times that of the original process (the original service life is about 8,000 hours).

[0169] Energy consumption optimization:

[0170] Through dynamic regeneration strategy, regeneration frequency is reduced by 15% and total energy consumption is reduced by 20%.

[0171] The coordinated optimization of jet velocity and voltage reduces the unit regeneration energy consumption by 12%.

[0172] Intelligent advantages:

[0173] Reduce manual intervention, the regeneration process is fully automatically controlled, and the risk of misoperation is reduced by 80%.

[0174] Real-time data feedback supports adaptive adjustment of process parameters, allowing the system to adapt to different flue gas load fluctuation scenarios.

[0175] 4. Parameter range summary

[0176] Regeneration gas ratio: O2:H2=1:1 (volume ratio), O2 concentration ≥30%, H2 concentration 3-5%.

[0177] Jet parameters: velocity 15-20 m / s, voltage 30-40 kV, pulse frequency 1.5-2.5 kHz.

[0178] Regeneration trigger threshold: bed pressure difference change ≥ 20% or Cl - Concentration ≥50ppm.

[0179] Regeneration cycle: Dynamic adjustment (18-30 hours), average regeneration time shortened to 1.8 hours / time.

[0180] Compared with the existing technology, the technical solution proposed in this application can bring the following beneficial effects:

[0181] 1. It can achieve simultaneous removal of CO and NOx.

[0182] 2. Compared with ammonia-based denitrification, using CO in flue gas as a reducing agent to catalytically reduce NO reduces material costs, reduces the safety issues of using ammonia to a certain extent, and also reduces environmental pollution caused by excessive CO emission concentrations.

[0183] 3. By utilizing the high-voltage electrode discharge effect, the heating device can be effectively replaced to achieve the heating effect, reducing energy consumption, space occupation and working costs.

[0184] The detailed explanations of the above-mentioned embodiments are intended only to explain the present invention so as to facilitate a better understanding of the present invention. However, these descriptions cannot be interpreted as limiting the present invention for any reason. In particular, the various features described in different embodiments may also be arbitrarily combined with each other to form other embodiments. Unless otherwise clearly described, these features should be understood to be applicable to any embodiment and are not limited to the described embodiments.

Claims

1. A method for collaboratively treating multiple pollutants in sintering flue gas, characterized in that: The sintering flue gas is desulfurized and dusted and then treated in a multifunctional catalytic bed layer, wherein the multifunctional catalytic bed layer comprises at least one layer of CO-NO x Catalytic bed for the CO-NO x Redox treatment; During the treatment process, CO is used to convert NO into x The catalytic reduction reaction generates N2 and CO2; the treated sintering flue gas meets emission standards.

2. The method for collaboratively treating multiple pollutants in sintering flue gas according to claim 1, characterized in that: The multifunctional catalytic bed also includes an alkali metal adsorption layer for adsorbing heavy metals in the flue gas.

3. The method for collaboratively treating multiple pollutants in sintering flue gas according to claim 1, characterized in that: The multifunctional catalytic bed also includes a dioxin oxidation layer, which is a honeycomb ceramic catalyst layer using V2O5-WO3 / TiO2 molecules and transition metals as carriers.

4. The method for collaboratively treating multiple pollutants in sintering flue gas according to claim 1, characterized in that: The CO-NO x The catalytic bed comprises a honeycomb ceramic molecular sieve composed of a catalyst and a transition metal.

5. The method for collaboratively treating multiple pollutants in sintering flue gas according to claim 4, characterized in that: When the CO concentration in the flue gas is ≤2000mg / m 3 When the CO-NO x The catalyst used in the catalytic bed is FeMn / US-SSY molecular catalyst.

6. The method for collaboratively treating multiple pollutants in sintering flue gas according to claim 5, characterized in that: In the CO-NO x H2 or CH4 is injected before the catalytic bed as a supplementary reducing agent.

7. The method for co-processing multiple pollutants in sintering flue gas according to claim 1, characterized in that: The mechanism of high-energy particles is that the active substances O- or OH- generated by discharge react with CO and NO x A bond breaking reaction occurs.

8. The method for co-processing multiple pollutants in sintering flue gas according to claim 7, characterized in that: The high-energy particle action mechanism uses a point power source to apply voltage to the jet generator, and through the action of the fan, the high-energy particles are sprayed into the CO-NO x The surface of the catalyst bed undergoes a catalytic reduction reaction with the sintering flue gas.

9. The method for co-processing multiple pollutants in sintering flue gas according to claim 8, characterized in that: The high-energy particle action mechanism also utilizes an in-situ regeneration mechanism to regenerate the catalyst in situ after the catalytic reduction reaction.

10. The method for co-processing multiple pollutants in sintering flue gas according to claim 8, characterized in that: The catalyst in situ regeneration includes: starting the jet generator once every preset time, alternately using high-oxygen gas and reducing gas H2 as gas sources, spraying high-energy particles at a preset speed, repeatedly cleaning for a preset cleaning time, and cycling for a preset number of times to remove the CO-NO x Substances attached to the surface of the catalyst in the catalytic bed.

11. The method for co-processing multiple pollutants in sintering flue gas according to any one of claims 1 to 10, characterized in that: The method for collaboratively treating multiple pollutants in sintering flue gas comprises: Step S1, pre-treating the sintering flue gas, wherein the pre-treatment includes desulfurization and dust removal; Step S2, homogenizing and pre-purifying the pretreated sintering flue gas; Step S3, performing multifunctional catalytic treatment on the sintering flue gas after primary purification, the multifunctional catalytic treatment comprising: Step S3.1, alkali metal adsorption treatment to remove alkali metals in the sintering flue gas; Step S3.2, dioxin oxidation treatment, oxidative degradation of PCDD / Fs in the sintering flue gas; Step S3.3, CO-NO x Catalytic reduction reaction treatment, injecting high-energy particles into the sintering flue gas; Step S4, discharging the treated sintering flue gas; Step S5, recovering waste heat from the sintering flue gas; Step S6: performing in-situ regeneration treatment on the catalyst in the multifunctional catalytic treatment.

12. The method for co-processing multiple pollutants in sintering flue gas according to any one of claims 1 to 10, characterized in that: The method for collaboratively treating multiple pollutants in sintering flue gas comprises: Step S1, pre-treating the sintering flue gas, wherein the pre-treatment includes desulfurization, dust removal and injection of a reducing agent; Step S2, homogenizing and pre-purifying the pretreated sintering flue gas; Step S3, performing multifunctional catalytic treatment on the sintering flue gas after primary purification, the multifunctional catalytic treatment comprising: Step S3.1, alkali metal adsorption treatment to remove more than 90% of the alkali metals in the sintering flue gas; Step S3.2, dioxin oxidation treatment, oxidatively degrading PCDD / Fs in the sintering flue gas, with a degradation rate of ≥85%; Step S3.3, CO-NO x Catalytic reduction reaction treatment, injecting high-energy particles into the sintering flue gas; Step S4, discharging the treated sintering flue gas; Step S5, recovering waste heat from the sintering flue gas; Step S6: performing in-situ regeneration treatment on the catalyst in the multifunctional catalytic treatment.

13. A system for coordinating the treatment of multiple pollutants in sintering flue gas, characterized in that: The system for coordinating the treatment of multiple pollutants in sintering flue gas comprises a flue and a multifunctional catalytic bed connected to the flue, wherein the multifunctional catalytic bed comprises at least one layer of CO-NO x Catalytic bed, the CO-NO x The catalytic bed is used to remove CO-NO in sintering flue gas. x Perform redox treatment; The system for coordinating the treatment of multiple pollutants in sintering flue gas also includes a high-energy particle emission device and an emission outlet. The high-energy particle emission device generates active substances O- or OH- or free radicals through discharge and injects them into the CO-NO x The catalytic bed layer, the emission outlet is connected to the multifunctional catalytic bed layer and is used to emit the treated sintering flue gas.

14. The system for coordinating the treatment of multiple pollutants in sintering flue gas according to claim 13, characterized in that: The high-energy particle emission device at least includes a point power source and a jet generator.

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