In-situ regeneration system and method for synergistic removal of catalyst for flue gas purification

Abstract

The invention discloses an in-situ regeneration system and method for synergistically removing a catalyst for flue gas purification, the system comprises a purification device, a regeneration gas spraying pipeline and a flue gas inlet channel, the purification device is connected to the flue gas inlet channel and is used for purifying flue gas; and the regenerated gas spraying pipeline is connected to the flue gas inlet channel and is used for sequentially spraying reducing gas and oxidizing gas into the purification device. By adopting the reducing gas and the oxidizing gas, the catalyst in the purification device can be regenerated and cleaned, sulfate and deposited carbon on the surface of the catalyst can be effectively removed, and the activity of the catalyst is recovered; moreover, in the regeneration cleaning process, the catalyst does not need to be taken out of the purification device, so that the operation complexity is reduced, and regeneration cleaning and maintenance are convenient.

Description

Technical Field

[0001] The present invention relates to the field of environmental protection technology, and more specifically, to an in-situ regeneration system for a synergistic removal catalyst for flue gas purification, and also to an in-situ regeneration method for a synergistic removal catalyst for flue gas purification using the system. Background Art

[0002] As a key pillar of the national economy, the steel industry plays an irreplaceable role in my country's industrialization. However, flue gas pollution from steel production is becoming increasingly serious and has become a major source of air pollution in my country. Sintering machine flue gas contains large amounts of carbon monoxide (CO), nitrogen oxides (NOx), and sulfides (SOx and COS). These pollutants not only pose serious risks to the environment and ecosystems, but also pose a threat to human health.

[0003] With increasingly stringent environmental regulations, the steel industry faces immense pressure to reduce emissions. Currently, steel flue gas purification technologies primarily include wet spraying, selective catalytic reduction (NH3-SCR), and catalytic oxidation. Catalytic purification, due to its high efficiency, stability, and environmental friendliness, has become the mainstream technology for steel flue gas treatment. The core of catalytic purification technology is the catalyst, whose performance directly determines the effectiveness of flue gas purification. However, steel flue gas has a complex composition, containing large amounts of sulfides and particulate matter, which can easily poison and deactivate the catalyst, seriously affecting its long-term stable operation.

[0004] Currently, when a catalyst becomes poisoned and deactivated after a period of use, the catalytic device needs to be disassembled and the catalyst replaced with a new active catalyst to maintain the catalytic purification effect on the flue gas. This not only makes the equipment operation cumbersome, but also incurs high catalyst costs.

[0005] Therefore, a new solution needs to be proposed to solve this problem. Summary of the Invention

[0006] The object of the present invention is to overcome the above-mentioned deficiencies of the prior art and to provide an in-situ regeneration system and method for synergistically removing a catalyst for flue gas purification.

[0007] In order to achieve the above object, the present invention adopts the following technical solutions:

[0008] An in-situ regeneration system for synergistically removing catalysts for flue gas purification comprises: a purification device, a regeneration gas spray pipeline and a flue gas inlet channel, wherein the purification device is connected to the flue gas inlet channel for purifying flue gas; the regeneration gas spray pipeline is connected to the flue gas inlet channel, and is used to spray reducing gas and oxidizing gas into the purification device in sequence.

[0009] The present invention is further configured such that the reducing gas is CO and the oxidizing gas is NO2.

[0010] The present invention is further configured to further include: a regeneration controller, a reducing gas source and an oxidizing gas source, wherein the regeneration controller can control the reducing gas source and the oxidizing gas source to be connected to the regeneration gas spray pipeline in sequence.

[0011] The present invention is further configured such that the regeneration controller is a three-way valve structure, which is connected to the reducing gas source, the oxidizing gas source and the regeneration gas spray pipeline respectively.

[0012] The present invention is further configured such that a first pollutant sensor is installed at the input port of the purification device, and a second pollutant sensor is installed at the output port of the purification device;

[0013] When the catalyst in the purification device is in a deactivated state, the regeneration controller starts the regeneration mode and introduces reducing gas and oxidizing gas into the regeneration gas spray pipeline in sequence; first, the reducing gas is introduced to decompose sulfate, and then the oxidizing gas is introduced to oxidize carbon deposits.

[0014] The present invention is further configured such that the purification device includes a housing, wherein two ends of the housing respectively have an input port and an output port, a catalytic module is installed inside the housing, and the catalytic module is provided with a plurality of catalytic channels, wherein two ends of the catalytic channels respectively face the input port and the output port, the catalytic channels are filled with catalysts, and the catalytic channels are arranged in an annular array;

[0015] The input port is equipped with a first flow guide, and the output port is equipped with a second flow guide. The first flow guide and the second flow guide are coaxially rotatably installed in the housing.

[0016] The deflector 1 includes a cover plate 1, and the deflector 2 includes a cover plate 2. The cover plate 1 and the cover plate 2 can simultaneously cover the two ends of two adjacent catalytic channels. The cover plate 1 includes an input part and an output part. The input part can spray gas toward the first catalytic channel, and the output part can allow the gas of the second catalytic channel to flow out; the cover plate 2 is provided with a connecting groove, and the connecting groove can connect the two catalytic channels.

[0017] The present invention is further configured such that the catalytic module includes a central tube and a plurality of partition plates, wherein the partition plates are distributed in an annular array outside the central tube, and adjacent partition plates are separated to form the catalytic channels.

[0018] The present invention is further configured such that a rotating shaft is installed at the center of the shell; the deflector 1 also includes a rotating sleeve 1, which is mounted on the outer periphery of the rotating shaft and can rotate synchronously with the rotating shaft, and the cover plate 1 is fixedly mounted on the outer periphery of the rotating sleeve 1; the deflector 2 also includes a rotating sleeve 2, which is mounted on the outer periphery of the rotating shaft and can rotate synchronously with the rotating shaft, and the cover plate 2 is fixedly mounted on the outer periphery of the rotating sleeve 2.

[0019] The present invention is further configured such that the deflector 1 also includes a rotating support ring 1, the rotating support ring 1 is rotatably connected to the inner circumference of the shell, and the rotating support ring 1 is fixedly connected to the rotating sleeve 1 via a support frame 1; the deflector 2 also includes a rotating support ring 2, the rotating support ring 2 is rotatably connected to the inner circumference of the shell, and the rotating support ring 2 is fixedly connected to the rotating sleeve 2 via a support frame 2.

[0020] The present invention is further configured such that an air jet chamber is provided inside the first cover plate, a nozzle is provided on the input portion facing the catalytic channel, and the nozzle is connected to the air jet chamber; an air guide channel is provided inside the first rotating sleeve, one end of the air guide channel is connected to the air jet chamber, and the other end extends away from the first cover plate;

[0021] A rotary joint is installed on the outer periphery of the rotary sleeve 1, and the air guide channel is connected to the regeneration gas spray pipeline through the rotary joint.

[0022] The present invention is further configured such that an input side grille is installed at the input port of the shell, and an output side grille is installed at the output port of the shell.

[0023] The present invention further provides that the end of the rotating shaft extends outside the catalytic module and is connected to a rotary actuator, which drives the rotating shaft to rotate. Specifically, the rotary actuator can be a stepper motor or a servo motor, which drives the rotating shaft to rotate, and each rotation adjustment can ensure that the first and second cover plates are properly positioned over the ports of the two catalytic channels, thereby covering the ports of the two catalytic channels.

[0024] The present invention also provides an in-situ regeneration method for a synergistic removal catalyst for flue gas purification, which uses the above-mentioned in-situ regeneration system for the synergistic removal catalyst for flue gas purification; the method comprises the following steps:

[0025] (1) When the concentration of flue gas pollutants at the output port of the purification device reaches the preset emission limit, the regeneration mode is triggered;

[0026] (2) CO gas at a temperature of 350-650°C is introduced into the purification device to decompose the sulfate on the catalyst surface through a reduction reaction;

[0027] (3) NO2 gas is introduced into the purification device, and the carbon deposits on the surface of the oxidation catalyst are converted to CO2;

[0028] (4) Repeat switching steps (3) and (4) to purify the catalyst in the purification device.

[0029] The present invention is further configured such that the flow rates of the CO gas and NO2 gas are monitored by a flow meter, and the input amounts are controlled by a regeneration controller.

[0030] The present invention is further configured to obtain a flue gas purification rate of the purification device by comparing the flue gas pollutant concentrations at the input port and the output port of the purification device.

[0031] The present invention is further configured such that, in step (2), the CO gas is introduced at a space velocity of 1000-10000 h -1 , CO concentration is 10-50%; in step (3), the introduction space velocity of NO2 gas is 1000-10000 h -1 , NO2 gas is 1-10%.

[0032] The present invention is further configured such that the NO2 gas is generated by the reaction of NH3 and O2 in a catalytic oxidation device, the reaction temperature is 400-600°C, and the catalyst is Pt / MoO3-CeO2.

[0033] The CO gas comes from the self-produced CO in the steel sintering flue gas, and the NO2 precursor NH3 comes from the decomposition of liquid ammonia, ammonia water or urea in the steel plant's denitrification system.

[0034] In summary, the present invention has the following beneficial effects:

[0035] By using reducing and oxidizing gases, the catalyst in the purification device can be regenerated and cleaned, effectively removing sulfate and carbon deposits on the catalyst surface and restoring the catalyst's activity. Moreover, during the regeneration and cleaning process, there is no need to remove the catalyst from the purification device, reducing operational complexity and facilitating regeneration, cleaning, and maintenance.

[0036] By using CO and NH3 contained in steel flue gas or produced by the steel plant as regeneration agents, the two are circulated and reacted to reduce the use of other chemical reagents and the risk of secondary pollution. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Figure 1 This is a schematic structural diagram of an in-situ regeneration system for collaborative removal of catalysts for flue gas purification according to the present invention;

[0038] Figure 2 is a three-dimensional cross-sectional view of the purification device of the present invention;

[0039] Figure 3 is a cross-sectional view of the purification device of the present invention;

[0040] Figure 4 A perspective view of a flow deflector 1 in the present invention;

[0041] Figure 5 is a cross-sectional view of the deflector 1 in the present invention;

[0042] Figure 6 is a three-dimensional diagram of the second deflector of the present invention;

[0043] Figure 7 This is a first perspective perspective view of the deflector 1, deflector 2 and catalytic module in the present invention;

[0044] Figure 8 This is a second perspective stereoscopic image of the deflector 1, deflector 2 and catalytic module in the present invention.

[0045] Figure numerals: purification device 100; pollutant sensor 1 200; pollutant sensor 2 300; ammonia nozzle 400; regeneration gas spray pipeline 500; flue gas inlet channel 600; shell 1; input port 101; output port 102; input side grid 2; output side grid 3; catalytic module 4; central tube 41; partition plate 42; catalytic channel 43; first catalytic channel 431; second catalytic channel 432; deflector 1 5; rotating sleeve 1 51; rotating support ring 1 52; support frame 1 53; cover plate 1 54; input part 55; output part 56; overflow notch 561; nozzle 57; jet chamber 58; air guide channel 59; deflector 2 6; rotating sleeve 2 61; rotating support ring 2 62; support frame 2 63; cover plate 2 64; connecting groove 65; rotating shaft 7; rotary joint 8. DETAILED DESCRIPTION

[0046] The following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0047] The present invention discloses an in-situ regeneration system for synergistically removing catalysts for flue gas purification, comprising: a purification device 100, a regeneration gas spray pipeline 500 and a flue gas inlet channel 600, wherein the purification device 100 is connected to the flue gas inlet channel 600 for purifying flue gas; the regeneration gas spray pipeline 500 is connected to the flue gas inlet channel 600, and the regeneration gas spray pipeline 500 is used to spray reducing gas and oxidizing gas into the purification device 100 in sequence.

[0048] The reducing gas is CO, which comes from the self-produced CO in the steel sintering flue gas. The NO2 precursor NH3 comes from the decomposition of liquid ammonia, ammonia water or urea in the steel plant's denitrification system. The oxidizing gas is NO2, which is generated by the reaction of NH3 and O2 in a catalytic oxidation device at a reaction temperature of 400-600℃ and a catalyst of Pt / MoO3-CeO2. The preparation process of CO gas and NO2 gas can be referred to Figure 1 The process is shown in the following figure.

[0049] The in-situ regeneration system also includes a regeneration controller, a reducing gas source, and an oxidizing gas source. The regeneration controller controls the reducing gas source and the oxidizing gas source to sequentially connect to the regeneration gas spray pipeline 500. The flow rates of CO and NO2 are monitored by flow meters, with the regeneration controller controlling the input amounts and adjusting other flow conditions of the two gases as needed.

[0050] Specifically, the regeneration controller is a three-way valve structure, which connects the reducing gas source, the oxidizing gas source and the regeneration gas spray pipeline 500 respectively, and can control the connection of the regeneration gas spray pipeline 500 to the reducing gas source and the oxidizing gas source to realize other options.

[0051] In this in-situ regeneration system, a pollutant sensor 1 200 is installed at the input port 101 of the purification device 100, and a pollutant sensor 2 300 is installed at the output port 102 of the purification device 100; by comparing the flue gas pollutant concentrations at the input port 101 and the output port 102 of the purification device 100, the flue gas purification rate of the purification device 100 can be obtained.

[0052] When the catalyst within the purification device 100 becomes deactivated, the regeneration controller activates regeneration mode. This is typically triggered when the flue gas pollutant concentration at the output port 102 of the purification device 100 reaches a preset emission limit. During regeneration mode, reducing gas and oxidizing gas are sequentially introduced into the regeneration gas spray line 500; the reducing gas is introduced first to decompose sulfates, followed by the oxidizing gas to oxidize carbon deposits.

[0053] The present invention also discloses an in-situ regeneration method for a synergistic removal catalyst for flue gas purification, which uses the above-mentioned in-situ regeneration system for the synergistic removal catalyst for flue gas purification; the method comprises the following steps:

[0054] (1) When the concentration of flue gas pollutants at the output port 102 of the purification device 100 reaches a preset emission limit, the regeneration mode is triggered;

[0055] (2) CO gas at a temperature of 350-650 °C is introduced into the purification device 100 to decompose the sulfate on the catalyst surface through a reduction reaction; the CO gas is introduced at a space velocity of 1000-10000 h -1, CO concentration is 10-50%; the concentration of the gas in the embodiment refers to the volume concentration;

[0056] (3) NO2 gas is introduced into the purification device 100, and the carbon deposits on the surface of the oxidation catalyst are CO2; the introduction space velocity of NO2 gas is 1000-10000 h -1 , NO2 gas is 1-10%.

[0057] (4) Repeat the switching between step (3) and step (4) to purify the catalyst in the purification device 100.

[0058] The following are specific embodiments of the regeneration method of the present invention, which are described separately according to different formulation systems of the catalyst in the purification device 100.

[0059] Example 1: Verification of synergistic regeneration effect under typical working conditions

[0060] 1. Catalyst formulation system in purification device 100

[0061] Synergistic removal catalyst: adopts a double-layer composite structure, the bottom layer is V2O5-WO3 / TiO2 (vanadium tungsten titanium system, denitrification functional layer), the surface layer is Pt / Al2O3 (platinum-based alumina, CO catalytic oxidation functional layer), the carrier is honeycomb ceramic, and the pore density is 300 cpsi.

[0062] Active component loading: V2O5 (1.5 wt%), WO3 (5 wt%), Pt (0.1 wt%).

[0063] 2. Regeneration process parameters

[0064] Reduction stage: introduce steel sintering flue gas to produce CO, concentration 30%, temperature 450℃, space velocity 5000 h -1 , lasting 1 hour.

[0065] Oxidation stage: NO2 (concentration 5%) generated by catalytic oxidation of NH3 and O2 was introduced, temperature 500℃, space velocity 5000 h -1 , lasting 1 hour.

[0066] Control mode: Closed-loop control, regeneration trigger threshold is output port 102 CO concentration > 10 ppm or denitrification efficiency < 85%.

[0067] 3. Activity data before and after regeneration

[0068]

[0069] 4. Effect Analysis

[0070] After regeneration, the catalyst activity recovered to more than 95% of the initial value. The DTA-TG table confirmed that the carbon deposit removal rate was >85%, and the ICP-MS confirmed that the sulfate decomposition rate was >90%, meeting the steel flue gas emission standards (CO <50 ppm, NOx <100 ppm).

[0071] Example 2: Low-temperature regeneration optimization and catalyst formulation improvement

[0072] 1. Catalyst formulation system in purification device 100

[0073] Synergistic removal catalyst: adopts a dual-functional single-layer structure, the carrier is a TiO2-SiO2 composite carrier, and the active components are Cu-Mn oxide (CO oxidation) and Fe-ZSM-5 molecular sieve (denitrification).

[0074] Active component loading: CuO (3 wt%), MnO2 (5 wt%), Fe-ZSM-5 (10 wt%).

[0075] 2. Regeneration process parameters

[0076] Reduction stage: external supplementary CO (concentration 20%), temperature 380 °C, space velocity 3000 h -1 , lasting 1.5 hours.

[0077] Oxidation stage: NO2 (concentration 3%), temperature 420℃, space velocity 3000 h -1 , lasting 1 hour.

[0078] Control method: Regeneration is triggered based on the NH3 concentration at output port 102 (>10 ppm).

[0079] 3. Activity data before and after regeneration

[0080]

[0081] 4. Effect Analysis

[0082] It can recover over 80% of its activity even at low-temperature regeneration (<400°C), making it suitable for low-energy steel mills. The composite carrier improves sulfur resistance, with residual sulfate levels below 5% after regeneration.

[0083] Example 3: Regeneration enhancement under high sulfur flue gas conditions

[0084] 1. Catalyst formulation system in purification device 100

[0085] Synergistic removal catalyst: adopts sulfur-resistant formula, the carrier is ZrO2-modified Al2O3, and the active components are Pd-CeO2 (CO oxidation) and Mo-VW / TiO2 (denitrification).

[0086] Active component loading: Pd (0.2 wt%), CeO2 (10 wt%), MoO3 (2 wt%), V2O5 (1 wt%), WO3 (5wt%).

[0087] 2. Regeneration process parameters

[0088] Reduction stage: high concentration CO (50%), temperature 600 °C, space velocity 8000 h -1 , lasting 0.5 hours.

[0089] Oxidation stage: NO2 (concentration 10%), temperature 650℃, space velocity 8000 h -1 , lasting 1 hour.

[0090] Control method: Regeneration is triggered based on the NO2 concentration at output port 102 (>200 ppm).

[0091] 3. Activity data before and after regeneration

[0092]

[0093] 4. Effect Analysis

[0094] In high-sulfur flue gas (SO2>500 ppm), the ZrO2 carrier inhibits the formation of sulfate, and the sulfur resistance of the catalyst is improved by 30% after regeneration, making it suitable for high-sulfur sintering flue gas scenarios.

[0095] Example 4: Fully automatic closed-loop control and process integration

[0096] 1. Catalyst formulation system in purification device 100

[0097] Synergistic removal catalyst: modular design, CO oxidation layer (Pt-Rh / Al2O3) and denitrification layer (Cu-SAPO-34 molecular sieve) are assembled separately.

[0098] Active component loading: Pt (0.15 wt%), Rh (0.05 wt%), Cu-SAPO-34 (8 wt%).

[0099] 2. Regeneration process parameters

[0100] Reduction stage: CO (concentration 40%), temperature 550°C, space velocity 10000 h -1 , lasting 0.5 hours.

[0101] Oxidation stage: NO2 (concentration 8%), temperature 600℃, space velocity 10000 h -1 , lasting 0.5 hours.

[0102] Control mode: Fully automatic closed-loop control, through monitoring the input port 101 and the output port 102, integrated DCS system, real-time adjustment of gas flow and temperature.

[0103] 3. Activity data before and after regeneration

[0104]

[0105] 4. Effect Analysis

[0106] Under fully automatic control, the regeneration cycle is shortened to 1 hour, the catalyst life is extended to 12 months (6 months with traditional methods), and the overall operating cost is reduced by 40%.

[0107] Comparative Example 1:

[0108] The difference between this comparative example and Example 1 is that:

[0109] 2. The regeneration process parameters are changed to:

[0110] Reduction stage: N2, temperature 450℃, space velocity 5000 h -1 , lasting 1 hour.

[0111] Oxidation stage: N2, temperature 500℃, space velocity 5000 h -1 , lasting 1 hour.

[0112] 3. Activity data before and after regeneration

[0113]

[0114] 4. Effect Analysis

[0115] The catalyst activity recovery ability after regeneration was poor. The carbon deposit removal rate was confirmed to be <10% by DTA-TG chart, and the sulfate decomposition rate was confirmed to be <15% by ICP-MS.

[0116] Comparative Example 2:

[0117] The difference between this comparative example and Example 1 is that:

[0118] 2. The regeneration process parameters are changed to:

[0119] Reduction stage: air is introduced, temperature is 450℃, air velocity is 5000 h -1 , lasting 1 hour.

[0120] Oxidation stage: air is introduced, temperature is 500℃, space velocity is 5000 h -1 , lasting 1 hour.

[0121] 3. Activity data before and after regeneration

[0122]

[0123] 4. Effect Analysis

[0124] The catalyst activity recovery ability after regeneration was poor. The carbon deposit removal rate was confirmed to be <12% by DTA-TG chart, and the sulfate decomposition rate was confirmed to be <8% by ICP-MS.

[0125] Comparative Example 3:

[0126] The difference between this comparative example and Example 2 is that:

[0127] 2. The regeneration process parameters are changed to:

[0128] Reduction stage: N2, temperature 380℃, space velocity 3000 h -1 , lasting 1.5 hours.

[0129] Oxidation stage: N2, temperature 420℃, space velocity 3000 h -1 , lasting 1 hour.

[0130] 3. Activity data before and after regeneration

[0131]

[0132] 4. Effect Analysis

[0133] Nitrogen regeneration effect is very poor, with basically no regeneration ability

[0134] Comparative Example 4:

[0135] The difference between this comparative example and Example 2 is that:

[0136] 2. The regeneration process parameters are changed to:

[0137] Reduction stage: air is introduced, temperature is 380℃, air velocity is 3000 h -1 , lasting 1.5 hours.

[0138] Oxidation stage: air is introduced, temperature is 420℃, air velocity is 3000 h -1 , lasting 1 hour.

[0139] 3. Activity data before and after regeneration

[0140]

[0141] 4. Effect Analysis

[0142] Compared with nitrogen, air has a worse regeneration effect.

[0143] Comparative Example 5:

[0144] The difference between this comparative example and Example 3 is that:

[0145] 2. The regeneration process parameters are changed to:

[0146] Reduction stage: N2, temperature 600℃, space velocity 8000 h -1 , lasting 0.5 hours.

[0147] Oxidation stage: N2, temperature 650℃, space velocity 8000 h -1 , lasting 1 hour.

[0148] 3. Activity data before and after regeneration

[0149]

[0150] 4. Effect Analysis

[0151] Nitrogen regeneration is poor and has little effect.

[0152] Comparative Example 6:

[0153] The difference between this comparative example and Example 3 is that:

[0154] 2. The regeneration process parameters are changed to:

[0155] Reduction stage: air is introduced, temperature is 600℃, air velocity is 8000 h -1 , lasting 0.5 hours.

[0156] Oxidation stage: air is introduced, temperature is 650℃, space velocity is 8000 h -1 , lasting 1 hour.

[0157] 3. Activity data before and after regeneration

[0158]

[0159] 4. Effect Analysis

[0160] Air regeneration has little effect.

[0161] Comparative Example 7:

[0162] The difference between this comparative example and Example 4 is that:

[0163] 2. The regeneration process parameters are changed to:

[0164] Reduction stage: N2 flow, temperature 550℃, space velocity 10000 h -1 , lasting 0.5 hours.

[0165] Oxidation stage: N2, temperature 600℃, space velocity 10000 h -1 , lasting 0.5 hours.

[0166] 3. Activity data before and after regeneration

[0167]

[0168] 4. Effect Analysis

[0169] Basically no effect.

[0170] Comparative Example 8:

[0171] The difference between this comparative example and Example 4 is that:

[0172] 2. The regeneration process parameters are changed to:

[0173] Reduction stage: air is introduced, temperature is 550℃, air velocity is 10000 h -1 , lasting 0.5 hours.

[0174] Oxidation stage: air is introduced, temperature is 600℃, space velocity is 10000 h -1 , lasting 0.5 hours.

[0175] 3. Activity data before and after regeneration

[0176]

[0177] 4. Effect Analysis

[0178] Basically no effect.

[0179] This embodiment also discloses an in-situ regeneration system for collaborative removal of catalyst for flue gas purification. Figures 2-8 The structure of the purification device 100 will be further described in detail.

[0180] Reference Figure 2 、 Figure 3 As shown, the purification device 100 includes a housing 1, with an input port 101 and an output port 102 at each end. A catalytic module 4 is installed inside the housing 1, and the catalytic module 4 is provided with a plurality of catalytic channels 43. The two ends of the catalytic channels 43 face the input port 101 and the output port 102, respectively. The catalytic channels 43 are filled with a catalyst, which can come into contact with the flue gas flowing through the catalytic channels 43 to purify the pollutants in the flue gas.

[0181] The catalytic channels 43 are arranged in a circular array. The catalytic module 4 includes a central tube 41 and a plurality of partition plates 42. The partition plates 42 are arranged in a circular array outside the central tube 41, with the partition plates 42 being located adjacent to each other to form the catalytic channels 43. The partition plates 42 form a structure that radiates from the center to the periphery.

[0182] The input port 101 of the housing 1 is installed with an input side grid 2, and the output port 102 of the housing 1 is installed with an output side grid 3. The two grids at both ends of the housing 1 can evenly guide the flue gas so that the flue gas can be evenly distributed in the purification device 100, making the flue gas circulation and purification more uniform.

[0183] A flow guide 1 5 is installed at the input port 101 of the purification device 100, and a flow guide 2 6 is installed at the output port 102. The flow guides 1 5 and 2 6 are coaxially mounted within the housing 1 to guide the air flowing through the input port 101 and the output port 102, particularly distributing the regeneration gas.

[0184] By rotating and adjusting the guide device 5, the regeneration gas can be delivered to different catalytic channels 43, so that the catalyst in the catalytic channels 43 can be regenerated and purified in a targeted manner.

[0185] A rotating shaft 7 is installed in the center of the shell 1. The end of the rotating shaft 7 extends out of the catalytic module 4 and is connected to a rotary driver. The rotary driver can drive the rotating shaft 7 to rotate, thereby controlling the rotation adjustment of the deflector 1 5 and the deflector 2 6.

[0186] The deflector 5 includes a cover plate 54 and a rotating sleeve 51. The rotating sleeve 51 is mounted on the outer periphery of the rotating shaft 7 and can rotate synchronously with the rotating shaft 7 to achieve rotational limit. The cover plate 54 is fixedly mounted on the outer periphery of the rotating sleeve 51. The deflector 5 also includes a rotating support ring 52, which is rotatably connected to the inner periphery of the housing 1. The rotating support ring 52 and the rotating sleeve 51 are fixedly connected via a support frame 53.

[0187] The second deflector 6 includes a second cover plate 64 and a second rotating sleeve 61. The second rotating sleeve 61 is mounted on the outer periphery of the rotating shaft 7 and can rotate synchronously with the rotating shaft 7. The second cover plate 64 can be fixedly mounted on the outer periphery of the second rotating sleeve 61. The second deflector 6 also includes a second rotating support ring 62, which is rotatably connected to the inner periphery of the housing 1. The second rotating support ring 62 and the second rotating sleeve 61 are fixedly connected via a second support frame 63.

[0188] The shapes of cover plate 1 54 and cover plate 2 64 are adapted to the shapes of the two catalytic channels 43, and can simultaneously cover both ends of two adjacent catalytic channels 43. Moreover, cover plate 1 54 and cover plate 2 64 are positioned axially opposite each other, thereby covering and sealing both ends of the two catalytic channels 43.

[0189] Reference Figure 4As shown, cover plate 1 54 includes an input portion 55 and an output portion 56. The input portion 55 and the output portion 56 are the sides of cover plate 1 54 facing the catalytic channel 43. The input portion 55 and the output portion 56 are both formed into a concave structure, and are separated by a blocking protrusion in the middle, which can separate the concave spaces of the input portion 55 and the output portion 56 from each other.

[0190] Among them, a nozzle 57 facing the catalytic channel 43 is formed at the input part 55, and an overflow notch 561 is formed at the side of the output part 56 facing away from the input part 55; a connecting groove 65 is formed on the side of the cover plate 2 64 facing the catalytic channel 43, and the connecting groove 65 can connect the two catalytic channels 43, that is, the connecting groove 65 connects the output side ports of the first catalytic channel 431 and the second catalytic channel 433.

[0191] Refer to 7. Figure 8 As shown, during the regeneration process, the nozzle 57 of the input part 55 of the cover plate 1 54 can be injected into the input side port of the first catalytic channel 431, flow through the first catalytic channel 431, and regenerate the catalyst in the first catalytic channel 431; then, the gas is injected from the output side port of the first catalytic channel 431 and enters the connecting groove 65 of the cover plate 2 64. The gas in the connecting groove 65 of the cover plate 2 64 can flow toward the second catalytic channel 432, and the regenerated gas flows from the output side port of the second catalytic channel 432 to the output side port, and then enters the recessed space of the output part 56 of the cover plate 1 54, and then flows out from the overflow notch 561 outside the output part 56, enters the input side of the catalytic module 4, and then the regenerated gas can be transported backward from each catalytic channel 43 of the gas of the catalytic module 4.

[0192] Reference Figure 3 、 Figure 5 As shown, an air injection chamber 58 is provided inside the cover plate 1 54 , and a nozzle 57 facing the catalytic channel 43 is provided in the input portion 55 , and the nozzle 57 is communicated with the air injection chamber 58 .

[0193] An air channel 59 is defined in the sidewall of rotating sleeve 1 51. One end of the channel connects to the jet chamber 58, and the other end extends away from cover plate 1 54. A rotary joint 8 is mounted on the outer periphery of rotating sleeve 1 51, connecting the channel 59 to the regeneration gas spray line 500 through the rotary joint 8.

[0194] When the regeneration gas spray pipeline 500 inputs the regeneration gas, the regeneration gas can pass through the rotary joint 8 and be input into the gas guide channel 59 of the rotating sleeve 51, and then enter the jet chamber 58 of the cover plate 54, and then be ejected from the nozzle 57 of the input part 55, and the regeneration gas is injected into the catalytic channel 43.

[0195] The regeneration gas can achieve forward and reverse flow when flowing through the two catalytic channels 43. The regeneration gas flows from the input port to the output port in the first catalytic channel 431, and from the output port to the input port in the second catalytic channel 432, forming two states of forward and reverse flow.

[0196] During the regeneration process, the rotating shaft 7 can be rotated by an external rotary driver. Specifically, the rotary driver can be a stepper motor or a servo motor, which can drive the rotating shaft 7 to rotate. After each rotation adjustment, the cover plate 1 54 and the cover plate 2 64 can be precisely positioned at the ends of the two catalytic channels 43 to cover the ends of the two catalytic channels 43.

[0197] As shaft 7 rotates, it drives deflector 1 5 and deflector 2 6 to rotate. In their current position, cover plates 1 54 and 2 64 block and cover two catalytic channels 43. As shaft 7 deflects, cover plates 1 54 and 2 64 block and cover the remaining two catalytic channels 43, shifting the flow patterns of the two channels. The rotation of deflector 1 5 and deflector 2 6 allows regeneration air to be injected forward and backward within the corresponding catalytic channels 43, impacting the catalyst surface in different directions. This improves the catalytic treatment efficiency and other impact effects on the catalyst, further enhancing the regeneration and purification effects of the catalyst.

[0198] The above description is merely a preferred embodiment of the present invention. The scope of protection of the present invention is not limited to the above embodiment. All technical solutions based on the concept of the present invention are within the scope of protection of the present invention. It should be noted that for those skilled in the art, various improvements and modifications that do not depart from the principles of the present invention should also be considered within the scope of protection of the present invention.

Claims

1. An in-situ regeneration system for collaborative removal of catalyst for flue gas purification, characterized in that: include: A purification device (100), a regeneration gas spray pipeline (500) and a flue gas inlet channel (600), wherein the purification device (100) is connected to the flue gas inlet channel (600) and is used for purifying flue gas; the regeneration gas spray pipeline (500) is connected to the flue gas inlet channel (600), and the regeneration gas spray pipeline (500) is used for spraying reducing gas and oxidizing gas into the purification device (100) in sequence.

2. The in-situ regeneration system for collaborative removal of catalyst for flue gas purification according to claim 1, characterized in that: The reducing gas is CO and the oxidizing gas is NO2.

3. The in-situ regeneration system for collaborative removal of catalyst for flue gas purification according to claim 1, characterized in that: Also includes: A regeneration controller, a reducing gas source and an oxidizing gas source, wherein the regeneration controller can control the reducing gas source and the oxidizing gas source to be connected to the regeneration gas spray pipeline (500) in sequence.

4. The in-situ regeneration system for collaborative removal of catalyst for flue gas purification according to claim 3, characterized in that: The regeneration controller is a three-way valve structure, which is connected to the reducing gas source, the oxidizing gas source and the regeneration gas spray pipeline (500) respectively.

5. The in-situ regeneration system for collaborative removal of catalyst for flue gas purification according to claim 3, characterized in that: The input port (101) of the purification device (100) is equipped with a pollutant sensor 1 (200), and the output port (102) of the purification device (100) is equipped with a pollutant sensor 2 (300); When the catalyst in the purification device (100) is in a deactivated state, the regeneration controller starts the regeneration mode and sequentially introduces reducing gas and oxidizing gas into the regeneration gas spray pipeline (500); first, the reducing gas is introduced to decompose sulfate, and then the oxidizing gas is introduced to oxidize carbon deposits.

6. The in-situ regeneration system for collaborative removal of catalyst for flue gas purification according to claim 1, characterized in that: The purification device (100) comprises a housing (1), wherein the housing (1) has an input port (101) and an output port (102) at both ends thereof, a catalytic module (4) is installed inside the housing (1), and the catalytic module (4) is provided with a plurality of catalytic channels (43), wherein the two ends of the catalytic channels (43) face the input port (101) and the output port (102) respectively, the catalytic channels (43) are filled with catalysts, and the catalytic channels (43) are arranged in a circular array; The input port (101) is installed with a deflector 1 (5), and the output port (102) is installed with a deflector 2 (6). The deflector 1 (5) and the deflector 2 (6) are coaxially rotatably installed in the housing (1). The deflector 1 (5) includes a cover plate 1 (54), and the deflector 2 (6) includes a cover plate 2 (64). The cover plate 1 (54) and the cover plate 2 (64) can simultaneously cover the two ends of two adjacent catalytic channels (43). The cover plate 1 (54) includes an input part (55) and an output part (56). The input part (55) can spray gas toward the first catalytic channel (431), and the output part (56) can allow gas from the second catalytic channel (432) to flow out. The cover plate 2 (64) is provided with a connecting groove (65), and the connecting groove (65) can connect the two catalytic channels (43).

7. The in-situ regeneration system for collaborative removal of catalyst for flue gas purification according to claim 6, characterized in that: A rotating shaft (7) is installed at the center of the housing (1); the deflector (5) further comprises a rotating sleeve (51), the rotating sleeve (51) is fitted on the outer periphery of the rotating shaft (7) and can rotate synchronously with the rotating shaft (7), and the cover (54) is fixedly installed on the outer periphery of the rotating sleeve (51); the deflector (6) further comprises a rotating sleeve (61), the rotating sleeve (61) is fitted on the outer periphery of the rotating shaft (7) and can rotate synchronously with the rotating shaft (7), and the cover (64) is fixedly installed on the outer periphery of the rotating sleeve (61); The first cover plate (54) has an air jet chamber (58) formed inside, and the input portion (55) has an air nozzle (57) facing the catalytic channel (43), and the air nozzle (57) is connected to the air jet chamber (58); the first rotating sleeve (51) has an air guide channel (59) formed inside, and one end of the air guide channel (59) is connected to the air jet chamber (58), and the other end extends away from the first cover plate (54); A rotary joint (8) is installed on the outer periphery of the rotary sleeve (51), and the air guide channel (59) is connected to the regeneration gas spray pipeline (500) through the rotary joint (8).

8. An in-situ regeneration method for a synergistic removal catalyst for flue gas purification, characterized in that: An in-situ regeneration system for collaborative removal of catalyst for flue gas purification according to any one of claims 1 to 7; The steps are as follows: (1) When the concentration of flue gas pollutants at the output port 102 of the purification device (100) reaches a preset emission limit, the regeneration mode is triggered; (2) CO gas at a temperature of 350-650°C is introduced into the purification device (100) to decompose sulfate on the catalyst surface through a reduction reaction; (3) NO2 gas is introduced into the purification device (100), and the carbon deposits on the surface of the oxidation catalyst are converted to CO2; (4) Repeat the switching between step (3) and step (4) to purify the catalyst in the purification device 100.

9. The in-situ regeneration method of the synergistic removal catalyst for flue gas purification according to claim 8, characterized in that: The flow rates of the CO gas and NO2 gas are monitored by flow meters, and the input amounts are controlled by a regeneration controller.

10. The in-situ regeneration method of the synergistic removal catalyst for flue gas purification according to claim 8, characterized in that: By comparing the flue gas pollutant concentrations at the input port (101) and the output port (102) of the purification device (100), the flue gas purification rate of the purification device (100) can be obtained.

Images