Combustible waste gas catalytic conversion unit and catalytic conversion equipment

Abstract

The invention belongs to the technical field of combustible waste gas catalysis, and particularly relates to a combustible waste gas catalytic conversion unit and catalytic conversion equipment. A first solid-state oxygen layer, a CO catalyst layer, a second solid-state oxygen layer, a non-methane CH compound catalyst layer, a third solid-state oxygen layer and an H2 and methane mixed catalyst layer which are sequentially arranged are arranged in the catalytic conversion unit in the flowing direction of combustible waste gas according to the catalytic temperature ranges of various combustible waste gas in the waste gas. Wherein the solid oxygen and the catalyst are divided into different layers according to different flue gas components; cO2 and solid oxygen react to generate O2 to provide an oxygen source required by catalytic oxidation, and heat is provided for subsequent catalytic oxidation reaction. And meanwhile, combustible gas containing C is catalytically oxidized, a certain amount of CO2 is released and continuously reacts with subsequent solid oxygen to release O2, and therefore the purpose of continuous oxygen supply is achieved. The combustible waste gas is gradually catalyzed and oxidized into non-toxic and harmless CO2 and H2O in the mode.

Description

Technical Field

[0001] The present invention belongs to the technical field of catalytic conversion of combustible exhaust gas, and in particular relates to a catalytic conversion unit of combustible exhaust gas and catalytic conversion equipment. Background Art

[0002] A large amount of flammable gases such as CO, H2, CH compounds are generated in chemical production processes such as liquefied petroleum gas leakage, methanol synthesis production, acetylene synthesis production, battery thermal runaway, and coal chemical industry. O2 is often absent or the O2 content is very low. There is a certain risk of leakage in the production process. If the flammable gas is not handled, fire, explosion and other hazards will occur, endangering people's lives and property safety.

[0003] In engineering, catalytic oxidation is often used to treat combustible waste gas, oxidizing the combustible waste gas into harmless substances such as CO2 and H2O. However, catalytic oxidation requires a certain amount of O2, and in the above-mentioned chemical production process, there is often no O2 component or very little O2 component in the combustible gas, and the initial temperature of the gas is low. Adding oxygen will increase production costs, expand the volume of the device, reduce the catalytic temperature, and thus reduce the performance of the catalyst. Moreover, chemical production leakage is a fast and unpredictable process, which requires the development of a method that can quickly purify these flue gases at any time.

[0004] For the treatment of combustible gases in oxygen-free or low-oxygen environments, "Microbial Extraction and Growth Metabolism Characteristics of CH4 and CO Gases in Metabolic Coals" (paper, DOI: 10.13800) uses microbial methods to remove combustible gases in coal mines to ensure safe mining; "Technology for Reducing Organic Waste Gas from Liquefied Petroleum Gas Desulfurization" (paper, DOI: 10.3969) replaces factory air with oxygen and increases raw material pretreatment for process integration. After the technology was implemented in a certain refining enterprise, the average volume fractions of oxygen and hydrocarbon components in the circulating gas were 9.7% and 21.7%, respectively, reducing organic waste gas in industrial flue gas;

[0005] The existing technology for treating combustible waste gas under oxygen-free or low-oxygen conditions mainly includes four categories: microbial method, adsorption, catalytic oxidation and combustion. However, the microbial method is relatively expensive and has a small scope of application; the adsorption method is difficult to treat H2 in flue gas; the combustion method requires a series of supporting facilities and is relatively expensive, so the catalytic oxidation method is the best solution for treating this type of flue gas. However, the traditional catalytic oxidation method often uses an external air or pure oxygen method for oxygen supply, in which the flowing airflow will take away most of the heat, making the catalytic reaction temperature lower and weakening the catalytic performance of the catalyst. Summary of the invention

[0006] In view of the above technical problems, the present invention provides a catalytic conversion unit for combustible exhaust gas and catalytic conversion equipment. The catalytic conversion unit uses the technical means of coupling solid oxygen with a high-performance catalyst to realize an integrated process flow of oxygen supply and catalysis, and at the same time utilizes the heat generated by the catalytic reaction to improve the catalytic performance of the catalyst, thereby improving the exhaust gas treatment efficiency and reducing the exhaust gas treatment cost.

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

[0008] A catalytic conversion unit for combustible exhaust gas is provided with a first solid oxygen layer, a CO catalyst layer, a second solid oxygen layer, a non-methane CH compound catalyst layer, a third solid oxygen layer, and a H2 and methane mixed catalyst layer arranged in sequence along the flow direction of the combustible exhaust gas and according to the catalytic temperature range of various combustible gases in the exhaust gas.

[0009] Furthermore, the combustible waste gas includes combustible gas and CO2; the combustible gas includes CO, non-methane CH compounds, H2 and methane.

[0010] Furthermore, components used in the first solid oxygen layer, the second solid oxygen layer and the third solid oxygen layer include any one of potassium superoxide, sodium peroxide and calcium superoxide.

[0011] Furthermore, according to the total amount of combustible waste gas to be treated and the content of different gas components in the combustible waste gas, the total consumption of solid oxygen is calculated according to the following formula:

[0012]

[0013] Among them, m 固态氧 is the mass of solid oxygen, in g; M solid oxygen is the relative molecular mass of solid oxygen, in g / mol; N is the molar volume of the gas, which is 22.4L / mol under standard conditions; V is the total volume of the combustible waste gas to be treated, in L; x, y, z, and p correspond to the contents of CO2, CO, non-methane CH compounds, and CH4 in the combustible waste gas to be treated, respectively, and the content of H2 is 1-xyzp; the values ​​of x, y, z, and p are all between 0 and 1; a and b are the reaction balancing coefficients for the reaction of solid oxygen and carbon dioxide to generate oxygen.

[0014] Furthermore, the CO catalyst layer uses a copper-manganese catalyst, the non-methane CH compound catalyst layer and the H2 and methane mixed catalyst layer both use precious metal catalysts, and the precious metal catalyst includes any one of Pt / Al2O3, Pd / Al2O3, Pt / TiO2, Pd / TiO2, Pt / C, and Pd / C.

[0015] Furthermore, the volume of each catalyst layer is determined according to the following formula.

[0016]

[0017] Where V 催化剂 represents the volume of the catalyst, m 3 ; Q represents the flue gas volume flow rate, m 3 / h; V s Indicates airspeed, ranging from 1000 to 1000000h -1 .

[0018] Furthermore, in the first solid oxygen layer, CO catalyst layer, second solid oxygen layer, non-methane CH compound catalyst layer, third solid oxygen layer, H2 and methane mixed catalyst layer, the gap between adjacent layers is no more than 5 mm. By controlling the gap between layers, space can be saved and the gas flow direction can be controlled.

[0019] A catalytic conversion device for combustible exhaust gas, the catalytic conversion device comprising at least one catalytic conversion unit.

[0020] Furthermore, the catalytic converter equipment has a simple structure, and has no other components except the catalytic converter unit, the housing and the connecting pipe. The structural form of the catalytic converter equipment includes any one of a disc shape, a cylindrical shape and a rectangular parallelepiped shape;

[0021] The catalytic conversion equipment also includes a heat dissipation reactor, the structure of which is any one of a heat sink and a corrugated plate, and is installed on the outside of the catalytic conversion unit.

[0022] An application of a catalytic conversion equipment for combustible waste gas, wherein the catalytic conversion equipment is used to treat combustible flue gas purification whose O2 content is lower than the O2 content required for catalytic oxidation of waste gas; including oxygen-free combustible gas generated during liquefied petroleum gas leakage, methanol synthesis production, acetylene synthesis production, battery thermal runaway, and coal chemical production. Among them, the oxygen content in the waste gas is lower than the oxygen content required for catalytic oxidation of combustible gas means that the combustible waste gas to be treated does not contain O2 or the oxygen content is less than 5%. The catalytic conversion equipment for combustible waste gas provided by the present invention can reduce the risk of explosion.

[0023] The beneficial effects of the present invention are:

[0024] This patent proposes a catalytic conversion unit and catalytic conversion equipment for combustible exhaust gas, which can realize the integrated treatment of combustible exhaust gas, and has the advantages of simple structure, small size, high exhaust gas treatment efficiency, and low cost. Its key technology is the coupling of high-performance catalysts and solid oxygen. The technical means of coupling solid oxygen and high-performance catalysts is used to realize the integrated process of oxygen supply and catalysis. At the same time, the heat generated by the catalytic reaction is used to improve the catalytic performance of the catalyst, improve the exhaust gas treatment efficiency, and reduce the exhaust gas treatment cost.

[0025] The existing flammable gas treatment technology often uses combustion and catalytic oxidation for treatment. However, the existing treatment methods generally have disadvantages such as complex process, high cost, and low treatment efficiency. This solution uses solid oxygen and high-performance catalyst coupling technology, which does not require additional oxygen sources and heating devices. It only relies on the oxygen and heat released by its own reaction to achieve the treatment of flammable gas, simplifying the process flow, reducing treatment costs, and expanding the scope of application. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 This is a schematic diagram of the combination of solid oxygen and catalyst inside a catalytic conversion unit for combustible exhaust gas in an embodiment of the present invention;

[0027] Figure 2 This is a flow chart of the layered catalytic oxidation of combustible gas by the catalytic conversion unit in an embodiment of the present invention. DETAILED DESCRIPTION

[0028] The technical solution of the present invention is further described below in conjunction with specific embodiments and drawings.

[0029] Example 1

[0030] A catalytic conversion unit for combustible exhaust gases, such as Figure 1 As shown, along the flow direction of the combustible exhaust gas and according to the catalytic temperature range of various combustible gases in the exhaust gas, a first solid oxygen layer, a CO catalyst layer (i.e., the first catalyst layer), a second solid oxygen layer, a non-methane CH compound catalyst layer (i.e., the second catalyst layer), a third solid oxygen layer, and a H2 and methane mixed catalyst layer (i.e., the third catalyst layer) are arranged in sequence in the catalytic conversion unit.

[0031] The optimal catalytic temperatures for combustible gases CO, non-methane CH compounds, H2 and methane are shown in Table 1.

[0032] Table 1 Optimal catalytic oxidation temperature for different combustible gases

[0033]

[0034] It can be seen that in the present invention, along the direction of flue gas flow, the arrangement rule of different combustible gas catalyst layers is: the combustible gas catalyst layers are arranged from low to high according to the optimal activation catalytic temperatures of the corresponding catalysts of different combustible gases; the arrangement layout of the above-mentioned different combustible gas catalyst layers can not only use the CO2 generated by the catalytic oxidation reaction to react with solid oxygen to produce O2, but also the reaction and the catalytic oxidation reaction are both exothermic reactions, and the released heat can increase the flue gas temperature, thereby allowing the next type of combustible gas to reach its optimal catalytic oxidation temperature.

[0035] like Figure 2 As shown, the catalytic conversion unit provided in the present invention first consumes the CO2 originally present in the mixed combustible exhaust gas, and CO2 reacts with the first layer of solid oxygen (solid oxygen is potassium superoxide as an example) to produce O2 (Formula 1). The necessary O2 is provided for the subsequent catalytic oxidation of CO, and the CO2 (Formula 2) produced by the catalytic oxidation of CO can continue to react with the second layer of solid oxygen to produce O2 (Formula 3), thereby providing the necessary O2 for the subsequent catalytic oxidation of non-methane CH compounds; while the CO2 (Formula 4) produced by the catalytic oxidation of non-methane CH compounds can continue to react with the third layer of solid oxygen to produce O2 (Formula 5), ​​thereby providing the necessary O2 for the subsequent catalytic oxidation of H2 and methane; and the CO2 (Formula 6) produced by the catalytic oxidation of methane can continue to react with the remaining solid oxygen in the third layer to produce O2 (Formula 7); finally, the H2 in the flue gas reacts with the remaining O2 (Formula 8), and the oxygen-free combustible gas is effectively removed through the coupling of solid oxygen and catalyst in Formulas (1) to (8), thereby reducing the explosion hazard. At the same time, the third layer catalyst is a composite catalyst of H2 and CH4, and the CH4 content in the flue gas is relatively small, so equations (6) to (8) will be carried out at the same time.

[0036] 4KO2+2CO2=2K2CO3+3O2 (1)

[0037] 2CO+O2=2CO2 (2)

[0038] 4KO2+2CO2=2K2CO3+3O2 (3)

[0039] 4C n H m + (4n+m) O2=4n CO2+2m H2O (4)

[0040] 4KO2+2CO2=2K2CO3+3O2 (5)

[0041] CH4+2O2=CO2+2H2O (6)

[0042] 4KO2+2CO2=2K2CO3+3O2 (7)

[0043] 2H2+O2=2H2O (8)

[0044] The combustible waste gas includes combustible gas and CO2; the combustible gas includes CO, non-methane CH compounds, H2 and methane.

[0045] According to the total volume of combustible waste gas to be treated and the content of different gas components in the combustible waste gas, the total consumption of solid oxygen is calculated according to the following formula:

[0046] a A+b CO2=c B+d O2 (9)

[0047] Among them, a, b, c, d are balancing coefficients, A is solid oxygen, B is the corresponding solid oxygen product, and the content of solid oxygen is:

[0048]

[0049] Among them, m 固态氧 is the mass of solid oxygen, in g; M solid oxygen is the relative molecular mass of solid oxygen, in g / mol; N is the gas molar volume, which is 22.4 L / mol under standard conditions; V is the total volume of the combustible waste gas to be treated, in L; x, y, z, and p correspond to the contents of CO2, CO, non-methane CH compounds, and CH4 in the combustible gas, respectively, and the content of H2 is 1-xyzp; the values ​​of x, y, z, and p are all between 0 and 1;

[0050] When potassium superoxide is used as solid oxygen, The value is 2; when sodium peroxide is used as solid oxygen, The value is 1; when calcium superoxide is used as solid oxygen, The value is 1.

[0051] The specific flue gas content and the amount of solid oxygen used in each part of the combustible waste gas to be treated are shown in Table 2:

[0052] Table 2 Gas components and solid oxygen content in combustible waste gas (x, y, z are all between 0 and 1)

[0053]

[0054] Wherein, V is the total volume of the combustible waste gas to be treated, in L, and its value can be calculated according to formula (11):

[0055] V=1000Qt (11)

[0056] Where Q is the flue gas flow rate, in m 3 / h; t is the smoke leakage time, in hours. In the present invention, the total volume of O2 generated can be calculated according to formula (12):

[0057] The total volume of O2 required for catalytic oxidation of CO, CH4 and H2 can be calculated according to formula (13):

[0058]

[0059] In order to completely catalyze the combustible gases in the flue gas, the volume of O2 produced and the volume of O2 consumed Should satisfy Calculation shows that when the content of each component in the combustible waste gas to be treated meets:

[0060] When the combustion gas is fully catalyzed.

[0061] According to common knowledge in this field, the waste gas components in the chemical production process include CO2, CO, C n H m , H2 and other combustible gases, among which the content of CO2 and CO often exceeds 30% (for example, in the production of methanol synthesis, 2tCO2 needs to be released to produce 1t methanol), which can basically meet the conditions.

[0062] For example, if the gas components in a certain waste gas are CO2 (16.8 vol%), CO (18.5 vol%), CH3OH (33.9 vol%) and H2 (30.6 vol%), etc., and the total volume of the flue gas is 35829.7 L, according to calculation and actual working conditions, the flue gas needs 157442.9 g of potassium superoxide as an oxygen source, and the catalyst is used to separate it into 38223.1 g, 42091.0 g and 77128.8 g, which react with CO2, CO catalytic oxidation and non-methane CH compound catalytic oxidation in the flue gas to generate O2. For the convenience of production, the mass of the above KO2 can be rounded to 38230 g, 42100 g and 77200 g, and the total mass of the required KO2 is 157530 g.

[0063] In this embodiment, the first solid oxygen layer, the second solid oxygen layer and the third solid oxygen layer are made of any one of potassium superoxide, sodium peroxide and calcium superoxide.

[0064] The CO catalyst layer uses a copper-manganese catalyst, the non-methane CH compound catalyst layer and the H2 and methane mixed catalyst layer both use precious metal catalysts, and the precious metal catalyst includes any one of Pt / Al2O3, Pd / Al2O3, Pt / TiO2, Pd / TiO2, Pt / C, and Pd / C.

[0065] Specifically, the catalysts in the CO catalyst layer, the non-methane CH compound catalyst layer, and the H2 and methane mixed catalyst layer are in any form of columnar, spherical, or flaky particles or coated on a carrier (such as a honeycomb).

[0066] The volume of each catalyst layer is determined according to the following formula.

[0067]

[0068] Where V 催化剂 represents the volume of the catalyst, m 3 ; Q represents the flue gas volume flow rate, m 3 / h; V s Indicates airspeed, ranging from 1000 to 1000000h -1 .

[0069] The gaps between adjacent layers of the first solid oxygen layer, CO catalyst layer, second solid oxygen layer, non-methane CH compound catalyst layer, third solid oxygen layer, and H2 and methane mixed catalyst layer are no greater than 5 mm. By controlling the gaps between layers, space can be saved and the gas flow direction can be controlled.

[0070] Example 2

[0071] A catalytic conversion equipment for combustible exhaust gas, the equipment comprising the catalytic conversion unit described in Example 1, the catalytic conversion equipment comprising at least one of the catalytic conversion units.

[0072] The catalytic converter equipment has a simple structure, and has no other components except the catalytic converter unit, the housing and the connecting pipe. The structural form of the catalytic converter equipment includes any one of a disc shape, a cylindrical shape, a rectangular parallelepiped shape and a spiral shape.

[0073] The catalytic conversion equipment also includes a heat dissipation reactor, the structure of which is any one of a heat sink and a corrugated plate, and is installed on one side of the catalytic conversion unit.

[0074] Example 3

[0075] An application of a catalytic conversion equipment for combustible waste gas, wherein the catalytic conversion equipment described in Example 2 is used for the purification of combustible waste gas with no oxygen or low oxygen content (<5 vol%). This includes oxygen-free combustible gas generated during liquefied petroleum gas leakage, methanol synthesis production, acetylene synthesis production, battery thermal runaway, and coal chemical production. The catalytic conversion equipment for combustible waste gas provided by the present invention can reduce the risk of explosion.

[0076] Example 4

[0077] Table 3 is a gas composition table. It can be seen from Table 3 that the flue gas composition is simple, but the total flue gas volume and flue gas flow rate are large.

[0078] Table 3 Flue gas components and removal rates generated after a period of leakage in a methanol synthesis plant

[0079]

[0080] The gas was treated by the catalytic conversion equipment described in Example 2, wherein the catalyst was coated on a honeycomb carrier, and the volume of each catalyst layer was 300 cm 3 , the amount of solid oxygen (potassium superoxide) used is 157530g. The removal rate of all combustible gases is more than 90%, indicating that the catalytic conversion equipment provided by the present invention has a good flue gas treatment effect.

[0081] Example 5

[0082] Table 4 is a gas composition table. It can be seen from Table 4 that the smoke composition is simple, but the total smoke volume and smoke flow rate are large.

[0083] Table 4 Flue gas components and removal rates generated after a period of leakage of a CO storage tank in a coal chemical plant

[0084]

[0085]

[0086] The gas was treated by the catalytic conversion equipment described in Example 2, wherein the catalyst was coated on a honeycomb carrier, and the volume of each catalyst layer was 600 cm 3 , the amount of solid oxygen (potassium superoxide) used is 380000g. The removal rate of all combustible gases is more than 90%, indicating that the catalytic conversion equipment provided by the present invention has a good flue gas treatment effect.

[0087] Example 6

[0088] Table 5 is a table of gas composition of thermal runaway of a battery. It can be seen from Table 5 that the proportion of combustible gas in the flue gas is relatively large and the flue gas flow rate is relatively fast.

[0089] Table 5 Smoke components and removal rates generated after thermal runaway of a single lithium battery

[0090]

[0091] The gas was treated by the catalytic conversion equipment described in Example 2, wherein the catalyst was spherical and the volume of each layer of catalyst was 5 cm 3 , the amount of solid oxygen (potassium superoxide) used is 980g. The removal rate of all combustible gases is more than 90%, indicating that the catalytic conversion equipment provided by the present invention has a good flue gas treatment effect.

[0092] Example 7

[0093] Table 6 is a gas composition table. It can be seen from Table 6 that the flue gas composition is simple, and the total flue gas volume and flue gas flow rate are large.

[0094] Table 6 Smoke components and removal rates generated after a period of leakage in a liquefied petroleum gas production pipeline

[0095]

[0096] The gas was treated by the catalytic conversion equipment described in Example 2, wherein the catalyst was coated on a honeycomb carrier, and the volume of each layer of catalyst was 50 cm 3 , the amount of solid oxygen (potassium superoxide) used is 62000g. The removal rate of all combustible gases is more than 90%, indicating that the catalytic conversion equipment provided by the present invention has a good flue gas treatment effect.

[0097] Example 8

[0098] Table 7 is a gas composition table. It can be seen from Table 7 that the flue gas composition is complex, and the total flue gas volume and flue gas flow rate are large.

[0099] Table 7 Composition and removal rate of flue gas generated after a period of leakage in a coal-based synthetic ammonia production pipeline

[0100]

[0101] The gas was treated by the catalytic conversion equipment described in Example 2, wherein the catalyst was coated on a honeycomb carrier, and the volume of each layer of catalyst was 80 cm 3 , the amount of solid oxygen (potassium superoxide) used is 21600g. The removal rate of all combustible gases is more than 90%, indicating that the catalytic conversion equipment provided by the present invention has a good flue gas treatment effect.

[0102] Comparative Example 1

[0103] The gas in Example 4 was treated by adding O2 (without solid oxygen), and the combustible flue gas removal rate is shown in Table 8. Compared with Example 4, the method of adding O2 saves costs to a certain extent (without solid oxygen consumption), but the external O2 will take away a large amount of heat when flowing through the flue gas, reducing the catalytic performance of the catalyst, thereby reducing the combustible flue gas removal rate.

[0104] Table 8 Flue gas components and removal rates after a period of leakage in a methanol synthesis plant

[0105]

[0106] Comparative Example 2

[0107] Only one layer of solid oxygen and one layer of catalyst are provided to treat the gas in Example 4, and other reaction conditions are the same. At this time, the removal rate of combustible flue gas is shown in Table 9. Compared with Example 4, the solid oxygen and the catalyst are not arranged in sequence according to a certain ratio, which will result in that the solid oxygen cannot be fully utilized. Although the CO removal rate is high in the early stage, there is not enough O2 to participate in the catalytic oxidation reaction in the subsequent reaction, thereby reducing the removal rate of combustible flue gas.

[0108] Table 9 Composition of flue gas produced by a methanol synthesis plant after leakage for a period of time and its removal rate

[0109]

[0110] Comparative Example 3

[0111] The gas in Example 4 was treated with ethylene glycol, organic ether, and ionic liquid treatment agents, and the removal rate of combustible smoke is shown in Table 10. Compared with Example 4, although this method has a relatively good organic waste gas removal rate, its removal rate of CO and H2 is low. At the same time, it also has the disadvantages of high treatment cost and difficult recycling of treatment agents.

[0112] Table 10 Flue gas components and removal rates generated after a period of leakage in a methanol synthesis plant

[0113]

[0114] The catalytic conversion equipment provided by the present invention is an integrated combustible gas processing equipment, which can be a disposable product or a recycled product according to actual needs. When it is a recycled product, the solid oxygen in the unit needs to be replaced each time it is used up.

[0115] Finally, it should be noted that the above is only a preferred embodiment of the present invention and is not intended to limit the present invention. For ordinary technicians in this field, they can still modify or transform the technical solutions described above, which all fall within the scope of protection of the present invention.

Claims

1. A catalytic conversion unit for combustible exhaust gas, characterized in that: Along the flow direction of the combustible exhaust gas and according to the catalytic temperature range of various combustible gases in the exhaust gas, a first solid oxygen layer, a CO catalyst layer, a second solid oxygen layer, a non-methane CH compound catalyst layer, a third solid oxygen layer, and a H2 and methane mixed catalyst layer are arranged in sequence in the catalytic conversion unit.

2. A catalytic conversion unit for combustible exhaust gas according to claim 1, characterized in that: The combustible waste gas includes combustible gas and CO2; the combustible gas includes CO, non-methane CH compounds, H2 and methane.

3. A catalytic conversion unit for combustible exhaust gas according to claim 1, characterized in that: The first solid oxygen layer, the second solid oxygen layer and the third solid oxygen layer may be made of any one of potassium superoxide, sodium peroxide and calcium superoxide.

4. A catalytic conversion unit for combustible exhaust gas according to claim 3, characterized in that: According to the total volume of combustible waste gas to be treated and the content of different gas components in the combustible waste gas, the total consumption of solid oxygen is calculated according to the following formula: Among them, m 固态氧 is the mass of solid oxygen, in g; M solid oxygen is the relative molecular mass of solid oxygen, in g / mol; N is the molar volume of the gas, which is 22.4L / mol under standard conditions; V is the total volume of the combustible waste gas to be treated, in L; x, y, z, and p correspond to the contents of CO2, CO, non-methane CH compounds, and CH4 in the combustible waste gas to be treated, respectively, and the content of H2 is 1-xyzp; the values ​​of x, y, z, and p are all between 0 and 1; a and b are the reaction balancing coefficients for the reaction of solid oxygen and carbon dioxide to generate oxygen.

5. A catalytic conversion unit for combustible exhaust gas according to claim 1, characterized in that: The CO catalyst layer uses a copper-manganese catalyst, the non-methane CH compound catalyst layer and the H2 and methane mixed catalyst layer both use precious metal catalysts, and the precious metal catalyst includes any one of Pt / Al2O3, Pd / Al2O3, Pt / TiO2, Pd / TiO2, Pt / C, and Pd / C.

6. A catalytic conversion unit for combustible exhaust gas according to claim 1, characterized in that: The volume of each catalyst layer is determined according to the following formula: Where V 催化剂 represents the volume of the catalyst, m 3 ; Q represents the flue gas volume flow rate, m 3 / h; V s Indicates airspeed, ranging from 1000 to 1000000h -1 .

7. A catalytic conversion unit for combustible exhaust gas according to claim 1, characterized in that: In the first solid oxygen layer, CO catalyst layer, second solid oxygen layer, non-methane CH compound catalyst layer, third solid oxygen layer, H2 and methane mixed catalyst layer, the gap between adjacent layers is not greater than 5 mm.

8. A catalytic conversion device for combustible exhaust gas, comprising the catalytic conversion unit according to any one of claims 1 to 6, characterized in that: The catalytic conversion equipment includes at least one catalytic conversion unit.

9. The catalytic conversion equipment for combustible exhaust gas according to claim 8, characterized in that: The structural form of the catalytic conversion equipment includes any one of a disc shape, a cylindrical shape, and a rectangular parallelepiped shape; The catalytic conversion equipment also includes a heat dissipation reactor, the structure of which is any one of a heat sink and a corrugated plate, and is installed on one side of the catalytic conversion unit.

10. The use of a catalytic conversion device for combustible exhaust gas according to claim 8, characterized in that: The catalytic conversion equipment is used to purify combustible flue gas with an O2 content lower than the O2 content required for catalytic oxidation exhaust gas, including liquefied petroleum gas leakage, methanol synthesis production, acetylene synthesis production, battery thermal runaway, and oxygen-free combustible gas generated during coal chemical production.

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