Organized catalysts, their preparation methods, and methods for simultaneous SOx and NOx removal from flue gas

Abstract

This invention relates to the field of catalytic cracking, and discloses a structured catalyst capable of simultaneously reducing SOx and NOx emissions, its preparation method, and a method for simultaneously removing SOx and NOx from flue gas. The catalyst comprises a structured support and an active component coating distributed on the inner and / or outer surfaces of the structured support. The active metal component contains: 1) 50-95% by weight, based on oxides, one or more metal components selected from rare earth groups and / or group IIA; 2) 5-50% by weight, based on oxides, one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB; and 3) 0.01-2% by weight, based on elements. Using the catalyst provided by this invention can reduce the total amount of active component added and enhance the emission reduction effect of the additives.

Description

Technical Field

[0001] This invention relates to a structured catalyst capable of simultaneously reducing SOx and NOx emissions, its preparation method, and a method for simultaneously removing SOx and NOx from flue gas. Prior Technology

[0002] During catalytic cracking, the reaction of hydrocarbons leads to the deposition of coke on the catalyst, reducing its activity. After the hydrocarbons adsorbed on the catalyst are removed in the stripping section, the coke-containing catalyst is transported to the regenerator. In the regenerator, the coke-containing catalyst comes into full contact with air at high temperatures, burning off the coke on the catalyst surface and restoring its activity. The burning of coke generates SOx and NOx, which are emitted into the air and pollute the atmosphere. With increasingly stringent environmental protection requirements, emission standards for flue gas pollutants are becoming more stringent.

[0003] The main technical measures to reduce NOx emissions from catalytic cracking regeneration flue gas include: regenerator optimization, flue gas aftertreatment, and the use of additives. Post-treatment technologies such as SCR (Sequencing Controlled Reduction) can utilize ammonia injection to reduce NOx, and wet desulfurization technology can utilize alkali injection to absorb SO2, but these require high equipment investment, have high operating costs, and suffer from problems such as ammonia slip and blue smoke tailing. Currently, mainstream desulfurization and denitrification additives mainly remove only one type of flue gas pollutant. For example, CN1334316A discloses a composition containing magnesium aluminum spinel and cerium / vanadium oxides as a sulfur transfer agent for removing SOx from catalytic cracking flue gas. CN101311248B provides a composition capable of reducing NOx emissions from catalytic cracking regeneration flue gas.

[0004] In addition, the above-mentioned processes and patent documents have good removal effects when removing SOx or NOx from regenerated flue gas alone, but cannot remove nitrogen oxides and sulfur oxides at the same time. Summary of the Invention

[0005] The purpose of this invention is to overcome the aforementioned problems in the prior art and provide a structured catalyst capable of simultaneously reducing SOx and NOx emissions, its preparation method, and a method for simultaneously removing SOx and NOx from catalytic cracking regenerated flue gas. Using the catalyst provided by this invention reduces the total amount added and enhances the emission reduction effect of the additives.

[0006] To achieve the above objectives, a first aspect of the present invention provides a structured catalyst capable of simultaneously reducing SOx and NOx emissions. The catalyst comprises a structured support and an active component coating distributed on the inner and / or outer surfaces of the structured support. Based on the total weight of the catalyst, the content of the active component coating is 1-50% by weight. The active component coating contains a matrix and an active metal component. Based on the total weight of the active component coating, the content of the matrix is ​​10-90% by weight, and the content of the active metal component is 10-90% by weight. The active metal component contains: 1) 50-95% by weight, based on oxides, one or more metal components selected from rare earth groups and / or group IIA; 2) 5-50% by weight, based on oxides, one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB; and 3) 0.01-2% by weight, based on elements.

[0007] In this invention, unless otherwise taught, "based on the total weight of the catalyst" means that the total weight of the catalyst is 100% by weight; "based on the total weight of the active component coating" means that the total weight of the active component coating is 100% by weight; and when the composition of the active metal component is involved, it is based on the total weight of the active metal component being 100% by weight.

[0008] A second aspect of this invention provides a method for preparing a structured catalyst capable of simultaneously reducing SOx and NOx emissions, the method comprising the following steps:

[0009] (1) Prepare a solution containing one or more rare earth and / or group IIA metal component precursors and one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB and IIB;

[0010] (2) The solution described in step (1) is subjected to a coprecipitation reaction with a coprecipitant, and then the resulting solid product is dried and calcined to obtain an active metal component precursor;

[0011] (3) Mix the active metal component precursor, matrix source and water to form a slurry, thereby obtaining the active component coating slurry;

[0012] (4) The active component coating slurry is used to coat the regular structure carrier and then dried and calcined to obtain a coating of some active components distributed on the inner and / or outer surfaces of the regular structure carrier, thus obtaining a catalyst semi-finished product;

[0013] (5) Impregnate the catalyst semi-finished product obtained in step (4) with a solution containing a noble metal component precursor, and then dry and / or calcine it to obtain an active component coating distributed on the inner and / or outer surfaces of a regular structured support;

[0014] The amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support in the prepared ordered structure catalyst are such that, based on the total weight of the catalyst, the content of the active component coating is 1-50% by weight, the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating, the content of the matrix is ​​10-90% by weight, the content of the active metal component is 10-90% by weight, and the active metal component contains: 1) 50-95% by weight, based on oxides, of one or more rare earth and / or group IIA metal components; 2) 5-50% by weight, based on oxides, of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB; 3) 0.01-2% by weight, based on elements.

[0015] The present invention provides a method for simultaneously removing SOx and NOx from catalytic cracking regenerated flue gas. The method includes: contacting the catalytic cracking regenerated flue gas with a catalyst under SOx and NOx removal conditions. The catalyst is a structured catalyst capable of simultaneously reducing SOx and NOx emissions as described in the first aspect of the present invention, or a structured catalyst capable of simultaneously reducing SOx and NOx emissions prepared by the preparation method described in the second aspect of the present invention.

[0016] This invention aims to remove SOx and NOx in combination, and develops a novel catalyst for the combined removal of pollutants from flue gas. The structured catalyst provided by this invention, capable of simultaneously reducing SOx and NOx emissions, exhibits high activity in pollutant removal, has a simple preparation method, and can effectively reduce SOx and NOx emissions from catalytic cracking regeneration flue gas. The catalyst provided by this invention is a structured material and can be directly used in flue gas channels. Furthermore, using the catalyst provided by this invention reduces the total amount of additives required, enhances the emission reduction effect of auxiliary agents, and significantly improves the competitiveness of auxiliary agent technology. Simple Explanation of the Diagram

[0017] none Implementation

[0018] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0019] In this invention, the term "regular structure catalyst" refers to a catalyst comprising a regular structure support and an active component coating distributed on the inner and / or outer surfaces of the support; "regular structure support" refers to a support having a regular structure.

[0020] The first aspect of this invention provides a structured catalyst capable of simultaneously reducing SOx and NOx emissions. The catalyst comprises a structured support and an active component coating distributed on the inner and / or outer surfaces of the structured support. Based on the total weight of the catalyst, the active component coating contains 1-50% by weight. The active component coating contains a matrix and an active metal component. Based on the total weight of the active component coating, the matrix contains 10-90% by weight, and the active metal component contains 10-90% by weight. The active metal component comprises: 1) 50-95% by weight, based on oxides, one or more metal components selected from rare earth groups and / or group IIA; 2) 5-50% by weight, based on oxides, one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB; and 3) 0.01-2% by weight, based on elements.

[0021] In the ordered structure catalyst provided by the present invention, specific types and amounts of active components exist in the form of active metal component coatings on the inner and / or outer surfaces of the ordered structure support. The active metals in the coatings have high dispersion, which significantly improves the activity of reducing SOx and NOx.

[0022] According to a preferred embodiment of the present invention, the content of the active component coating is 5-40% by weight, preferably 10-35% by weight, based on the total weight of the catalyst.

[0023] According to the well-structured catalyst provided by the present invention, preferably, based on the total weight of the active component coating, the content of the matrix is ​​40-90% by weight and the content of the active metal component is 10-60% by weight; more preferably, the content of the matrix is ​​50-80% by weight and the content of the active metal component is 20-50% by weight.

[0024] According to the ordered structure catalyst provided by the present invention, preferably, the active metal component contains: 1) 60-90% by weight of a metal component selected from rare earth groups and / or group IIA, based on oxides; 2) 10-40% by weight of a non-precious metal component selected from groups VB, VIIB, VIII, IB and IIB, based on oxides; and 3) 0.02-1.5% by weight of a precious metal component, based on elements.

[0025] More preferably, the active metal component contains: 1) 65-85% by weight of one or more metal components selected from rare earth groups and / or group IIA, based on oxides; 2) 15-35% by weight of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, based on oxides; and 3) 0.03-1.2% by weight of precious metal components, based on elements.

[0026] According to a preferred embodiment of the present invention, the active metal component simultaneously contains rare earth metal components and Group IIA metal components. This preferred embodiment is more advantageous in improving the catalyst's ability to simultaneously remove SOx and NOx from flue gas. More preferably, based on the total amount of the active metal component, the content of the rare earth metal component is 30-80% by weight, more preferably 40-75% by weight; the content of the Group IIA metal component is 5-40% by weight, more preferably 10-30% by weight.

[0027] According to a preferred embodiment of the present invention, the active metal component simultaneously contains one or more non-precious metal components selected from Groups VB, VIII, IB, and IIB, as well as a Group VIIB non-precious metal component. In this preferred embodiment, the catalyst's ability to simultaneously remove SOx and NOx from flue gas is further improved. More preferably, based on the total amount of the active metal component, the content of one or more non-precious metal components from Groups VB, VIII, IB, and IIB is 3-30% by weight, preferably 5-20% by weight; and the content of the Group VIIB non-precious metal component is 3-20% by weight, preferably 5-15% by weight.

[0028] According to a particularly preferred embodiment of the invention, the molar ratio of lanthanum to cobalt is (0.5-15):1, for example (1-10):1, or (1-6):1, (2-5):1, or (2.5-3.5):1, or (2.6-3.4):1, or (2.7-3.3):1, or (2.8-3.2):1, or (2.9-3.1):1, or (2.95-3.05):1. This preferred embodiment is more advantageous in improving the combined removal performance of SOx and NOx by the catalyst.

[0029] In this invention, the content of each component in the structured catalyst was determined by X-ray fluorescence spectroscopy (RIPP experimental method for petrochemical analysis, edited by Yang Cuiding et al., published by Science Press in 1990).

[0030] In this invention, a Siemens D5005 diffractometer was used to perform powder X-ray diffraction (XRD) analysis on the catalyst sample. CuKα (λ = 0.15418 nm) radiation was generated at 40 kV and 40 mA and filtered by Ni. The diffraction signal was recorded in the range of 2θ5~70° with a step size of 0.02°.

[0031] According to the present invention, all conventionally defined rare earth metals can be used in the present invention. In order to further improve the performance of the ordered catalyst in removing SOx and NOx simultaneously, the rare earth metal component is preferably selected from one or more of lanthanum, cerium, tungsten and neodymium, more preferably lanthanum and / or cerium, and even more preferably lanthanum.

[0032] According to the present invention, the group IIA metal component is selected from one or more of beryllium, magnesium, calcium, strontium and barium, preferably magnesium.

[0033] According to the present invention, the Group VB non-precious metal component may be selected from at least one of vanadium, niobium and tantalum; preferably, the Group VIIB non-precious metal component is manganese; the Group VIII non-precious metal component may be selected from at least one of iron, cobalt and nickel; the Group IB non-precious metal component may be copper; and the Group IIB non-precious metal component may be selected from at least one of zinc, cadmium and mercury.

[0034] Preferably, the non-precious metal component selected from groups VB, VIIB, VIII, IB and IIB is selected from manganese, iron, cobalt, nickel, copper, zinc and vanadium, more preferably at least one of cobalt, iron and manganese, even more preferably manganese, as well as cobalt and / or iron, and most preferably manganese and cobalt.

[0035] According to the ordered structure catalyst provided by the present invention, preferably, the noble metal component is selected from one or more of ruthenium, rhodium, rhenium, platinum, palladium, silver, iridium and gold, more preferably from one or more of platinum, palladium and rhodium, and most preferably palladium.

[0036] According to the well-structured catalyst provided by the present invention, preferably, the matrix is ​​selected from at least one of alumina, spinel, perovskite, silica-alumina, zeolite, kaolin, diatomite and perlite, more preferably from at least one of alumina, spinel and perovskite, further preferably from at least one of alumina, spinel and perovskite, and even more preferably from alumina.

[0037] According to the structured catalyst of the present invention, the structured support can be used in a catalyst bed provided in a fixed-bed reactor. The structured support can be a monolithic support block with an internally formed hollow channel structure. A catalyst coating can be distributed on the inner wall of the channels, and the channel space can be used as a fluid flow space. Preferably, the structured support is selected from an integral support with a parallel channel structure open at both ends. The structured support can also be a honeycomb structured support (referred to as a honeycomb support) with a honeycomb-shaped opening in its cross-section.

[0038] According to the ordered structure catalyst of the present invention, preferably, the pore density of the cross-section of the ordered structure carrier is 10-300 pores / square inch, more preferably 20-300 pores / square inch; the porosity of the cross-section of the ordered structure carrier is 20-80%, more preferably 50-80%. The pores can be regular or irregular in shape, and the shapes of the individual pores can be the same or different, and each pore can be one of square, equilateral triangle, regular hexagon, circle, and corrugated.

[0039] In the preferred embodiment of the ordered structure catalyst according to the present invention, the ordered structure support may be selected from at least one of cordierite honeycomb support, mullite honeycomb support, diamond honeycomb support, corundum honeycomb support, zirconium corundum honeycomb support, quartz honeycomb support, nepheline honeycomb support, feldspar honeycomb support, alumina honeycomb support and metal alloy honeycomb support.

[0040] This invention does not exclude the rare earth metal elements, group IIA metal elements, and non-precious metal elements of groups IVB, VB, VIB, VIIB, VIII, IB, and IIB from containing elements other than La, Co, Mg, and Mn, such as Sr, Ca, and Ni.

[0041] According to a particularly preferred embodiment of the present invention, the catalyst comprises a structured support and an active component coating distributed on the inner and / or outer surfaces of the structured support. Based on the total weight of the catalyst, the content of the active component coating is 10-35% by weight. The active component coating contains a matrix and an active metal component. Specifically, based on the total weight of the active component coating, the content of the matrix is ​​50-80% by weight, and the content of the active metal component is 20-50% by weight. The active metal component contains: 1) based on oxides... The composition comprises: 65-85% by weight of one or more metal components selected from rare earth groups and / or group IIA; 2) 15-35% by weight of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB, based on oxides; and 3) 0.03-1.2% by weight of precious metal components, based on elements. The rare earth metal component is lanthanum, the group IIA metal component is magnesium, the non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB are manganese and cobalt, and the precious metal component is palladium. In this particularly preferred embodiment, using La, Co, Mg, Mn, and precious metals as a combination of metal elements can significantly improve the ability to remove SOx and NOx, and the NOx adsorbed by the catalyst can also promote the absorption of SOx by the catalyst.

[0042] In this invention, unless otherwise specified, La as an oxide means La as La₂O₃, Mg as an oxide means MgO, Co as an oxide means Co₂O₃, and Mn as an oxide means MnO.

[0043] A second aspect of this invention provides a method for preparing a structured catalyst capable of simultaneously reducing SOx and NOx emissions, the method comprising the following steps:

[0044] (1) Prepare a solution containing one or more rare earth and / or group IIA metal component precursors and one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB and IIB;

[0045] (2) The solution described in step (1) is subjected to a coprecipitation reaction with a coprecipitant, and then the resulting solid product is dried and calcined to obtain an active metal component precursor;

[0046] (3) Mix the active metal component precursor, matrix source and water to form a slurry, thereby obtaining the active component coating slurry;

[0047] (4) The active component coating slurry is used to coat the regular structure carrier and then dried and calcined to obtain a coating of some active components distributed on the inner and / or outer surfaces of the regular structure carrier, thus obtaining a catalyst semi-finished product;

[0048] (5) Impregnate the catalyst semi-finished product obtained in step (4) with a solution containing a noble metal component precursor, and then dry and / or calcine it to obtain an active component coating distributed on the inner and / or outer surfaces of a regular structured support;

[0049] The amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support in the prepared ordered structure catalyst are such that, based on the total weight of the catalyst, the content of the active component coating is 1-50% by weight, the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating, the content of the matrix is ​​10-90% by weight, the content of the active metal component is 10-90% by weight, and the active metal component contains: 1) 50-95% by weight, based on oxides, of one or more rare earth and / or group IIA metal components; 2) 5-50% by weight, based on oxides, of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB; 3) 0.01-2% by weight, based on elements.

[0050] According to the preparation method provided by the present invention, the specific range of selection for rare earth metal components, group IIA metal components, one or more non-precious metal components of groups VB, VIIB, VIII, IB and IIB, as well as precious metal components, matrix and regular structure carrier is as described in the first aspect above, and will not be repeated here.

[0051] Preferably, the matrix source is a substance that can be transformed into a matrix under the calcination conditions in step (4). Those skilled in the art can make appropriate selections based on the types of matrices described above, and the present invention does not have any particular limitations in this regard. When the matrix is ​​preferably alumina, the matrix source can be a precursor of alumina, for example, the matrix source is selected from at least one of gibbsite, boehmite, diaspore, boehmite, and pseudoboehmite, with pseudoboehmite being the most preferred.

[0052] According to the method provided by the present invention, when the matrix is ​​alumina, preferably, the matrix source is subjected to an acidification and sol-gel treatment before pulping. The acidification and sol-gel treatment can be carried out according to conventional techniques in the art. More preferably, the acid used in the acidification and sol-gel treatment is hydrochloric acid.

[0053] The present invention has a wide range of options for the acidification and sol-gel treatment conditions. Preferably, the acidification and sol-gel treatment conditions include: an acid-aluminum ratio of 0.12-0.22:1 and a time of 10-40 min.

[0054] In this invention, unless otherwise specified, the acid-aluminum ratio refers to the mass ratio of hydrochloric acid (calculated as 36% by weight of concentrated hydrochloric acid) to the mass of alumina precursor (calculated on a dry basis).

[0055] According to the present invention, preferably, the precursors containing one or more rare earth and / or group IIA metal components and the precursors containing one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB can each be independently selected from water-soluble salts of the respective metal components, such as nitrates, chlorides, chlorates, or sulfates, preferably nitrates and / or chlorides. In particular, the precursor for manganese can be potassium permanganate and / or manganese chloride.

[0056] The present invention does not particularly limit the method for obtaining the solution in step (1), as long as the precursors of each metal component are mixed evenly. For example, the precursors of each metal component can be dissolved in water and stirred thoroughly.

[0057] According to a preferred embodiment of the present invention, the amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursor, and ordered structure support are such that, based on the total weight of the catalyst, the content of the active component coating in the prepared ordered structure catalyst is 5-40% by weight, and the active component coating contains a matrix and an active metal component, wherein the active component... Based on the total weight of the coating, the matrix content is 40-90% by weight, the active metal component content is 10-60% by weight, and the active metal component contains: 1) 60-90% by weight of one or more metal components selected from rare earth groups and / or group IIA, calculated as oxides; 2) 10-40% by weight of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, calculated as oxides; 3) 0.02-1.5% by weight of precious metal components, calculated as elements.

[0058] More preferably, the amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and structured support are such that, based on the total weight of the catalyst, the content of the active component coating in the prepared structured catalyst is 10-35% by weight, and the active component coating contains a matrix and an active metal component, wherein, based on the active component coating... Based on the total weight, the content of the matrix is ​​50-80% by weight, the content of the active metal component is 20-50% by weight, and the active metal component contains: 1) 65-85% by weight of one or more metal components selected from rare earth groups and / or group IIA, calculated as oxides; 2) 15-35% by weight of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, calculated as oxides; 3) 0.03-1.2% by weight of precious metal components, calculated as elements.

[0059] According to the method provided by the present invention, the method for providing the active metal component precursor can be a co-precipitation method or a sol-gel method, with the co-precipitation method being more preferred. However, it should be understood that the sol-gel method is also within the scope of protection of the present invention.

[0060] The type and amount of the coprecipitant described in this invention can be selected according to conventional techniques, as long as the coprecipitation reaction proceeds smoothly. The type of coprecipitant can be a conventional choice in the art; preferably, the coprecipitant is a carbonate, more preferably selected from at least one of ammonium carbonate, potassium carbonate, and sodium carbonate, and even more preferably ammonium carbonate.

[0061] In step (2), the coprecipitant can be introduced in solution form to coprecipitate with the solution. This invention does not particularly limit the concentration of the solution and the coprecipitant solution, as long as the solution concentration is less than the solubility when the solution is provided, thereby ensuring that the coprecipitation reaction can occur sufficiently.

[0062] Preferably, the coprecipitation reaction is carried out at a pH of 8-10, preferably 8.5-9.5. The pH of the coprecipitation reaction can be adjusted by adding acid and / or alkali, and there is no particular limitation on the specific type; for example, ammonia can be used. The present invention does not particularly limit the temperature of the coprecipitation reaction, and it can be carried out at room temperature.

[0063] The method provided by the present invention further includes solid-liquid separation of the reaction product obtained by the coprecipitation reaction (e.g., by filtration or centrifugation) to obtain the solid product.

[0064] Preferably, the roasting conditions in step (2) include: a temperature of 300-800℃ and a time of 1-8 h.

[0065] In this invention, preferably, the solid content of the active component coating slurry in step (3) is 5-45% by weight.

[0066] According to the method provided by the present invention, there are no particular limitations on the method of mixing and pulping the active metal component precursor, matrix source and water, nor are there any limitations on the order of adding the active metal component precursor, matrix source and water. As long as the active metal component precursor, matrix source and water are brought into contact and then pulped to obtain the slurry, it is acceptable.

[0067] In this invention, the content of the active component coating can be adjusted by adjusting the parameters in the coating process, for example, by adjusting the amount of active component coating slurry and regularized structure carrier used in the coating process.

[0068] The coating method provided by this invention can involve applying an active component coating slurry to the inner and / or outer surfaces of a structured carrier using various coating methods. The coating method can be a water-based coating, an immersion coating, or a spray coating. Specific coating operations can be performed according to the method described in CN1199733C. Preferably, the coating is performed using a water-based coating method. During the coating process, one end of the structured carrier is immersed in the active component coating slurry, while a vacuum is applied to the other end, allowing the active component coating slurry to continuously pass through the pores of the structured carrier. The volume of the active component coating slurry passing through the pores of the structured carrier can be 2-20 times the volume of the structured carrier, the applied vacuum pressure can be -0.1 MPa to -0.01 MPa, the coating temperature can be 10-70℃, and the coating time can be 0.1-300 seconds. The structured carrier coated with the active component coating slurry is then dried and calcined to obtain a coating of partially active components distributed on the inner and / or outer surfaces of the structured carrier, resulting in a catalyst semi-finished product. The coating of the partially active components refers to the catalyst semi-finished product obtained in this stage that does not contain precious metal active components, so it is recorded as a coating of partially active components. After the impregnation in step (5) is completed, it is then dried and / or calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the regular structure carrier.

[0069] In step (5) of this invention, the impregnated material may be dried only, or the impregnated material may be roasted only, or the impregnated material may be dried and then roasted. This invention does not have a particular limitation on these methods, but it is preferred that the impregnated material be dried and then roasted. This invention does not have a particular limitation on the roasting conditions in step (5), and they can be carried out according to conventional techniques in the art. For example, the roasting in step (5) can be carried out in air or an inert atmosphere (e.g., nitrogen). This invention does not have a particular limitation on the roasting conditions in step (5), but preferably includes: a temperature of 300-700℃ and a time of 0.1-5 h.

[0070] The present invention does not particularly limit the drying conditions described in steps (2), (4) and (5), and can be carried out in accordance with conventional technical means in the field. For example, the drying conditions described in steps (2), (4) and (5) can each independently include: a temperature of 60-200℃ and a time of 2-10 h.

[0071] According to the present invention, there is no particular limitation on the impregnation described in step (5), and it can be carried out according to conventional techniques in the art. Those skilled in the art can obtain the specific noble metal content in the catalyst through impregnation. The impregnation described in the present invention can be saturated impregnation or excessive impregnation.

[0072] According to the present invention, preferably, in step (5), the noble metal component precursor is hydrolyzed in an acid solution to provide the solution. Specifically, after the hydrolysis, the solution may be diluted (by adding water) or concentrated (by evaporation) before the impregnation is performed to provide a catalyst with a specific noble metal component loading.

[0073] Preferably, the acid is selected from water-soluble inorganic acids and / or organic acids, and more preferably from at least one of hydrochloric acid, nitric acid, phosphoric acid and acetic acid.

[0074] According to the present invention, preferably, the amount of acid used is such that the pH value of the impregnation solution is less than 6.0, more preferably less than 5.0. This preferred embodiment is more conducive to the uniform dispersion of the active component and improves the wear resistance of the finished catalyst.

[0075] The present invention provides a method for obtaining the solid product by filtering the mixture obtained after impregnation. The filtration can be performed using conventional techniques in the art.

[0076] This invention, in cooperation with a manufacturer, provides a method for simultaneously removing SOx and NOx from catalytic cracking regenerated flue gas. The method includes: contacting the catalytic cracking regenerated flue gas with a catalyst under SOx and NOx removal conditions. The catalyst is either a structured catalyst capable of simultaneously reducing SOx and NOx emissions as described in the first aspect of this invention, or a structured catalyst capable of simultaneously reducing SOx and NOx emissions prepared by the method described in the second aspect. The catalyst provided by this invention is particularly suitable for treating catalytic cracking regenerated flue gas containing both SOx and NOx.

[0077] The present invention allows for a wide selection range of SOx and NOx contents in the catalytic cracking regeneration flue gas; the simultaneous presence of both SOx and NOx is beneficial for their removal. Preferably, the SOx content in the catalytic cracking regeneration flue gas is 0.001-0.5% by volume, and the NOx content is 0.001-0.3% by volume; more preferably, the SOx content in the catalytic cracking regeneration flue gas is 0.002-0.2% by volume, and the NOx content is 0.002-0.2% by volume.

[0078] Preferably, the volume ratio of SOx to NOx in the flue gas is 1-1.4:1, more preferably 1-1.2:1. This preferred embodiment is more conducive to improving the removal efficiency of both.

[0079] In this invention, the catalytic cracking regeneration flue gas may also contain gases other than SOx and NOx, including but not limited to CO, CO2 and H2O.

[0080] According to the method provided by the present invention, preferably, the contact conditions include: a temperature of 300-1000℃, a reaction pressure of 0-0.5 MPa (gauge pressure), and a catalytic cracking regeneration flue gas volume hourly space velocity of 200-20000 h⁻¹; more preferably, a temperature of 450-750℃, a reaction pressure of 0.05-0.3 MPa (gauge pressure), and a catalytic cracking regeneration flue gas volume hourly space velocity of 1000-10000 h⁻¹.

[0081] According to the method provided by the present invention, preferably, the contact is carried out in a flue gas channel provided after the cyclone separator and / or after the CO incinerator. During complete regeneration, the flue gas after the cyclone separator at the regenerator outlet has high SOx and NOx concentrations and low catalyst fine particulate matter content. High temperature is conducive to improving the reaction conversion rate, and low particulate matter content makes it less likely to clog the channels. Therefore, preferably, the contact between the fully regenerated flue gas and the catalyst is carried out in a flue gas channel provided after the cyclone separator to simultaneously catalytically convert SOx and NOx. During incomplete regeneration, due to the low excess oxygen content and high CO concentration in the flue gas, the NOx concentration in the flue gas at the regenerator outlet is very low, while the concentration of reduced nitrogen compounds such as NH3 and HCN is relatively high. These reduced nitrogen compounds flow downstream with the flue gas and, if fully oxidized in the CO incinerator used for energy recovery, generate NOx. Therefore, preferably, the contact between the incompletely regenerated flue gas and the catalyst is carried out in a flue gas channel provided after the CO incinerator and / or after the CO incinerator to simultaneously catalytically convert SOx and NOx.

[0082] The present invention does not particularly limit the CO incinerator, and various CO incinerators conventionally used in the art can be used, such as vertical CO incinerators or horizontal CO incinerators.

[0083] In this invention, the cyclone separator is preferably a three-stage cyclone separator.

[0084] In a preferred embodiment, the structured catalyst exists in the form of a catalyst bed. In the method provided by this invention, the structured catalyst can be set as a fixed catalyst bed in the flue gas channel after the cyclone separator and / or after the CO incinerator. The flowing catalytic cracking regeneration flue gas can flow through the structured catalyst bed, that is, it can flow through the pores within the structured carrier, and react with the active component coating distributed on the pore walls.

[0085] The present invention also provides the following technical solutions:

[0086] 1. A structured catalyst capable of simultaneously reducing SOx and NOx emissions, the catalyst comprising a structured support and an active component coating distributed on the inner and / or outer surfaces of the structured support, wherein, based on the total weight of the catalyst, the content of the active component coating is 1-50% by weight, the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating, the content of the matrix is ​​10-90% by weight, the content of the active metal component is 10-90% by weight, the active metal component contains: 1) 50-95% by weight, based on oxides, one or more metal components selected from rare earth groups and / or group IIA; 2) 5-50% by weight, based on oxides, one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB; 3) 0.01-2% by weight, based on elements.

[0087] 2. The structured catalyst according to any one of the foregoing technical solutions, wherein,

[0088] Based on the total weight of the catalyst, the content of the active component coating is 5-40% by weight;

[0089] And / or, based on the total weight of the active component coating, the content of the matrix is ​​40-90% by weight, and the content of the active metal component is 10-60% by weight;

[0090] And / or, the active metal component contains: 1) 60-90% by weight, based on oxides, one or more metal components selected from rare earth groups and / or group IIA; 2) 10-40% by weight, based on oxides, one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB; 3) 0.02-1.5% by weight, based on elements;

[0091] Preferably,

[0092] Based on the total weight of the catalyst, the content of the active component coating is 10-35% by weight;

[0093] And / or, based on the total weight of the active component coating, the content of the matrix is ​​50-80% by weight, and the content of the active metal component is 20-50% by weight;

[0094] And / or, the active metal component contains: 1) 65-85% by weight of one or more metal components selected from rare earth groups and / or group IIA, based on oxides; 2) 15-35% by weight of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, based on oxides; and 3) 0.03-1.2% by weight of precious metal components, based on elements.

[0095] 3. The well-structured catalyst according to any one of the foregoing technical solutions, wherein the matrix is ​​selected from at least one of alumina, spinel, perovskite, silica-alumina, zeolite, kaolin, diatomite, and perlite, preferably selected from at least one of alumina, spinel, and perovskite, and more preferably alumina;

[0096] Preferably, the regular structure carrier is selected from an integral carrier with a parallel channel structure open at both ends;

[0097] Preferably, the pore density of the cross-section of the regular structure carrier is 10-300 pores / square inch, and the porosity is 20-80%.

[0098] Preferably, the regular structure carrier is selected from at least one of cordierite honeycomb carrier, mullite honeycomb carrier, diamond honeycomb carrier, corundum honeycomb carrier, zirconium corundum honeycomb carrier, quartz honeycomb carrier, nepheline honeycomb carrier, feldspar honeycomb carrier, alumina honeycomb carrier, and metal alloy honeycomb carrier.

[0099] 4. The well-structured catalyst according to any one of the foregoing technical solutions, wherein,

[0100] The rare earth metal component is selected from one or more of lanthanum, cerium, tungsten, and neodymium, preferably lanthanum and / or cerium, and more preferably lanthanum;

[0101] The group IIA metal component is selected from one or more of beryllium, magnesium, calcium, strontium, and barium, preferably magnesium;

[0102] The non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB are selected from manganese, iron, cobalt, nickel, copper, zinc, and vanadium, preferably at least one of cobalt, iron, and manganese, more preferably manganese, and cobalt and / or iron, and even more preferably manganese and cobalt;

[0103] The precious metal component is selected from one or more of ruthenium, rhodium, rhenium, platinum, palladium, silver, iridium and gold, preferably one or more of platinum, palladium and rhodium, and more preferably palladium.

[0104] 5. The well-structured catalyst according to any one of the foregoing technical solutions, wherein, based on the total amount of the active metal components, the ratio of the content of one or more metal components selected from rare earth groups and / or groups IIA to the content of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, based on oxides, is 1-8, preferably 1.5-6, more preferably 2-4.

[0105] 6. The well-structured catalyst according to any one of the foregoing technical solutions, wherein,

[0106] The active metal component contains or consists of the following components:

[0107] 1a) Based on oxides, a metallic component selected from one or more rare earth elements; preferably, lanthanum;

[0108] 1b) Based on oxides, one or more metallic components selected from Group IIA; preferably, magnesium;

[0109] 2a) Based on oxides, one or more non-precious metal components selected from groups VB, VIII, IB, and IIB; preferably, cobalt;

[0110] 2b) Based on oxides, one or more non-precious metal components selected from Group VIIB; preferably, manganese;

[0111] 3) Selected from one or more of platinum, palladium and rhodium, based on the element; preferably, palladium.

[0112] 7. The structured catalyst according to technical solution 6, wherein, based on the total amount of the active metal component (100% by weight),

[0113] The content of 1a) is 30-80% by weight, for example, 35-75% by weight, or 40-70% by weight.

[0114] The content of 1b) is 5-40% by weight, for example 10-30% by weight.

[0115] The content of 2a) is 5-40% by weight, for example 3-30% by weight, or 5-20% by weight.

[0116] The content of 2b) is 3-20% by weight, for example 5-15% by weight.

[0117] c) The content is 0.01-0.2% by weight.

[0118] 8. The structured catalyst according to technical solution 6, wherein,

[0119] The molar ratio of lanthanum to cobalt is (0.5-15):1, for example (1-10):1, or (1-6):1, (2-5):1, or (2.5-3.5):1, or (2.6-3.4):1, or (2.7-3.3):1, or (2.8-3.2):1, or (2.9-3.1):1, or (2.95-3.05):1.

[0120] 9. The catalyst according to any one of the foregoing technical solutions, wherein the catalyst has characteristic peaks in the powder XRD spectrum at 2θ = 33.0°±0.1°, 33.5°±0.1° and 47.5°±0.1° and at 27.0°±0.1°, 28.0°±0.1° and 39.5°±0.1°.

[0121] 10. The catalyst according to any one of the foregoing technical solutions, wherein the catalyst has been treated by exposure to an atmosphere containing SO2;

[0122] For example, the catalyst is treated by exposure to an atmosphere containing SO2 at a temperature of 350-1000°C, a pressure of 0-8 MPa, and a SO2 content of 0.001-100% by volume; or

[0123] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 400-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0124] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 450-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0125] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 500-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0126] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 550-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0127] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 600-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0128] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 650-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0129] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 400-800℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0130] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 450-800℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0131] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 500-800℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0132] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 550-800℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0133] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 600-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0134] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 650-900℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0135] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 400-750°C, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0136] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 450-750°C, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0137] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 500-750°C, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0138] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 550-750°C, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0139] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 600-750℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0140] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 650-750°C, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0141] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 400-700℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0142] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 450-700℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0143] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 500-700℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0144] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 550-700℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0145] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 600-700℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0146] The catalyst is treated by exposure to an atmosphere containing SO2 for at least 1 minute, wherein the temperature of the SO2-containing atmosphere is 650-700℃, the pressure is 0-5 MPa, and the SO2 content is 0.001-5% by volume; or

[0147] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 400-900℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0148] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 450-900℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0149] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 500-900℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0150] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 550-900℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0151] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 600-900℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0152] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 650-900℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0153] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 400-800℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0154] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 450-800℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0155] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 500-800℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0156] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 550-800℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0157] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 600-800℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0158] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 650-800℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0159] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 400-750℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0160] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 450-750℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0161] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 500-750℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0162] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 550-750℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0163] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 600-750℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0164] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 650-750℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0165] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 400-700℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0166] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 450-700℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0167] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 500-700℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0168] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 550-700℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0169] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 600-700℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0170] The catalyst is treated by exposure to an atmosphere containing SO2 for 30-480 minutes, wherein the temperature of the SO2-containing atmosphere is 650-700℃, the pressure is 0-2 MPa, and the SO2 content is 0.01-1% by volume; or

[0171] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 400-900℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0172] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 450-900℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0173] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 500-900℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0174] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 550-900℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0175] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 600-900℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0176] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 650-900℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0177] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 400-800℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0178] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 450-800℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0179] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 500-800℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0180] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 550-800℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0181] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 600-800℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0182] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 650-800℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0183] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 400-750℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0184] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 450-750℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0185] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 500-750℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0186] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 550-750℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0187] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 600-750℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0188] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 650-750℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0189] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 650-750℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0190] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 400-700℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0191] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 450-700℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0192] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 500-700℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0193] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 550-700℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0194] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2-containing atmosphere is 600-700℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume; or

[0195] The catalyst is treated by exposure to an atmosphere containing SO2 for 60-120 minutes, wherein the temperature of the SO2 atmosphere is 650-700℃, the pressure is 0-0.5 MPa, and the SO2 content is 0.02-0.5% by volume.

[0196] 11. The catalyst according to any one of the foregoing technical solutions, wherein the catalyst is treated by exposure to an atmosphere containing SO2, and the catalyst has characteristic peaks in the powder XRD spectrum at 2θ = 28.6° ± 0.1°, 30.0° ± 0.1° and 50.4° ± 0.1°.

[0197] 12. A method for preparing a structured catalyst capable of simultaneously reducing SOx and NOx emissions, the method comprising the following steps:

[0198] (1) Prepare a solution containing one or more rare earth and / or group IIA metal component precursors and one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB and IIB;

[0199] (2) The solution described in step (1) is subjected to a coprecipitation reaction with a coprecipitant, and then the resulting solid product is dried and calcined to obtain an active metal component precursor;

[0200] (3) Mix the active metal component precursor, matrix source and water to form a slurry, thereby obtaining the active component coating slurry;

[0201] (4) The active component coating slurry is used to coat the regular structure carrier and then dried and calcined to obtain a coating of some active components distributed on the inner and / or outer surfaces of the regular structure carrier, thus obtaining a catalyst semi-finished product;

[0202] (5) Impregnate the catalyst semi-finished product obtained in step (4) with a solution containing a noble metal component precursor, and then dry and / or calcine it to obtain an active component coating distributed on the inner and / or outer surfaces of a regular structured support;

[0203] The amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support in the prepared ordered structure catalyst are such that, based on the total weight of the catalyst, the content of the active component coating is 1-50% by weight, the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating, the content of the matrix is ​​10-90% by weight, the content of the active metal component is 10-90% by weight, and the active metal component contains: 1) 50-95% by weight, based on oxides, of one or more rare earth and / or group IIA metal components; 2) 5-50% by weight, based on oxides, of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB; 3) 0.01-2% by weight, based on elements.

[0204] 13. The preparation method according to any one of the foregoing technical solutions, wherein the amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB and IIB, matrix source, precious metal component precursors and regular structure support are such that, based on the total weight of the catalyst, the content of the active component coating in the prepared regular structure catalyst is 5-40% by weight, and the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the catalyst, the content of the active component coating is 5-40% by weight, and the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the catalyst, the content of the active component coating is 5-40% by weight. Based on the total weight of the active component coating, the matrix content is 40-90% by weight, the active metal component content is 10-60% by weight, and the active metal component contains: 1) 60-90% by weight of one or more metal components selected from rare earth groups and / or group IIA, calculated as oxides; 2) 10-40% by weight of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB, calculated as oxides; and 3) 0.02-1.5% by weight of precious metal components, calculated as elements.

[0205] Preferably,

[0206] The amount of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support used in the prepared ordered structure catalyst is such that, based on the total weight of the catalyst, the content of the active component coating is 10-35% by weight, and the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating... Based on this, the content of the matrix is ​​50-80% by weight, the content of the active metal component is 20-50% by weight, and the active metal component contains: 1) 65-85% by weight of one or more metal components selected from rare earth groups and / or group IIA, based on oxides; 2) 15-35% by weight of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, based on oxides; and 3) 0.03-1.2% by weight of precious metal components, based on elements.

[0207] 14. The preparation method according to any one of the foregoing technical solutions, wherein the amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB and IIB, matrix source, precious metal component precursors and regular structure support are such that the prepared regular structure catalyst contains...

[0208] Based on the total amount of the active metal components, the ratio of the content of one or more metal components selected from rare earth groups and / or groups IIA to the content of one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, calculated as oxides, is 1-8, preferably 1.5-6, and more preferably 2-4.

[0209] 15. The preparation method according to any one of the foregoing technical solutions, wherein the amounts of one or more rare earth and / or group IIA metal component precursors, one or more non-precious metal component precursors selected from groups VB, VIIB, VIII, IB and IIB, matrix source, precious metal component precursors and regular structure support are such that the prepared regular structure catalyst contains...

[0210] The active metal component contains or consists of the following components:

[0211] 1a) Based on oxides, a metallic component selected from one or more rare earth elements; preferably, lanthanum;

[0212] 1b) Based on oxides, one or more metallic components selected from Group IIA; preferably, magnesium;

[0213] 2a) Based on oxides, one or more non-precious metal components selected from groups VB, VIII, IB, and IIB; preferably, cobalt;

[0214] 2b) Based on oxides, one or more non-precious metal components selected from Group VIIB; preferably, manganese;

[0215] 3) Selected from one or more of platinum, palladium, and rhodium, based on elemental composition; preferably, palladium;

[0216] Preferably, based on the total amount of the active metal component (100% by weight),

[0217] The content of 1a) is 30-80% by weight, for example, 35-75% by weight, or 40-70% by weight.

[0218] The content of 1b) is 5-40% by weight, for example 10-30% by weight.

[0219] The content of 2a) is 5-40% by weight, for example 3-30% by weight, or 5-20% by weight.

[0220] The content of 2b) is 3-20% by weight, for example 5-15% by weight.

[0221] c) The content is 0.01-0.2% by weight; and / or

[0222] Preferably, the molar ratio of lanthanum to cobalt is (0.5-15):1, for example (1-10):1, or (1-6):1, (2-5):1, or (2.5-3.5):1, or (2.6-3.4):1, or (2.7-3.3):1, or (2.8-3.2):1, or (2.9-3.1):1, or (2.95-3.05):1.

[0223] 16. The preparation method according to any one of the foregoing technical solutions, wherein the matrix source is a substance that can be transformed into a matrix under the calcination conditions in step (4);

[0224] The matrix is ​​selected from at least one of alumina, spinel, perovskite, silica-alumina, zeolite, kaolin, diatomite, and perlite, preferably from at least one of alumina, spinel, and perovskite, and more preferably from alumina;

[0225] Preferably, the regular structure carrier is selected from an integral carrier with a parallel channel structure open at both ends;

[0226] Preferably, the pore density of the cross-section of the regular structure carrier is 10-300 pores / square inch, and the porosity is 20-80%.

[0227] Preferably, the regular structure carrier is selected from at least one of cordierite honeycomb carrier, mullite honeycomb carrier, diamond honeycomb carrier, corundum honeycomb carrier, zirconium corundum honeycomb carrier, quartz honeycomb carrier, nepheline honeycomb carrier, feldspar honeycomb carrier, alumina honeycomb carrier, and metal alloy honeycomb carrier.

[0228] 17. The preparation method according to any one of the foregoing technical solutions, wherein,

[0229] The rare earth metal component is selected from one or more of lanthanum, cerium, tungsten, and neodymium, preferably lanthanum and / or cerium, and more preferably lanthanum;

[0230] The group IIA metal component is selected from one or more of beryllium, magnesium, calcium, strontium, and barium, preferably magnesium;

[0231] The non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB are selected from manganese, iron, cobalt, nickel, copper, zinc, and vanadium, preferably at least one of cobalt, iron, and manganese, more preferably manganese, and cobalt and / or iron, and even more preferably manganese and cobalt;

[0232] The precious metal component is selected from one or more of ruthenium, rhodium, rhenium, platinum, palladium, silver, iridium and gold, preferably one or more of platinum, palladium and rhodium, and more preferably palladium.

[0233] 18. The preparation method according to any one of the foregoing technical solutions, wherein the precursor containing one or more rare earth group and / or group IIA metal components and the precursor containing one or more non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB are each independently selected from the nitrates and / or chlorides of their respective metal components;

[0234] Preferably, the coprecipitant is a carbonate, and more preferably, it is selected from at least one of ammonium carbonate, potassium carbonate, and sodium carbonate;

[0235] Preferably, the coprecipitation reaction is carried out at a pH of 8-10;

[0236] Preferably, the roasting conditions in step (2) include: a temperature of 300-800℃ and a time of 1-8 h.

[0237] 19. The preparation method according to any one of the foregoing technical solutions, wherein the solid content of the active component coating slurry in step (3) is 5-45% by weight;

[0238] Preferably, the calcination conditions in step (4) include: a temperature of 300-800℃ and a time of 1-5 h;

[0239] Preferably, in step (5), the noble metal component precursor is hydrolyzed in an acid solution to provide the solution;

[0240] Preferably, the acid is selected from water-soluble inorganic acids and / or organic acids, and more preferably from at least one of hydrochloric acid, nitric acid, phosphoric acid, and acetic acid;

[0241] Preferably, the amount of acid used is such that the pH value of the impregnation solution is less than 6.0, more preferably less than 5.0;

[0242] Preferably, the roasting conditions in step (5) include: a temperature of 300-700℃ and a time of 0.1-5 h.

[0243] 20. A method for simultaneously removing SOx and NOx from catalytic cracking regenerated flue gas, the method comprising: contacting the catalytic cracking regenerated flue gas with a catalyst under SOx and NOx removal conditions, wherein the catalyst is a structured catalyst capable of simultaneously reducing SOx and NOx emissions according to any one of the foregoing technical solutions, or a structured catalyst capable of simultaneously reducing SOx and NOx emissions prepared according to any one of the foregoing technical solutions;

[0244] Preferably, the contact between the catalytic cracking regenerated flue gas and the structured catalyst takes place in a flue gas channel located after the catalytic cracking cyclone separator and / or after the CO incinerator;

[0245] Preferably, the contact conditions include: a temperature of 300-1000℃, for example 500-800℃, or 600-750℃, or 625-750℃, or 650-750℃, or 675-750℃, or 700-750℃, or 725-750℃, or 600-725℃, or 625-725℃, or 650-725℃, or 6 75-725℃, or 700-725℃, or 600-700℃, or 625-700℃, or 650-700℃, or 675-700℃, or 600-675℃, or 625-675℃, or 650-675℃, or 600-650℃, or 625-650℃, or 600-625℃, with a gauge pressure of 0-4 MPa, for example 0.01-4 MPa, or 0.02-4 MPa, or 0-0.5 MPa; the volume hourly space velocity of the catalytic cracking regeneration flue gas is 100-50000 h⁻¹ or 200-20000 h⁻¹, 500-10000 h⁻¹, 1000-5000 h⁻¹, for example, the volume hourly space velocity of the catalytic cracking regeneration flue gas is 200-20000 h⁻¹.

[0246] 21. A method for simultaneously removing SOx and NOx from flue gas, the method comprising: contacting the flue gas with a catalyst under SOx and NOx removal conditions, wherein the catalyst is a catalyst according to any one of the foregoing technical solutions or a catalyst prepared according to any one of the foregoing technical solutions;

[0247] Preferably, the flue gas contains both SOx and NOx at certain concentrations, including but not limited to catalytic cracking regeneration flue gas;

[0248] Preferably, the volume fractions of SOx and NOx in the flue gas are 1~3000 μL / L, and the molar ratio of SOx to NOx is 0.5:1-2:1;

[0249] Preferably, the contact conditions include: a temperature of 300-1000℃, for example 500-800℃, or 600-750℃, or 625-750℃, or 650-750℃, or 675-750℃, or 700-750℃, or 725-750℃, or 600-725℃, or 625-725℃, or 650-725℃, or 6 The temperature ranges from 75-725℃, or 700-725℃, or 600-700℃, or 625-700℃, or 650-700℃, or 675-700℃, or 600-675℃, or 625-675℃, or 650-675℃, or 600-650℃, or 625-650℃, or 600-625℃. The reaction pressure, measured in gauge pressure, is 0-4 MPa, for example, 0.01-4 MPa, or 0.02-4 MPa, or 0-0.5 MPa. The volume hourly space velocity (VHSV) of the flue gas is 100-50000 h⁻¹ or 200-20000 h⁻¹, 500-10000 h⁻¹, or 1000-5000 h⁻¹. For example, the VHSV of the catalytic cracking regeneration flue gas is 200-20000 h⁻¹.

[0250] In this invention, there are no particular limitations on the calcination conditions. For example, calcination can be carried out in air or an inert atmosphere (e.g., nitrogen); the calcination conditions can be: a temperature of 300-900°C, for example, a temperature range consisting of any two of 400, 500, 600, 700, 800°C, and these values; and a time of 0.1-12 h, for example, 0.1-5 h. The pressure can be below atmospheric pressure, atmospheric pressure, or above atmospheric pressure (e.g., 0-5 MPa).

[0251] In this invention, the drying conditions are not particularly limited. For example, the drying conditions can be: a temperature of 25-250°C, a time of 0.1-12 hours, and a pressure of vacuum (e.g., absolute pressure 0-1 kPa, 0-5 kPa, 0-10 kPa, 0-20 kPa, 0-30 kPa, 0-40 kPa, 0-50 kPa, 0-60 kPa, 0-70 kPa, 0-80 kPa, 0-90 kPa, 0-100 kPa) or atmospheric pressure (absolute pressure 0.1 MPa). In this invention, when performing the operation of drying followed by calcination, the drying temperature is lower than the calcination temperature.

[0252] In this invention, unless otherwise specified, ppm refers to volume concentration.

[0253] In this invention, SOx refers to a mixture of sulfur oxides (e.g., a mixture of SO2 and SO3, the molar ratio of which is not particularly limited, such as 1:10 to 10:1), and NOx refers to a mixture of nitrogen oxides (e.g., a mixture of NO2 and NO, the molar ratio of which is not particularly limited, such as 1:10 to 10:1).

[0254] The inventors of this invention discovered during their research that using specific amounts of rare earth metals (e.g., La) and Group VIII non-precious metals (e.g., Co) in combination with at least one precious metal (e.g., Pt) as active components, along with a specific ratio of rare earth metals to Group VIII non-precious metals, can effectively reduce SOx and NOx emissions from flue gas simultaneously. Furthermore, introducing Group IIA metals (e.g., Mg) and / or Group VIIB metals (e.g., Mn) can further enhance the catalyst's ability to remove NOx and SOx. When the catalyst of this invention is contacted with SO2, it is believed that sulfur can be converted to different valence states, with the lower valence state of sulfur favoring the conversion of NOx in the flue gas. Thus, the entire process can promote the conversion of SOx and NOx in a direction conducive to pollution reduction.

[0255] The present invention will be described in detail below through examples. In the following examples, the component content parameters were determined by X-ray fluorescence spectroscopy (XRF); the raw materials used were: lanthanum nitrate (analytical grade, Aladdin Biochemical), magnesium nitrate (analytical grade, Sinopharm Chemical Reagent Co., Ltd.), potassium chloride (analytical grade, Beijing Chemical Plant), cobalt nitrate (analytical grade, Beijing Innocare Technology Co., Ltd.), ammonium carbonate (analytical grade, Beijing Chemical Plant), ammonia water (analytical grade, 25%, Tianjin Damao Chemical Plant), palladium chloride (China National Pharmaceutical Group Beijing Procurement and Supply Station), hydrochloric acid (Beijing Chemical Plant), and OX50-SiO2 (Sinopec Catalyst Co., Ltd.).

[0256] In the following examples, the component content in the catalyst was determined by X-ray fluorescence spectroscopy (XRF), as detailed in Petrochemical Analytical Methods (RIPP Experimental Methods), edited by Yang Cuiding et al., published by Science Press in 1990.

[0257] In the following examples, powder X-ray diffraction (XRD) analysis of the catalyst samples was performed using a Siemens D5005 diffractometer, where CuKα (λ = 0.15418 nm) radiation was generated at 40 kV and 40 mA and filtered through Ni. The diffraction signal was recorded in the range of 2θ5–70° with a step size of 0.02°.

[0258] Example 1

[0259] Weigh 320 mL of deionized water into a beaker, and add 20 g of lanthanum nitrate (based on the mass of La₂O₃), 4 g of magnesium nitrate (based on the mass of MgO), 5 g of cobalt nitrate (based on the mass of Co₂O₃), and 3 g of manganese chloride (based on the mass of MnO) while stirring until completely dissolved to obtain a solution of the non-precious metal component precursor. Weigh 48 g of ammonium carbonate and dissolve it in 200 mL of deionized water, stirring until fully dissolved. Add the mixed solution of metal nitrates to the ammonium carbonate solution while stirring, and add a certain amount of ammonia water to maintain the pH of the solution at 9. Filter the completely precipitated mixture and rinse with deionized water. Dry the filter cake mixture obtained by filtration at 120°C, calcine it at 700°C in air for 5 hours, and then grind it to obtain the active metal component precursor.

[0260] Weigh 30 g of aluminum (based on Al₂O₃), add 160 mL of water and 4.5 g of 36% hydrochloric acid, and slurry. Weigh 20 g of the active metal precursor and add it to the acidified inorganic oxide matrix, mix and stir to obtain the active component coating slurry.

[0261] The above-obtained active component coating slurry was coated onto 300 g of cordierite structured support with 200 pores / square inch and dried and calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support. The obtained components were dried at 120°C and calcined at 700°C in air for 4 hours to obtain a structured catalyst semi-finished product.

[0262] The palladium precursor was weighed and mixed with dilute hydrochloric acid at a mass ratio of 1:1. The mixture was then diluted with deionized water to prepare a palladium chloride solution. A certain amount of palladium chloride solution containing 0.009 g of palladium was weighed and used as an impregnation solution to impregnate the above-mentioned catalyst semi-finished product to obtain a solid product. The solid product was then dried at 120°C and calcined at 600°C in air for 4 hours to obtain catalyst S-1. The content of the active component coating was 14.3% by weight, based on the total weight of the structured catalyst.

[0263] A portion of the active component coating was taken and subjected to XRD analysis. Characteristic peaks were observed in the XRD spectrum at approximately 2θ = 33.0°, 33.5°, and 47.5°, and at approximately 2θ = 27.0°, 28.0°, and 39.5°.

[0264] A portion of the active component coating was taken and exposed to an atmosphere containing SO2 for 1 minute. The SO2 atmosphere had a temperature of 800°C, a pressure of 0 MPa, and a SO2 content of 0.001% by volume. After exposure to SO2, the coating was subjected to XRD analysis. In the XRD spectrum, characteristic peaks were observed at 2θ angles of approximately 28.6°, 30.0°, and 50.4°.

[0265] Example 2

[0266] Weigh 250 mL of deionized water into a beaker, and add 10 g of lanthanum nitrate (based on the mass of La₂O₃), 7 g of magnesium nitrate (based on the mass of MgO), 5 g of cobalt nitrate (based on the mass of Co₂O₃), and 3 g of manganese chloride (based on the mass of MnO) while stirring until completely dissolved to obtain a solution of the non-precious metal component precursor. Weigh 38 g of ammonium carbonate and dissolve it in 150 mL of deionized water, stirring until fully dissolved. Add the mixed solution of metal nitrates to the ammonium carbonate solution while stirring, and add a certain amount of ammonia water to maintain the pH of the solution at 9. Filter the completely precipitated mixture and rinse with deionized water. Dry the filter cake mixture obtained by filtration at 120°C, calcine it at 700°C in air for 5 hours, and then grind it to obtain the active metal component precursor.

[0267] Weigh 40 g of aluminum (based on Al₂O₃), add 180 mL of water and 6 g of 36% hydrochloric acid, and slurry. Weigh 10 g of the active metal precursor and add it to the acidified inorganic oxide matrix, mix and stir to obtain the active component coating slurry.

[0268] The above-obtained active component coating slurry was coated onto 300 g of cordierite structured support with 200 pores / square inch and dried and calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support. The obtained components were dried at 120°C and calcined at 700°C in air for 4 hours to obtain a structured catalyst semi-finished product.

[0269] The palladium precursor was weighed and mixed with dilute hydrochloric acid at a mass ratio of 1:1. The mixture was then diluted with deionized water to prepare a palladium chloride solution. A certain amount of palladium chloride solution containing 0.018 g of palladium was weighed and used as an impregnation solution to impregnate the above-mentioned catalyst semi-finished product to obtain a solid product. The solid product was then dried at 120°C and calcined at 600°C in air for 4 hours to obtain catalyst S-2. The content of the active component coating was 14.3% by weight, based on the total weight of the structured catalyst.

[0270] A portion of the active component coating was taken and subjected to XRD analysis. Characteristic peaks were observed in the XRD spectrum at approximately 2θ = 33.0°, 33.5°, and 47.5°, and at approximately 2θ = 27.0°, 28.0°, and 39.5°.

[0271] A portion of the active component coating was taken and exposed to an atmosphere containing SO2 for 5 minutes. The SO2 atmosphere had a temperature of 700°C, a pressure of 0.1 MPa, and a SO2 content of 0.01% by volume. After exposure to SO2, the coating was subjected to XRD analysis. In the XRD spectrum, characteristic peaks were observed at 2θ angles of approximately 28.6°, 30.0°, and 50.4°.

[0272] Example 3

[0273] Weigh 360 mL of deionized water into a beaker, and add 25 g of lanthanum nitrate (based on the mass of La₂O₃), 5 g of magnesium nitrate (based on the mass of MgO), 2.6 g of cobalt nitrate (based on the mass of Co₂O₃), and 3.4 g of manganese chloride (based on the mass of MnO) while stirring until completely dissolved to obtain a solution of the non-precious metal component precursor. Weigh 54 g of ammonium carbonate and dissolve it in 210 mL of deionized water, stirring until fully dissolved. Add the mixed solution of metal nitrates to the ammonium carbonate solution while stirring, and add a certain amount of ammonia water to maintain the pH of the solution at 9. Filter the completely precipitated mixture and rinse with deionized water. Dry the filter cake mixture obtained by filtration at 120°C, calcine it at 700°C in air for 5 hours, and then grind it to obtain the active metal component precursor.

[0274] Weigh 20 g of aluminum (based on Al₂O₃), add 120 mL of water and 3 g of 36% hydrochloric acid, and slurry. Weigh 20 g of the active metal precursor and add it to the acidified inorganic oxide matrix, mix and stir to obtain the active component coating slurry.

[0275] The above-obtained active component coating slurry was coated onto 300 g of cordierite structured support with 200 pores / square inch and dried and calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support. The obtained components were dried at 120°C and calcined at 700°C in air for 4 hours to obtain a structured catalyst semi-finished product.

[0276] The palladium precursor was weighed and mixed with dilute hydrochloric acid at a mass ratio of 1:1. The mixture was then diluted with deionized water to prepare a palladium chloride solution. A certain amount of palladium chloride solution containing 0.004 g of palladium was weighed and used as an impregnation solution to impregnate the above-mentioned catalyst semi-finished product to obtain a solid product. The solid product was then dried at 120°C and calcined at 600°C in air for 4 hours to obtain catalyst S-3. The content of the active component coating was 11.8% by weight, based on the total weight of the structured catalyst.

[0277] A portion of the active component coating was taken and subjected to XRD analysis. Characteristic peaks were observed in the XRD spectrum at approximately 2θ = 33.0°, 33.5°, and 47.5°, and at approximately 2θ = 27.0°, 28.0°, and 39.5°.

[0278] A portion of the active component coating was taken and exposed to an atmosphere containing SO2 for 15 minutes. The SO2 atmosphere had a temperature of 650°C, a pressure of 0 MPa, and a SO2 content of 0.001% by volume. After exposure to SO2, the coating was subjected to XRD analysis. In the XRD spectrum, characteristic peaks were observed at 2θ angles of approximately 28.6°, 30.0°, and 50.4°.

[0279] Example 4

[0280] Weigh 310 mL of deionized water into a beaker, and add 12 g of lanthanum nitrate (based on the mass of La₂O₃), 4 g of magnesium nitrate (based on the mass of MgO), 12 g of cobalt nitrate (based on the mass of Co₂O₃), and 3 g of manganese chloride (based on the mass of MnO) while stirring until completely dissolved to obtain a solution of the non-precious metal component precursor. Weigh 47 g of ammonium carbonate and dissolve it in 200 mL of deionized water, stirring until fully dissolved. Add the mixed solution of metal nitrates to the ammonium carbonate solution while stirring, and add a certain amount of ammonia water to maintain the pH of the solution at 9. Filter the completely precipitated mixture and rinse with deionized water. Dry the filter cake mixture obtained by filtration at 120°C, calcine it at 700°C in air for 5 hours, and then grind it to obtain the active metal component precursor.

[0281] Weigh 30 g of aluminum (based on Al₂O₃), add 160 mL of water and 4.5 g of 36% hydrochloric acid, and slurry. Weigh 20 g of the active metal precursor and add it to the acidified inorganic oxide matrix, mix and stir to obtain the active component coating slurry.

[0282] The above-obtained active component coating slurry was coated onto 300 g of cordierite structured support with 200 pores / square inch and dried and calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support. The obtained components were dried at 120°C and calcined at 700°C in air for 4 hours to obtain a structured catalyst semi-finished product.

[0283] The palladium precursor was weighed and mixed with dilute hydrochloric acid at a mass ratio of 1:1. The mixture was then diluted with deionized water to prepare a palladium chloride solution. A certain amount of palladium chloride solution containing 0.009 g of palladium was weighed and used as an impregnation solution to impregnate the above-mentioned catalyst semi-finished product to obtain a solid product. The solid product was then dried at 120°C and calcined at 600°C in air for 4 hours to obtain catalyst S-4. The content of the active component coating was 14.3% by weight, based on the total weight of the structured catalyst.

[0284] A portion of the active component coating was taken and subjected to XRD analysis. Characteristic peaks were observed in the XRD spectrum at approximately 2θ = 33.0°, 33.5°, and 47.5°, and at approximately 2θ = 27.0°, 28.0°, and 39.5°.

[0285] A portion of the active component coating was taken and exposed to an atmosphere containing SO2 for 30 minutes. The SO2 atmosphere had a temperature of 675°C, a pressure of 0.2 MPa, and a SO2 content of 0.001% by volume. After exposure to SO2, the coating was subjected to XRD analysis. In the XRD spectrum, characteristic peaks were observed at 2θ angles of approximately 28.6°, 30.0°, and 50.4°.

[0286] Example 5

[0287] Weigh 320 mL of deionized water into a beaker, and add 20 g of lanthanum nitrate (based on the mass of La₂O₃), 4 g of magnesium nitrate (based on the mass of MgO), 5 g of cobalt nitrate (based on the mass of Co₂O₃), and 3 g of manganese chloride (based on the mass of MnO) while stirring until completely dissolved to obtain a solution of the non-precious metal component precursor. Weigh 48 g of ammonium carbonate and dissolve it in 200 mL of deionized water, stirring until fully dissolved. Add the mixed solution of metal nitrates to the ammonium carbonate solution while stirring, and add a certain amount of ammonia water to maintain the pH of the solution at 9. Filter the completely precipitated mixture and rinse with deionized water. Dry the filter cake mixture obtained by filtration at 120°C, calcine it at 700°C in air for 5 hours, and then grind it to obtain the active metal component precursor.

[0288] Weigh 30 g of aluminum (based on Al₂O₃), add 160 mL of water and 4.5 g of 36% hydrochloric acid, and slurry. Weigh 20 g of the active metal precursor and add it to the acidified inorganic oxide matrix, mix and stir to obtain the active component coating slurry.

[0289] The above-obtained active component coating slurry was coated onto 300 g of cordierite structured support with 200 pores / square inch and dried and calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support. The obtained components were dried at 120°C and calcined at 700°C in air for 4 hours to obtain a structured catalyst semi-finished product.

[0290] The ruthenium precursor was weighed and mixed with dilute hydrochloric acid at a mass ratio of 1:1. The mixture was then diluted with deionized water to prepare a ruthenium chloride solution. A certain amount of the ruthenium chloride solution containing 0.009 g of ruthenium was weighed and used as an impregnation solution to impregnate the above-mentioned catalyst semi-finished product to obtain a solid product. The solid product was then dried at 120°C and calcined at 600°C in air for 4 hours to obtain catalyst S-5. The content of the active component coating was 14.3% by weight, based on the total weight of the structured catalyst.

[0291] Example 6

[0292] Weigh 320 mL of deionized water into a beaker, and add 20 g of cerium nitrate (based on CeO₂), 4 g of magnesium nitrate (based on MgO), 5 g of ferric nitrate (based on Fe₂O₃), and 3 g of manganese chloride (based on MnO) while stirring until completely dissolved to obtain a solution of the non-precious metal component precursor. Weigh 48 g of ammonium carbonate and dissolve it in 200 mL of deionized water, stirring until fully dissolved. Add the mixed solution of metal nitrates to the ammonium carbonate solution while stirring, and add a certain amount of ammonia water to maintain the pH of the solution at 9. Filter the completely precipitated mixture and rinse with deionized water. Dry the filter cake mixture obtained by filtration at 120°C, calcine it at 700°C in air for 5 hours, and then grind it to obtain the active metal component precursor.

[0293] Weigh 30 g of aluminum (based on Al₂O₃), add 160 mL of water and 4.5 g of 36% hydrochloric acid, and slurry. Weigh 20 g of the active metal precursor and add it to the acidified inorganic oxide matrix, mix and stir to obtain the active component coating slurry.

[0294] The above-obtained active component coating slurry was coated onto 300 g of cordierite structured support with 200 pores / square inch and dried and calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support. The obtained components were dried at 120°C and calcined at 700°C in air for 4 hours to obtain a structured catalyst semi-finished product.

[0295] The palladium precursor was weighed and mixed with dilute hydrochloric acid at a mass ratio of 1:1. The mixture was then diluted with deionized water to prepare a palladium chloride solution. A certain amount of palladium chloride solution containing 0.009 g of palladium was weighed and used as an impregnation solution to impregnate the above-mentioned catalyst semi-finished product to obtain a solid product. The solid product was then dried at 120°C and calcined at 600°C in air for 4 hours to obtain catalyst S-6. The content of the active component coating was 14.3% by weight, based on the total weight of the structured catalyst.

[0296] Compare with Example 1

[0297] Weigh 20 g of La₂O₃ and 5 g of Co₂O₃, and mix them thoroughly by mechanical mixing to obtain a mixed precursor.

[0298] Weigh 30 g of aluminum (based on Al₂O₃), add 380 mL of water and 4.5 g of 36% hydrochloric acid, and slurry. Add 20 g of the mixed precursor to the acidified inorganic oxide matrix and mix to obtain the active component coating slurry.

[0299] The above-obtained active component coating slurry was coated onto 300 g of a cordierite structured support with 200 pores / square inch, and then dried and calcined to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support. The obtained component was dried at 120°C and calcined at 700°C in air for 4 hours to obtain catalyst D-1. The active component coating content was 14.3% by weight, based on the total weight of the structured catalyst.

[0300] The composition of the catalysts obtained above is listed in Table 1.

[0301] Table 1: Composition of the catalyst (wt%) Example Rare Earth Group Metal IIA family Metal Group VIIB Non-precious metals VB, VIII, IB, IIB families Non-precious metals precious metals 1 25 5 3.8 6.2 0.018 2 8 5.6 2.4 4 0.036 3 34.7 6.9 4.7 3.6 0.010 4 15.5 5.2 3.8 15.5 0.018 5 25 5 3.8 6.2 0.018 6 25 5 3.8 6.2 0.018 Note: The content of each component in Table 1 is based on the total amount of active component coating.

[0302] Experimental Example 1

[0303] This experiment was used to evaluate the effect of the catalysts provided in the above examples and control examples on simultaneously reducing NO and SO2 emissions in flue gas. The catalytic cracking reaction-regeneration evaluation was conducted on a small fixed-bed simulated flue gas device. A structured catalyst was packed in the catalyst bed at a loading of 20 g. The reaction temperature was 650℃, the pressure was 0.1 MPa, the feed gas volumetric flow rate (standard conditions) was 1000 mL / min, and the volume hourly space velocity (VHSV) was approximately 3000 h⁻¹. After the reactor temperature stabilized, the catalyst was pretreated for 30 min under a N₂ atmosphere to thoroughly remove adsorbed species from the catalyst surface. At the start of the reaction, the feed gas contained 1200 ppm (v / v) NO and 1200 ppm (v / v) SO₂, with the remainder being N₂. The gaseous products were analyzed using an online infrared analyzer to obtain the SO₂ and NO concentrations after the reaction. The results for an evaluation time of 0.5 h are listed in Table 2, and the results for an evaluation time of 1.5 h are listed in Table 3.

[0304] Table 2: Comparison of desulfurization and denitrification performance of different catalysts within 0.5 h Total conversion rate (%) in 0.5 h Combination - NO Combination - SO 2 Alone - NO standalone - SO 2 S-1 57 66 <2 59 S-2 44 37 <2 35 S-3 42 35 <2 32 S-4 twenty two twenty two <2 twenty one S-5 46 49 <2 42 S-6 41 50 <2 46 D-1 <2 twenty three <2 twenty two Note: In Table 2, "single-NO" and "single-SO2" refer to the feed gas containing only NO or SO2, respectively.

[0305] Table 3: Comparison of desulfurization and denitrification performance of different catalysts within 1.5 h Total conversion rate (%) in 1.5 h Combination - NO Combination - SO 2 Alone - NO standalone - SO 2 S-1 49 56 <2 50 S-2 41 35 <2 34 S-3 38 32 <2 30 S-4 20 20 <2 20 S-5 40 43 <2 37 S-6 37 44 <2 40 D-1 <2 17 <2 16 Note: In Table 3, "single -NO" and "single -SO 2" refer to the feed gas containing only NO or SO 2, respectively.

[0306] The results in Tables 2 and 3 show that the catalyst provided by this invention can effectively improve the combined removal of SOx and NOx and reduce SOx and NOx emissions.

[0307] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combining the various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

[0308] none

Claims

1. A structured catalyst capable of simultaneously reducing SOx and NOx emissions, the catalyst comprising a structured support and an active component coating distributed on the inner and / or outer surfaces of the structured support, wherein, based on the total weight of the catalyst, the content of the active component coating is 1-50% by weight, and the active component coating contains a matrix and an active metal component, wherein, Based on the total weight of the active component coating, the matrix content is 10-90% by weight, the active metal component content is 10-90% by weight, and the active metal component contains: based on 100% by weight of the total amount of the active metal component, 1) as oxides, 50-95% by weight of metal components selected from rare earth groups and groups IIA; 2) as oxides, 5-50% by weight of non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB; 3) as elements, 0.01-2% by weight of precious metal components; Component 1) contains: 1a) one or more metal components selected from rare earth groups, wherein the rare earth group metal components are selected from lanthanum, cerium, ilium, and neodymium; and 1b) one or more metal components selected from group IIA; Component 2) contains: 2a) one or more non-precious metal components selected from groups VB, VIII, IB, and IIB; and 2b) One or more non-precious metal components selected from Group VIIB; said component 3) contains one or more precious metal components selected from ruthenium, rhodium, platinum and palladium.

2. The well-structured catalyst as described in claim 1, wherein, Based on the total weight of the catalyst, the content of the active component coating is 5-40% by weight; and / or, based on the total weight of the active component coating, the content of the matrix is ​​40-90% by weight, and the content of the active metal component is 10-60% by weight; and / or, the active metal component contains: 60-90% by weight of component 1) as oxides, based on 100% by weight of the total amount of the active metal component; 10-40% by weight of component 2) as oxides; and 0.02-1.5% by weight of component 3 as an element.

3. The well-structured catalyst as described in claim 1, wherein, Based on the total weight of the catalyst, the content of the active component coating is 10-35 wt%; and / or, based on the total weight of the active component coating, the content of the matrix is ​​50-80 wt%, and the content of the active metal component is 20-50 wt%; and / or, the active metal component contains: 65-85 wt% of component 1) as oxides based on 100 wt% of the total amount of the active metal component; 15-35 wt% of component 2) as oxides; and 0.03-1.2 wt% of component 3 as an element.

4. The well-structured catalyst as described in claim 1, wherein, The matrix is ​​selected from at least one of alumina, spinel, perovskite, silica-alumina, zeolite, kaolin, diatomite, and perlite; the regular structure carrier is selected from an integral carrier with a parallel channel structure open at both ends; the pore density of the cross section of the regular structure carrier is 10-300 pores / square inch, and the porosity is 20-80%; the regular structure carrier is selected from at least one of cordierite honeycomb carrier, mullite honeycomb carrier, diamond honeycomb carrier, corundum honeycomb carrier, zirconium corundum honeycomb carrier, quartz honeycomb carrier, nepheline honeycomb carrier, feldspar honeycomb carrier, alumina honeycomb carrier, and metal alloy honeycomb carrier.

5. The well-structured catalyst as described in claim 1, wherein, The rare earth metal component is lanthanum and / or cerium; the group IIA metal component is selected from beryllium, magnesium, calcium, strontium and barium; the non-precious metal component selected from groups VB, VIIB, VIII, IB and IIB is selected from manganese, iron, cobalt, nickel, copper, zinc and vanadium; the precious metal component is selected from ruthenium, rhodium and palladium.

6. The well-structured catalyst as described in claim 1, wherein, The rare earth metal component is lanthanum and / or cerium; the group IIA metal component is magnesium; the non-precious metal component selected from groups VB, VIIB, VIII, IB and IIB is manganese, and cobalt and / or iron; the precious metal component is ruthenium or palladium.

7. The well-structured catalyst as claimed in claim 1, wherein, Based on the total amount of the active metal components, the ratio of the content of metal components selected from rare earth groups and groups IIA to the content of non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, calculated as oxides, is 1-8.

8. The well-structured catalyst as claimed in claim 1, wherein, Based on the total amount of the active metal components, the ratio of the content of metal components selected from rare earth groups and groups IIA to the content of non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB, calculated as oxides, is 2-4.

9. The well-structured catalyst as claimed in claim 1, wherein, Based on a total amount of 100% by weight of the active metal component, the active metal component comprises: 30-80% by weight of component 1a) as oxide; 5-40% by weight of component 1b) as oxide; 3-30% by weight of non-precious metal component 2a) as oxide; 3-20% by weight of non-precious metal component 2b) as oxide; and 0.01-0.2% by weight of precious metal component 3 selected from ruthenium, rhodium, and palladium as an element.

10. The well-structured catalyst as claimed in claim 9, wherein, Component 1a) contains lanthanum; Component 1b) contains magnesium; Component 2a) contains cobalt; Component 2b) contains manganese; Component 3) contains palladium.

11. The well-structured catalyst as claimed in claim 10, wherein, The molar ratio of lanthanum to cobalt is (1-6):

1.

12. The well-structured catalyst as claimed in claim 10, wherein, The molar ratio of lanthanum to cobalt is (2.5-3.5):

1.

13. The catalyst as claimed in any one of claims 1-12, wherein the catalyst has characteristic peaks in the powder XRD pattern at 2θ = 33.0° ± 0.1°, 33.5° ± 0.1° and 47.5° ± 0.1° and at 27.0° ± 0.1°, 28.0° ± 0.1° and 39.5° ± 0.1°.

14. The catalyst as claimed in any one of claims 1-12 above, wherein the catalyst has been treated by exposure to an atmosphere containing SO2.

15. The catalyst as claimed in any one of claims 1-12, wherein the catalyst has been treated with exposure to an atmosphere containing SO2, and the catalyst has characteristic peaks in the powder XRD pattern at 2θ = 28.6° ± 0.1°, 30.0° ± 0.1°, and 50.4° ± 0.1°.

16. A method for preparing a structured catalyst capable of simultaneously reducing SOx and NOx emissions, the method comprising the following steps: (1) preparing a solution containing rare earth and group IIA metal component precursors and non-noble metal component precursors selected from groups VB, VIIB, VIII, IB and IIB; (2) co-precipitating the solution in step (1) with a coprecipitant, and then drying and calcining the resulting solid product to obtain an active metal component precursor; (3) mixing and slurrying the active metal component precursor, a matrix source and water to obtain an active component coating slurry; (4) coating a structured support with the active component coating slurry and drying and calcining to obtain a coating of partially active components distributed on the inner and / or outer surfaces of the structured support, to obtain a catalyst semi-finished product; (5) impregnating the catalyst semi-finished product obtained in step (4) with a solution containing noble metal component precursors, and then drying and / or calcining to obtain an active component coating distributed on the inner and / or outer surfaces of the structured support; wherein, The amounts of rare earth and group IIA metal precursors, non-precious metal precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal precursors, and ordered structure support in the prepared ordered structure catalyst are such that, based on the total weight of the catalyst, the content of the active component coating is 1-50% by weight, the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating, the content of the matrix is ​​10-90% by weight, the content of the active metal component is 10-90% by weight, and the active metal component contains: based on 100% by weight of the total amount of the active metal component, 1) as oxides, 50-95% by weight of metals selected from rare earth and group IIA; 2) as oxides, 5-50% by weight of non-precious metals selected from groups VB, VIIB, VIII, IB, and IIB; and 3) as elements, 0.01-2% by weight of precious metals. Component 1) contains: 1a) one or more metal components selected from rare earth groups, wherein the rare earth group metal components are selected from lanthanum, cerium, tungsten, and neodymium; and 1b) one or more metal components selected from group IIA; Component 2) contains: 2a) one or more non-precious metal components selected from groups VB, VIII, IB, and IIB; and 2b) one or more non-precious metal components selected from group VIIB; Component 3) contains one or more precious metal components selected from ruthenium, rhodium, platinum, and palladium.

17. The preparation method as described in claim 16, wherein, The amounts of rare earth and group IIA metal component precursors, non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support are such that, based on the total weight of the catalyst, the content of the active component coating in the ordered structure catalyst is 5-40% by weight, the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating, the content of the matrix is ​​40-90% by weight, the content of the active metal component is 10-60% by weight, and the active metal component contains: 60-90% by weight of component 1) as oxides based on 100% of the total amount of the active metal component; 10-40% by weight of component 2) as oxides; and 0.02-1.5% by weight of component 3 as an element.

18. The preparation method as described in claim 16, wherein, The amounts of rare earth and group IIA metal component precursors, non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support are such that, based on the total weight of the catalyst, the content of the active component coating in the ordered structure catalyst is 10-35% by weight, the active component coating contains a matrix and an active metal component, wherein, based on the total weight of the active component coating, the content of the matrix is ​​50-80% by weight, the content of the active metal component is 20-50% by weight, and the active metal component contains: 65-85% by weight of component 1) as oxides based on 100% of the total amount of the active metal component; 15-35% by weight of component 2) as oxides; and 0.03-1.2% by weight of component 3 as an element.

19. The preparation method as described in claim 16, wherein, The amounts of rare earth and group IIA metal component precursors, non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support are such that in the prepared ordered structure catalyst, based on the total amount of said active metal components, the ratio of the content of metal components selected from rare earth and group IIA to the content of non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB, calculated as oxides, is 1-8.

20. The preparation method as described in claim 16, wherein, The amounts of rare earth and group IIA metal component precursors, non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support are such that in the prepared ordered structure catalyst, based on the total amount of the active metal components, the ratio of the content of metal components selected from rare earth and group IIA to the content of non-precious metal components selected from groups VB, VIIB, VIII, IB, and IIB, calculated as oxides, is 2-4.

21. The preparation method as described in claim 16, wherein, The amounts of rare earth and group IIA metal component precursors, non-precious metal component precursors selected from groups VB, VIIB, VIII, IB, and IIB, matrix source, precious metal component precursors, and ordered structure support in the prepared ordered structure catalyst are such that, based on the total amount of 100% by weight of the active metal component, the active metal component contains: 30-80% by weight of component 1a) as oxide; 5-40% by weight of component 1b) as oxide; 3-30% by weight of component 2a) as oxide; 3-20% by weight of component 2b) as oxide; and 0.01-0.2% by weight of precious metal component 3 selected from ruthenium, rhodium, and palladium as an element.

22. The preparation method as claimed in claim 21, wherein component 1a) contains lanthanum; component 1b) contains magnesium; component 2a) contains cobalt; component 2b) contains manganese; and component 3) contains palladium.

23. The preparation method as described in claim 16, wherein, The matrix source is a substance that can be transformed into a matrix under the calcination conditions in step (4); the matrix is ​​selected from at least one of alumina, spinel, perovskite, silica-alumina, zeolite, kaolin, diatomite, and perlite; the regular structure carrier is selected from an integral carrier with a parallel channel structure open at both ends; the pore density of the cross section of the regular structure carrier is 10-300 pores / square inch, and the porosity is 20-80%; the regular structure carrier is selected from at least one of cordierite honeycomb carrier, mullite honeycomb carrier, diamond honeycomb carrier, corundum honeycomb carrier, zirconium corundum honeycomb carrier, quartz honeycomb carrier, nepheline honeycomb carrier, feldspar honeycomb carrier, alumina honeycomb carrier, and metal alloy honeycomb carrier.

24. The preparation method as described in claim 16, wherein, The rare earth metal component is lanthanum and / or cerium; the group IIA metal component is selected from beryllium, magnesium, calcium, strontium and barium; the non-precious metal component selected from groups VB, VIIB, VIII, IB and IIB is selected from manganese, iron, cobalt, nickel, copper, zinc and vanadium; the precious metal component is selected from ruthenium, rhodium and palladium.

25. The preparation method as described in claim 16, wherein, The rare earth metal component is selected from lanthanum and / or cerium; the group IIA metal component is magnesium; the non-precious metal component selected from groups VB, VIIB, VIII, IB and IIB is manganese, and cobalt and / or iron; the precious metal component is ruthenium or palladium.

26. The preparation method as described in claim 16, wherein, The precursors containing rare earth and group IIA metal components and the precursors containing non-precious metal components selected from groups VB, VIIB, VIII, IB and IIB are each independently selected from the nitrates and / or chlorides of their respective metal components; the co-precipitant is at least one of ammonium carbonate, potassium carbonate and sodium carbonate. The coprecipitation reaction was carried out at a pH of 8-10. The roasting conditions in step (2) include: a temperature of 300-800℃ and a time of 1-8 h.

27. The preparation method as described in claim 16, wherein, The solid content of the active component coating slurry in step (3) is 5-45% by weight. The calcination conditions in step (4) include: a temperature of 300-800℃ and a time of 1-5 h; In step (5), the noble metal component precursor is hydrolyzed in an acid solution to provide the solution; The acid is selected from at least one of hydrochloric acid, nitric acid, phosphoric acid and acetic acid; The amount of acid used is such that the pH value of the impregnation solution is less than 6.0; The calcination conditions in step (5) include: a temperature of 300-700℃ and a time of 0.1-5 h.

28. A method for simultaneously removing SOx and NOx from catalytic cracking regenerated flue gas, the method comprising: Under conditions of SOx and NOx removal, the catalytic cracking regenerated flue gas is contacted with a catalyst, said catalyst being any one of the aforementioned claims 1-15; The contact is carried out in a flue gas channel located after the cyclone separator and / or after the CO incinerator; the contact conditions include: a temperature of 300-1000℃, a reaction pressure of 0-0.5 MPa (gauge pressure gauge), and a catalytic cracking regeneration flue gas volume space velocity of 200-20000 h-1.

29. A method for simultaneously removing SOx and NOx from flue gas, the method comprising: Under conditions of SOx and NOx removal, the flue gas is contacted with a catalyst, said catalyst being any one of the aforementioned claims 1-15; The volume fractions of SOx and NOx in the flue gas are 1~3000 μL / L, and the molar ratio of SOx to NOx is 0.5:1-2:

1. The contact conditions include: a temperature of 300-1000℃, a reaction pressure of 0-0.5 MPa (gauge pressure), and a flue gas volume hourly space velocity of 200-20000 h-1.