A deno x and decarbon monoxide reactor, a method for calculating the temperature rise of flue gas in the reactor and application thereof

Abstract

The present application belongs to the technical field of catalytic purification of industrial flue gas, and particularly relates to a NOx and CO removal reactor, a flue gas temperature lifting calculation method and application. The reactor comprises at least a reactor shell, a flue gas inlet arranged at the upper part of the reactor shell, and a flue gas outlet arranged at the lower part of the reactor shell. The reactor further comprises SCR denitration catalyst modules and CO catalytic oxidation catalyst modules arranged in the reactor shell and independent of each other and having consistent external dimensions. Two adjacent SCR denitration catalyst modules and CO catalytic oxidation catalyst modules, SCR denitration catalyst modules or CO catalytic oxidation catalyst modules are in surface-to-surface contact and arranged in a multi-layer catalyst structure, so that the heat transfer efficiency and temperature rising rate are greatly improved. The heat transfer efficiency of the present application is improved by more than 30% compared with the traditional "solid-gas-solid" mode, and the energy consumption and operating cost are significantly reduced, the operation stability and maintainability are good, and the NOx removal efficiency is improved. The flue gas temperature lifting calculation is accurate and reliable.

Description

Technical Field

[0001] This invention belongs to the field of industrial flue gas catalytic purification technology, specifically relating to a NOx and CO removal reactor, a method for calculating flue gas temperature rise in the reactor, and its application. Background Technology

[0002] With industrial development and increasingly stringent environmental standards, the synergistic control of multiple pollutants in industrial flue gas has become an important development direction. NOx and CO commonly coexist in flue gas from industries such as steelmaking, coking, and waste incineration.

[0003] Selective catalytic reduction (SCR) technology is currently the mainstream denitrification technology, but the optimal activity temperature window of its catalyst is usually between 200-400℃. However, after undergoing upstream desulfurization and dust removal processes, the temperature of many industrial flue gases drops below 100℃, far below the activity temperature of the SCR catalyst. Therefore, it is necessary to install equipment such as hot air furnaces or heat exchangers to reheat the flue gas, which not only increases equipment investment but also brings additional fuel or energy consumption.

[0004] Meanwhile, CO in flue gas, in addition to being a harmful pollutant, also has certain fuel characteristics. Its catalytic oxidation to CO2 is a strongly exothermic reaction (ΔH=-283kJ / mol), which makes it possible to use its heat of reaction to increase the flue gas temperature and achieve energy conservation and consumption reduction.

[0005] Based on this, researchers have proposed integrating CO catalytic oxidation into SCR denitrification reactors to achieve synergistic removal of NOx and CO and self-utilization of reaction heat. Currently, several technical solutions exist to achieve this goal, but all have certain drawbacks: The first type is the traditional series arrangement. For example, Chinese patent CN209348416U discloses a sintering flue gas treatment system, in which the flue gas first enters the SCR denitrification unit and then enters the catalytic CO removal unit. The heat released by CO oxidation is exchanged with the low-temperature flue gas at the inlet through a GGH flue gas heat exchanger (Gas-Gas Heater), thereby increasing the inlet temperature of the denitrification reaction. The CO oxidation catalyst and the SCR denitrification catalyst are located in different reaction zones or equipment, and the heat transfer depends on the flue gas as a medium, proceeding through a solid-gas-solid process. This heat transfer path is long and inefficient, and the heat exchange equipment such as the GGH itself has problems such as high power consumption, large footprint, and high operation and maintenance costs.

[0006] The second approach is an integrated, layered arrangement. To overcome the drawbacks of separate devices, researchers integrate the two catalysts into the same reactor. For example, Chinese patent CN111664717B discloses an integrated device in which a CO removal catalyst layer and a multi-stage SCR denitrification catalyst layer are sequentially arranged within the reaction system. When flue gas flows through the CO removal catalyst layer, the exothermic oxidation of CO directly heats the flue gas, which then enters the SCR denitrification catalyst layer for reaction. Although this method eliminates the need for an external gas-heating generator (GGH), it is essentially still a series structure. The heat transfer from the CO catalyst to the SCR catalyst still mainly relies on flue gas convection heat exchange, which limits the heat transfer rate and results in a less rapid and direct heating effect.

[0007] In summary, existing technologies have not solved the core problems of low CO oxidation heat utilization efficiency, slow heat transfer rate, and high system energy consumption. Summary of the Invention

[0008] This invention provides a NOx and CO removal reactor, a method for calculating flue gas temperature rise in the reactor, and its application. The aim is to address the problems of low CO oxidation heat utilization efficiency, slow heat transfer rate, high system energy consumption, and large equipment footprint in existing technologies. By refining the stage setup and modular distribution, and based on the full utilization of CO oxidation reaction heat, it achieves NOx removal from low-temperature flue gas. x It achieves efficient synergistic removal of CO and provides a precise calculation method for flue gas temperature rise.

[0009] To achieve the above objectives, the technical solution adopted by the present invention is as follows: A NOx and CO removal reactor includes at least a reactor shell; a flue gas inlet is provided at the upper part of the reactor shell, and a flue gas outlet is provided at the lower part of the shell; it also includes an SCR denitrification catalyst module and a CO catalytic oxidation catalyst module, which are independent of each other and have the same external dimensions and are disposed inside the reactor shell; two adjacent SCR denitrification catalyst modules and the CO catalytic oxidation catalyst module, or the SCR denitrification catalyst module or the CO catalytic oxidation catalyst module, are in surface contact and have a multi-layered catalyst structure.

[0010] The top layer near the flue gas inlet is a pure SCR denitrification catalyst protective layer composed of SCR denitrification catalyst modules; each layer below this layer is composed of SCR denitrification catalyst modules and CO catalytic oxidation catalyst modules arranged alternately in a surface contact manner, with CO catalytic oxidation catalyst modules in the same layer arranged at intervals, and CO catalytic oxidation catalyst modules in adjacent layers arranged vertically in an alternating manner.

[0011] The thickness of the protective layer of the pure SCR denitrification catalyst is 100-200 mm, preferably 150 mm.

[0012] Along the flue gas flow direction from the flue gas inlet to the flue gas outlet, the catalyst structure is divided into 6 to 8 levels. In each level, the volume proportion of the CO catalytic oxidation catalyst module gradually decreases, while the volume proportion of the SCR denitrification catalyst module gradually increases.

[0013] The ratio of the total volume of the SCR denitrification catalyst module to the total volume of the CO catalytic oxidation catalyst module is 3:1 to 2:1; the operating space velocity of the SCR denitrification catalyst is 2000-4000 h⁻¹. -1 The operating space velocity of the CO catalytic oxidation catalyst is 6000-12000 h⁻¹. -1 .

[0014] The catalyst structure is divided into six levels: a low-temperature layer, a sub-low-temperature layer, a medium-low-temperature layer, a medium-temperature layer, a medium-high-temperature layer, and a high-temperature layer. In the low-temperature and sub-low-temperature layers, SCR denitrification catalyst modules and CO catalytic oxidation catalyst modules are arranged alternately in front, behind, left, and right directions within the same layer, and SCR denitrification catalyst modules and CO catalytic oxidation catalyst modules are arranged alternately vertically in different layers. In the medium-low-temperature and medium-temperature layers, multiple SCR denitrification catalyst modules and fewer CO catalytic oxidation catalyst modules are arranged alternately. In the medium-high-temperature and high-temperature layers, multiple SCR denitrification catalyst modules and dispersed CO catalytic oxidation catalyst modules are arranged alternately, with the CO catalytic oxidation catalyst modules dispersed between the SCR denitrification catalyst modules.

[0015] The SCR denitrification catalyst module is a V2O5-WO3 / TiO2 system plate or honeycomb catalyst; the CO catalytic oxidation catalyst module is a cordierite honeycomb ceramic catalyst supported on Pt, Pd, CuO or CeO2; the external dimensions of the SCR denitrification catalyst module and the CO catalytic oxidation catalyst module are both length × width × height = 150mm × 150mm × (150mm~1200mm).

[0016] The SCR denitrification catalyst module and the CO catalytic oxidation catalyst module are bonded together with a thermally conductive enhancement layer; the thermally conductive enhancement layer is a graphene thermally conductive film, a metal thermally conductive sheet or a ceramic thermally conductive coating with a thickness of 0.1-1.0 mm; wherein the graphene thermally conductive film is preferably selected with a thermal conductivity ≥1500W / (m·K).

[0017] A method for calculating flue gas temperature rise using a NOx and CO removal reactor; the flue gas temperature rise is calculated by balancing the effective heat released by the CO oxidation reaction with the heat absorbed by the flue gas, as detailed below: Step 1: Obtain flue gas parameters; Flue gas parameters include standard flue gas volumetric flow rate, initial CO concentration in flue gas, enthalpy change of CO oxidation reaction, CO molar mass, standard flue gas average density, actual CO conversion rate, average isobaric specific heat capacity of flue gas, and correction factor. Step 2: Calculate the total heat released by the complete oxidation of CO. ; The following formula is used for calculation:

[0018] in: The volumetric flow rate of flue gas under standard conditions is expressed in Nm³ / h. The initial CO concentration in the flue gas is expressed in mg / Nm³. 3 ; The enthalpy change for the CO oxidation reaction is taken as -283 kJ / mol; The value is the molar mass of CO, taken as 28 g / mol; Step 3: Calculate the theoretical flue gas temperature rise ; The following corrected formula is used for calculation: , In the formula: k is a correction factor, with a value ranging from 0.95 to 0.98; This represents the total heat released during the complete oxidation of CO, expressed in kJ / h. This represents the actual CO conversion rate, expressed in % (%). This refers to the flue gas mass flow rate, expressed in kg / h. The average isobaric specific heat capacity of flue gas is expressed in kJ / (kg·℃), with a value ranging from 1.05 to 1.10 kJ / (kg·℃), calculated based on the weighted average of the flue gas components O2, H2O, N2, and CO2. The calculation formula is:

[0019] in: The standard average density of the flue gas is taken as 1.2-1.4 kg / Nm³. 3 .

[0020] Step 4: Output theoretical flue gas temperature rise Calculate the deviation between the calculated value and the actual measured value; The calculated value should deviate from the actual measured value by ≤5%.

[0021] The NOx and CO removal reactor was applied to the synergistic purification of NOx and CO in low-temperature flue gas from the steel, coking, and waste incineration industries.

[0022] Beneficial effects: 1. Significantly improved heat transfer efficiency and heating rate. This invention constructs a solid-solid direct heat transfer channel by alternating surface contact layers, coupled with a thermally conductive enhancement layer. The heat of CO oxidation reaction is rapidly transferred to the SCR denitrification catalyst module via thermal conduction. The heat transfer efficiency is improved by more than 30% compared to the traditional "solid-gas-solid" mode, and the SCR catalyst can reach the high-efficiency active temperature zone within 35 minutes, solving the core problem of slow heating.

[0023] 2. Significantly reduced energy consumption and operating costs. This invention achieves efficient in-situ utilization of the heat of CO oxidation. When the CO concentration in the flue gas is high, it can completely replace additional heating and heat exchange equipment such as hot blast stoves and GGH heat exchangers, saving fuel and electricity consumption and reducing operating costs by 50%-80%.

[0024] 3. Optimization of energy utilization and adaptability to operating conditions. This invention achieves precise matching between energy output and demand through a tiered arrangement. The high-proportion CO catalytic oxidation catalyst module in the low-temperature inlet section generates heat to raise the temperature, while the low-proportion CO catalytic oxidation catalyst module in the high-temperature outlet section avoids local overheating, and the high-proportion SCR denitrification catalyst module ensures denitrification depth and improves NOx removal efficiency. By adjusting the total volume ratio of the SCR denitrification catalyst module to the CO catalytic oxidation catalyst module to 3:1~2:1, it can be flexibly adapted to different low-temperature flue gas operating conditions.

[0025] 4. Accurate and reliable calculation of flue gas temperature rise: The flue gas temperature rise calculation formula established in this invention introduces heat loss and heat transfer efficiency correction coefficients. The deviation between the calculation results and the actual measured values ​​is ≤5%, which can realize accurate prediction of flue gas temperature rise and provide a theoretical basis for catalyst structure stage design and operating parameter adjustment.

[0026] 5. Good operational stability and maintainability: The SCR denitrification catalyst module and the CO catalytic oxidation catalyst module in this invention are independent physical modules, which facilitates individual replacement and maintenance, avoids the deactivation of a single catalyst leading to the shutdown of the entire system, and reduces equipment maintenance costs and downtime losses.

[0027] The above description is merely an overview of the technical solution of the present invention. In order to better understand the technical means of the present invention and to implement it in accordance with the contents of the specification, the preferred embodiments of the present invention are described in detail below with reference to the accompanying drawings. Attached Figure Description

[0028] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0029] Figure 1 This is a front view of the tiered arrangement of the catalyst module in Embodiment 1 of the present invention.

[0030] Figure 2 This is a top view of the catalyst bed layer arrangement in Example 1 of the present invention.

[0031] Figure 3 This is a schematic diagram of the solid-solid heat transfer interface between catalyst modules of the present invention.

[0032] Figure 4 This is a flowchart illustrating the calculation process for flue gas temperature rise in this invention.

[0033] In the diagram: 1. Reactor shell; 2. Flue gas inlet; 3. Pure SCR denitrification catalyst protective layer; 4. Low temperature layer; 5. Sub-low temperature layer; 6. Medium-low temperature layer; 7. Medium temperature layer; 8. Medium-high temperature layer; 9. High temperature layer; 10. Flue gas outlet; 11. CO catalytic oxidation catalyst module; 12. SCR denitrification catalyst module; 13. Thermal conductivity enhancement layer. Detailed Implementation

[0034] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of the present invention.

[0035] Example 1: according to Figures 1-3 The NOx and CO removal reactor shown includes at least a reactor shell 1; a flue gas inlet 2 is provided at the upper part of the reactor shell 1, and a flue gas outlet 10 is provided at the lower part of the shell; it also includes an SCR denitrification catalyst module 12 and a CO catalytic oxidation catalyst module 11, which are independent of each other and have the same external dimensions and are disposed inside the reactor shell 1; two adjacent SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11, SCR denitrification catalyst modules 12 or CO catalytic oxidation catalyst modules 11 are in surface contact with each other, and the catalyst structure is multi-layered.

[0036] The technical solution of this invention constructs a solid-solid direct heat transfer channel by alternating surface contact and superposition, and with the addition of a thermally conductive enhancement layer, the heat of CO oxidation reaction is rapidly transferred to the SCR denitrification catalyst module by thermal conduction. The heat transfer efficiency is improved by more than 30% compared with the traditional "solid-gas-solid" mode, and the SCR catalyst can reach the high-efficiency active temperature zone within 35 minutes, solving the core problem of slow heating.

[0037] This invention enables efficient in-situ utilization of CO oxidation heat. When the CO concentration in the flue gas is high, it can completely replace additional heating and heat exchange equipment such as hot blast stoves and GGH heat exchangers, saving fuel and electricity consumption and reducing system operating costs by 50%-80%.

[0038] In this invention, the SCR denitrification catalyst module and the CO catalytic oxidation catalyst module are independent physical modules, which facilitates individual replacement and maintenance, avoids the deactivation of a single catalyst leading to the shutdown of the entire system, and reduces equipment maintenance costs and downtime losses.

[0039] Example 2: according to Figures 1-3 The NOx and CO removal reactor shown differs from that in Example 1 in that: the top layer near the flue gas inlet 2 is a pure SCR denitrification catalyst protective layer 3 composed of SCR denitrification catalyst modules 12; each layer below this layer is composed of SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11 arranged alternately in a surface contact manner, and the CO catalytic oxidation catalyst modules 11 in the same layer are arranged at intervals, while the CO catalytic oxidation catalyst modules 11 in adjacent layers are arranged vertically in an alternating manner.

[0040] Furthermore, the thickness of the pure SCR denitrification catalyst protective layer 3 is 100-200 mm, preferably 150 mm.

[0041] In actual use, the layer closest to the flue gas inlet 2, i.e. the top layer, is equipped with a pure SCR denitrification catalyst protective layer. This effectively prevents harmful components such as SO2 in the flue gas from poisoning the CO catalytic oxidation catalyst, while also preventing the injected denitrification reducing agent NH3 from being over-oxidized, thus ensuring the activity and stability of both catalysts.

[0042] Furthermore, along the flue gas flow direction from flue gas inlet 2 to flue gas outlet 10, the catalyst structure is divided into 6 to 8 levels, with the volume ratio of CO catalytic oxidation catalyst module 11 gradually decreasing and the volume ratio of SCR denitrification catalyst module 12 gradually increasing in each level.

[0043] Furthermore, the ratio of the total volume of the SCR denitrification catalyst module 12 to the total volume of the CO catalytic oxidation catalyst module 11 is 3:1 to 2:1; the operating space velocity of the SCR denitrification catalyst is 2000-4000 h⁻¹.-1 The operating space velocity of the CO catalytic oxidation catalyst is 6000-12000 h⁻¹. -1 To adapt to the operating conditions of different pollutant loads.

[0044] Furthermore, the catalyst structure is divided into six levels: a low-temperature layer 4, a sub-low-temperature layer 5, a medium-low-temperature layer 6, a medium-temperature layer 7, a medium-high-temperature layer 8, and a high-temperature layer 9. The low-temperature layer 4 and the sub-low-temperature layer 5 employ an alternating arrangement of SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11 in the same layer, with the SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11 arranged vertically in different layers. The medium-low-temperature layer 6 and the medium-temperature layer 7 employ an alternating arrangement of multiple SCR denitrification catalyst modules 12 and fewer CO catalytic oxidation catalyst modules 11. The medium-high-temperature layer 8 and the high-temperature layer 9 employ an alternating arrangement of multiple SCR denitrification catalyst modules 12 and dispersed CO catalytic oxidation catalyst modules 11, with the CO catalytic oxidation catalyst modules 11 dispersed in the gaps between the SCR denitrification catalyst modules 12.

[0045] In actual use, the SCR denitrification catalyst module 12 and CO catalytic oxidation catalyst module 11 in the upper and lower adjacent layers are arranged vertically correspondingly or staggeredly, which ensures that the waste heat generated by CO oxidation is directly conducted to the SCR denitrification catalyst module 12 that needs to be heated. There is no physical barrier between adjacent layers, which ensures that the flue gas flow channel is unobstructed.

[0046] Example 3: according to Figures 1-3 The NOx and CO removal reactor shown differs from that in Example 1 or Example 2 in that: the SCR denitrification catalyst module 12 is a V2O5-WO3 / TiO2 system plate or honeycomb catalyst; the CO catalytic oxidation catalyst module 11 is a cordierite honeycomb ceramic catalyst supported on Pt, Pd, CuO or CeO2; and the external dimensions of both the SCR denitrification catalyst module 12 and the CO catalytic oxidation catalyst module 11 are length × width × height = 150mm × 150mm × (150mm~1200mm).

[0047] In actual use, the SCR denitrification catalyst module 12 and the CO catalytic oxidation catalyst module 11 have the same external dimensions. The module bonding gap is controlled at 0.05 to 0.15 mm, and the effective contact area ratio is not less than 95%. The height is designed according to the flue gas treatment volume and pollutant treatment concentration to ensure the tightness of the surface contact and avoid flue gas short circuit and heat transfer loss.

[0048] Example 4: according to Figures 1-3The NOx and CO removal reactor shown differs from those in Example 1, Example 2, or Example 3 in that: a thermally conductive enhancement layer 13 is attached to the side of the SCR denitrification catalyst module 12 and the CO catalytic oxidation catalyst module 11; the thermally conductive enhancement layer 13 is a graphene thermally conductive film, a metal thermally conductive sheet, or a ceramic thermally conductive coating with a thickness of 0.1-1.0 mm; wherein the graphene thermally conductive film is preferably selected with a thermal conductivity ≥1500 W / (m·K).

[0049] In practical use, the design of the thermally conductive enhancement layer 13 enhances the solid-solid heat transfer efficiency between modules.

[0050] Example 5: Reference Figures 1-4 As shown, a method for calculating flue gas temperature rise is employed using a NOx and CO removal reactor. The flue gas temperature rise (ΔT) is calculated by balancing the effective heat released by the CO oxidation reaction with the heat absorbed by the flue gas. The specific method is as follows: Step 1: Obtain flue gas parameters; Flue gas parameters include standard flue gas volumetric flow rate, initial CO concentration in flue gas, enthalpy change of CO oxidation reaction, CO molar mass, standard flue gas average density, actual CO conversion rate, average isobaric specific heat capacity of flue gas, and correction factor. Step 2: Calculate the total heat released by the complete oxidation of CO. ; The following formula is used for calculation:

[0051] in: The volumetric flow rate of flue gas under standard conditions is expressed in Nm³ / h. The initial CO concentration in the flue gas is expressed in mg / Nm³. 3 ; The enthalpy change for the CO oxidation reaction is taken as -283 kJ / mol; The value is the molar mass of CO, taken as 28 g / mol; Step 3: Calculate the theoretical flue gas temperature rise ; The following corrected formula is used for calculation: , In the formula: k is a correction factor, ranging from 0.95 to 0.98. The correction factor k is adjusted according to the thermal insulation performance of the reactor and the type of thermal conductivity enhancement layer. The better the thermal insulation performance and the higher the thermal conductivity, the closer the value of k is to 0.98. This represents the total heat released during the complete oxidation of CO, expressed in kJ / h. The actual CO conversion rate, expressed as a percentage, is determined by the actual catalyst activity and is calculated using the CO concentrations at the reactor inlet and outlet, as detailed below:

[0052] C CO,in The measured CO concentration at the reactor inlet is expressed in mg / Nm³. C CO,out The measured CO concentration at the reactor outlet is expressed in mg / Nm³. This refers to the flue gas mass flow rate, expressed in kg / h. The average isobaric specific heat capacity of flue gas is expressed in kJ / (kg·℃), with a value ranging from 1.05 to 1.10 kJ / (kg·℃), calculated based on the weighted average of the flue gas components O2, H2O, N2, and CO2. The calculation formula is:

[0053] in: The standard average density of the flue gas is taken as 1.2-1.4 kg / Nm³. 3 .

[0054] Step 4: Output theoretical flue gas temperature rise Calculate the deviation between the calculated value and the actual measured value; The calculated value should deviate from the actual measured value by ≤5%.

[0055] The flue gas temperature rise calculation formula established in this invention introduces heat loss and heat transfer efficiency correction coefficients. The deviation between the calculation results and the actual measured values ​​is ≤5%, which can realize accurate prediction of flue gas temperature rise and provide a theoretical basis for catalyst structure stage design and operating parameter adjustment.

[0056] This invention determines a reasonable range for the correction coefficient k through extensive experimental fitting, ensuring that the deviation between the calculation results and the actual measured values ​​is ≤5%, thus significantly improving the calculation accuracy.

[0057] Example 6: The NOx and CO removal reactor is applied to the synergistic purification of NOx and CO in low-temperature flue gas from industries such as steel, coking, and waste incineration.

[0058] This invention utilizes an alternating arrangement of SCR denitrification catalyst module 12 and CO catalytic oxidation catalyst module 11, with the CO catalytic oxidation catalyst module 11 arranged in a tiered manner to form a solid-solid direct heat transfer interface. This allows for the synergistic removal of NOx and CO from low-temperature flue gas at ≤180℃, constructing a highly efficient and direct heat transfer channel. It fully utilizes the heat energy of CO oxidation to rapidly increase the temperature of the SCR catalyst, while simultaneously improving the adaptability to operating conditions and engineering practicality.

[0059] The SCR denitrification catalyst module and the CO catalytic oxidation catalyst module are standardized plate or honeycomb structures. The two catalyst modules have the same external dimensions: length × width × height = 150mm × 150mm × (150mm~1200mm). The height is designed according to the flue gas treatment volume and pollutant treatment concentration to ensure tight contact of the surfaces and avoid flue gas short circuit and heat transfer loss.

[0060] Example 7: Reference Figures 1-4 A NOx and CO removal reactor.

[0061] I. Catalyst Module Preparation S1: Preparation of SCR denitration catalyst module 12; The V2O5-WO3 / TiO2 system plate catalyst has a standardized size of 150mm×150mm×150mm. S2: Preparation of CO catalytic oxidation catalyst module 11; A Pt-Pd dual noble metal supported cordierite honeycomb ceramic catalyst was used to prepare a standardized module of 150mm×150mm×150mm that is completely identical to the SCR denitrification catalyst module 12, ensuring the fit of the contact surfaces between modules. S3: Apply a thermally conductive enhancement layer 13 to the SCR denitrification catalyst module 12 and the CO catalytic oxidation catalyst module 11; A 0.5mm thick graphene thermal conductive film and a thermally conductive enhancement layer 13 with a thermal conductivity of 1800W / (m·K) are selected and attached to the side of each SCR denitrification catalyst module 12 and CO catalytic oxidation catalyst module 11 to enhance the heat transfer effect between modules.

[0062] II. Catalyst Structure Assembly The reactor shell 1 has a square cross-section with dimensions of 1200mm × 1200mm. A catalyst structure with a total thickness of 1050mm is arranged along the flue gas flow direction. The total volume ratio of the SCR denitrification catalyst module 12 and the CO catalytic oxidation catalyst module 11 is 2.7:1, and the specific arrangement is as follows: S1: Pure SCR denitrification catalyst protective layer 3: The uppermost layer near the flue gas inlet 2 is composed of a 150mm thick pure SCR denitrification catalyst module 12, which serves as a protective layer for the flue gas inlet 2 to prevent CO catalyst poisoning and excessive NH3 oxidation. S2: Level 1, i.e., low temperature layer 4, has a thickness of 150mm and an SCR:CO volume ratio of 1:1. It consists of 32 SCR denitrification catalyst modules 12 and 32 CO catalytic oxidation catalyst modules 11. The modules are arranged in an alternating and close arrangement, with one SCR denitrification catalyst module 12 and one CO catalytic oxidation catalyst module 11. The modules are bonded together by a graphene thermal conductive film. Each module is aligned and arranged without gaps to ensure solid-solid heat transfer. S3: Layer 2, also known as the sub-low temperature layer 5, has a thickness of 150mm and an SCR:CO volume ratio of 1:1. It consists of 32 SCR denitrification catalyst modules 12 and 32 CO catalytic oxidation catalyst modules 11. One SCR denitrification catalyst module 12 and one CO catalytic oxidation catalyst module 11 are arranged alternately and closely, with the modules bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst module 11 in this layer is tightly bonded to the SCR denitrification catalyst module 12 in layer 1, and is staggered with the CO catalytic oxidation catalyst module 11 in layer 1. S4: Layer 3, namely the medium-low temperature layer 6, has a thickness of 150mm and an SCR:CO volume ratio of 2.05:1. It consists of 43 SCR denitrification catalyst modules 12 and 21 CO catalytic oxidation catalyst modules 11. The modules are arranged in an alternating manner with more SCR denitrification catalyst modules 12 and fewer CO catalytic oxidation catalyst modules 11. The modules are bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 in this layer are all arranged directly below the SCR denitrification catalyst modules 12 in layer 2. S5: Layer 4, i.e., the intermediate temperature layer 7, has a thickness of 150mm and an SCR:CO volume ratio of 3:1. It consists of 48 SCR denitrification catalyst modules 12 and 16 CO catalytic oxidation catalyst modules 11, arranged in an alternating manner with more SCR denitrification catalyst modules 12 and fewer CO catalytic oxidation catalyst modules 11. The modules are bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 in this layer are all arranged directly below the SCR denitrification catalyst modules 12 in layer 3.

[0063] S6: Layer 5, i.e., medium-high temperature layer 8, has a thickness of 150mm and an SCR:CO volume ratio of 4.82:1. It consists of 53 SCR denitrification catalyst modules 12 and 11 CO catalytic oxidation catalyst modules 11. The SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11 are arranged in a dispersed manner, with the modules bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 are dispersed in the gaps between the SCR denitrification catalyst modules 12 and are arranged directly below the SCR denitrification catalyst modules 12 in layer 4.

[0064] S7: Layer 6, also known as high-temperature layer 9, has a thickness of 150mm and an SCR:CO volume ratio of 6.1:1. It consists of 55 SCR denitrification catalyst modules 12 and 9 CO catalytic oxidation catalyst modules 11. The SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11 are arranged in a dispersed manner, with the modules bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 are dispersed in the gaps between the SCR denitrification catalyst modules 12 and are arranged directly below the SCR denitrification catalyst modules 12 in layer 5.

[0065] III. Experimental Conditions a. Simulated flue gas composition: NOx = 400 mg / Nm³ 3 CO=8000mg / Nm 3 NH 3 NOx molar ratio = 1.0, O2 = 16 vol%, dust = 10 mg / Nm³ 3 SO2 = 30 mg / Nm 3 CO2 = 7 vol%, H2O = 12 vol%, N2 is the balance, inlet flue gas temperature = 100℃, flue gas flow rate = 4400 Nm 3 / h.

[0066] b. Operating airspeed: Total volume of SCR catalyst = 1.1 m³ 3 Operating airspeed = 4400 Nm 3 / h÷1.1m 3 =4000h -1 ; Total volume of CO catalyst = 0.408 m³ 3 Operating airspeed = 4400 Nm 3 / h÷0.408m 3 =10784h -1 .

[0067] c. Correction factor k: The reactor shell 1 is provided with a rock wool insulation layer (thickness 50mm), and the thermal conductivity enhancement layer 13 is a graphene thermal conductive film. The value of k is 0.97.

[0068] IV. Calculation of Smoke Temperature Rise S1: Calculate the total heat released by the complete oxidation of CO. ;

[0069] =4400Nm 3 / h×8000mg / Nm 3 ×283kJ / mol÷28g / mol×10 -3 =355771kJ / h; S2: Calculate flue gas mass flow rate ; =4400Nm 3 / h×1.28Kg / Nm 3 =5632kg / h; S3: Substitute into the corrected formula to calculate the theoretical flue gas temperature rise. ; Actual measurement =99.2%, =1.08 kJ / (kg·℃)

[0070] =0.97×355771kJ / h×99.2%÷5632kg / h÷1.08kJ / (kg·℃)=56.28℃ V. Experimental Results a. Pollutant removal efficiency, measured: CO removal efficiency 99.2%, NOx removal efficiency 96.5%.

[0071] b. Flue gas temperature rise: Actual measurement: inlet flue gas temperature 99.9℃, outlet flue gas temperature 154.5℃, flue gas temperature rise 54.6℃, calculated value deviates from actual value by 3%.

[0072] c. Startup stabilization time: 32 minutes.

[0073] Example 8: Reference Figures 1-4 A NOx and CO removal reactor.

[0074] I. Catalyst Module Preparation S1: Preparation of SCR denitration catalyst module 12; The honeycomb catalyst using the V2O5-WO3 / TiO2 system has a standardized size of 150mm×150mm×200mm. S2: Preparation of CO catalytic oxidation catalyst module 11; A standardized module of 150mm×150mm×200mm, identical to the SCR denitrification catalyst module 12, was prepared using Pt-CeO2-supported cordierite honeycomb ceramic catalyst to ensure the fit of the contact surfaces between modules. S3: Apply a thermally conductive enhancement layer 13 to the SCR denitrification catalyst module 12 and the CO catalytic oxidation catalyst module 11; A 0.4mm thick graphene thermal conductive film and a thermally conductive enhancement layer 13 with a thermal conductivity of 1600W / (m·K) are selected and attached to the side of each SCR denitrification catalyst module 12 and CO catalytic oxidation catalyst module 11 to enhance the heat transfer effect between modules.

[0075] II. Catalyst Structure Assembly The reactor shell 1 has a square cross-section with dimensions of 1200mm × 1200mm. A catalyst structure with a total thickness of 1350mm is arranged along the flue gas flow direction. The total volume ratio of the SCR denitrification catalyst module 12 and the CO catalytic oxidation catalyst module 11 is 2.43:1, and the specific arrangement is as follows: S1: Pure SCR denitrification catalyst protective layer 3: The uppermost layer near the flue gas inlet 2 is composed of a 150mm thick pure SCR denitrification catalyst module 12, which serves as a protective layer for the flue gas inlet 2 to prevent CO catalyst poisoning and excessive NH3 oxidation. S2: Level 1, i.e., low temperature layer 4, has a thickness of 200mm and an SCR:CO volume ratio of 1:1. It consists of 32 SCR denitrification catalyst modules 12 and 32 CO catalytic oxidation catalyst modules 11. The modules are arranged in an alternating and close arrangement, with one SCR denitrification catalyst module 12 and one CO catalytic oxidation catalyst module 11. The modules are bonded together by a graphene thermal conductive film. Each module is aligned and arranged without gaps to ensure solid-solid heat transfer. S3: Layer 2, also known as the sub-low temperature layer 5, has a thickness of 200mm and an SCR:CO volume ratio of 1:1. It consists of 32 SCR denitrification catalyst modules 12 and 32 CO catalytic oxidation catalyst modules 11. One SCR denitrification catalyst module 12 and one CO catalytic oxidation catalyst module 11 are arranged alternately and closely, with the modules bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst module 11 in this layer is tightly bonded to the SCR denitrification catalyst module 12 in layer 1, and is staggered with the CO catalytic oxidation catalyst module 11 in layer 1. S4: Layer 3, namely the medium and low temperature layer 6, has a thickness of 200mm and an SCR:CO volume ratio of 1.9:1. It consists of 43 SCR denitrification catalyst modules 12 and 21 CO catalytic oxidation catalyst modules 11. The modules are arranged in an alternating manner with more SCR denitrification catalyst modules 12 and fewer CO catalytic oxidation catalyst modules 11. The modules are bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 in this layer are all arranged directly below the SCR denitrification catalyst modules 12 in layer 2. S5: Layer 4, i.e., the intermediate temperature layer 7, has a thickness of 200mm and an SCR:CO volume ratio of 3:1. It consists of 48 SCR denitrification catalyst modules 12 and 16 CO catalytic oxidation catalyst modules 11, arranged in an alternating manner with more SCR denitrification catalyst modules 12 and fewer CO catalytic oxidation catalyst modules 11. The modules are bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 in this layer are all arranged directly below the SCR denitrification catalyst modules 12 in layer 3.

[0076] S6: Layer 5, i.e., medium-high temperature layer 8, has a thickness of 200mm and an SCR:CO volume ratio of 3.92:1. It consists of 53 SCR denitrification catalyst modules 12 and 11 CO catalytic oxidation catalyst modules 11. The SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11 are arranged in a dispersed manner, with the modules bonded together by a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 are dispersed in the gaps between the SCR denitrification catalyst modules 12 and are arranged directly below the SCR denitrification catalyst modules 12 in layer 4.

[0077] S7: Level 6, i.e., the high-temperature layer, has a thickness of 200mm and an SCR:CO volume ratio of 4.82:1. It consists of 55 SCR denitrification catalyst modules 12 and 9 CO catalytic oxidation catalyst modules 11. The SCR denitrification catalyst modules 12 and CO catalytic oxidation catalyst modules 11 are arranged in a dispersed manner, with the modules bonded to a graphene thermal conductive film. The CO catalytic oxidation catalyst modules 11 are dispersed in the gaps between the SCR denitrification catalyst modules 12 and are arranged directly below the SCR denitrification catalyst modules 12 in Level 5.

[0078] III. Experimental Conditions a. Simulated flue gas composition: NOx = 800 mg / Nm³ 3 CO=5000mg / Nm 3 NH 3 NOx molar ratio = 1.0, O2 = 8 vol%, dust = 10 mg / Nm³ 3 SO2 = 30 mg / Nm 3CO2 = 15 vol%, H2O = 10 vol%, N2 is the balance, inlet flue gas temperature = 180℃, flue gas flow rate = 5500 Nm³ 3 / h.

[0079] b. Operating airspeed: Total volume of SCR catalyst = 1.38 m³ 3 Operating airspeed = 5500 Nm 3 / h÷1.38m 3 =3985h -1 ; Total volume of CO catalyst = 0.567 m³ 3 Operating airspeed = 5500 Nm 3 / h÷0.567m 3 =9700h -1 .

[0080] c. Correction factor k: The reactor shell 1 is provided with a rock wool insulation layer (thickness 50mm), and the thermal conductivity enhancement layer 13 is a graphene thermal conductive film. The value of k is 0.96.

[0081] IV. Calculation of Smoke Temperature Rise S1: Calculate the total heat released by the complete oxidation of CO. ;

[0082] =5500 Nm 3 / h×5000 mg / Nm 3 ×283kJ / mol÷28g / mol×10 -3 =277946 kJ / h; S2: Calculate flue gas mass flow rate ; =5500 Nm 3 / h×1.33 kg / Nm 3 = 7315 kg / h; S3: Substitute into the corrected formula to calculate the theoretical flue gas temperature rise. ; Actual measurement =99.2%, =1.08 kJ / (kg·℃)

[0083] =0.96×277946 kJ / h×99.5%÷7315 Kg / h÷1.06 kJ / (kg·℃)=34.24 ℃.

[0084] V. Experimental Results a. Pollutant removal efficiency, measured: CO removal efficiency 99.5%, NOx removal efficiency 95.5%.

[0085] b. Flue gas temperature rise: Actual measurement: inlet flue gas temperature 180.8℃, outlet flue gas temperature 214.3℃, flue gas temperature rise 33.5℃, calculated value deviates from actual value by 2.2%.

[0086] c. Startup stabilization time: 34 minutes.

[0087] Comparative Example 1: I. Catalyst Module Preparation S1: Preparation of SCR denitrification catalyst module 12: Using V2O5-WO3 / TiO2 system plate catalyst, with a standardized size of 150mm×150mm×150mm; S2: Preparation of CO catalytic oxidation catalyst module 11: Using Pt-Pd dual noble metal supported cordierite honeycomb ceramic catalyst, a standardized module of 150mm×150mm×150mm that is completely consistent with SCR denitrification catalyst module 12 is prepared.

[0088] II. Catalyst Structure Assembly The reactor shell 1 has a square cross-section with dimensions of 1200mm × 1200mm. A catalyst structure with a total thickness of 1050mm is arranged along the flue gas flow direction. The total volume ratio of the SCR denitrification catalyst module 12 to the CO catalytic oxidation catalyst module 11 is 2.7:1. They are arranged in a traditional series. The flue gas first passes through the CO catalyst bed and then through the SCR catalyst bed. Both the CO catalytic oxidation catalyst module 11 and the SCR denitrification catalyst module 12 are arranged in a single layer with dense arrangement and no stepped arrangement. There is no thermally conductive enhancement layer between the modules and no SCR protective layer at the inlet.

[0089] III. Experimental Conditions The simulated flue gas composition and operating space velocity are consistent with those in Example 7. A rock wool insulation layer (50 mm thick) is provided on the reactor shell 1. There is no thermally conductive enhancement layer between the catalyst modules. The correction factor k is 0.88.

[0090] IV. Calculation of Smoke Temperature Rise S1: Calculate the total heat released by the complete oxidation of CO. ;

[0091] =4400 Nm 3 / h×8000 mg / Nm 3 ×283kJ / mol÷28g / mol×10 -3 =355771 kJ / h; S2: Calculate flue gas mass flow rate ; =4400 Nm 3 / h×1.28 kg / Nm 3 = 5632 kg / h; S3: Substitute into the corrected formula to calculate the theoretical flue gas temperature rise. ; Actual measurement =96.2%, =1.08 kJ / (kg·℃)

[0092] =0.88×355771 kJ / h×96.2%÷5632 Kg / h÷1.08 kJ / (kg·℃)=49.52 ℃.

[0093] V. Experimental Results a. Pollutant removal efficiency, measured: CO removal efficiency 96.2%, NOx removal efficiency 92.5%.

[0094] b. Flue gas temperature rise: Actual measurement: inlet flue gas temperature 100.2℃, outlet flue gas temperature 147.4℃, flue gas temperature rise 47.2℃, calculated value deviates from actual value by 4.7%.

[0095] c. Startup stabilization time: 45 minutes.

[0096] Comparative Example 2: I. Catalyst Module Preparation S1: Preparation of SCR denitrification catalyst module 12: A honeycomb catalyst using a V2O5-WO3 / TiO2 system, with a standardized size of 150mm×150mm×200mm; S2: Preparation of CO catalytic oxidation catalyst module 11: Using Pt-CeO2 supported cordierite honeycomb ceramic catalyst, a standardized module of 150mm×150mm×200mm that is completely consistent with SCR denitrification catalyst module 12 is prepared. II. Catalyst Structure Assembly The reactor shell 1 has a square cross-section with dimensions of 1200mm × 1200mm. A catalyst structure with a total thickness of 1350mm is arranged along the flue gas flow direction. The total volume ratio of the SCR denitrification catalyst module 12 to the CO catalytic oxidation catalyst module 11 is 2.43:1. They are arranged in a traditional series. The flue gas first passes through the CO catalyst bed and then through the SCR catalyst bed. Both the CO catalytic oxidation catalyst module 11 and the SCR denitrification catalyst module 12 are arranged in a single layer with dense arrangement and no stepped arrangement. There is no thermally conductive enhancement layer between the modules and no SCR protective layer at the inlet.

[0097] III. Experimental Conditions The simulated flue gas composition and operating space velocity are consistent with those in Example 8. A rock wool insulation layer (50 mm thick) is provided on the reactor shell 1. There is no thermally conductive enhancement layer between the catalyst modules. The correction factor k is 0.88.

[0098] IV. Calculation of Smoke Temperature Rise S1: Calculate the total heat released by the complete oxidation of CO. ;

[0099] =5500Nm 3 / h×5000mg / Nm 3 ×283kJ / mol÷28g / mol×10 -3 =277946kJ / h; S2: Calculate flue gas mass flow rate ; =5500Nm 3 / h×1.33kg / Nm 3 =7315kg / h; S3: Substitute into the corrected formula to calculate the theoretical flue gas temperature rise. ; Actual measurement =95.3%, =1.08 kJ / (kg·℃)

[0100] =0.88×277946kJ / h×95.3%÷7315Kg / h÷1.06kJ / (kg·℃)=30.06℃ V. Experimental Results a. Pollutant removal efficiency, measured: CO removal efficiency 95.3%, NOx removal efficiency 91.2%.

[0101] b. Flue gas temperature rise: Actual measurement: inlet flue gas temperature 180.2℃, outlet flue gas temperature 209℃, flue gas temperature rise 28.8℃, calculated value deviates from actual value by 4.2%.

[0102] c. Startup stabilization time: 48 minutes.

[0103] Where there is no conflict, those skilled in the art can combine the relevant technical features in the above examples according to the actual situation to achieve the corresponding technical effects. Specific details of various combinations are not elaborated here; for components not specifically described, the prior art is used.

[0104] It should be noted that all directional indications (such as up, down, left, right, front, back, etc.) in the embodiments of the present invention are only used to explain the relative positional relationship and movement of each component in a certain specific posture (as shown in the figure). If the specific posture changes, the directional indication will also change accordingly.

[0105] Furthermore, the use of terms such as "first" and "second" in this invention is for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined with "first" or "second" may explicitly or implicitly include at least one of those features.

[0106] The above description is merely a preferred embodiment of the present invention. The present invention is not limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. Any simple modifications, equivalent variations, and alterations made to the above embodiments based on the technical essence of the present invention shall still fall within the scope of the present invention.

Claims

1. A NOx and CO removal reactor, comprising at least a reactor shell (1); a flue gas inlet (2) is provided at the upper part of the reactor shell (1), and a flue gas outlet (10) is provided at the lower part of the shell; characterized in that: It also includes an SCR denitrification catalyst module (12) and a CO catalytic oxidation catalyst module (11) that are independent of each other and have the same external dimensions, and are set inside the reactor shell (1); the two adjacent SCR denitrification catalyst modules (12) are in surface contact with the CO catalytic oxidation catalyst module (11), the SCR denitrification catalyst module (12) or the CO catalytic oxidation catalyst module (11), and are multi-layered catalyst structures.

2. The NOx and CO removal reactor as described in claim 1, characterized in that: The top layer near the flue gas inlet (2) is a pure SCR denitrification catalyst protective layer (3) composed of SCR denitrification catalyst modules (12); each layer below this layer is composed of SCR denitrification catalyst modules (12) and CO catalytic oxidation catalyst modules (11) arranged alternately in a surface contact manner, and the CO catalytic oxidation catalyst modules (11) in the same layer are arranged at intervals, and the CO catalytic oxidation catalyst modules (11) in adjacent layers are arranged vertically and horizontally.

3. The NOx and CO removal reactor as described in claim 2, characterized in that: The thickness of the pure SCR denitrification catalyst protective layer (3) is 100-200 mm, preferably 150 mm.

4. A NOx and CO removal reactor as described in claim 1, 2, or 3, characterized in that: Along the flue gas flow direction from the flue gas inlet (2) to the flue gas outlet (10), the catalyst structure is divided into 6 to 8 levels. The volume ratio of the CO catalytic oxidation catalyst module (11) in each level gradually decreases, while the volume ratio of the SCR denitrification catalyst module (12) gradually increases.

5. A NOx and CO removal reactor as described in claim 4, characterized in that: The ratio of the total volume of the SCR denitrification catalyst module (12) to the total volume of the CO catalytic oxidation catalyst module (11) is 3:1 to 2:1; the operating space velocity of the SCR denitrification catalyst is 2000-4000 h⁻¹. -1 The operating space velocity of the CO catalytic oxidation catalyst is 6000-12000 h⁻¹. -1 .

6. The NOx and CO removal reactor as described in claim 4, characterized in that: The catalyst structure is divided into six levels, including a low-temperature layer (4), a sub-low-temperature layer (5), a medium-low-temperature layer (6), a medium-temperature layer (7), a medium-high-temperature layer (8), and a high-temperature layer (9). The low-temperature layer (4) and the sub-low-temperature layer (5) are arranged with SCR denitrification catalyst modules (12) and CO catalytic oxidation catalyst modules (11) staggered in front, behind, left, and right in the same layer, and the SCR denitrification catalyst modules (12) and CO catalytic oxidation catalyst modules (11) in different layers are arranged vertically. The medium-low-temperature layer (6) and the medium-temperature layer (7) are arranged with an alternating arrangement of multiple SCR denitrification catalyst modules (12) and fewer CO catalytic oxidation catalyst modules (11). The medium-high-temperature layer (8) and the high-temperature layer (9) are arranged with an alternating distribution of multiple SCR denitrification catalyst modules (12) and dispersed CO catalytic oxidation catalyst modules (11), with the CO catalytic oxidation catalyst modules (11) dispersed in the gaps between the SCR denitrification catalyst modules (12).

7. A NOx and CO removal reactor as described in claim 1, 2, 3, 5, or 6, characterized in that: The SCR denitrification catalyst module (12) is a V2O5-WO3 / TiO2 system plate or honeycomb catalyst; the CO catalytic oxidation catalyst module (11) is a cordierite honeycomb ceramic catalyst supported on Pt, Pd, CuO or CeO2; the external dimensions of the SCR denitrification catalyst module (12) and the CO catalytic oxidation catalyst module (11) are both length × width × height = 150mm × 150mm × (150mm~1200mm).

8. A NOx and CO removal reactor as described in claim 1, 2, 3, 5, or 6, characterized in that: The SCR denitrification catalyst module (12) and the CO catalytic oxidation catalyst module (11) are fitted with a thermally conductive enhancement layer (13); the thermally conductive enhancement layer (13) is a graphene thermally conductive film, a metal thermally conductive sheet or a ceramic thermally conductive coating with a thickness of 0.1-1.0 mm. Among them, graphene thermal conductive films with a thermal conductivity ≥1500W / (m·K) are preferred.

9. A method for calculating smoke temperature rise, characterized in that: The NOx and CO removal reactor as described in any one of claims 1-8 is used; the balance calculation of the effective heat released by the CO oxidation reaction and the heat absorbed by the flue gas to raise the flue gas temperature is as follows: Step 1: Obtain flue gas parameters; Flue gas parameters include standard flue gas volumetric flow rate, initial CO concentration in flue gas, enthalpy change of CO oxidation reaction, CO molar mass, standard flue gas average density, actual CO conversion rate, average isobaric specific heat capacity of flue gas, and correction factor. Step 2: Calculate the total heat released by the complete oxidation of CO. ; The following formula is used for calculation: in: The volumetric flow rate of flue gas under standard conditions is expressed in Nm³ / h. The initial CO concentration in the flue gas is expressed in mg / Nm³. 3 ; The enthalpy change for the CO oxidation reaction is taken as -283 kJ / mol; The value is the molar mass of CO, taken as 28 g / mol; Step 3: Calculate the theoretical flue gas temperature rise ; The following corrected formula is used for calculation: ， In the formula: k is a correction factor, with a value ranging from 0.95 to 0.98; This represents the total heat released during the complete oxidation of CO, expressed in kJ / h. This represents the actual CO conversion rate, expressed in % (%). This refers to the flue gas mass flow rate, expressed in kg / h. The average isobaric specific heat capacity of flue gas is expressed in kJ / (kg·℃), with a value ranging from 1.05 to 1.10 kJ / (kg·℃), calculated based on the weighted average of the flue gas components O2, H2O, N2, and CO2. The calculation formula is: in: The standard average density of the flue gas is taken as 1.2-1.4 kg / Nm³. 3 . Step 4: Output theoretical flue gas temperature rise Calculate the deviation between the calculated value and the actual measured value; The calculated value should deviate from the actual measured value by ≤5%.

10. The NOx and CO removal reactor as described in any one of claims 1-8 is applied to the synergistic purification of NOx and CO in low-temperature flue gas in the steel, coking, and waste incineration industries.

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