Organic exhaust gas treatment system and method for reducing nitrogen oxides

Abstract

This invention relates to an organic waste gas treatment system and method for reducing nitrogen oxides. The system primarily involves a direct-fired incinerator (TO) discharging waste gas containing at least one nitrogen oxide (NOx) into a treatment output pipeline. At least a portion of the gas after secondary adsorption is then transported to the treatment output pipeline via a clean gas discharge bypass pipeline. This allows the gas to mix with the waste gas in the treatment output pipeline, thereby reducing its temperature. The mixture then enters an ammonia-free catalyst device for denitrification. This process improves the efficiency of volatile organic waste gas treatment and reduces nitrogen oxide emissions.

Description

Technical Field

[0001] This invention relates to an organic exhaust gas treatment system and method for reducing nitrogen oxides, particularly to an volatile organic exhaust gas treatment system or similar equipment that can improve the efficiency of volatile organic exhaust gas treatment and reduce nitrogen oxide emissions, and is applicable to the semiconductor industry, optoelectronic industry or chemical-related industries. Prior Technology

[0002] Currently, volatile organic compounds (VOCs) are generated during the manufacturing processes of the semiconductor and optoelectronic industries. These VOCs contain compounds such as nitrogen oxides (NOx) and sulfur oxides (SOx), which are important causes of photochemical smog, acid rain, and human respiratory diseases.

[0003] In recent years, due to increased environmental awareness and increasingly stringent environmental laws, denitrification equipment after combustion has gradually gained attention. Traditional denitrification technologies, such as selective catalytic reduction (SCR) or selective non-catalytic reduction (SNCR), treat nitrogen oxides (NOx) by injecting urea or ammonia as reducing agents to carry out the reaction.

[0004] Therefore, in view of the above-mentioned deficiencies, the inventors aim to propose an organic exhaust gas treatment system and method for reducing nitrogen oxide emissions, which does not require the injection of urea or ammonia as a reducing agent for the reaction, and is easy for users to operate and assemble. The inventors have devoted themselves to research, design and assembly to provide convenience for users, which is the motivation for the invention. Summary of the Invention

[0005] The main objective of this invention is to provide an organic waste gas treatment system and method for reducing nitrogen oxides. The system primarily involves sending treated waste gas containing at least one nitrogen oxide (NOx) from the outlet of a direct-fired incinerator (TO) into a treated output pipeline. At least a portion of the gas after secondary adsorption is then transported to the treated output pipeline through a clean gas discharge bypass pipeline. This allows the gas to mix with at least a portion of the treated waste gas in the treated output pipeline, thereby reducing the temperature of the treated waste gas. The mixture then enters an ammonia-free catalyst device for a denitrification reaction. This improves the efficiency of volatile organic waste gas treatment and reduces nitrogen oxide emissions, thus increasing overall practicality.

[0006] A second objective of this invention is to provide an organic exhaust gas treatment system and method for reducing nitrogen oxides. The system generates ozone through an ozone generator and delivers it to an ammonia-free catalyst device via an ozone delivery pipeline. The inlet of the ammonia-free catalyst device is connected to the other end of the treatment output pipeline, allowing at least a portion of the mixed exhaust gas to enter the ammonia-free catalyst device for a denitrification reaction. The ammonia-free catalyst device is equipped with at least one catalyst. The denitrification reaction in the ammonia-free catalyst device utilizes oxygen and the catalyst to oxidize at least one nitrogen oxide (NOx) in the exhaust gas, generating a denitrification reaction gas, which is then output to the chimney for emission via the ammonia-free catalyst output pipeline. This improves the efficiency of nitrogen oxide (NOx) removal, thereby improving the efficiency of nitrogen oxide (NOx) emission reduction and increasing overall efficiency.

[0007] Another objective of this invention is to provide an organic exhaust gas treatment system and method for reducing nitrogen oxides. A dust collector is installed in the treatment output pipeline, and the dust collector has an inlet and an outlet. When at least a portion of the treated exhaust gas in the treatment output pipeline contains at least one particulate matter, the at least a portion of the treated exhaust gas enters the dust collector through the inlet to collect the at least one particulate matter, and then exits it to the treatment output pipeline through the outlet of the dust collector, thus achieving a dust removal effect and increasing the overall usability.

[0008] Another objective of this invention is to provide an organic exhaust gas treatment system and method for reducing nitrogen oxides. The system allows the gas to be treated (e.g., a mixture containing one or more volatile organic compounds and air) to be transported to the outlet via an air duct, and then flows out through an air passage between the outlet and the surrounding shield to the front of the combustion flame generated by the burner. This increases the efficiency of destroying the volatile organic compounds contained in the gas to be treated. On the other hand, the combustion gas (e.g., air or oxygen) entering the combustion gas inlet of the burner is designed to be increased by more than 20% to 30% of the combustion equivalent. This excess combustion gas lowers the temperature of the combustion flame generated by the burner. Therefore, the production of nitrogen oxides by the gas to be treated (e.g., a mixture containing one or more volatile organic compounds and air) is reduced after passing through the combustion flame, thus reducing nitrogen oxide production and improving overall operability.

[0009] To further understand the features, characteristics, and technical content of this invention, please refer to the following detailed description and accompanying drawings. However, the accompanying drawings are provided for reference and illustration only and are not intended to limit the invention. Simple Explanation of the Diagram

[0010]

[0011] Figure 1 is a schematic diagram of the system architecture of the present invention.

[0012] Figure 2 is a schematic diagram of the system architecture of the present invention with a dust collector.

[0013] Figure 3 is a schematic diagram of the system architecture of the present invention with a fan.

[0014] Figure 4 is a schematic diagram of the system architecture of the present invention, which includes a fan and a dust collector.

[0015] Figure 5 is a flowchart of the main steps of this invention.

[0016] Figure 6 is a flowchart of the present invention with the step of inputting the first cooling gas.

[0017] Figure 7 is a flowchart of the step of inputting a second cooling gas according to the present invention. Implementation

[0018] Please refer to Figures 1-7, which are schematic diagrams of embodiments of the present invention. The preferred embodiment of the organic exhaust gas treatment system and method for reducing nitrogen oxides of the present invention is applied to volatile organic exhaust gas treatment systems or similar equipment in the semiconductor industry, optoelectronic industry or chemical-related industries. It can improve the efficiency of volatile organic exhaust gas treatment and has the effect of reducing nitrogen oxide emissions.

[0019] The organic exhaust gas treatment system for reducing nitrogen oxides of the present invention mainly includes a direct-fired incinerator (TO) 10, a first heat exchanger 11, a second heat exchanger 12, a third heat exchanger 13, a fourth heat exchanger 14, a first cold-side conveying pipeline 21, a fourth cold-side conveying pipeline 22, a first adsorption rotor 30, a second adsorption rotor 40, a chimney 50, a chimney conveying pipeline 51, a clean gas emission bypass pipeline 60, and a non-toxic... The ammonia catalyst unit 70 is designed as shown in Figures 1 to 4. The first heat exchanger 11 has a first cold-side pipe 111 and a first hot-side pipe 112; the second heat exchanger 12 has a second cold-side pipe 121 and a second hot-side pipe 122; the third heat exchanger 13 has a third cold-side pipe 131 and a third hot-side pipe 132; and the fourth heat exchanger 14 has a fourth cold-side pipe 141 and a fourth hot-side pipe 142. The direct-fired incinerator (TO) 10 has a burner head 101 and a furnace chamber 102, which are connected. The first heat exchanger 11, the second heat exchanger 12, the third heat exchanger 13, and the fourth heat exchanger 14 are respectively located in the furnace chamber 10 of the direct-fired incinerator (TO) 10. Inside 02, the direct-fired incinerator (TO) 10 is provided with an inlet 103, an outlet 104, a processing output pipe 15, an air duct 16, and an enclosing cover 17 (as shown in Figures 1 to 4). The inlet 103 is located at the burner head 101, and the outlet 104 is located at the furnace chamber 102. One end of the processing output pipe 15 is connected to the outlet 104 of the direct-fired incinerator (TO) 10. The direct-fired incinerator (TO) 10 generates a processing exhaust gas, which contains at least one nitrogen oxide (NOx), and the processing exhaust gas is output to the processing output pipe 15 through the outlet 104 of the direct-fired incinerator (TO) 10.

[0020] The air duct 16 is located inside the direct-fired incinerator (TO) 10, and the burner head 101 is attached to the direct-fired incinerator (TO) 10. The air duct 16 is connected to the inlet 103 of the direct-fired incinerator (TO) 10. The burner head 101 is provided with a channel 1011, and the burner head 101 is provided with a burner head cover 1012, a gas fuel pipe 1013, and a combustion-supporting gas inlet 1017 (as shown in Figures 1 to 2). As shown in Figure 4, the combustion-supporting gas inlet 1017 can be located at one end or the side of the channel 1011, and the combustion-supporting gas inlet 1017 is for a combustion-supporting gas (not shown) to enter, wherein the combustion-supporting gas system is either air or oxygen, and a fan (not shown) can be provided at one end of the channel 1011 to increase the flow rate of the combustion-supporting gas and enable the combustion-supporting gas to enter the channel 1011 of the burner head 101.

[0021] The gas fuel pipe 1013 has a gas fuel inlet 1014, at least one first gas outlet 1015 and at least one second gas outlet 1016. The at least one first gas outlet 1015 of the gas fuel pipe 1013 is located in the channel 1011 of the burner head 101, and the burner head cover 1012 is located at the second gas outlet 1016 of the gas fuel pipe 1013. The gas fuel inlet 1014 is for a gas fuel (not shown) to enter, wherein the gas fuel is either natural gas or coal gas. The gas fuel is ejected from the channel 1011 of the burner head 101 through the first gas outlet 1015, and the gas fuel is ejected from the second gas outlet 1016, generating a combustion flame 1018. Furthermore, the burner head cover 1012 is equipped with a mounting panel (not shown) and is mounted on the direct-fired incinerator (TO) 10 through the mounting panel, so that part of the burner head 101 is exposed outside the direct-fired incinerator (TO) 10. The gas fuel inlet 1014 of the gas fuel pipe 1013 is located outside the direct-fired incinerator (TO) 10, so that the gas fuel can easily enter through the gas fuel inlet 1014. The combustion gas inlet 1017 is also located outside the direct-fired incinerator (TO) 10, so that the combustion gas can easily enter through the combustion gas inlet 1017.

[0022] Furthermore, at least one heat insulation cotton 163 is provided between the air duct 16 and the direct-fired incinerator (TO) 10 to form a barrier protection. The air duct 16 is made of metal and is connected to the inlet 103 of the direct-fired incinerator (TO) 10, so that the desorbed concentrated gas (such as a mixture containing one or more volatile organic compounds and air) can enter the air duct 16. The air duct 16 is provided with an air outlet 161. In addition, one part of the air duct 16 is provided for the burner head cover 1012 of the burner head 101, and the burner head cover 1012 corresponds to the air outlet 161. Furthermore, the enclosure 17 is installed inside the direct-fired incinerator (TO) 10. The enclosure 17 is made of metal and can be any one of the following shapes: conical, spherical, trumpet-shaped, square, or circular, designed to fit the current situation. One end of the enclosure 17 is attached to the burner head cover 1012, and the other end of the enclosure 17 extends from the air outlet 161 of the air duct 16. The air outlet 161 of the air duct 16 is larger than the enclosure 17, so that the air outlet 161 of the air duct 16 and the enclosure 17 are connected. An air passage 162 is provided between the enclosures 17. When the gaseous fuel is ejected from the second air port 1016 and the combustion flame 1018 is generated, the combustion flame 1018 passes through the enclosure 17 from the burner head cover 1012 of the burner head 101. The enclosure 17 prevents the combustion flame 1018 from being affected by the desorbed concentrated gas (such as a mixture of air containing one or more volatile organic compounds) entering and affecting the direction of the combustion flame 1018. This allows the combustion flame 1018 to be concentrated into a bundle, thus achieving a focused effect.

[0023] The aforementioned air duct 16 allows the desorbed and concentrated gas to be directly delivered to the air outlet 161, and then flows out through the air passage 162 left between the air outlet 161 and the surrounding shield 17 to the front end of the combustion flame 1018 generated by the burner head 101. This increases the combustion gas 1 entering from the combustion gas inlet 1017 of the burner head 101 by more than 20% to 30% of its combustion equivalent. When the combustion gas 1 enters the passage 1011 of the burner head 101, it first interacts with the gas injected from the first gas port 1015 of the gas fuel pipe 1013 within the passage 1011 of the burner head 101. The gaseous fuel is premixed, and the combustion-supporting gas of the mixed gaseous fuel flows to the second gas port 1016 of the gaseous fuel pipe 1013, where it is mixed again with the gaseous fuel injected from the second gas port 1016. In this way, through the two-stage injection of gaseous fuel, the premixing sequence and distribution of the combustion flame 1018 can be made more uniform. The excess combustion-supporting gas can cause the temperature of the combustion flame 1018 generated by the burner head 101 to drop, so that the desorbed and concentrated gas can reduce the generation of nitrogen oxides after passing through the combustion flame 1018, thus having the effect of reducing nitrogen oxide generation.

[0024] The exhaust gas in the direct-fired incinerator (TO) 10 is first transported to one side of the fourth hot-side pipe 142 of the fourth heat exchanger 14 for heat exchange, and then from the other side of the fourth hot-side pipe 142 of the fourth heat exchanger 14 to one side of the third hot-side pipe 132 of the third heat exchanger 13 for heat exchange, and then from the other side of the third hot-side pipe 132 of the third heat exchanger 13 to one side of the second hot-side pipe 122 of the second heat exchanger 12 for heat exchange, and then from the other side of the second hot-side pipe 122 of the second heat exchanger 12 to one side of the first hot-side pipe 112 of the first heat exchanger 11 for heat exchange, and finally from the other side of the first hot-side pipe 112 of the first heat exchanger 11 to the outlet 104 of the direct-fired incinerator (TO) 10 (as shown in Figures 1 to 4).

[0025] Furthermore, the first adsorption rotor 30 of the present invention is provided with an adsorption zone 301, a cooling zone 302, and a desorption zone 303. The first adsorption rotor 30 is connected to an organic gas inlet pipe 31, a first purified gas outlet pipe 32, a first cooling gas inlet pipe 33, a first cooling gas delivery pipe 34, a first hot gas delivery pipe 35, and a first desorption concentrated gas pipe 36 (as shown in Figures 1 to 4). The second adsorption rotor 40 is provided with an adsorption zone 401, a cooling zone 402, and a desorption zone 403. The second adsorption rotor 40 is connected to a second purified gas outlet pipe 41, a second cooling gas inlet pipe 42, a second cooling gas delivery pipe 43, a second hot gas delivery pipe 44, and a second desorption concentrated gas pipe 45 (as shown in Figures 1 to 4). The first adsorption rotor 30 and the second adsorption rotor 40 are respectively zeolite concentration rotors or concentration rotors made of other materials.

[0026] One end of the organic gas inlet pipe 31 is connected to one side of the adsorption zone 301 of the first adsorption rotor 30, so that exhaust gas containing volatile organic compounds (VOCs) can be sent into one side of the adsorption zone 301 of the first adsorption rotor 30 for adsorption through the organic gas inlet pipe 31. One end of the first purified gas outlet pipe 32 is connected to the other side of the adsorption zone 301 of the first adsorption rotor 30, and the other end of the first purified gas outlet pipe 32 is connected to one side of the adsorption zone 401 of the second adsorption rotor 40 (as shown in Figures 1 to 4), so that the volatile organic compounds (VOCs) can be adsorbed by the adsorption zone 301 of the first adsorption rotor 30, and the adsorbed gas is transported to the adsorption zone 401 of the second adsorption rotor 40 through the first purified gas outlet pipe 32 from the other side of the adsorption zone 301 of the first adsorption rotor 30. The other side of the adsorption zone 401 of the second adsorption rotor 40 is connected to the second purified gas discharge pipe 41, and the other end of the second purified gas discharge pipe 41 is connected to the chimney 50, so as to transport the adsorbed gas in the first purified gas discharge pipe 32 to one side of the adsorption zone 401 of the second adsorption rotor 40 for adsorption (as shown in Figures 1 to 4). The adsorption zone 401 of the second adsorption rotor 40 generates a second adsorbed gas, and the second adsorbed gas is then output to the chimney 50 through the second purified gas discharge pipe 41 from the other side of the adsorption zone 401 of the second adsorption rotor 40. The second purified gas discharge pipe 41 is equipped with a fan 411 (as shown in Figures 3 and 4), so that the second adsorbed gas in the second purified gas discharge pipe 41 can be pushed and pulled into the chimney 50 for discharge through the fan 411.

[0027] One side of the cooling zone 302 of the first adsorption rotor 30 is connected to the first cooling gas inlet pipe 33 to supply cooling gas to the cooling zone 302 of the first adsorption rotor 30 for cooling. The other side of the cooling zone 302 of the first adsorption rotor 30 is connected to one end of the first cooling gas delivery pipe 34. The other end of the first cooling gas delivery pipe 34 is connected to one end of the third cold side pipe 131 of the third heat exchanger 13 to transport the gas entering the cooling zone 302 of the first adsorption rotor 30 to the third heat exchanger 13 for heat exchange (as shown in Figures 1 to 4). Furthermore, one end of the first hot gas conveying pipe 35 is connected to the other side of the desorption zone 303 of the first adsorption rotor 30, and the other end of the first hot gas conveying pipe 35 is connected to the other end of the third cold side pipe 131 of the third heat exchanger 13, so that the high-temperature hot gas that has undergone heat exchange through the third heat exchanger 13 can be conveyed through the first hot gas conveying pipe 35 to the desorption zone 303 of the first adsorption rotor 30 for desorption (as shown in Figures 1 to 4).

[0028] The cooling zone 302 of the first adsorption rotor 30 is provided in two embodiments. In the first embodiment, the first cooling air inlet pipe 33 connected to one side of the cooling zone 302 of the first adsorption rotor 30 is for the intake of fresh air or outside air (as shown in Figure 1), and the cooling zone 302 of the first adsorption rotor 30 is cooled by the fresh air or outside air. In another embodiment, the organic gas inlet pipe 31 is provided with an organic gas connecting pipe 37, which is connected to the first cooling gas inlet pipe 33 (as shown in Figure 3). This allows at least a portion of the exhaust gas containing volatile organic compounds (VOCs) in the organic gas inlet pipe 31 to be transported to the cooling zone 302 of the first adsorption rotor 30 for cooling. The organic gas connecting pipe 37 is also provided with an organic gas connecting control valve 371 (as shown in Figure 3) to control the airflow of the organic gas connecting pipe 37.

[0029] One side of the cooling zone 402 of the second adsorption rotor 40 is connected to the second cooling gas inlet pipe 42 to supply cooling gas to the cooling zone 402 of the second adsorption rotor 40 for cooling. The other side of the cooling zone 402 of the second adsorption rotor 40 is connected to one end of the second cooling gas delivery pipe 43. The other end of the second cooling gas delivery pipe 43 is connected to one end of the second cold side pipe 121 of the second heat exchanger 12 to transport the gas entering the cooling zone 402 of the second adsorption rotor 40 to the second heat exchanger 12 for heat exchange (as shown in Figures 1 to 4). Furthermore, one end of the second hot gas conveying pipe 44 is connected to the other side of the desorption zone 403 of the second adsorption rotor 40, and the other end of the second hot gas conveying pipe 44 is connected to the other end of the second cold side pipe 121 of the second heat exchanger 12, so that the high-temperature hot gas that has undergone heat exchange through the second heat exchanger 12 can be conveyed through the second hot gas conveying pipe 44 to the desorption zone 403 of the second adsorption rotor 40 for desorption (as shown in Figures 1 to 4).

[0030] The cooling zone 402 of the second adsorption rotor 40 is provided in two embodiments. In the first embodiment, the second cooling air inlet pipe 42 connected to one side of the cooling zone 402 of the second adsorption rotor 40 is for the intake of fresh air or outside air (as shown in Figure 2), and the cooling zone 402 of the second adsorption rotor 40 is cooled by the fresh air or outside air. In another embodiment, the first clean air discharge pipe 32 is provided with a first clean air connecting pipe 38, and the other end of the first clean air connecting pipe 38 is connected to the second cooling air inlet pipe 42 (as shown in Figures 3 and 4). This allows at least a portion of the adsorbed gas in the first clean air discharge pipe 32 to be transported to the cooling zone 402 of the second adsorption rotor 40 for cooling. The first clean air connecting pipe 38 is also provided with a first clean air connecting control valve 381 (as shown in Figures 3 and 4) to control the airflow of the first clean air connecting pipe 38.

[0031] Furthermore, one end of the first desorption concentrated gas pipeline 36 is connected to one side of the desorption zone 303 of the first adsorption rotor 30, and the other end of the first desorption concentrated gas pipeline 36 is connected to one end of the first cold side pipeline 111 of the first heat exchanger 11 (as shown in Figures 1 to 4). The other end of the first cold side pipeline 111 of the first heat exchanger 11 is connected to one end of the first cold side conveying pipeline 21, and the other end of the first cold side conveying pipeline 21 is connected to one end of the fourth cold side pipeline 141 of the fourth heat exchanger 14. Furthermore, the other end of the fourth cold-side pipe 141 of the fourth heat exchanger 14 is connected to one end of the fourth cold-side conveying pipe 22, and the other end of the fourth cold-side conveying pipe 22 is connected to the inlet 103 of the direct-fired incinerator (TO) 10 (as shown in Figures 1 to 4). The volatile organic compounds (VOCs) adsorbed by the first adsorption rotor 30 are desorbed through the desorption zone 303 of the first adsorption rotor 30, and a desorbed concentrated gas is output from one side of the desorption zone 303 of the first adsorption rotor 30 to the first desorbed concentrated gas pipe 36. The desorbed concentrated gas is then transported to the first cold-side pipe 11 of the first heat exchanger 11 through the first desorbed concentrated gas pipe 36. Within 1, the desorbed and concentrated gas system is transported from the other end of the first cold-side pipeline 111 of the first heat exchanger 11 to one end of the first cold-side conveying pipeline 21, and from the other end of the first cold-side conveying pipeline 21 to one end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14, and from the other end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14 to one end of the fourth cold-side conveying pipeline 22, and finally from the other end of the fourth cold-side conveying pipeline 22 to the inlet 103 of the direct-fired incinerator (TO) 10, so that the burner head 101 of the direct-fired incinerator (TO) 10 can perform high-temperature pyrolysis to reduce volatile organic compounds (VOCs). Furthermore, the first desorbed concentrated gas pipeline 36 is equipped with a fan 361 (as shown in Figures 3 and 4) to push or pull the desorbed concentrated gas into one end of the first cold side pipeline 111 of the first heat exchanger 11.

[0032] One end of the second desorption concentrated gas pipeline 45 is connected to one side of the desorption zone 403 of the second adsorption rotor 40, and the hot gas is transported to the desorption zone 403 of the second adsorption rotor 40 for desorption through the second hot gas delivery pipeline 44 connected to the second cold side pipeline 121 of the second heat exchanger 12 (as shown in Figures 1 to 4). The volatile organic compounds (VOCs) adsorbed by the second adsorption rotor 40 are desorbed through the desorption zone 403 of the second adsorption rotor 40, and the re-desorbed concentrated gas is output from one side of the desorption zone 403 of the second adsorption rotor 40 to the second desorption concentrated gas pipeline 45, and then output through the second desorption concentrated gas pipeline 45. The second desorption and concentration gas pipeline 45 has two implementation methods. In the first implementation, the other end of the second desorption and concentration gas pipeline 45 is connected to the organic gas inlet pipeline 31 (as shown in Figures 1 and 3), allowing the re-desorbed and concentrated gas to re-enter the adsorption zone 301 of the first adsorption rotor 30 via the organic gas inlet pipeline 31 for re-adsorption. In the second implementation, the other end of the second desorption and concentration gas pipeline 45 is connected to the first cooling gas inlet pipeline 33 (as shown in Figures 2 and 4), allowing the re-desorbed and concentrated gas to re-enter the cooling zone 302 of the first adsorption rotor 30 via the first cooling gas inlet pipeline 33 for cooling. Furthermore, the second desorption and concentration gas pipeline 45 is equipped with a fan (not shown) to push or pull the re-desorbed and concentrated gas into the organic gas inlet pipeline 31 or the first cooling gas inlet pipeline 33. The re-desorbed concentrated gas generated through the desorption zone 403 of the second adsorption rotor 40 can enter the adsorption zone 301 of the first adsorption rotor 30 or the cooling zone 302 of the first adsorption rotor 30 for recycling.

[0033] One end of the chimney conveying pipe 51 is connected to the processing output pipe 15, and the other end of the chimney conveying pipe 51 is connected to the chimney 50 (as shown in Figures 1 to 4). Either the chimney conveying pipe 51 or the processing output pipe 15 is equipped with at least one control valve 80 (as shown in Figures 1 and 3) to control the flow direction of at least a portion of the processed exhaust gas in the processing output pipe 15. The control valve 80 can be any of a two-way valve, a three-way valve, or an electric valve, primarily implemented in conjunction with the pipe design. When the at least one control valve 80 is installed in the chimney conveying pipe 51, the control valve 80 is a chimney control valve 801, controlling the airflow of at least a portion of the processed exhaust gas in the processing output pipe 15 to the chimney 50. When at least one control valve 80 is installed on the processing output pipeline 15, the control valve 80 is a processing output control valve 802, which controls the airflow of at least a portion of the processed exhaust gas in the processing output pipeline 15 to the ammonia-free catalyst device 70. Alternatively, when at least one control valve 80 is installed on both the processing output pipeline 15 and the chimney conveying pipeline 51 (as shown in Figures 2 and 4), the control valve 802 on the processing output pipeline 15 controls the airflow of at least a portion of the processed exhaust gas in the processing output pipeline 15 to the ammonia-free catalyst device 70, while the control valve 801 on the chimney conveying pipeline 51 controls the airflow of at least a portion of the processed exhaust gas in the processing output pipeline 15 to the chimney 50.

[0034] One end of the purified gas discharge bypass pipe 60 is connected to the second purified gas discharge pipe 41, while the other end of the purified gas discharge bypass pipe 60 is connected to the treatment output pipe 15 (as shown in Figures 1 to 4). At least a portion of the gas system after the second adsorption in the second purified gas discharge pipe 41 is transported to the treatment output pipe 15 through the purified gas discharge bypass pipe 60, allowing at least a portion of the gas after the second adsorption to react with at least a portion of the treated exhaust gas in the treatment output pipe 15. The mixture is used to reduce the temperature of at least a portion of the treated exhaust gas in the treatment output pipeline 15. The clean gas discharge bypass pipeline 60 is equipped with a clean gas discharge bypass control valve 601 (as shown in Figures 1 to 4) to control the airflow of at least a portion of the gas after the second adsorption to the treatment output pipeline 15. The clean gas discharge bypass pipeline 60 is also equipped with a fan 61 (as shown in Figures 3 and 4) to push or pull the at least a portion of the adsorbed gas into the treatment output pipeline 15. The main purpose of introducing at least a portion of the second adsorption gas from the second clean gas discharge pipeline 41 through the clean gas discharge bypass pipeline 60 is to ensure that the operating temperature of the ammonia-free catalyst device 70 is below 200°C. However, the exhaust gas produced after high-temperature pyrolysis treatment in the direct-fired incinerator (TO) 10 may exceed 200°C (e.g., 220°C or 250°C), which may damage the ammonia-free catalyst device 70. Therefore, it is necessary to introduce at least a portion of the second adsorption gas from the second clean gas discharge pipeline 41 for mixing and cooling to achieve a temperature that allows it to enter the ammonia-free catalyst device 70 (e.g., below 200°C), thereby protecting the ammonia-free catalyst device 70.

[0035] Furthermore, the ammonia-free catalyst device 70 is equipped with an inlet 701, an outlet 702, an ozone inlet 703, an ammonia-free catalyst output pipe 71, and an ozone delivery pipe 72 (as shown in Figures 1 to 4). One end of the ozone delivery pipe 72 is connected to the ozone inlet 703 of the ammonia-free catalyst device 70, and the other end is connected to an ozone generator 74. The ozone generator 74 generates ozone using any one of the following methods: high-voltage discharge, ultraviolet irradiation, or electrolysis. The high-voltage discharge method (Figure...) (Not shown) This ozone generator uses a high-voltage current of a certain frequency to create a high-voltage electric field, causing oxygen molecules within or around the electric field to undergo an electrochemical reaction, thereby producing ozone. The high-voltage discharge type ozone generator 74 can be classified into three types according to the high-voltage frequency: low-frequency (50~60Hz), medium-frequency (400~1000Hz), and high-frequency (greater than 1000Hz). It can also be classified into oxygen-type and air-type according to the gas raw material used, water-cooled and air-cooled according to the cooling method, and quartz tube, ceramic plate, ceramic tube, glass tube, and enamel tube according to the dielectric material. Ozone is generated through the ozone generator 74 and delivered to the ozone inlet 703 of the ammonia-free catalyst device 70 via the ozone delivery pipeline 72. The inlet 701 of the ammonia-free catalyst device 70 is connected to the other end of the treatment output pipeline 15. The ammonia-free catalyst device 70 is equipped with at least one catalyst 73 (as shown in Figures 1 to 4), allowing at least a portion of the treated exhaust gas after mixing to enter the inlet 701 of the ammonia-free catalyst device 70 through the treatment output pipeline 15. This allows at least a portion of the treated exhaust gas after mixing to undergo a denitrification reaction with the ozone. In other words, the ozone and the catalyst 73 are used to oxidize at least a nitrogen oxide (NOx) in the at least a portion of the treated exhaust gas after mixing. The nitrogen oxide (NOx) includes nitric oxide and ammonia dioxide, etc., and produces a denitrification reaction gas. After the ammonia-free catalyst device 70 performs the denitrification reaction, the denitrification reaction gas, namely nitrogen (N2), is output through the outlet 702 of the ammonia-free catalyst device 70. The outlet 702 of the ammonia-free catalyst device 70 is connected to one end of the ammonia-free catalyst output pipeline 71, and the other end of the ammonia-free catalyst output pipeline 71 is connected to the chimney 50. The nitrogen (N2) after the reaction is transported to the chimney 50 through the ammonia-free catalyst output pipeline 71 by the ammonia-free catalyst device 70, thereby improving the efficiency of nitrogen oxide (NOx) removal and improving the efficiency of nitrogen oxide (NOx) emission.

[0036] Another embodiment of the present invention involves installing a dust collector 90 (as shown in Figures 2 and 4) on the processing output pipeline 15. The dust collector 90 is primarily located on the processing output pipeline 15 connected to the outlet 104 of the direct-fired incinerator (TO) 10, and is also the front end of the connection between one end of the chimney conveying pipeline 51 and the processing output pipeline 15. The dust collector 90 has an inlet 901 and an outlet 902. When the processed exhaust gas output from the direct-fired incinerator (TO) 10 after combustion contains particulate matter, also known as suspended particulate matter (PM2.5),... Matter), where particulate matter refers to a mixture of solid particles and liquid droplets in a gas. Some particulate matter is large enough to be considered as dust or dirt. When at least a portion of the exhaust gas in the processing output pipeline 15 contains at least one particulate matter, at least a portion of the exhaust gas in the processing output pipeline 15 enters the dust collector 90 through the inlet 901 of the dust collector 90, so that the at least one particulate matter can be collected by the dust collector 90. This allows at least a portion of the exhaust gas in the processing output pipeline 15 to collect the particulate matter first, thereby reducing the discharge of the particulate matter, and then it is discharged to the processing output pipeline 15 through the outlet 902 of the dust collector 90, so as to achieve the effect of dust removal. Furthermore, when using the dust collector 90 to collect the particulate matter, the flow direction of at least a portion of the treated exhaust gas in the treatment output pipeline 15 can be controlled by at least one control valve 80 provided in either the chimney conveying pipeline 51 or the treatment output pipeline 15 (as shown in Figures 2 and 4). This mainly allows most of the treated exhaust gas in the treatment output pipeline 15 to flow to the chimney conveying pipeline 51 and be discharged through the chimney 50. A small portion of the treated exhaust gas in the treatment output pipeline 15 is first mixed with at least a portion of the gas after the second adsorption, which is transported through the clean gas discharge bypass pipeline 60, before flowing into the ammonia-free catalyst device 70 for denitrification reaction. This improves the efficiency of volatile organic exhaust gas treatment and reduces nitrogen oxide emissions.

[0037] The organic exhaust gas treatment method for reducing ammonia oxides of the present invention is mainly used in an organic exhaust gas treatment system, and is equipped with a combination design of a direct-fired incinerator (TO) 10, a first heat exchanger 11, a second heat exchanger 12, a third heat exchanger 13, a fourth heat exchanger 14, a first cold-side conveying pipeline 21, a fourth cold-side conveying pipeline 22, a first adsorption rotor 30, a second adsorption rotor 40, a chimney 50, a chimney conveying pipeline 51, a clean gas emission bypass pipeline 60, and an ammonia-free catalyst device 70 (as shown in Figures 1 to 4).

[0038] The main steps of this organic exhaust gas treatment method include: Step S100: First adsorption rotor adsorption: Exhaust gas containing volatile organic compounds is sent to one side of the adsorption zone 301 of the first adsorption rotor 30 through the organic gas inlet pipe 31 for adsorption, and the adsorbed gas is output to the adsorption zone 401 of the second adsorption rotor 40 through the first clean gas discharge pipe 32 from the other side of the adsorption zone 301 of the first adsorption rotor 30. After completing the above step S100, the next step S110 is performed.

[0039] In step S100 above, the first adsorption rotor 30 is provided with an adsorption zone 301, a cooling zone 302, and a desorption zone 303. The first adsorption rotor 30 is connected to an organic gas inlet pipe 31, a first purified gas outlet pipe 32, a first cooling gas inlet pipe 33, a first cooling gas delivery pipe 34, a first hot gas delivery pipe 35, and a first desorption concentrated gas pipe 36 (as shown in Figures 1 to 4). The second adsorption rotor 40 is provided with an adsorption zone 401, a cooling zone 402, and a desorption zone 403. The second adsorption rotor 40 is connected to a second purified gas outlet pipe 41, a second cooling gas inlet pipe 42, a second cooling gas delivery pipe 43, a second hot gas delivery pipe 44, and a second desorption concentrated gas pipe 45 (as shown in Figures 1 to 4). The first adsorption rotor 30 and the second adsorption rotor 40 are respectively zeolite concentration rotors or concentration rotors made of other materials.

[0040] One end of the organic gas inlet pipe 31 is connected to one side of the adsorption zone 301 of the first adsorption rotor 30, so that exhaust gas containing volatile organic compounds (VOCs) can be sent into one side of the adsorption zone 301 of the first adsorption rotor 30 for adsorption through the organic gas inlet pipe 31. One end of the first purified gas outlet pipe 32 is connected to the other side of the adsorption zone 301 of the first adsorption rotor 30, and the other end of the first purified gas outlet pipe 32 is connected to one side of the adsorption zone 401 of the second adsorption rotor 40 (as shown in Figures 1 to 4), so that the volatile organic compounds (VOCs) can be adsorbed by the adsorption zone 301 of the first adsorption rotor 30, and the adsorbed gas is transported to the adsorption zone 401 of the second adsorption rotor 40 through the first purified gas outlet pipe 32 from the other side of the adsorption zone 301 of the first adsorption rotor 30.

[0041] Furthermore, after the adsorption step S100 of the first adsorption rotor, the following step S101 is provided: inputting the first cooling gas: delivering the cooling gas to the cooling zone 302 of the first adsorption rotor 30 through the other end of the first cooling gas inlet pipe 33 for cooling, and then delivering the cooling gas that has passed through the cooling zone 302 of the first adsorption rotor 30 to one end of the third cold side pipe 131 of the third heat exchanger 13 through the other end of the first cooling gas delivery pipe 34.

[0042] In step S101 above, one side of the cooling zone 302 of the first adsorption rotor 30 is connected to the first cooling gas inlet pipe 33 to supply cooling gas to the cooling zone 302 of the first adsorption rotor 30 for cooling. The other side of the cooling zone 302 of the first adsorption rotor 30 is connected to one end of the first cooling gas delivery pipe 34. The other end of the first cooling gas delivery pipe 34 is connected to one end of the third cold side pipe 131 of the third heat exchanger 13 to transport the gas entering the cooling zone 302 of the first adsorption rotor 30 to the third heat exchanger 13 for heat exchange (as shown in Figures 1 to 4).

[0043] The cooling zone 302 of the first adsorption rotor 30 is provided in two embodiments. In the first embodiment, the first cooling air inlet pipe 33 connected to one side of the cooling zone 302 of the first adsorption rotor 30 is for the intake of fresh air or outside air (as shown in Figure 1), and the cooling zone 302 of the first adsorption rotor 30 is cooled by the fresh air or outside air. In another embodiment, the organic gas inlet pipe 31 is provided with an organic gas connecting pipe 37, which is connected to the first cooling gas inlet pipe 33 (as shown in Figure 3). This allows at least a portion of the exhaust gas containing volatile organic compounds (VOCs) in the organic gas inlet pipe 31 to be transported to the cooling zone 302 of the first adsorption rotor 30 for cooling. The organic gas connecting pipe 37 is also provided with an organic gas connecting control valve 371 (as shown in Figure 3) to control the airflow of the organic gas connecting pipe 37.

[0044] In the next step, S110, hot gas is delivered for desorption: hot gas is delivered to the desorption zone 303 of the first adsorption rotor 30 through the first hot gas delivery pipeline 35, which is connected to the third cold-side pipeline 131 of the third heat exchanger 13, to desorb the volatile organic compounds adsorbed by the first adsorption rotor 30. A desorbed concentrated gas is then output from one side of the desorption zone 303 of the first adsorption rotor 30 to the first desorbed concentrated gas pipeline 36, and then delivered to the first cold-side pipeline 111 of the first heat exchanger 11 through the first desorbed concentrated gas pipeline 36. After completing the above step S110, the next step S120 is performed.

[0045] In step S110 above, one end of the first hot gas conveying pipe 35 is connected to the other side of the desorption zone 303 of the first adsorption rotor 30, and the other end of the first hot gas conveying pipe 35 is connected to the other end of the third cold side pipe 131 of the third heat exchanger 13, so that the high-temperature hot gas that has undergone heat exchange through the third heat exchanger 13 can be conveyed through the first hot gas conveying pipe 35 to the desorption zone 303 of the first adsorption rotor 30 for desorption (as shown in Figures 1 to 4).

[0046] Furthermore, in the next step S120, the desorbed concentrated gas is transported as follows: the desorbed concentrated gas system is transported through the first cold-side transport pipeline 21, which is connected to the first cold-side pipeline 111 of the first heat exchanger 11, to one end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14, and then through the fourth cold-side transport pipeline 22, which is connected to the other end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14, to the inlet 103 of the direct-fired incinerator (TO) 10. After completing the above step S120, the next step S130 is performed.

[0047] In step S120 above, one end of the first desorption concentrated gas pipeline 36 is connected to one side of the desorption zone 303 of the first adsorption rotor 30, and the other end of the first desorption concentrated gas pipeline 36 is connected to one end of the first cold side pipeline 111 of the first heat exchanger 11 (as shown in Figures 1 to 4). The other end of the first cold side pipeline 111 of the first heat exchanger 11 is connected to one end of the first cold side conveying pipeline 21, and the other end of the first cold side conveying pipeline 21 is connected to one end of the fourth cold side pipeline 141 of the fourth heat exchanger 14. Furthermore, the other end of the fourth cold-side pipe 141 of the fourth heat exchanger 14 is connected to one end of the fourth cold-side conveying pipe 22, and the other end of the fourth cold-side conveying pipe 22 is connected to the inlet 103 of the direct-fired incinerator (TO) 10 (as shown in Figures 1 to 4). The volatile organic compounds (VOCs) adsorbed by the first adsorption rotor 30 are desorbed through the desorption zone 303 of the first adsorption rotor 30, and a desorbed concentrated gas is output from one side of the desorption zone 303 of the first adsorption rotor 30 to the first desorbed concentrated gas pipe 36. The desorbed concentrated gas is then transported to the first cold-side pipe 11 of the first heat exchanger 11 through the first desorbed concentrated gas pipe 36. Within 1, the desorbed and concentrated gas system is transported from the other end of the first cold-side pipeline 111 of the first heat exchanger 11 to one end of the first cold-side conveying pipeline 21, and from the other end of the first cold-side conveying pipeline 21 to one end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14, and from the other end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14 to one end of the fourth cold-side conveying pipeline 22, and finally from the other end of the fourth cold-side conveying pipeline 22 to the inlet 103 of the direct-fired incinerator (TO) 10, so that the burner head 101 of the direct-fired incinerator (TO) 10 can perform high-temperature pyrolysis to reduce volatile organic compounds (VOCs). Furthermore, the first desorbed concentrated gas pipeline 36 is equipped with a fan 361 (as shown in Figures 3 and 4) to push or pull the desorbed concentrated gas into one end of the first cold side pipeline 111 of the first heat exchanger 11.

[0048] In step S120 above, the direct-fired incinerator (TO) 10 is provided with a burner head 101 and a furnace chamber 102. The burner head 101 is connected to the furnace chamber 102. The first heat exchanger 11, the second heat exchanger 12, the third heat exchanger 13, and the fourth heat exchanger 14 are respectively located in the furnace chamber 102 of the direct-fired incinerator (TO) 10. The direct-fired incinerator (TO) 10 is provided with an inlet 103, an outlet 104, a processing and output pipeline 15, an air duct 16, and an enclosure. The hood 17 (as shown in Figures 1 to 4) has an inlet 103 located at the burner head 101 and an outlet 104 located at the furnace chamber 102. One end of the processing output pipeline 15 is connected to the outlet 104 of the direct-fired incinerator (TO) 10. The direct-fired incinerator (TO) 10 generates a processing exhaust gas containing at least one nitrogen oxide (NOx), which is output to the processing output pipeline 15 via the outlet 104 of the direct-fired incinerator (TO) 10. The first heat exchanger 11 is provided with a first cold-side pipe 111 and a first hot-side pipe 112, the second heat exchanger 12 is provided with a second cold-side pipe 121 and a second hot-side pipe 122, the third heat exchanger 13 is provided with a third cold-side pipe 131 and a third hot-side pipe 132, and the fourth heat exchanger 14 is provided with a fourth cold-side pipe 141 and a fourth hot-side pipe 142.

[0049] The air duct 16 is located inside the direct-fired incinerator (TO) 10. The burner head 101 is attached to the direct-fired incinerator (TO) 10. The air duct 16 is connected to the inlet 103 of the direct-fired incinerator (TO) 10. The burner head 101 is provided with a channel 1011, and the burner head 101 is provided with a burner head cover 1012, a gas fuel pipe 1013, and a combustion-supporting gas inlet 1017 (as shown in Figures 1 to 4). The combustion-supporting gas inlet 1017 can be located at one end or the side of the channel 1011. 17 is supplied with a combustion-supporting gas (not shown), wherein the combustion-supporting gas system is either air or oxygen, and one end of the channel 1011 may be equipped with a fan (not shown) to increase the flow rate of the combustion-supporting gas and enable the combustion-supporting gas to enter the channel 1011 of the burner head 101.

[0050] The gas fuel pipe 1013 has a gas fuel inlet 1014, at least one first gas outlet 1015 and at least one second gas outlet 1016. The at least one first gas outlet 1015 of the gas fuel pipe 1013 is located in the channel 1011 of the burner head 101, and the burner head cover 1012 is located at the second gas outlet 1016 of the gas fuel pipe 1013. The gas fuel inlet 1014 is for a gas fuel (not shown) to enter, wherein the gas fuel is either natural gas or coal gas. The gas fuel is ejected from the channel 1011 of the burner head 101 through the first gas outlet 1015, and the gas fuel is ejected from the second gas outlet 1016, generating a combustion flame 1018. Furthermore, the burner head cover 1012 is equipped with a mounting panel (not shown) and is mounted on the direct-fired incinerator (TO) 10 through the mounting panel, so that part of the burner head 101 is exposed outside the direct-fired incinerator (TO) 10. The gas fuel inlet 1014 of the gas fuel pipe 1013 is located outside the direct-fired incinerator (TO) 10, so that the gas fuel can easily enter through the gas fuel inlet 1014. The combustion gas inlet 1017 is also located outside the direct-fired incinerator (TO) 10, so that the combustion gas can easily enter through the combustion gas inlet 1017.

[0051] Furthermore, at least one heat insulation cotton 163 is provided between the air duct 16 and the direct-fired incinerator (TO) 10 to form a barrier protection. The air duct 16 is made of metal and is connected to the inlet 103 of the direct-fired incinerator (TO) 10, so that the desorbed concentrated gas (such as a mixture containing one or more volatile organic compounds and air) can enter the air duct 16. The air duct 16 is provided with an air outlet 161. In addition, one part of the air duct 16 is provided for the burner head cover 1012 of the burner head 101, and the burner head cover 1012 corresponds to the air outlet 161. Furthermore, the enclosure 17 is installed inside the direct-fired incinerator (TO) 10. The enclosure 17 is made of metal and can be any one of the following shapes: conical, spherical, trumpet-shaped, square, or circular, designed to fit the current situation. One end of the enclosure 17 is attached to the burner head cover 1012, and the other end of the enclosure 17 extends from the air outlet 161 of the air duct 16. The air outlet 161 of the air duct 16 is larger than the enclosure 17, so that the air outlet 161 of the air duct 16 and the enclosure 17 are connected. An air passage 162 is provided between the enclosures 17. When the gaseous fuel is ejected from the second air port 1016 and the combustion flame 1018 is generated, the combustion flame 1018 passes through the enclosure 17 from the burner head cover 1012 of the burner head 101. The enclosure 17 prevents the combustion flame 1018 from being affected by the desorbed concentrated gas (such as a mixture of air containing one or more volatile organic compounds) entering and affecting the direction of the combustion flame 1018. This allows the combustion flame 1018 to be concentrated into a bundle, thus achieving a focused effect.

[0052] The aforementioned air duct 16 allows the desorbed and concentrated gas to be directly delivered to the air outlet 161, and then flows out through the air passage 162 left between the air outlet 161 and the surrounding shield 17 to the front end of the combustion flame 1018 generated by the burner head 101. This increases the combustion gas 1 entering from the combustion gas inlet 1017 of the burner head 101 by more than 20% to 30% of its combustion equivalent. When the combustion gas 1 enters the passage 1011 of the burner head 101, it is pre-mixed with a portion of the gaseous fuel ejected from the first gas port 1015 of the gas fuel pipe 1013. The mixed combustion gas then flows to the second gas port 1016 of the gas fuel pipe 1013 and mixes again with the gaseous fuel ejected from the second gas port 1016. Thus, By injecting gas fuel in two stages, the premixing sequence and distribution of the combustion flame 1018 can be made more uniform. The excess combustion gas can cause the temperature of the combustion flame 1018 generated by the burner head 101 to drop. This reduces the generation of nitrogen oxides in the desorbed and concentrated gas after passing through the combustion flame 1018, thus achieving the effect of reducing nitrogen oxide generation.

[0053] Furthermore, the next step, S130, involves treating the exhaust gas output: the direct-fired incinerator (TO) 10 processes the desorbed and concentrated gas to produce a treated exhaust gas containing at least one nitrogen oxide (NOx), which is then output from outlet 104 of the direct-fired incinerator (TO) 10 into the treated output pipeline 15. After completing step S130, the next step, S140, is then performed.

[0054] In step S130 above, the treated exhaust gas in the direct-fired incinerator (TO) 10 is first transported to one side of the fourth hot-side pipe 142 of the fourth heat exchanger 14 for heat exchange, and then transported from the other side of the fourth hot-side pipe 142 of the fourth heat exchanger 14 to one side of the third hot-side pipe 132 of the third heat exchanger 13 for heat exchange, and then from the other side of the third hot-side pipe 132 of the third heat exchanger 13 to one side of the second hot-side pipe 122 of the second heat exchanger 12 for heat exchange, and then from the other side of the second hot-side pipe 122 of the second heat exchanger 12 to one side of the first hot-side pipe 112 of the first heat exchanger 11 for heat exchange, and finally from the other side of the first hot-side pipe 112 of the first heat exchanger 11 to the outlet 104 of the direct-fired incinerator (TO) 10 (as shown in Figures 1 to 4).

[0055] Furthermore, the next step, S140, involves the second adsorption rotor: the adsorbed gas in the first purified gas discharge pipe 32 is transported to one side of the adsorption zone 401 of the second adsorption rotor 40 for adsorption, and a second adsorbed gas is generated through the adsorption zone 401 of the second adsorption rotor 40. This second adsorbed gas is then discharged to the chimney 50 through the second purified gas discharge pipe 41 from the other side of the adsorption zone 401 of the second adsorption rotor 40. After completing step S140, the next step, S150, is performed.

[0056] In step S140 above, the other side of the adsorption zone 401 of the second adsorption rotor 40 is connected to the second purified gas discharge pipe 41, and the other end of the second purified gas discharge pipe 41 is connected to the chimney 50, so as to transport the adsorbed gas in the first purified gas discharge pipe 32 to one side of the adsorption zone 401 of the second adsorption rotor 40 for adsorption (as shown in Figures 1 to 4), and generate a second adsorbed gas through the adsorption zone 401 of the second adsorption rotor 40. Then, the second adsorbed gas is output to the chimney 50 through the second purified gas discharge pipe 41 from the other side of the adsorption zone 401 of the second adsorption rotor 40. The second purified gas discharge pipe 41 is equipped with a fan 411 (as shown in Figures 3 and 4), so that the second adsorbed gas in the second purified gas discharge pipe 41 can be pushed and pulled into the chimney 50 for discharge through the fan 411.

[0057] Furthermore, after the adsorption step S140 of the second adsorption rotor, the following step S141 is provided: inputting the second cooling gas: cooling gas is delivered to the cooling zone 402 of the second adsorption rotor 40 through the other end of the second cooling gas inlet pipe 42 for cooling, and then the cooling gas passing through the cooling zone 402 of the second adsorption rotor 40 is delivered to one end of the second cold side pipe 121 of the second heat exchanger 12 through the other end of the second cooling gas delivery pipe 43.

[0058] In step S141 above, one side of the cooling zone 402 of the second adsorption rotor 40 is connected to the second cooling gas inlet pipe 42 to supply cooling gas to the cooling zone 402 of the second adsorption rotor 40 for cooling. The other side of the cooling zone 402 of the second adsorption rotor 40 is connected to one end of the second cooling gas delivery pipe 43. The other end of the second cooling gas delivery pipe 43 is connected to one end of the second cold side pipe 121 of the second heat exchanger 12 to transport the gas entering the cooling zone 402 of the second adsorption rotor 40 to the second heat exchanger 12 for heat exchange (as shown in Figures 1 to 4).

[0059] The cooling zone 402 of the second adsorption rotor 40 is provided in two embodiments. In the first embodiment, the second cooling air inlet pipe 42 connected to one side of the cooling zone 402 of the second adsorption rotor 40 is for the intake of fresh air or outside air (as shown in Figure 2), and the cooling zone 402 of the second adsorption rotor 40 is cooled by the fresh air or outside air. In another embodiment, the first clean air discharge pipe 32 is provided with a first clean air connecting pipe 38, and the other end of the first clean air connecting pipe 38 is connected to the second cooling air inlet pipe 42 (as shown in Figures 3 and 4). This allows at least a portion of the adsorbed gas in the first clean air discharge pipe 32 to be transported to the cooling zone 402 of the second adsorption rotor 40 for cooling. The first clean air connecting pipe 38 is also provided with a first clean air connecting control valve 381 (as shown in Figures 3 and 4) to control the airflow of the first clean air connecting pipe 38.

[0060] In the next step, S150, a second hot gas desorption process is performed: hot gas is delivered to the desorption zone 403 of the second adsorption rotor 40 through the second hot gas delivery pipeline 44, which is connected to the second cold-side pipeline 121 of the second heat exchanger 12, to desorb the volatile organic compounds adsorbed by the second adsorption rotor 40. The re-desorbed concentrated gas is then output from one side of the desorption zone 403 of the second adsorption rotor 40 to the second desorbed concentrated gas pipeline 45, and then output through the second desorbed concentrated gas pipeline 45. After completing step S150, the next step, S160, is performed.

[0061] In step S150 above, one end of the second hot gas conveying pipe 44 is connected to the other side of the desorption zone 403 of the second adsorption rotor 40, and the other end of the second hot gas conveying pipe 44 is connected to the other end of the second cold side pipe 121 of the second heat exchanger 12, so that the high-temperature hot gas that has undergone heat exchange through the second heat exchanger 12 can be conveyed through the second hot gas conveying pipe 44 to the desorption zone 403 of the second adsorption rotor 40 for desorption (as shown in Figures 1 to 4).

[0062] One end of the second desorption concentrated gas pipeline 45 is connected to one side of the desorption zone 403 of the second adsorption rotor 40, and the hot gas is transported to the desorption zone 403 of the second adsorption rotor 40 for desorption through the second hot gas delivery pipeline 44 connected to the second cold side pipeline 121 of the second heat exchanger 12 (as shown in Figures 1 to 4). The volatile organic compounds (VOCs) adsorbed by the second adsorption rotor 40 are desorbed through the desorption zone 403 of the second adsorption rotor 40, and the re-desorbed concentrated gas is output from one side of the desorption zone 403 of the second adsorption rotor 40 to the second desorption concentrated gas pipeline 45, and then output through the second desorption concentrated gas pipeline 45. The second desorption and concentration gas pipeline 45 has two implementation methods. In the first implementation, the other end of the second desorption and concentration gas pipeline 45 is connected to the organic gas inlet pipeline 31 (as shown in Figures 1 and 3), allowing the re-desorbed and concentrated gas to re-enter the adsorption zone 301 of the first adsorption rotor 30 via the organic gas inlet pipeline 31 for re-adsorption. In the second implementation, the other end of the second desorption and concentration gas pipeline 45 is connected to the first cooling gas inlet pipeline 33 (as shown in Figures 2 and 4), allowing the re-desorbed and concentrated gas to re-enter the cooling zone 302 of the first adsorption rotor 30 via the first cooling gas inlet pipeline 33 for cooling. Furthermore, the second desorption and concentration gas pipeline 45 is equipped with a fan (not shown) to push or pull the re-desorbed and concentrated gas into the organic gas inlet pipeline 31 or the first cooling gas inlet pipeline 33. The re-desorbed concentrated gas generated through the desorption zone 403 of the second adsorption rotor 40 can enter the adsorption zone 301 of the first adsorption rotor 30 or the cooling zone 302 of the first adsorption rotor 30 for recycling.

[0063] Furthermore, in the next step S160, the flow direction is controlled by a valve: at least one control valve 80 is installed in either the chimney conveying pipeline 51 or the processing output pipeline 15 to control the flow direction of at least a portion of the processed exhaust gas in the processing output pipeline 15. After completing the above step S160, the next step S170 is performed.

[0064] In step S160 above, one end of the chimney conveying pipe 51 is connected to the processing output pipe 15, and the other end of the chimney conveying pipe 51 is connected to the chimney 50 (as shown in Figures 1 to 4). Either the chimney conveying pipe 51 or the processing output pipe 15 is equipped with at least one control valve 80 (as shown in Figures 1 and 3) to control the flow direction of at least a portion of the processed exhaust gas in the processing output pipe 15. The control valve 80 can be any of a two-way valve, a three-way valve, or an electric valve, mainly implemented in conjunction with the pipe design. When at least one control valve 80 is installed in the chimney conveying pipe 51, the control valve 80 is a chimney control valve 801, controlling the airflow of at least a portion of the processed exhaust gas in the processing output pipe 15 to the chimney 50. When at least one control valve 80 is installed on the processing output pipeline 15, the control valve 80 is a processing output control valve 802, which controls the airflow of at least a portion of the processed exhaust gas in the processing output pipeline 15 to the ammonia-free catalyst device 70. Alternatively, when at least one control valve 80 is installed on both the processing output pipeline 15 and the chimney conveying pipeline 51 (as shown in Figures 2 and 4), the control valve 802 on the processing output pipeline 15 controls the airflow of at least a portion of the processed exhaust gas in the processing output pipeline 15 to the ammonia-free catalyst device 70, while the control valve 801 on the chimney conveying pipeline 51 controls the airflow of at least a portion of the processed exhaust gas in the processing output pipeline 15 to the chimney 50.

[0065] Furthermore, the next step, S170, involves the bypass delivery and mixing of purified gas: at least a portion of the post-adsorption gas system within the second purified gas discharge pipe 41 is transported through the purified gas discharge bypass pipe 60 to the processing output pipe 15, allowing at least a portion of the post-adsorption gas to mix with at least a portion of the processed tail gas within the processing output pipe 15, thereby reducing the temperature of at least a portion of the processed tail gas within the processing output pipe 15. After completing step S170, the next step, S180, is performed.

[0066] In step S170 above, one end of the purified gas discharge bypass pipe 60 is connected to the second purified gas discharge pipe 41, and the other end of the purified gas discharge bypass pipe 60 is connected to the processing output pipe 15 (as shown in Figures 1 to 4). At least a portion of the gas system after the second adsorption in the second purified gas discharge pipe 41 is transported to the processing output pipe 15 through the purified gas discharge bypass pipe 60, allowing at least a portion of the gas after the second adsorption to react with at least a portion of the gas system in the processing output pipe 15. The exhaust gas is mixed to reduce the temperature of at least a portion of the exhaust gas in the treatment output pipeline 15. The clean gas discharge bypass pipeline 60 is equipped with a clean gas discharge bypass control valve 601 (as shown in Figures 1 to 4) to control the airflow of at least a portion of the gas after the second adsorption to the treatment output pipeline 15. The clean gas discharge bypass pipeline 60 is also equipped with a fan 61 (as shown in Figures 3 and 4) to push or pull the at least a portion of the adsorbed gas into the treatment output pipeline 15. The main purpose of introducing at least a portion of the second adsorption gas from the second clean gas discharge pipeline 41 through the clean gas discharge bypass pipeline 60 is to ensure that the operating temperature of the ammonia-free catalyst device 70 is below 200°C. However, the exhaust gas produced after high-temperature pyrolysis treatment in the direct-fired incinerator (TO) 10 may exceed 200°C (e.g., 220°C or 250°C), which may damage the ammonia-free catalyst device 70. Therefore, it is necessary to introduce at least a portion of the second adsorption gas from the second clean gas discharge pipeline 41 for mixing and cooling to achieve a temperature that allows it to enter the ammonia-free catalyst device 70 (e.g., below 200°C), thus protecting the ammonia-free catalyst device 70.

[0067] In addition, the next step, S180, is the denitrification of the ammonia-free catalyst device: the ozone generator 74 generates ozone and delivers it to the ammonia-free catalyst device 70 via the ozone delivery pipeline 72. The inlet 701 of the ammonia-free catalyst device 70 is connected to the other end of the treatment output pipeline 15, allowing at least a portion of the treated exhaust gas after mixing to enter the ammonia-free catalyst device 70 for denitrification reaction and generate a denitrification reaction gas, which is then output to the chimney 50 for emission via the ammonia-free catalyst output pipeline 71.

[0068] In step S180 above, the ammonia-free catalyst device 70 is equipped with an inlet 701, an outlet 702, an ozone inlet 703, an ammonia-free catalyst output pipe 71, and an ozone delivery pipe 72 (as shown in Figures 1 to 4). One end of the ozone delivery pipe 72 is connected to the ozone inlet 703 of the ammonia-free catalyst device 70, and the other end is connected to an ozone generator 74. The ozone generator 74 generates ozone using any one of the following methods: high-voltage discharge, ultraviolet irradiation, or electrolysis. The discharge type (not shown) uses a high-voltage current of a certain frequency to create a high-voltage electric field, causing oxygen molecules within or around the electric field to undergo an electrochemical reaction, thereby producing ozone. This high-voltage discharge type ozone generator 74 can be classified into three types according to the high-voltage frequency: low-frequency (50~60Hz), medium-frequency (400~1000Hz), and high-frequency (greater than 1000Hz). It can also be classified into oxygen-type and air-type according to the gas raw material used, water-cooled and air-cooled according to the cooling method, and quartz tube, ceramic plate, ceramic tube, glass tube, and enamel tube according to the dielectric material. Ozone is generated through this ozone generator 74 and delivered to the ozone inlet 703 of the ammonia-free catalyst device 70 via the ozone delivery pipeline 72. The inlet 701 of the ammonia-free catalyst device 70 is connected to the other end of the treatment output pipeline 15. The ammonia-free catalyst device 70 is equipped with at least one catalyst 73 (as shown in Figures 1 to 4), allowing at least a portion of the treated exhaust gas after mixing to enter the inlet 701 of the ammonia-free catalyst device 70 through the treatment output pipeline 15. This allows at least a portion of the treated exhaust gas after mixing to undergo a denitrification reaction with the ozone. In other words, the ozone and the catalyst 73 are used to oxidize at least a nitrogen oxide (NOx) in the at least a portion of the treated exhaust gas after mixing. The nitrogen oxide (NOx) includes nitric oxide and nitrogen dioxide, etc., and produces a denitrification reaction gas. After the ammonia-free catalyst device 70 performs the denitrification reaction, the denitrification reaction gas, namely nitrogen (N2), is output through the outlet 702 of the ammonia-free catalyst device 70. The outlet 702 of the ammonia-free catalyst device 70 is connected to one end of the ammonia-free catalyst output pipeline 71, and the other end of the ammonia-free catalyst output pipeline 71 is connected to the chimney 50. The nitrogen (N2) after the reaction is transported to the chimney 50 through the ammonia-free catalyst output pipeline 71 by the ammonia-free catalyst device 70, thereby improving the efficiency of nitrogen oxide (NOx) removal and improving the efficiency of nitrogen oxide (NOx) emission.

[0069] Another embodiment of the present invention involves installing a dust collector 90 (as shown in Figures 2 and 4) on the processing output pipeline 15. The dust collector 90 is primarily located on the processing output pipeline 15 connected to the outlet 104 of the direct-fired incinerator (TO) 10, and is also the front end of the connection between one end of the chimney conveying pipeline 51 and the processing output pipeline 15. The dust collector 90 has an inlet 901 and an outlet 902. When the processed exhaust gas output from the direct-fired incinerator (TO) 10 after combustion contains particulate matter, also known as suspended particulate matter (PM2.5),... Matter), where particulate matter refers to a mixture of solid particles and liquid droplets in a gas. Some particulate matter is large enough to be considered as dust or dirt. When at least a portion of the exhaust gas in the processing output pipeline 15 contains at least one particulate matter, at least a portion of the exhaust gas in the processing output pipeline 15 enters the dust collector 90 through the inlet 901 of the dust collector 90, so that the at least one particulate matter can be collected by the dust collector 90. This allows at least a portion of the exhaust gas in the processing output pipeline 15 to collect the particulate matter first, thereby reducing the discharge of the particulate matter, and then it is discharged to the processing output pipeline 15 through the outlet 902 of the dust collector 90, so as to achieve the effect of dust removal. Furthermore, when using the dust collector 90 to collect the particulate matter, the flow direction of at least a portion of the treated exhaust gas in the treatment output pipeline 15 can be controlled by at least one control valve 80 provided in either the chimney conveying pipeline 51 or the treatment output pipeline 15 (as shown in Figures 2 and 4). This mainly allows most of the treated exhaust gas in the treatment output pipeline 15 to flow to the chimney conveying pipeline 51 and be discharged through the chimney 50. A small portion of the treated exhaust gas in the treatment output pipeline 15 is first mixed with at least a portion of the gas after the second adsorption, which is transported through the clean gas discharge bypass pipeline 60, before flowing into the ammonia-free catalyst device 70 for denitrification reaction. This improves the efficiency of volatile organic exhaust gas treatment and reduces nitrogen oxide emissions.

[0070] The above detailed description should make it clear to those skilled in the art that the present invention can indeed achieve the aforementioned objectives and has met the requirements of the Patent Law. Therefore, an invention patent application is hereby filed.

[0071] However, the above description is only a preferred embodiment of the present invention and should not be construed as limiting the scope of the present invention. Therefore, any simple equivalent changes and modifications made in accordance with the scope of the patent application and the contents of the specification of the present invention should still fall within the scope of the patent of the present invention.

[0072] 10: Direct-fired incinerator (TO)

[0073] 101: Stove

[0074] 1011: Channel

[0075] 1012: Stove cover

[0076] 1013: Gas fuel pipe

[0077] 1014: Gas fuel inlet

[0078] 1015: First air inlet

[0079] 1016: Second air inlet

[0080] 1017: Combustion-supporting gas inlet

[0081] 1018: Burning Flame

[0082] 102: Furnace

[0083] 103: Entrance

[0084] 104: Exports

[0085] 11: First heat exchanger

[0086] 111: First cold side piping

[0087] 112: First hot side piping

[0088] 12: Second heat exchanger

[0089] 121: Second cold side piping

[0090] 122: Second hot side piping

[0091] 13: Third heat exchanger

[0092] 131: Third cold side piping

[0093] 132: Third hot side piping

[0094] 14: Fourth heat exchanger

[0095] 141: Fourth cold-side piping

[0096] 142: Fourth hot side piping

[0097] 15: Handling the output piping

[0098] 16: Air duct

[0099] 161: Air vent

[0100] 162: Airway

[0101] 163: Insulation cotton

[0102] 17: Surround Mask

[0103] 21: First cold-side delivery pipeline

[0104] 22: Fourth cold-side delivery pipeline

[0105] 30: First Adsorption Rotary Wheel

[0106] 301: Adsorption Region

[0107] 302: Cooling Area

[0108] 303: Desorption Zone

[0109] 31: Organic gas inlet pipeline

[0110] 32: First clean air emission pipeline

[0111] 33: First cooling air intake pipe

[0112] 34: First cooling gas delivery pipeline

[0113] 35: First hot gas delivery pipeline

[0114] 36: First desorption and concentration gas pipeline

[0115] 361: Fan

[0116] 37: Organic gas connecting pipeline

[0117] 371: Organic gas connection control valve

[0118] 38: First clean air connection pipeline

[0119] 381: First clean air connection control valve

[0120] 40: Second Adsorption Rotor

[0121] 401: Adsorption Region

[0122] 402: Cooling Area

[0123] 403: Desorption Zone

[0124] 41: Second clean air discharge pipeline

[0125] 411: Fan

[0126] 42: Second cooling air intake pipe

[0127] 43: Second cooling gas delivery pipeline

[0128] 44: Second hot gas delivery pipeline

[0129] 45: Second desorption and concentration gas pipeline

[0130] 50: Chimney

[0131] 51: Chimney delivery pipeline

[0132] 60: Clean gas emission bypass pipeline

[0133] 601: Clean gas discharge bypass control valve

[0134] 61: Fan

[0135] 70: Ammonia-free catalyst unit

[0136] 701: Entrance

[0137] 702: Export

[0138] 703: Ozone Inlet

[0139] 71: Ammonia-free catalyst output pipeline

[0140] 72: Ozone delivery pipeline

[0141] 73:Catalyst

[0142] 74: Ozone Generator

[0143] 80: Control valve

[0144] 801: Chimney Control Valve

[0145] 802: Processing output control valve

[0146] 90: Dust collector

[0147] 901: Entrance

[0148] 902: Export

[0149] S100: First adsorption wheel adsorption

[0150] S101: Input first cooling gas

[0151] S110: Conveying the first hot gas desorption

[0152] S120: Desorption and Concentration Gas Delivery

[0153] S130: Exhaust gas processing

[0154] S140: Second adsorption wheel adsorption

[0155] S141: Input second cooling gas

[0156] S150: Conveying second hot gas for desorption

[0157] S160: Control valve controls the flow direction

[0158] S170: Clean gas bypass delivery mixing

[0159] S180: Ammonia-free catalyst denitrification unit

Claims

1. An organic exhaust gas treatment system for reducing nitrogen oxides, comprising: A direct-fired incinerator (TO) is provided, comprising an inlet, an outlet, and a treatment output pipeline. One end of the treatment output pipeline is connected to the outlet of the direct-fired incinerator (TO). The direct-fired incinerator (TO) generates a treatment exhaust gas containing at least one nitrogen oxide (NOx). The treatment exhaust gas is discharged from the outlet of the direct-fired incinerator (TO) into the treatment output pipeline. The direct-fired incinerator (TO) is provided with an air duct, a burner head, and an enclosing hood. The air duct is located within the direct-fired incinerator (TO). The burner head is attached to the direct-fired incinerator (TO). The air duct is connected to the inlet of the direct-fired incinerator (TO) and has an air outlet. The burner head has a channel and includes a burner head cover, a gas fuel pipe, and a combustion-supporting gas inlet. The gas fuel pipe has a gas fuel inlet, at least one first gas outlet, and at least one second gas outlet. The burner head cover is located at the second gas outlet of the gas fuel pipe. One end of the cover is attached to the burner head cover, and the other end of the cover extends through the air outlet of the air duct. The air outlet of the air duct is... The enclosure is larger than the surrounding shield, leaving an air passage between the air outlet of the air duct and the surrounding shield; a first heat exchanger, which is installed inside the direct-fired incinerator (TO), and the first heat exchanger is provided with a first cold-side pipe and a first hot-side pipe; a second heat exchanger, which is installed inside the direct-fired incinerator (TO), and the second heat exchanger is provided with a second cold-side pipe and a second hot-side pipe; a third heat exchanger, which is installed inside the direct-fired incinerator (TO), and the third heat exchanger is provided with a third cold-side pipe and a third hot-side pipe. Piping; a fourth heat exchanger, which is located inside the direct-fired incinerator (TO), the fourth heat exchanger having a fourth cold-side pipeline and a fourth hot-side pipeline; a first cold-side conveying pipeline, one end of which is connected to the other end of the first cold-side pipeline, and the other end of the first cold-side conveying pipeline is connected to one end of the fourth cold-side pipeline; a fourth cold-side conveying pipeline, one end of which is connected to the other end of the fourth cold-side pipeline, and the other end of the fourth cold-side conveying pipeline is connected to the inlet of the direct-fired incinerator (TO);A first adsorption rotor is provided, comprising an adsorption zone, a cooling zone, and a desorption zone. The first adsorption rotor is connected to an organic gas inlet pipe, a first purified gas outlet pipe, a first cooling gas inlet pipe, a first cooling gas delivery pipe, a first hot gas delivery pipe, and a first desorption concentrated gas pipe. One end of the organic gas inlet pipe is connected to one side of the adsorption zone of the first adsorption rotor, one end of the first purified gas outlet pipe is connected to the other side of the adsorption zone of the first adsorption rotor, one end of the first cooling gas inlet pipe is connected to one side of the cooling zone of the first adsorption rotor, and one end of the first cooling gas delivery pipe is connected to the other side of the first adsorption rotor. The other side of the cooling zone is connected to the other end of the first cooling gas delivery pipe, which is connected to one end of the third cold-side pipe of the third heat exchanger. One end of the first hot gas delivery pipe is connected to the other side of the desorption zone of the first adsorption rotor. The other end of the first hot gas delivery pipe is connected to the other end of the third cold-side pipe of the third heat exchanger. One end of the first desorbed concentrated gas pipe is connected to one side of the desorption zone of the first adsorption rotor. The other end of the first desorbed concentrated gas pipe is connected to one end of the first cold-side pipe of the first heat exchanger. A second adsorption rotor is provided with an adsorption zone, a cooling zone, and a desorption zone. The second adsorption rotor is connected to... The system is connected to a second purified gas discharge pipeline, a second cooling gas inlet pipeline, a second cooling gas delivery pipeline, a second hot gas delivery pipeline, and a second desorption and concentration gas pipeline. One end of the first purified gas discharge pipeline is connected to one side of the adsorption zone of the second adsorption rotor, and one end of the second purified gas discharge pipeline is connected to the other side of the adsorption zone of the second adsorption rotor. One end of the second cooling gas inlet pipeline is connected to one side of the cooling zone of the second adsorption rotor, and one end of the second cooling gas delivery pipeline is connected to the other side of the cooling zone of the second adsorption rotor. The other end of the second cooling gas delivery pipeline is connected to one end of the second cold-side pipeline of the second heat exchanger. One end of the delivery pipeline is connected to the other side of the desorption zone of the second adsorption rotor, the other end of the second hot gas delivery pipeline is connected to the other end of the second cold side pipeline of the second heat exchanger, and one end of the second desorbed concentrated gas pipeline is connected to one side of the desorption zone of the second adsorption rotor; a chimney, the other end of the second clean gas discharge pipeline is connected to the chimney; a chimney delivery pipeline, one end of the chimney delivery pipeline is connected to the processing output pipeline, the other end of the chimney delivery pipeline is connected to the chimney, and either the chimney delivery pipeline or the processing output pipeline is provided with at least one control valve to control the flow direction of at least a portion of the processed tail gas in the processing output pipeline;A purified gas discharge bypass pipeline, one end of which is connected to a second purified gas discharge pipeline, and the other end of which is connected to a treatment output pipeline. At least a portion of the gas system after the second adsorption in the second purified gas discharge pipeline is transported to the treatment output pipeline through the purified gas discharge bypass pipeline, allowing the at least a portion of the gas after the second adsorption to mix with at least a portion of the treated exhaust gas in the treatment output pipeline, thereby reducing the temperature of at least a portion of the treated exhaust gas in the treatment output pipeline; and an ammonia-free catalyst device, which is provided with an inlet, an outlet, an ozone inlet, an ammonia-free catalyst output pipeline, and an ozone supply... The outlet of the ammonia-free catalyst device is connected to one end of the ammonia-free catalyst output pipeline, and the other end of the ammonia-free catalyst output pipeline is connected to the chimney. One end of the ozone delivery pipeline is connected to the ozone inlet of the ammonia-free catalyst device, and the other end of the ozone delivery pipeline is connected to an ozone generator. The ozone generator produces ozone, which is then delivered to the ammonia-free catalyst device via the ozone delivery pipeline. The inlet of the ammonia-free catalyst device is connected to the other end of the treatment output pipeline, allowing at least a portion of the mixed exhaust gas to enter the ammonia-free catalyst device for denitrification reaction, producing a denitrification gas, which is then discharged to the chimney via the ammonia-free catalyst output pipeline.

2. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the ammonia-free catalyst device is further provided with at least one catalyst, and the denitrification reaction of the ammonia-free catalyst device utilizes the ozone and the catalyst to oxidize the exhaust gas containing at least one nitrogen oxide (NOx).

3. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the treatment output pipeline is further equipped with a dust collector having an inlet and an outlet. When at least a portion of the treated exhaust gas in the treatment output pipeline contains at least one particulate matter, the at least a portion of the treated exhaust gas in the treatment output pipeline enters the dust collector through the inlet to collect the at least one particulate matter, and then exits to the treatment output pipeline through the outlet of the dust collector.

4. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein when the at least one control valve is further provided in the chimney delivery pipeline, the control valve is a chimney control valve to control the air volume of at least a portion of the treated exhaust gas in the treated output pipeline delivered to the chimney.

5. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein when the at least one control valve is further provided in the treatment output pipeline, the control valve is a treatment output control valve to control the air volume of at least a portion of the treated exhaust gas in the treatment output pipeline delivered to the ammonia-free catalyst device.

6. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein when the at least one control valve is further provided on the treatment output pipeline and the chimney conveying pipeline, the control valve on the treatment output pipeline is a treatment output control valve to control the air volume of at least a portion of the treated exhaust gas in the treatment output pipeline delivered to the ammonia-free catalyst device, and the control valve on the chimney conveying pipeline is a chimney control valve to control the air volume of at least a portion of the treated exhaust gas in the treatment output pipeline delivered to the chimney.

7. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the clean gas discharge bypass pipeline is further provided with a clean gas discharge bypass control valve to control the air volume of at least a portion of the gas after the second adsorption being delivered to the treatment output pipeline.

8. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the first cooling gas inlet duct is further configured to supply fresh air or outside air.

9. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the second cooling gas inlet duct is further configured to supply fresh air or outside air.

10. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the organic gas inlet pipe is further provided with an organic gas connecting pipe, the organic gas connecting pipe is connected to the first cooling gas inlet pipe, and the organic gas connecting pipe is further provided with an organic gas connecting control valve to control the air volume of the organic gas connecting pipe.

11. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the first clean gas discharge pipeline is further provided with a first clean gas connection pipeline, the first clean gas connection pipeline is connected to the second cooling gas inlet pipeline, and the first clean gas connection pipeline is further provided with a first clean gas connection control valve to control the air volume of the first clean gas connection pipeline.

12. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the first desorbed concentrated gas pipeline is further provided with a fan.

13. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the second desorption and concentration gas pipeline is further provided with a fan.

14. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the second clean gas emission line is further provided with a fan.

15. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the clean gas emission bypass line is further provided with a fan.

16. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the other end of the second desorbed concentrated gas pipeline is further connected to the organic gas inlet pipeline.

17. The organic exhaust gas treatment system for reducing nitrogen oxides as described in claim 1, wherein the other end of the second desorbed concentrated gas line is further connected to the first cooling gas inlet line.

18. A method for treating organic waste gas to reduce nitrogen oxides, mainly used in an organic waste gas treatment system, and comprising a direct-fired incinerator (TO), a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a first cold-side conveying pipeline, a fourth cold-side conveying pipeline, a first adsorption rotor, a second adsorption rotor, a chimney, a chimney conveying pipeline, a clean gas emission bypass pipeline, and an ammonia-free catalyst device. The direct-fired incinerator (TO) is provided with an inlet, an outlet, and a treatment output pipeline. One end of the treatment output pipeline is connected to the outlet of the direct-fired incinerator (TO), one end of the chimney conveying pipeline is connected to the treatment output pipeline, and the other end of the chimney conveying pipeline is connected to the chimney. The first heat exchanger is provided with a first cold-side pipeline and... The first heat exchanger has a first hot-side pipeline, the second heat exchanger has a second cold-side pipeline and a second hot-side pipeline, the third heat exchanger has a third cold-side pipeline and a third hot-side pipeline, and the fourth heat exchanger has a fourth cold-side pipeline and a fourth hot-side pipeline. One end of the first cold-side pipeline is connected to the other end of the first cold-side pipeline, and the other end of the first cold-side pipeline is connected to one end of the fourth cold-side pipeline. One end of the fourth cold-side pipeline is connected to the other end of the fourth cold-side pipeline, and the other end of the fourth cold-side pipeline is connected to the inlet of the direct-fired incinerator (TO). The first suction... The auxiliary transfer system includes an adsorption zone, a cooling zone, and a desorption zone. The first adsorption rotor is connected to an organic gas inlet pipe, a first purified gas outlet pipe, a first cooling gas inlet pipe, a first cooling gas delivery pipe, a first hot gas delivery pipe, and a first desorption concentrated gas pipe. The second adsorption rotor includes an adsorption zone, a cooling zone, and a desorption zone. The second adsorption rotor is connected to a second purified gas outlet pipe, a second cooling gas inlet pipe, a second cooling gas delivery pipe, a second hot gas delivery pipe, and a second desorption concentrated gas pipe. One end of the purified gas outlet bypass pipe... The device is connected to the second purified gas emission pipeline, and the other end of the second purified gas emission bypass pipeline is connected to the treatment output pipeline. The ammonia-free catalyst device is equipped with an inlet, an outlet, an ozone inlet, an ammonia-free catalyst output pipeline, and an ozone delivery pipeline. The outlet of the ammonia-free catalyst device is connected to one end of the ammonia-free catalyst output pipeline, and the other end of the ammonia-free catalyst output pipeline is connected to the chimney. One end of the ozone delivery pipeline is connected to the ozone inlet of the ammonia-free catalyst device, and the other end of the ozone delivery pipeline is connected to an ozone generator. The main steps of the organic exhaust gas treatment method include: First adsorption rotor adsorption: An exhaust gas containing volatile organic compounds is sent to one side of the adsorption zone of the first adsorption rotor through the organic gas inlet pipe for adsorption, and the adsorbed gas is output to the adsorption zone of the second adsorption rotor through the first clean gas discharge pipe from the other side of the adsorption zone of the first adsorption rotor; First hot gas desorption: Hot gas is transported to the desorption zone of the first adsorption rotor for desorption through the first hot gas transport pipe connected to the third cold side pipe of the third heat exchanger, so as to desorb the volatile organic compounds adsorbed by the first adsorption rotor, and a desorbed concentrated gas is output from one side of the desorption zone of the first adsorption rotor to the first desorbed concentrated gas pipe, and then the desorbed concentrated gas is transported to the first cold side pipe of the first heat exchanger through the first desorbed concentrated gas pipe; Desorbed and concentrated gas delivery: The desorbed and concentrated gas system delivers the gas to one end of the fourth cold-side pipeline of the fourth heat exchanger via the first cold-side delivery pipeline connected to the first cold-side pipeline of the first heat exchanger, and then delivers it to the inlet of the direct-fired incinerator (TO) via the fourth cold-side delivery pipeline connected to the other end of the fourth cold-side pipeline of the fourth heat exchanger; Treatment of exhaust gas output: The direct-fired incinerator (TO) treats the desorbed and concentrated gas and produces a treated exhaust gas containing at least one nitrogen oxide (NOx), which is then output from the outlet of the direct-fired incinerator (TO) into the treated output pipeline. The direct-fired incinerator (TO) is equipped with a duct and a... The combustion chamber includes a burner head and a surrounding shield. An air duct is located within the direct-fired incinerator (TO). The burner head is attached to the direct-fired incinerator (TO). The air duct is connected to the inlet of the direct-fired incinerator (TO) and has an air outlet. The burner head has a channel and includes a burner head shield, a gas fuel pipe, and a combustion-supporting gas inlet. The gas fuel pipe has a gas fuel inlet, at least one first gas outlet, and at least one second gas outlet. The burner head shield is located at the second gas outlet of the gas fuel pipe. One end of the surrounding shield is attached to the burner head shield, and the other end of the surrounding shield extends from the air outlet of the air duct. The air outlet of the air duct is larger than the surrounding shield, allowing for a wider air outlet. An air duct is provided between the air vent and the surrounding shield; Second adsorption rotor adsorption: The adsorbed gas in the first clean gas discharge pipe is transported to one side of the adsorption zone of the second adsorption rotor for adsorption, and a second adsorbed gas is generated through the adsorption zone of the second adsorption rotor. This second adsorbed gas is then discharged to the chimney through the second clean gas discharge pipe from the other side of the adsorption zone of the second adsorption rotor; Second hot gas desorption: Hot gas is transported to the desorption zone of the second adsorption rotor through the second hot gas delivery pipe connected to the second cold-side pipe of the second heat exchanger for desorption, thereby desorbing the volatile organic compounds adsorbed by the second adsorption rotor, and the volatile organic compounds are discharged through the desorption zone of the second adsorption rotor. One side outputs the desorbed and concentrated gas to the second desorbed and concentrated gas pipeline, and then outputs it through the second desorbed and concentrated gas pipeline; control valve controls the flow direction: at least one control valve is provided in either the chimney conveying pipeline or the processing output pipeline to control the flow direction of at least a portion of the processing tail gas in the processing output pipeline; clean gas bypass conveying and mixing: at least a portion of the second adsorption gas system in the second clean gas discharge pipeline is conveyed to the processing output pipeline through the clean gas discharge bypass pipeline, so that at least a portion of the second adsorption gas can be mixed with at least a portion of the processing tail gas in the processing output pipeline to reduce the temperature of at least a portion of the processing tail gas in the processing output pipeline;And the ammonia-free catalytic denitrification device: The ozone generator produces ozone, which is then transported to the ammonia-free catalytic device via an ozone delivery pipeline. The inlet of the ammonia-free catalytic device is connected to the other end of the treatment output pipeline, allowing at least a portion of the mixed exhaust gas to enter the ammonia-free catalytic device for denitrification reaction, producing a denitrification reaction gas, which is then discharged to the chimney via the ammonia-free catalytic output pipeline.

19. The method for denitrification of volatile organic exhaust gas as described in claim 18, wherein the ammonia-free catalyst device is further provided with at least one catalyst, and the denitrification reaction of the ammonia-free catalyst device utilizes the ozone and the catalyst to oxidize the exhaust gas containing at least one nitrogen oxide (NOx).

20. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein the treatment output pipeline is further equipped with a dust collector having an inlet and an outlet. When at least a portion of the treated exhaust gas in the treatment output pipeline contains at least one particulate matter, the at least a portion of the treated exhaust gas in the treatment output pipeline enters the dust collector through the inlet of the dust collector to collect the at least one particulate matter, and then exits to the treatment output pipeline through the outlet of the dust collector.

21. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein when the at least one control valve is further provided in the chimney delivery pipeline, the control valve is a chimney control valve to control the air volume of at least a portion of the treated exhaust gas in the treated output pipeline delivered to the chimney.

22. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein when the at least one control valve is further provided in the treatment output pipeline, the control valve is a treatment output control valve to control the air volume of at least a portion of the treated exhaust gas in the treatment output pipeline delivered to the ammonia-free catalyst device.

23. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein when the at least one control valve is further provided on the treatment output pipeline and the chimney conveying pipeline respectively, the treatment output pipeline is a treatment output control valve to control the air volume of at least a portion of the treated exhaust gas in the treatment output pipeline delivered to the ammonia-free catalyst device, and the chimney conveying pipeline is a chimney control valve to control the air volume of at least a portion of the treated exhaust gas in the treatment output pipeline delivered to the chimney.

24. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein the clean gas discharge bypass pipeline is further provided with a clean gas discharge bypass control valve to control the air volume of at least a portion of the gas after the second adsorption being delivered to the treatment output pipeline.

25. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein after the adsorption step of the first adsorption rotor, the following steps are further provided: inputting a first cooling gas: cooling gas is delivered to the cooling zone of the first adsorption rotor for cooling through the other end of the first cooling gas inlet pipe, and then the cooling gas passing through the cooling zone of the first adsorption rotor is delivered to one end of the third cold side pipe of the third heat exchanger through the other end of the first cooling gas delivery pipe.

26. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 25, wherein the first cooling gas inlet pipe is further configured to supply fresh air or outside air.

27. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 25, wherein the first cooling gas inlet pipe is further connected to an organic gas communication pipe, the organic gas communication pipe is connected to the organic gas inlet pipe, and the organic gas communication pipe is further provided with an organic gas communication control valve to control the air volume of the organic gas communication pipe.

28. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein after the adsorption step of the second adsorption rotor, the following step is further provided: inputting a second cooling gas: cooling gas is delivered to the cooling zone of the second adsorption rotor for cooling through the other end of the second cooling gas inlet pipe, and then the cooling gas passing through the cooling zone of the second adsorption rotor is delivered to one end of the second cold side pipe of the second heat exchanger through the other end of the second cooling gas delivery pipe.

29. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 28, wherein the second cooling gas inlet pipe is further configured to supply fresh air or outside air.

30. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 28, wherein the second cooling gas inlet pipe is further connected to a first clean gas connection pipe, the first clean gas connection pipe is connected to the first clean gas discharge pipe, and the first clean gas connection pipe is further provided with a first clean gas connection control valve to control the air volume of the first clean gas connection pipe.

31. The method for treating organic exhaust gas to reduce nitrogen oxides as described in claim 18, wherein the first desorption and concentration gas pipeline is further provided with a fan.

32. The method for treating organic exhaust gas to reduce nitrogen oxides as described in claim 18, wherein the second desorption and concentration gas pipeline is further provided with a fan.

33. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein the second clean gas emission pipeline is further provided with a fan.

34. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein the clean gas emission bypass pipeline is further provided with a fan.

35. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein the second desorption and concentration gas pipeline is further connected to the organic gas inlet pipeline.

36. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein the second desorbed concentrated gas pipeline is further connected to the first cooling gas inlet pipeline.

37. The organic exhaust gas treatment method for reducing nitrogen oxides as described in claim 18, wherein in the step of treating the exhaust gas output, the treated exhaust gas is further transported via the fourth hot side pipe of the fourth heat exchanger to the third hot side pipe of the third heat exchanger, and via the third hot side pipe of the third heat exchanger to the second hot side pipe of the second heat exchanger, and then via the second hot side pipe of the second heat exchanger to the first hot side pipe of the first heat exchanger, and finally transported from the other end of the first hot side pipe of the first heat exchanger to the outlet of the direct-fired incinerator (TO).