Organic waste gas treatment method and treatment device

Abstract

The invention relates to an organic waste gas treatment method and device, organic waste gas enters a catalytic oxidation reactor after passing through a heating system, the reactor is filled with a plurality of layers of honeycomb matrix catalysts, the first layer to the nth layer are in contact with the waste gas firstly, n is more than or equal to 5 and less than or equal to 50, and the pore density of the honeycomb matrix of each layer of catalyst is reduced in a stepped manner. According to the invention, scouring of gas to a catalyst bed layer under a high-temperature condition can be slowed down, loss of active components of the catalyst and deformation and collapse of a surface structure are avoided, the service life of the catalyst is ensured, and long-term stable operation of the device is maintained.

Description

Technical Field

[0001] The present invention belongs to the technical field of environmental protection and atmospheric pollution control, and in particular relates to a method and a device for treating organic waste gas. Background Art

[0002] Volatile organic compounds (VOCs) are characteristic pollutants in oil refining and petrochemical industries. Catalytic oxidation is a widely used process for treating VOC-containing waste gas. The specific process is as follows: After the VOC waste gas is heated, it enters the catalytic oxidation reactor. The organic matter in the waste gas undergoes a catalytic oxidation reaction at 300-550°C under the action of a catalyst, producing CO2 and H2O, releasing a large amount of reaction heat. The purified gas is then discharged after heat exchange.

[0003] Currently, the most common catalytic oxidation catalyst is a monolithic catalyst, whose matrix is ​​a monolithic honeycomb matrix, and the matrix material is generally based on cordierite. For example, a honeycomb-type precious metal catalyst is a honeycomb rectangular matrix coated with a precious metal active coating for catalyzing VOCs exhaust gas and a carrier coating for adsorbing the active coating. When this type of catalyst is loaded into a reactor, it becomes a fixed bed reactor. When organic waste gas passes through the catalyst bed for catalytic oxidation, a large amount of heat is released, which increases the reaction temperature. If the exhaust gas concentration is high, the high-temperature gas under this condition will flush the catalyst surface for a long time, causing the loss of active components on the catalyst surface, and even the collapse and deformation of the surface structure of the catalyst carrier, which reduces the treatment effect of the catalyst and the exhaust gas cannot meet the relevant emission requirements. In order to meet increasingly stringent emission indicators, it is necessary to further increase the catalytic oxidation reaction temperature, forming a vicious cycle and seriously shortening the service life of the catalyst.

[0004] CN207025073U discloses an energy-saving and highly adaptable catalytic oxidation waste gas treatment device, comprising a heat exchanger, a heater, a catalytic oxidation reactor, an air cooler, a reflux air system, and a heat exchanger bypass system. The reflux air system includes a reflux air device and a control component, wherein the heat exchanger cold stream outlet is connected to the heater inlet, the heater outlet is connected to the catalytic oxidation reactor inlet, the catalytic oxidation reactor outlet is divided into two paths, one connected to the heat exchanger hot stream inlet, and the other connected to the reflux air device inlet; the heat exchanger hot stream outlet is connected to the air cooler inlet, the air cooler outlet is divided into two paths, one connected to the exhaust pipe, and the other connected to the reflux air device inlet, and the reflux air device outlet is connected to the heater exhaust inlet; the heat exchanger hot stream outlet is connected to the air cooler inlet, and the air cooler outlet is divided into two paths, one connected to the exhaust pipe and the other connected to the reflux air device inlet, and the reflux air device outlet is connected to the heater exhaust inlet; the heat exchanger bypass system connects the heat exchanger hot stream inlet and outlet. This patent can efficiently and energy-savingly treat intermittently discharged waste gas with large fluctuations in organic matter concentration, and achieve safe and stable operation of the waste gas treatment device. However, when faced with higher environmental protection requirements such as deep purification of exhaust gas, it is often necessary to further increase the reaction temperature, resulting in the end of the catalytic reactor bed being in a high-temperature environment for a long time. In this environment, the high-speed flow of gas will lead to a decrease in catalyst activity and a shortened service life.

[0005] CN105650651A discloses a method for purifying high-concentration organic waste gas, in which the organic waste gas is passed into a catalytic combustion reactor after heat exchange and preheating. An isolated catalyst bed is set in the reactor, and each bed is provided with a waste gas inlet and outlet. An oxygen supply port and a pipeline mixer are provided on the waste gas inlet pipeline. The organic matter in the waste gas undergoes a partial catalytic combustion reaction in each bed by means of segmented oxygen supply; according to the direction of waste gas flow, the waste gas outlet of the previous catalyst bed is connected to the waste gas inlet of the next bed through a heat recovery device, thereby taking out the reaction heat released by the catalytic combustion and realizing heat recovery. This invention can avoid the safety hazards caused by the deflagration of combustible gases and prevent the catalyst sintering caused by the excessive temperature of the catalyst bed. However, in order to avoid the bed from overheating, the catalyst bed temperature is prevented from being too high by means of segmented heat extraction, which makes its reactor structure more complicated and increases the investment and operation difficulty.

[0006] At present, in actual industrial production, in order to meet relevant emission requirements or achieve deep purification requirements, it is often necessary to further increase the reaction temperature of catalytic oxidation, which puts higher requirements on the regulation of the catalyst and the reaction process. In particular, because the oxidation reaction is exothermic, the heated airflow flushes the catalyst terminal bed at high temperature and high flow rate for a long time, which can easily cause the loss of active components of the catalyst and even cause the deformation and collapse of the catalyst surface structure, greatly reducing the service life of the catalyst. Summary of the Invention

[0007] To address the shortcomings of existing technologies, the present invention provides a method and device for treating organic waste gas. This method can mitigate the impact of gas on the catalyst bed under high-temperature conditions, preventing the loss of active catalyst components and surface structural deformation and collapse, thereby extending the catalyst's service life and maintaining long-term stable operation of the device.

[0008] The first aspect of the present invention provides a method for treating organic waste gas, comprising the following contents:

[0009] After passing through the heating system, the organic waste gas enters the catalytic oxidation reactor. The reactor is filled with several layers of honeycomb matrix catalysts. The first layer contacts the waste gas, followed by the nth layer, where 5≤n≤50. The pore density of the honeycomb matrix of each layer of catalyst decreases step by step.

[0010] In the present invention, the pore density of the honeycomb substrate of the first layer of catalyst is generally 100-500 pores / in 2 , preferably 200-300 holes / in 2 The pore density of the honeycomb matrix of the nth layer catalyst is generally 20-150 pores / in 2 , preferably 20-100 holes / in 2 The pore density of the honeycomb matrix of two adjacent catalyst layers varies from 10 to 100 pores / in. 2 .

[0011] In the present invention, from the first layer to the nth layer, the pore density of the honeycomb substrate of two adjacent catalyst layers has the same change range or changes in an arithmetic progression, and the tolerance of the arithmetic progression is 2-10.

[0012] In the present invention, each catalyst layer is composed of a plurality of honeycomb-based catalyst layers with the same pore density. The cross-section of each honeycomb-based catalyst layer is a polygonal shape that can be densely packed. The densely packed shape can be selected according to the cross-sectional shape of the catalytic oxidation reactor. The polygonal shape can be any of triangles, quadrilaterals, and regular hexagons, preferably squares, rectangles, and regular hexagons. The cross-sectional dimensions of each honeycomb-based catalyst layer are determined according to the packing requirements and range from 100 to 600 mm, with a preferred side length of 125 to 300 mm.

[0013] In the present invention, each honeycomb catalyst substrate generally has a rectangular parallelepiped or cube-shaped structure, and is generally 20-100 mm tall. The height of each layer of honeycomb catalyst substrate is determined based on the total loading height of the catalyst bed. The height of each layer can be the same or vary step by step. Each layer of honeycomb catalyst substrate has the same pore density.

[0014] In the present invention, the honeycomb substrate is preferably a cordierite honeycomb substrate, more preferably a cordierite honeycomb ceramic substrate.

[0015] In the present invention, the honeycomb substrate catalyst adopts a conventional catalytic oxidation catalyst, such as coating a carrier coating of an adsorption active coating on a honeycomb substrate, and then coating a precious metal active coating for catalyzing VOCs exhaust gas.

[0016] The active coating layer is an active metal conventionally used in catalytic oxidation catalysts, preferably a noble metal component, more preferably Pt and / or Pd, with a loading amount of 0.01%-0.15%.

[0017] The carrier coating is at least one of an alumina coating, a silica coating, and a molecular sieve coating, and the coating content is 5%-15% of the mass of the honeycomb matrix. A modified TS-1 molecular sieve is further preferably used, and the modification method is as follows: TS-1 molecular sieve, tetrachlorosilane, and acetone are mixed, refluxed at 70-80°C, filtered, washed, and dried to obtain the modified TS-1 molecular sieve. The specific surface area of ​​TS-1 molecular sieve is 400-450m 2 / g, pore volume is 0.39-0.41cm 3 / g. TS-1 molecular sieve, tetrachlorosilane, and acetone are mixed in a mass ratio of 1:20-30:10-20. After mixing, reflux the mixture at 70-80°C for 6-10 hours. After the reaction, filter the mixture, rinse with ethanol until no chloride ions are detected, and dry at 100-120°C for 2-5 hours to obtain the modified TS-1 molecular sieve.

[0018] In the present invention, the heating system mainly includes a heat exchanger and / or a heater, which heats the organic waste gas to the starting temperature required for the catalytic oxidation reaction, generally 100-500°C, preferably 250-450°C. The heat exchanger preferably uses the high-temperature purified gas discharged from the reactor as the heat medium in the heat exchanger. If the temperature cannot reach the starting temperature after heat exchange, it is heated by the heater. In principle, the heater is used at the start-up of the device and is no longer activated when the entire reaction system reaches thermal equilibrium.

[0019] In the present invention, the total hydrocarbon concentration in the organic waste gas is generally 2000-8000 mg / m 3 , preferably 3500-5500mg / m 3 .

[0020] The second aspect of the present invention also provides a treatment device for the above-mentioned organic waste gas treatment method of the present invention, which includes a heating system and a catalytic oxidation reactor in sequence according to the flow direction of the waste gas, wherein the heating system is used to heat the waste gas to the starting temperature required for the catalytic oxidation reaction; the catalytic oxidation reactor is filled with a honeycomb matrix catalyst, and the first layer contacts the waste gas, followed by the nth layer, where 5≤n≤50, and the pore density of the honeycomb matrix of each layer of catalyst decreases step by step.

[0021] In the device of the present invention, the heating system primarily comprises a heat exchanger and / or a heater. Preferably, the high-temperature purified gas discharged from the reactor outlet serves as the heat medium in the heat exchanger. If the temperature cannot reach the starting temperature after heat exchange, the heater is used for heating. In principle, the heater is used at device startup and is not activated after the entire reaction system reaches thermal equilibrium. The heat exchanger can be any of a heat pipe, shell-and-tube, or plate type, with a plate type being preferred. The heater can be any of an electric heater, a gas heater, or a fuel oil heater, with an electric heater being preferred.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] The catalytic oxidation reactor of the present invention is filled with several layers of honeycomb matrix catalysts, and the pore density of the honeycomb matrix of each layer of catalyst is reduced in a step-by-step manner according to the flow of exhaust gas. When treating high-concentration VOCs-containing exhaust gas, on the one hand, it can effectively slow down the scouring of the catalyst surface by the high-temperature gas at the end of the catalyst bed, thereby avoiding the loss of active components; on the other hand, the reduction in pore density can reduce the pressure of the high-temperature gas at the end of the bed on the catalyst, thereby reducing the deformation and collapse of the catalyst carrier structure caused by high temperature and high pressure, thereby effectively maintaining the activity and service life of the catalyst and maintaining the long-term stable operation of the device.

[0024] The method of the present invention can flexibly respond to changes in exhaust gas concentration and the requirements of the reaction system for improved emission standards, making it more flexible to increase the reaction temperature to improve the purification depth, thereby ensuring the reaction activity and service life of the catalyst.

[0025] The carrier coating of the honeycomb substrate catalyst of the present invention adopts modified TS-1 molecular sieve, that is, TS-1 molecular sieve modified by synergistically using tetrachlorosilane and acetone, has excellent binding force, avoids loss of active metals, and has good long-term operation stability. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 This is a process flow chart of the waste gas treatment method of the present invention; wherein, 1-blower, 2-heat exchanger, 3-heater, 4-catalytic oxidation reactor, 5-exhaust pipe.

[0027] Figure 2 It is a side view of the honeycomb matrix catalyst of the present invention loaded according to the variation of pore density. DETAILED DESCRIPTION

[0028] The following examples further illustrate the technical solution of the present invention and its effects. The examples are implemented based on the technical solution of the present invention, and provide detailed implementation methods and specific operating processes, but the protection scope of the present invention is not limited to the following examples.

[0029] The experimental methods in the following examples, unless otherwise specified, are all conventional methods in the art. The experimental materials used in the following examples, unless otherwise specified, can all be purchased from biochemical reagent stores.

[0030] The waste gas treatment device of the present invention is as shown in the attached Figure 1 As shown, according to the exhaust gas flow direction, it includes a heating system and a catalytic oxidation reactor in sequence, wherein the heating system mainly includes a heat exchanger 1 and a heater 2, which are used to heat the exhaust gas to the starting temperature required for the catalytic oxidation reaction; the catalytic oxidation reactor is filled with a honeycomb matrix catalyst, and according to the exhaust gas flow direction, the pore density of the honeycomb matrix of each layer of catalyst decreases step by step, that is, the first layer to contact with the exhaust gas is the first layer, and the pore density decreases step by step to the nth layer, where 5≤n≤50, and the pore density decreases step by step from the first layer to the nth layer.

[0031] In the present invention, the preparation method of the honeycomb substrate catalyst is as follows: (1) selecting or preparing a honeycomb substrate with different pore densities according to the filling requirements; (2) immersing the honeycomb substrate in a carrier coating slurry, wherein the carrier coating is at least one of an alumina coating, a silica coating, a molecular sieve coating, etc., and the coating content is 5%-15% of the mass of the honeycomb substrate; further preferably, a modified TS-1 molecular sieve is used, and the modification method is as follows: mixing TS-1 molecular sieve, tetrachlorosilane, and acetone, reflux reaction at 70-80°C, filtering, washing, and drying to obtain the modified TS-1 molecular sieve; and (3) coating a precious metal active coating, wherein the active metal is Pt and / or Pd, and the loading amount is 0.01%-0.15%.

[0032] Example 1

[0033] The preparation method of honeycomb matrix catalyst is as follows: (1) according to the filling requirements, the pore density is selected as 200 pores / in 2 、190 holes / in 2 、180 holes / in 2 、170 holes / in 2 、160 holes / in 2 、150 holes / in 2 、140 holes / in 2 、130 holes / in 2 、120 holes / in 2 、110 holes / in 2 The cordierite honeycomb ceramic substrate is a rectangular parallelepiped structure with dimensions of 150×150×50 mm. (2) The honeycomb substrate is immersed in a carrier coating slurry. The carrier coating is an alumina coating with a coating content of 10% of the honeycomb substrate mass. (3) The precious metal active coating is then applied. The active metals are Pt and Pd, with a loading of 0.08%, respectively. Honeycomb substrate catalysts with different pore densities are obtained after calcination at 500°C for 120 minutes and drying for 5 hours.

[0034] The honeycomb matrix catalyst is placed in the order of the first layer that contacts the exhaust gas, and then in the order of the tenth layer, starting from the first layer with 200 holes / in 2 To the 10th layer hole 110 holes / in 2 The density of each layer is gradually reduced by 10 holes / in 2 Filling.

[0035] The total hydrocarbon concentration in organic waste gas is 4000-5000 mg / m 3 After being heated to 350°C, it enters the catalytic oxidation reactor. During the startup phase, the heater is used for heating. When the entire reaction system reaches thermal equilibrium, the heater is no longer activated. The high-temperature purified gas discharged from the reactor is used as the heat medium in the heat exchanger. If the temperature cannot reach the starting temperature after heat exchange, the heater is activated again.

[0036] After about 6 months of stable operation, the concentration of non-methane total hydrocarbons in the discharged purified gas has always been lower than 60mg / m 3 No catalyst hot spots or overheating at the end of the fixed bed have occurred during long-term operation. 150 holes / in with the same number of layers as the original filling. 2 Compared with the catalyst bed solution, the catalyst service life is increased by 8%.

[0037] Example 2

[0038] The preparation method of honeycomb matrix catalyst is as follows: (1) according to the filling requirements, the pore density is selected to be 275 pores / in 2 、250 holes / in 2 、225 holes / in 2 , 200 holes / in 2 、175 holes / in 2 、150 holes / in 2 、125 holes / in 2 、100 holes / in 2 , 75 holes / in 2 、50 holes / in 2 (1) preparing a cuboid cordierite honeycomb ceramic substrate with dimensions of 150 × 150 × 50 mm; (2) immersing the honeycomb substrate in a carrier coating slurry, wherein the carrier coating is a silica coating with a coating content of 10% of the honeycomb substrate mass; (3) coating the substrate with a precious metal active coating, wherein the active metal is Pt with a loading of 0.08%. The catalysts were calcined at 500°C for 120 minutes and dried for 5 hours to obtain honeycomb substrate catalysts with different pore densities.

[0039] The honeycomb matrix catalyst is filled in the order of decreasing pore density, with the pore density decreasing by 25 pores / in per layer from the 1st to the 10th layer. 2 Filling is done in the order of 275 holes / in 2、250 holes / in 2 、225 holes / in 2 , 200 holes / in 2 、175 holes / in 2 、150 holes / in 2 、125 holes / in 2 、100 holes / in 2 , 75 holes / in 2 、50 holes / in 2 Filling.

[0040] The total hydrocarbon concentration in organic waste gas is 4500-5500 mg / m 3 After being heated to 400°C, it enters the catalytic oxidation reactor. During the startup phase, the heater is used for heating. When the entire reaction system reaches thermal equilibrium, the heater is no longer activated. The high-temperature purified gas discharged from the reactor is used as the heat medium in the heat exchanger. If the temperature cannot reach the starting temperature after heat exchange, the heater is activated again.

[0041] After about 6 months of stable operation, the concentration of non-methane total hydrocarbons in the discharged purified gas has always been below 50mg / m 3 No catalyst hot spots or overheating at the end of the fixed bed have occurred during long-term operation. The same layer as the original filling is uniform with 200 holes / in 2 Compared with the catalyst bed solution, the catalyst service life is increased by 11%.

[0042] Example 3

[0043] The preparation method of honeycomb matrix catalyst is as follows: (1) according to the filling requirements, the pore density is selected to be 300 pores / in 2 -60 holes / in 2 The cordierite honeycomb ceramic matrix has a reduction of 20 holes / in per layer. 2 The cordierite honeycomb ceramic substrate is a rectangular parallelepiped with dimensions of 150×150×50 mm. (2) The honeycomb substrate is immersed in a carrier coating slurry, wherein the carrier coating is a TS-1 molecular sieve coating with a coating content of 10% of the honeycomb substrate mass. (3) A precious metal active coating is then applied, wherein the active metal is Pd with a loading of 0.08%. The honeycomb substrate catalyst is calcined at 500°C for 120 minutes and dried for 5 hours.

[0044] The honeycomb matrix catalyst is filled in the order of decreasing pore density, with the pore density decreasing by 20 pores / in per layer from the 1st to the 10th layer. 2 Filling is carried out, that is, 300 holes / in 2 、280 holes / in 2 、260 holes / in 2 、…140 holes / in 2、120 holes / in 2 Filling.

[0045] The total hydrocarbon concentration in organic waste gas is 4000-5500 mg / m 3 After being heated to 380°C, it enters the catalytic oxidation reactor. During the startup phase, the heater is used for heating. When the entire reaction system reaches thermal equilibrium, the heater is no longer activated. The high-temperature purified gas discharged from the reactor is used as the heat medium in the heat exchanger. If the temperature cannot reach the starting temperature after heat exchange, the heater is activated again.

[0046] After about 6 months of stable operation, the concentration of non-methane total hydrocarbons in the discharged purified gas has always been lower than 54mg / m 3 No catalyst hot spots or overheating at the end of the fixed bed have occurred during long-term operation. The same layer as the original filling is uniform with 200 holes / in 2 Compared with the catalyst bed solution, the catalyst service life is increased by 7%.

[0047] Example 4

[0048] Same as Example 3, except that: from the 1st layer to the nth layer, the variation range of the pore density of each layer is arithmetic, with a tolerance of 5, and the pore density of the honeycomb matrix selected from the 1st to the 10th layer is 300 pores / in 2 、290 holes / in 2 、275 holes / in 2 、255 holes / in 2 、230 holes / in 2 , 200 holes / in 2 、165 holes / in 2 、125 holes / in 2 、80 holes / in 2 、30 holes / in 2 Filling.

[0049] After about 6 months of stable operation, the concentration of non-methane total hydrocarbons in the discharged purified gas has always been lower than 45mg / m 3 No catalyst hot spots or overheating at the end of the fixed bed have occurred during long-term operation. The same layer as the original filling is uniform with 200 holes / in 2 Compared with the catalyst bed solution, the catalyst service life is increased by 12%.

[0050] Example 5

[0051] Same as Example 2, except that the cross section of the honeycomb matrix is ​​an equilateral triangle with a side length of 150 mm and a height of 50 mm. After about 6 months of stable operation, the concentration of non-methane total hydrocarbons in the discharged purified gas is always lower than 57 mg / m 3No catalyst hot spots or overheating at the end of the fixed bed have occurred during long-term operation. The same layer as the original filling is uniform with 200 holes / in 2 Compared with the catalyst bed solution, the catalyst service life is increased by 8.5%.

[0052] Example 7

[0053] The same as Example 2, except that the coating carrier uses modified TS-1 molecular sieve, TS-1 molecular sieve, tetrachlorosilane, and acetone are mixed in a mass ratio of 1:20:20, refluxed at 75°C for 6 hours, filtered, washed with ethanol until no chloride ions are detected, and dried at 100°C for 5 hours to obtain modified TS-1 molecular sieve. The specific surface area of ​​TS-1 molecular sieve is 400m 2 / g, and the pore volume is 0.4cm 3 / g.

[0054] After about 6 months of stable operation, the concentration of non-methane total hydrocarbons in the discharged purified gas has always been lower than 33mg / m 3 , no catalyst high temperature hot spots and fixed bed end overheating phenomenon occurred during long-term operation. The same layer as the original filling is uniform with 200 holes / in 2 Compared with the catalyst bed solution, the catalyst service life is increased by 18%.

[0055] Comparative Example 1

[0056] Same as Example 2, except that the density of honeycomb matrix catalyst pores remains unchanged and the same number of layers are loaded, with each layer having 275 pores / in. 2 Under the same test conditions as in Example 1, after about 6 months of operation, the concentration of non-methane total hydrocarbons in the discharged purified gas was stable at less than 50 mg / m 3 , catalyst service life and uniformity 200 holes / in 2 Compared with the design of 10 catalyst beds, the service life of the catalyst is reduced by 3%.

[0057] Comparative Example 2

[0058] Same as Example 2, except that the density of honeycomb matrix catalyst pores remains unchanged and the same number of layers are loaded, with 50 pores / in each layer. 2 Under the same test conditions as in Example 1, after about 6 months of operation, the non-methane total hydrocarbon content of the purified gas could not meet the 120 mg / m 3 indicators.

Claims

1. A method for treating organic waste gas, characterized in that It includes the following contents: After passing through the heating system, the organic waste gas enters the catalytic oxidation reactor. Several layers of honeycomb matrix catalysts are loaded in the reactor. The first layer contacts the waste gas, followed by the nth layer, where 5≤n≤50. The pore density of the honeycomb matrix of each layer of catalyst decreases step by step.

2. The method according to claim 1, wherein: The pore density of the honeycomb substrate of the first layer of catalyst is 100-500 pores / in 2 , preferably 200-300 holes / in 2 The pore density of the honeycomb matrix of the nth layer catalyst is 10-150 pores / in 2 , preferably 20-120 holes / in 2 .

3. The method according to claim 1, wherein: The pore density of the honeycomb matrix of two adjacent catalyst layers varies from 10 to 100 pores / in 2 .

4. The method according to claim 1 or 3, characterized in that: From the first layer to the nth layer, the pore density of the honeycomb substrate of two adjacent catalyst layers has the same change range or changes in an arithmetic progression, and the tolerance of the arithmetic progression is 2-10.

5. The method according to claim 1, wherein: Each catalyst layer is composed of a number of honeycomb matrix catalysts with the same pore density. The cross-section of each honeycomb matrix catalyst is a densely packed polygon, which is densely packed according to the cross-sectional shape of the catalytic oxidation reactor. The polygon is selected from any one of a triangle, a quadrilateral, and a regular hexagon, preferably any one of a square, a rectangle, and a regular hexagon.

6. The method according to claim 1 or 5, characterized in that: The cross-sectional size of each honeycomb substrate catalyst is determined according to the filling requirements, and is generally 100-600 mm, with a preferred side length of 125-300 mm.

7. The method according to claim 1 or 5, characterized in that: Each honeycomb matrix catalyst is in the form of a rectangular parallelepiped or cube structure, and is generally 20-100 mm in height.

8. The method according to claim 1, wherein: The honeycomb matrix is ​​preferably a cordierite honeycomb matrix, more preferably a cordierite honeycomb ceramic matrix.

9. The method according to claim 1, wherein: The honeycomb substrate catalyst adopts a carrier coating of an adsorption active coating coated on a honeycomb substrate, and then coated with a precious metal active coating for catalyzing VOCs exhaust gas; wherein the active coating is an active metal conventionally used for catalytic oxidation catalysts, preferably a precious metal component, more preferably Pt and / or Pd, with a loading amount of 0.01%-0.15%.

10. The method according to claim 9, characterized in that: The carrier coating is at least one of an aluminum oxide coating, a silicon dioxide coating, and a molecular sieve coating, and the coating content is 5%-15% of the mass of the honeycomb substrate.

11. The method according to claim 9 or 10, characterized in that: The carrier coating adopts modified TS-1 molecular sieve, and the modification method is: TS-1 molecular sieve, tetrachlorosilane and acetone are mixed, refluxed at 70-80 DEG C for reaction, filtered, washed and dried to obtain the modified TS-1 molecular sieve.

12. The method according to claim 11, characterized in that: The specific surface area of ​​TS-1 molecular sieve is 400-450m 2 / g, pore volume is 0.39-0.41cm 3 / g; TS-1 molecular sieve, tetrachlorosilane and acetone are mixed in a mass ratio of 1:20-30:10-20; after mixing, reflux reaction is carried out at 70-80°C for 6-10 hours; after the reaction is completed, it is filtered, washed with ethanol until no chloride ions are detected, and dried at 100-120°C for 2-5 hours to obtain a modified TS-1 molecular sieve.

13. The method according to claim 1, wherein: The heating system includes a heat exchanger and / or a heater to heat the organic waste gas to 100-500°C, preferably 250-450°C.

14. The method according to claim 13, wherein: The heat exchanger uses the high-temperature purified gas discharged from the reactor as the heat medium in the heat exchanger. If the temperature cannot reach the starting temperature after heat exchange, it is heated by a heater. In principle, the heater is used when the device is started. When the entire reaction system reaches heat balance, the heater is no longer started.

15. The method according to claim 1, wherein: The total hydrocarbon concentration in the organic waste gas is 2000-8000 mg / m 3 , preferably 3500-5500mg / m 3 .

16. A treatment device for the organic waste gas treatment method according to any one of claims 1 to 15, characterized in that: According to the flow direction of exhaust gas, the system includes a heating system and a catalytic oxidation reactor, wherein the heating system is used to heat the exhaust gas to the starting temperature required for the catalytic oxidation reaction; the catalytic oxidation reactor is filled with a honeycomb matrix catalyst, and the first layer to contact with the exhaust gas is the first layer, followed by the nth layer, where 5≤n≤50, and the pore density of the honeycomb matrix of each layer of catalyst decreases step by step.

17. The processing device according to claim 16, characterized in that: The heating system includes a heat exchanger and / or a heater. The heat exchanger is any one of a heat pipe type, a shell and tube type, and a plate type heat exchanger, preferably a plate type heat exchanger; the heater is any one of an electric heater, a gas heater, and a fuel heater, preferably an electric heater.

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