Organic tail gas treatment system and method for reducing nitrogen oxides

Abstract

The invention relates to an organic tail gas treatment system for reducing nitrogen oxide and a method thereof, which are mainly characterized in that treatment tail gas containing at least one nitrogen oxide (NOx) is output from an outlet of a direct-fired incinerator (TO) into a treatment output pipeline; at least one part of the secondarily adsorbed gas is conveyed to the treatment output pipeline through the purified gas discharge bypass pipeline, so that the at least one part of the secondarily adsorbed gas can be mixed with at least one part of treated tail gas in the treatment output pipeline; the temperature of at least one part of the treatment tail gas in the treatment output pipeline is reduced, and then the treatment tail gas enters the ammonia-free catalyst device to be subjected to denitration reaction, so that the efficiency of treating the volatile organic tail gas can be improved, and the effect of reducing the emission of nitrogen oxides is achieved.

Description

Technical Field

[0001] The present invention relates to an organic tail gas treatment system and method for reducing nitrogen oxides, particularly to a volatile organic tail gas treatment system or similar equipment that can improve the treatment efficiency of volatile organic tail gas and has the effect of reducing nitrogen oxide emissions, and is applicable to the semiconductor industry, optoelectronic industry or chemical-related industries. Background Art

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

[0003] In recent years, due to the improvement of environmental awareness and the increasingly strict environmental protection laws and regulations, post-combustion denitration equipment has gradually received attention. For traditional denitration technologies, using selective catalytic reduction (SCR) or selective non-catalytic reduction (SNCR) to treat nitrogen oxides (NOx), urea or ammonia is injected as a reducing agent for reaction.

[0004] Therefore, in view of the above deficiencies, the inventor hopes to propose an organic tail gas treatment system and method for reducing nitrogen oxides that has the effect of reducing nitrogen oxide emissions, and does not require injecting urea or ammonia as a reducing agent for reaction, so that users can easily operate and assemble. Summary of the Invention

[0005] The main object of the present invention is to provide an organic tail gas treatment system and method for reducing nitrogen oxides. Specifically, the treated tail gas containing at least one nitrogen oxide (NOx) is output from the outlet of the direct combustion incinerator (TO) into the treatment output pipeline, and at least a part of the second adsorbed gas is transported to the treatment output pipeline through the clean gas discharge bypass pipeline, so that at least a part of the second adsorbed gas can be mixed with at least a part of the treated tail gas in the treatment output pipeline to reduce the temperature of at least a part of the treated tail gas in the treatment output pipeline, and then enter the ammonia-free catalyst device for denitration reaction. Thereby, the treatment efficiency of volatile organic tail gas can be improved, and the effect of reducing nitrogen oxide emissions can be achieved, thereby increasing the overall practicality.

[0006] The next objective of the present invention is to provide an organic tail gas treatment system and method for reducing nitrogen oxides. An ozone is generated by the ozone generator and transported through the ozone transport pipeline into the ammonia-free catalyst device. The inlet of the ammonia-free catalyst device is connected to the other end of the treatment output pipeline, so that at least a part of the treated tail gas after mixing enters the ammonia-free catalyst device for denitrification reaction. The ammonia-free catalyst device is provided with at least one catalyst, and the denitrification reaction of the ammonia-free catalyst device uses the ozone and the catalyst to oxidize at least one nitrogen oxide (NOx) in the treated tail gas and generate a gas after the denitrification reaction, which is then output through the ammonia-free catalyst output pipeline to the chimney for emission, so as to improve the efficiency of removing nitrogen oxides (NOx), achieve the effect of improving the emission of nitrogen oxides (NOx), and further increase the overall efficiency.

[0007] Another objective of the present invention is to provide an organic tail gas treatment system and method for reducing nitrogen oxides. A dust collector is installed in the treatment output pipeline. The dust collector is provided with an inlet and an outlet. When at least a part of the treated tail gas in the treatment output pipeline contains at least one particulate matter, at least a part of the treated tail gas in the treatment output pipeline enters the dust collector through the inlet of the dust collector for collecting the at least one particulate matter, and then is output from the outlet of the dust collector to the treatment output pipeline, so as to achieve the effect of dust removal and further increase the overall usability.

[0008] Another objective of the present invention is to provide an organic tail gas treatment system and method for reducing nitrogen oxides. Through the air duct, the gas to be treated (such as a mixture of one or more volatile organic compounds and air) can be transported to the air outlet and flow out through the air duct left between the air outlet and the surrounding shield to the front end of the combustion flame generated by the burner head, so as to increase the destruction efficiency of the volatile organic compounds contained in the gas to be treated. On the other hand, the combustion-supporting gas (such as air or oxygen) entering from the combustion-supporting gas inlet of the burner head is designed to be increased by more than 20% to 30% of the combustion equivalence ratio. The excess combustion-supporting gas can reduce the temperature of the combustion flame generated by the burner head. Therefore, the gas to be treated (such as a mixture of one or more volatile organic compounds and air) can reduce the generation of nitrogen oxides after passing through the generated combustion flame, and has the effect of reducing the generation of nitrogen oxides, and further increases the overall operability.

[0009] In order to further understand the features, characteristics and technical content of the present invention, please refer to the following detailed description and drawings of the present invention. The attached drawings are only for reference and illustration, and are not intended to limit the present invention. Description of the Drawings

[0010] Figure 1 It is a schematic diagram of the system architecture of the present invention.

[0011] Figure 2 Schematic diagram of the system architecture of the present invention provided with a dust collector.

[0012] Figure 3 Schematic diagram of the system architecture of the present invention provided with a fan.

[0013] Figure 4 Schematic diagram of the system architecture of the present invention provided with a fan and a dust collector.

[0014] Figure 5 Flow chart of the main steps of the present invention.

[0015] Figure 6 Flow chart of the step of inputting the first cooling gas in the present invention

[0016] Figure 7 Flow chart of the step of inputting the second cooling gas in the present invention.

[0017] Explanation of reference numerals in the drawings:

[0018] 10, Direct-fired incinerator (TO) 101, Burner head

[0019] 1011, Channel 1012, Burner head shield

[0020] 1013, Gas fuel pipe 1014, Gas fuel inlet

[0021] 1015, First-stage gas port 1016, Second-stage gas port

[0022] 1017, Combustion-supporting gas inlet 1018, Combustion flame

[0023] 102, Furnace chamber 103, Inlet

[0024] 104, Outlet 11, First heat exchanger

[0025] 111, First cold-side pipeline 112, First hot-side pipeline

[0026] 12, Second heat exchanger 121, Second cold-side pipeline

[0027] 122, Second hot-side pipeline 13, Third heat exchanger

[0028] 131, Third cold-side pipeline 132, Third hot-side pipeline

[0029] 14, Fourth heat exchanger 141, Fourth cold-side pipeline

[0030] 142, Fourth hot-side pipeline 15, Processing output pipeline

[0031] 16, Air duct 161, Air outlet

[0032] 162. Airway 163. Heat insulation cotton

[0033] 17. Enclosing shield

[0034] 21. First cold-side delivery pipeline 22. Fourth cold-side delivery pipeline

[0035] 30. First adsorption wheel 301. Adsorption zone

[0036] 302. Cooling zone 303. Desorption zone

[0037] 31. Organic gas inlet pipeline 32. First clean gas discharge pipeline

[0038] 33. First cooling gas inlet pipeline 34. First cooling gas delivery pipeline

[0039] 35. First hot gas delivery pipeline 36. First desorption concentrated gas pipeline

[0040] 361. Fan 37. Organic gas connection pipeline

[0041] 371. Organic gas connection control valve 38. First clean gas connection pipeline

[0042] 381. First clean gas connection control valve 40. Second adsorption wheel

[0043] 401. Adsorption zone 402. Cooling zone

[0044] 403. Desorption zone 41. Second clean gas discharge pipeline

[0045] 411. Fan 42. Second cooling gas inlet pipeline

[0046] 43. Second cooling gas delivery pipeline 44. Second hot gas delivery pipeline

[0047] 45. Second desorption concentrated gas pipeline 451. Fan

[0048] 50. Chimney 51. Chimney delivery pipeline

[0049] 60. Clean gas discharge bypass pipeline 601. Clean gas discharge bypass control valve

[0050] 61. Fan

[0051] 70. Ammonia-free catalyst device 701. Inlet

[0052] 702. Outlet 703. Ozone inlet

[0053] 71. Ammonia-free catalyst output pipeline 72. Ozone delivery pipeline

[0054] 73. Catalyst 74. Ozone generator

[0055] 80. Control valve 801. Chimney control valve

[0056] 802. Process output control valve 90. Dust collector

[0057] 901. Inlet 902. Outlet

[0058] S100. First adsorption wheel adsorption

[0059] S101. Input first cooling gas

[0060] S110. Convey first hot gas for desorption

[0061] S120. Convey desorbed and concentrated gas

[0062] S130. Process and output treatment of tail gas

[0063] S140. Second adsorption wheel adsorption

[0064] S141. Input second cooling gas

[0065] S150. Convey second hot gas for desorption

[0066] S160. Control the flow direction of the control valve

[0067] S170. Convey and mix the clean gas through the bypass

[0068] S180. Denitrification by the ammonia-free catalyst device Specific embodiments

[0069] Please refer to Figures 1 to 7 , which is a schematic diagram of an embodiment of the present invention. The best embodiment of the organic tail gas treatment system and method for reducing nitrogen oxides of the present invention is applied to the volatile organic exhaust gas treatment system or similar equipment in the semiconductor industry, optoelectronic industry or chemical-related industry, mainly to improve the efficiency of volatile organic tail gas treatment and have the effect of reducing nitrogen oxide emissions.

[0070] The organic tail gas treatment system for reducing nitrogen oxides of the present invention mainly includes a combination design of a direct combustion 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 wheel 30, a second adsorption wheel 40, a chimney 50, a chimney conveying pipeline 51, a clean gas discharge bypass pipeline 60 and an ammonia-free catalyst device 70 (as Figures 1 to 4As shown in the figure, the first heat exchanger 11 is provided with a first cold-side pipeline 111 and a first hot-side pipeline 112, the second heat exchanger 12 is provided with a second cold-side pipeline 121 and a second hot-side pipeline 122, the third heat exchanger 13 is provided with a third cold-side pipeline 131 and a third hot-side pipeline 132, and the fourth heat exchanger 14 is provided with a fourth cold-side pipeline 141 and a fourth hot-side pipeline 142. Additionally, the direct-fired incinerator (TO) 10 is provided with a burner head 101 and a furnace chamber 102. The burner head 101 communicates with the furnace chamber 102, and the first heat exchanger 11, the second heat exchanger 12, the third heat exchanger 13, and the fourth heat exchanger 14 are respectively disposed within 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 treatment output pipeline 15, an air duct 16, and a surrounding shield 17 (as Figures 1 to 4 shown), and the inlet 103 is disposed at the burner head 101, while the outlet 104 is disposed at the furnace chamber 102. Additionally, one end of the treatment output pipeline 15 is connected to the outlet 104 of the direct-fired incinerator (TO) 10, and the direct-fired incinerator (TO) 10 generates a treatment tail gas. The treatment tail gas contains at least one nitrogen oxide (NOx), and the treatment tail gas is output from the outlet 104 of the direct-fired incinerator (TO) 10 into the treatment output pipeline 15.

[0071] Additionally, the air duct 16 is disposed within the direct-fired incinerator (TO) 10. The burner head 101 is coupled to the direct-fired incinerator (TO) 10, and the air duct 16 is connected to the inlet 103 of the direct-fired incinerator (TO) 10. Additionally, the burner head 101 is provided with a passage 1011, and the burner head 101 is provided with a burner head shield 1012, a gaseous fuel pipe 1013, and a combustion-supporting gas inlet 1017 (as Figures 1 to 4 shown), wherein the combustion-supporting gas inlet 1017 can be disposed at one end or on the side of the passage 1011, and the combustion-supporting gas inlet 1017 supplies a combustion-supporting gas (not shown in the figure) to enter. The combustion-supporting gas is any one of air and oxygen, and a fan (not shown in the figure) can be disposed at one end of the passage 1011 to increase the flow rate of the combustion-supporting gas and enable the combustion-supporting gas to enter the passage 1011 of the burner head 101.

[0072] In addition, the gas fuel pipe 1013 has a gas fuel inlet 1014, at least one first-stage gas port 1015, and at least one second-stage gas port 1016. At least one first-stage gas port 1015 of the gas fuel pipe 1013 is located in the passage 1011 of the burner head 101, and the burner head shield 1012 is located at the second-stage gas port 1016 of the gas fuel pipe 1013. The gas fuel inlet 1014 allows a gas fuel (not shown in the figure) to enter. The gas fuel is any one of natural gas and gas. The gas fuel is ejected from the first-stage gas port 1015 into the passage 1011 of the burner head 101. In addition, the gas fuel is ejected from the second-stage gas port 1016 to generate a combustion flame 1018. Furthermore, the burner head shield 1012 is provided with a mounting panel (not shown in the figure) and is mounted on the direct-fired incinerator (TO) 10 through the mounting panel, so that a 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 provided outside the direct-fired incinerator (TO) 10 to facilitate the entry of the gas fuel through the gas fuel inlet 1014. In addition, the combustion-supporting gas inlet 1017 is also provided outside the direct-fired incinerator (TO) 10 to facilitate the entry of the combustion-supporting gas through the combustion-supporting gas inlet 1017.

[0073] In addition, 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 a metal material and is connected to the inlet 103 of the direct-fired incinerator (TO) 10, so that the desorption 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, a burner shield 1012 for arranging the burner 101 is provided at a place of the air duct 16, and the burner shield 1012 corresponds to the air outlet 161. Furthermore, the surrounding shield 17 is arranged in the direct-fired incinerator (TO) 10 and is made of a metal material. The surrounding shield 17 is any one of a cone, a conical body, a horn-shaped body, a square body, and a circular body, and is designed and implemented according to the actual situation. One end of the surrounding shield 17 is combined with the burner shield 1012, and the other end of the surrounding shield 17 passes out of the air outlet 161 of the air duct 16. The air outlet 161 of the air duct 16 is larger than the surrounding shield 17, so that an air duct 162 is left between the air outlet 160 of the air duct 16 and the surrounding shield 17. When the gaseous fuel is ejected from the second-stage gas port 1016 and generates the combustion flame 1018, the combustion flame 1018 passes through the burner shield 1012 of the burner 101 and passes through the surrounding shield 17, and the surrounding shield 17 enables the combustion flame 1018 to avoid being affected by the desorption concentrated gas (such as a mixture containing one or more volatile organic compounds and air) entering and affecting the ejection direction of the combustion flame 1018, so that the combustion flame 1018 can be aggregated into a bundle shape and has a concentrated effect.

[0074] The above-mentioned air duct 16 can directly transport the desorption concentrated gas to the air outlet 161, and flow out through the air duct 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 101. Then, when the combustion-supporting gas 1 entering from the combustion-supporting gas inlet 1017 of the burner 101 is increased by more than 20% to 30% of the combustion equivalent and can enter the passage 1011 of the burner 101 through the combustion-supporting gas 1, the combustion-supporting gas can first be pre-mixed with a part of the gaseous fuel ejected from the first-stage gas port 1015 of the gaseous fuel pipe 1013 in the passage 1011 of the burner 101. The combustion-supporting gas mixed with the part of the gaseous fuel then flows to the second-stage gas port 1016 of the gaseous fuel pipe 1013 and is re-mixed with the gaseous fuel ejected from the second-stage gas port 1016. Thus, through the two-stage injection of the gaseous fuel, the pre-mixing sequence and distribution of the generated combustion flame 1018 can be more uniform, and the excess combustion-supporting gas can reduce the temperature of the combustion flame 1018 generated by the burner 101, so that the desorption concentrated gas can reduce the generation of nitrogen oxides after passing through the generated combustion flame 1018, and has the effect of reducing the generation of nitrogen oxides.

[0075] In the above-mentioned direct-fired incinerator (TO) 10, the treated tail gas is first transported to one side of the fourth heat side pipeline 142 of the fourth heat exchanger 14 for heat exchange, and then transported from the other side of the fourth heat side pipeline 142 of the fourth heat exchanger 14 to one side of the third heat side pipeline 132 of the third heat exchanger 13 for heat exchange. Then, it is transported from the other side of the third heat side pipeline 132 of the third heat exchanger 13 to one side of the second heat side pipeline 122 of the second heat exchanger 12 for heat exchange. After that, it is transported from the other side of the second heat side pipeline 122 of the second heat exchanger 12 to one side of the first heat side pipeline 112 of the first heat exchanger 11 for heat exchange. Finally, it is transported from the other side of the first heat side pipeline 112 of the first heat exchanger 11 to the outlet 104 of the direct-fired incinerator (TO) 10 (as Figures 1 to 4 shown).

[0076] In addition, 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 with an organic gas inlet pipeline 31, a first clean gas discharge pipeline 32, a first cooling gas inlet pipeline 33, a first cooling gas transport pipeline 34, a first hot gas transport pipeline 35 and a first desorption concentrated gas pipeline 36 (as Figures 1 to 4 shown). 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 with a second clean gas discharge pipeline 41, a second cooling gas inlet pipeline 42, a second cooling gas transport pipeline 43, a second hot gas transport pipeline 44 and a second desorption concentrated gas pipeline 45 (as Figures 1 to 4 shown). The first adsorption rotor 30 and the second adsorption rotor 40 are respectively zeolite concentration rotors or concentration rotors made of other materials.

[0077] One end of the organic gas inlet pipeline 31 is connected to one side of the adsorption zone 301 of the first adsorption rotor 30, so that an exhaust gas containing volatile organic compounds (VOCs) can be sent into one side of the adsorption zone 301 of the first adsorption rotor 30 through the organic gas inlet pipeline 31 for adsorption. One end of the first clean gas discharge pipeline 32 is connected to the other side of the adsorption zone 301 of the first adsorption rotor 30, and one end of the first clean gas discharge pipeline 32 is connected to one side of the adsorption zone 401 of the second adsorption rotor 40 (as Figures 1 to 4As shown in the figure, volatile organic compounds (VOCs) are adsorbed in the adsorption zone 301 of the first adsorption wheel 30, and the adsorbed gas is transported through the first clean gas discharge pipeline 32 to the adsorption zone 401 of the second adsorption wheel 40 from the other side of the adsorption zone 301 of the first adsorption wheel 30. On the other side of the adsorption zone 401 of the second adsorption wheel 40, there is a connection to the second clean gas discharge pipeline 41, and the other end of the second clean gas discharge pipeline 41 is connected to the chimney 50 to transport the adsorbed gas in the first clean gas discharge pipeline 32 to one side of the adsorption zone 401 of the second adsorption wheel 40 for adsorption (as Figures 1 to 4 shown), and after the second adsorption of the gas is generated through the adsorption zone 401 of the second adsorption wheel 40, the second adsorbed gas is output to the chimney 50 for discharge from the other side of the adsorption zone 401 of the second adsorption wheel 40 through the second clean gas discharge pipeline 41. Additionally, a fan 411 is provided in the second clean gas discharge pipeline 41 (as Figure 3 and Figure 4 shown), enabling the second adsorbed gas in the second clean gas discharge pipeline 41 to be pushed and pulled into the chimney 50 for discharge through the fan 411.

[0078] On one side of the cooling zone 302 of the first adsorption wheel 30, there is a connection to the first cooling gas inlet pipeline 33 for transporting cooling gas to the cooling zone 302 of the first adsorption wheel 30 for cooling use. On the other side of the cooling zone 302 of the first adsorption wheel 30, there is a connection to one end of the first cooling gas transmission pipeline 34, and the other end of the first cooling gas transmission pipeline 34 is connected to one end of the third cold side pipeline 131 of the third heat exchanger 13 to transport the gas after entering the cooling zone 302 of the first adsorption wheel 30 into the third heat exchanger 13 for heat exchange (as Figures 1 to 4 shown). Furthermore, one end of the first hot gas transmission pipeline 35 is connected to the other side of the desorption zone 303 of the first adsorption wheel 30, and the other end of the first hot gas transmission pipeline 35 is connected to the other end of the third cold side pipeline 131 of the third heat exchanger 13, enabling the high-temperature hot gas that has undergone heat exchange in the third heat exchanger 13 to be transported to the desorption zone 303 of the first adsorption wheel 30 through the first hot gas transmission pipeline 35 for desorption use (as Figures 1 to 4 shown).

[0079] There are two implementation methods for the cooling zone 302 of the first adsorption wheel 30 described above. The first implementation method is that the first cooling gas inlet pipeline 33 connected to one side of the cooling zone 302 of the first adsorption wheel 30 is for fresh air or outside air to enter (as Figure 1As shown, the cooling air for cooling the cooling zone 303 of the first adsorption wheel 30 is provided by the fresh air or outside air. In another second embodiment, an organic gas communication pipeline 37 is provided in the organic gas inlet pipeline 31, and the organic gas communication pipeline 37 is connected to the first cooling air inlet pipeline 33 (as Figure 3 shown), so that at least a part of the exhaust gas containing volatile organic compounds (VOCs) in the organic gas inlet pipeline 31 can be transported to the cooling zone 302 of the first adsorption wheel 30 through the organic gas communication pipeline 37 for cooling use. In addition, an organic gas communication control valve 371 is provided in the organic gas communication pipeline 37 (as Figure 3 shown) to control the air volume of the organic gas communication pipeline 37.

[0080] On the other hand, one side of the cooling zone 402 of the second adsorption wheel 40 is connected to the second cooling air inlet pipeline 42 for transporting cooling air to the cooling zone 402 of the second adsorption wheel 40 for cooling use. The other side of the cooling zone 402 of the second adsorption wheel 40 is connected to one end of the second cooling air transport pipeline 43, and the other end of the second cooling air transport pipeline 43 is connected to one end of the second cold side pipeline 121 of the second heat exchanger 12 to transport the gas after entering the cooling zone 402 of the second adsorption wheel 40 into the second heat exchanger 12 for heat exchange (as Figures 1 to 4 shown). Furthermore, one end of the second hot air transport pipeline 44 is connected to the other side of the desorption zone 403 of the second adsorption wheel 40, and the other end of the second hot air transport pipeline 44 is connected to the other end of the second cold side pipeline 121 of the second heat exchanger 12, so that the high-temperature hot air that has undergone heat exchange through the second heat exchanger 12 can be transported to the desorption zone 403 of the second adsorption wheel 40 through the second hot air transport pipeline 44 for desorption use (as Figures 1 to 4 shown).

[0081] There are two implementation modes for the cooling zone 402 of the second adsorption wheel 40 described above. In the first implementation mode, the second cooling air inlet pipeline 42 connected to one side of the cooling zone 402 of the second adsorption wheel 40 is for fresh air or outside air to enter (as Figure 2 shown), and the fresh air or outside air is used to provide cooling for the cooling zone 402 of the second adsorption wheel 40. In another second implementation mode, a first clean gas communication pipeline 38 is provided in the first clean gas discharge pipeline 32, and the other end of the first clean gas communication pipeline 38 is connected to the second cooling air inlet pipeline 42 (as Figure 3 and Figure 4As shown in the figure, at least a part of the adsorbed gas in the first clean gas discharge pipeline 32 can be transported to the cooling zone 402 of the second adsorption wheel 40 through the first clean gas connection pipeline 38 for cooling use. Additionally, a first clean gas connection control valve 381 is provided on the first clean gas connection pipeline 38 (as shown in Figure 3 and Figure 4 shown in the figure) to control the air volume of the first clean gas connection pipeline 38.

[0082] One end of the first desorption and concentration gas pipeline 36 is connected to one side of the desorption zone 303 of the first adsorption wheel 30, and the other end of the first desorption and concentration 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 shown in the figure). 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 delivery pipeline 21, and the other end of the first cold side delivery 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 pipeline 141 of the fourth heat exchanger 14 is connected to one end of the fourth cold side delivery pipeline 22, and the other end of the fourth cold side delivery pipeline 22 is connected to the inlet 103 of the direct combustion incinerator (TO) 10 (as shown in Figures 1 to 4 shown in the figure). The desorption zone 303 of the first adsorption wheel 30 is used to desorb the volatile organic compounds (VOCs) adsorbed by the first adsorption wheel 30, and a desorption and concentration gas is output from one side of the desorption zone 303 of the first adsorption wheel 30 to the first desorption and concentration gas pipeline 36. Then, the desorption and concentration gas is transported into one end of the first cold side pipeline 111 of the first heat exchanger 11 through the first desorption and concentration gas pipeline 36. The desorption and concentration gas is transported into one end of the first cold side delivery pipeline 21 through the other end of the first cold side pipeline 111 of the first heat exchanger 11, and then transported into one end of the fourth cold side pipeline 141 of the fourth heat exchanger 14 through the other end of the first cold side delivery pipeline 21. Next, it is transported into one end of the fourth cold side delivery pipeline 22 through the other end of the fourth cold side pipeline 141 of the fourth heat exchanger 14, and finally transported into the inlet 103 of the direct combustion incinerator (TO) 10 through the other end of the fourth cold side delivery pipeline 22, enabling the burner 101 of the direct combustion incinerator (TO) 10 to perform high-temperature cracking to reduce volatile organic compounds (VOCs). Additionally, a fan 361 is provided on the first desorption and concentration gas pipeline 36 (as shown in Figure 3 and Figure 4 shown in the figure) to push and pull the desorption and concentration gas into one end of the first cold side pipeline 111 of the first heat exchanger 11.

[0083] In addition, one end of the second desorption and concentration gas pipeline 45 is connected to one side of the desorption zone 403 of the second adsorption rotor 40, and hot gas is transported to the desorption zone 403 of the second adsorption rotor 40 through the second hot gas transportation pipeline 44 connected to the second cold side pipeline 121 of the second heat exchanger 12 for desorption (as Figures 1 to 4 shown), and the volatile organic compound (VOCs) adsorbed by the second adsorption rotor 40 is desorbed through the desorption zone 403 of the second adsorption rotor 40, and a re-desorbed and concentrated gas is output from one side of the desorption zone 403 of the second adsorption rotor 40 to the second desorption and concentration gas pipeline 45, and then output through the second desorption and concentration gas pipeline 45. The other end of the second desorption and concentration gas pipeline 45 has two implementation manners. The first implementation manner is that the other end of the second desorption and concentration gas pipeline 45 is connected to the organic gas inlet pipeline 31 (as Figure 1 and Figure 3 shown), so that the re-desorbed and concentrated gas can enter the adsorption zone 301 of the first adsorption rotor 30 through the organic gas inlet pipeline 31 for re-adsorption. The second implementation manner is that the other end of the second desorption and concentration gas pipeline 45 is connected to the first cooling gas inlet pipeline 33 (as Figure 2 and Figure 4 shown), so that the re-desorbed and concentrated gas can enter the cooling zone 302 of the first adsorption rotor 30 through the first cooling gas inlet pipeline 33 for cooling use. Furthermore, a fan 45 is provided on the second desorption and concentration gas pipeline 45 (as Figure 3 and Figure 4 shown) to push and 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 and concentrated gas generated through the desorption zone 403 of the second adsorption rotor 40 can enter the adsorption zone 301 or the cooling zone 302 of the first adsorption rotor 30 for recycling.

[0084] In addition, one end of the chimney transportation pipeline 51 is connected to the treatment output pipeline 15, and the other end of the chimney transportation pipeline 51 is connected to the chimney 50 (as Figures 1 to 4 shown), and at least one control valve 80 is provided in any one of the chimney transportation pipeline 51 and the treatment output pipeline 15 (as Figure 1 and Figure 3as shown in the figure), to control the flow direction of at least a part of the treated exhaust gas in the treatment output pipeline 15, where the control valve 80 can be any one of a two-way valve, a three-way valve, and an electric valve, mainly implemented in cooperation with the pipeline design. When the at least one control valve 80 is disposed on the chimney conveying pipeline 51, the control valve 80 is the chimney control valve 801 to control the air volume of at least a part of the treated exhaust gas in the treatment output pipeline 15 conveyed to the chimney 50. And when the at least one control valve 80 is disposed on the treatment output pipeline 15, the control valve 80 is the treatment output control valve 802 to control the air volume of at least a part of the treated exhaust gas in the treatment output pipeline 15 conveyed to the ammonia-free catalyst device 70. Additionally, when one control valve 80 is respectively disposed on the treatment output pipeline 15 and the chimney conveying pipeline 51 (such as Figure 2 and Figure 4 as shown in the figure), on the treatment output pipeline 15 is the treatment output control valve 802 to control the air volume of at least a part of the treated exhaust gas in the treatment output pipeline 15 conveyed to the ammonia-free catalyst device 70, and on the chimney conveying pipeline 51 is the chimney control valve 801 to control the air volume of at least a part of the treated exhaust gas in the treatment output pipeline 15 conveyed to the chimney 50.

[0085] In addition, one end of the clean gas discharge bypass pipeline 60 is connected to the second clean gas discharge pipeline 41, and the other end of the clean gas discharge bypass pipeline 60 is connected to the treatment output pipeline 15 (such as Figures 1 to 4 as shown in the figure), and at least a part of the gas after the second adsorption in the second clean gas discharge pipeline 41 is conveyed to the treatment output pipeline 15 through the clean gas discharge bypass pipeline 60, so that at least a part of the gas after the second adsorption can be mixed with at least a part of the treated exhaust gas in the treatment output pipeline 15 to reduce the temperature of at least a part of the treated exhaust gas in the treatment output pipeline 15, where the clean gas discharge bypass pipeline 60 is provided with a clean gas discharge bypass control valve 601 (such as Figures 1 to 4 as shown in the figure) to control the air volume of at least a part of the gas after the second adsorption conveyed to the treatment output pipeline 15. Additionally, the clean gas discharge bypass pipeline 60 is provided with a fan 61 (such as Figure 3 and Figure 4As shown in the figure, at least a part of the adsorbed gas can be pushed and pulled into the treatment output pipeline 41. The main purpose of transporting at least a part of the second adsorbed gas in the second clean gas discharge pipeline 41 through the clean gas discharge bypass pipeline 601 is that the operating temperature of the ammonia-free catalyst device 70 needs to be lower than 200 °C. The treatment tail gas generated after high-temperature cracking treatment by the direct-fired incinerator (TO) 10 may be higher than 200 °C (such as 220 °C or 250 °C, etc.), which may damage the ammonia-free catalyst device 70. Therefore, it is necessary to introduce at least a part of the second adsorbed gas in the second clean gas discharge pipeline 41 for mixing and cooling to reach a temperature (such as lower than 200 °C) that can enter the ammonia-free catalyst device 70, so as to achieve the effect of protecting the ammonia-free catalyst device 70.

[0086] Furthermore, the ammonia-free catalyst device 70 is provided with an inlet 701, an outlet 702, an ozone inlet 703, an ammonia-free catalyst output pipeline 71 and an ozone delivery pipeline 72 (as Figures 1 to 4 shown). One end of the ozone delivery pipeline 72 is connected to the ozone inlet 703 of the ammonia-free catalyst device 70, and the other end of the ozone delivery pipeline 72 is connected to an ozone generator 74. The ozone generator 74 uses any one of the high-voltage discharge type, ultraviolet irradiation type, and electrolysis type to generate ozone. Among them, the high-voltage discharge type (not shown in the figure) uses a high-voltage current of a certain frequency to create a high-voltage electric field, causing the oxygen molecules in or around the electric field to undergo an electrochemical reaction to generate ozone. The high-voltage discharge type ozone generator 74 can be divided into three types according to the high-voltage electric frequency: low frequency (50 - 60 Hz), medium frequency (400 - 1000 Hz), and high frequency (greater than 1000 Hz). According to the gas raw materials used, it can be divided into oxygen type and air type. According to the cooling method, it can be divided into water-cooled type and air-cooled type. According to the dielectric material, it can be divided into several types such as quartz tube, ceramic plate, ceramic tube, glass tube, and enamel tube. The ozone generator 74 can generate ozone and send it into the ozone inlet 703 of the ammonia-free catalyst device 70 through 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 provided with at least one catalyst 73 (as Figures 1 to 4As shown, at least a part of the treated exhaust gas after mixing can enter the inlet 701 of the ammonia-free catalyst device 70 through the treated output pipeline 15, so that at least a part of the treated exhaust gas after mixing can react with the ozone for denitrification, that is, using the ozone and the catalyst 73 to oxidize at least one nitrogen oxide (NOx) in at least a part of the treated exhaust gas after mixing. The nitrogen oxide (NOx) includes nitric oxide and nitrogen dioxide, etc., and a denitrification reaction gas is generated. After the ammonia-free catalyst device 70 performs the denitrification reaction, the denitrification reaction gas is output through the outlet 702 of the ammonia-free catalyst device 70, that is, nitrogen (N 2 ), wherein 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, so that the nitrogen (N 2 ) after the reaction is transported to the chimney 50 through the ammonia-free catalyst output pipeline 71 for discharge through the ammonia-free catalyst device 70, so as to improve the efficiency of removing nitrogen oxides (NOx) and achieve the effect of improving the emission of nitrogen oxides (NOx).

[0087] In another embodiment of the present invention, a dust collector 90 is installed in the treated output pipeline 15 (as Figure 2 and Figure 4 shown). The dust collector 90 is mainly located on the treated output pipeline 15 connected to the outlet 104 of the direct-fired incinerator (TO) 10, and is also at the front end where one end of the chimney conveying pipeline 51 is connected to the treated output pipeline 15. The dust collector 90 is provided with an inlet 901 and an outlet 902. When the treated exhaust gas output after the direct-fired incinerator (TO) 10 burns contains particulate matter, which can also be called suspended particulate matter (Particulate Matter). The particulate matter refers to a mixture of solid particles and liquid droplets in the gas. Some particulate matters are large enough to be regarded as dust or dirt. When at least a part of the treated exhaust gas in the treated output pipeline 15 contains at least one particulate matter, at least a part of the treated exhaust gas in the treated output pipeline 15 enters the dust collector 90 through the inlet 901 of the dust collector 90, so as to collect the at least one particulate matter through the dust collector 90, so that at least a part of the treated exhaust gas in the treated output pipeline 15 can collect the particulate matter first to reduce the discharge of the particulate matter, and then be output from the outlet 902 of the dust collector 90 to the treated output pipeline 15, so as to have the effect of dust removal. Furthermore, when using the dust collector 90 to collect the particulate matter, the flow direction of at least a part of the treated exhaust gas in the treated output pipeline 15 can be controlled by at least one control valve 80 provided in any one of the chimney conveying pipeline 51 and the treated output pipeline 15 (as Figure 2 and Figure 4As shown in the figure, the main purpose is to make most of the treated exhaust gas in at least a part of the treated output pipeline 15 flow to the chimney conveying pipeline 51 and be discharged through the chimney 50, while a small part of the treated exhaust gas in at least a part of the treated output pipeline 15 first mixes with at least a part of the gas after the second adsorption conveyed through the clean gas discharge bypass pipeline 60, and then flows into the ammonia-free catalyst device 70 for denitrification reaction. Thereby, the efficiency of volatile organic exhaust gas treatment can be improved, and the effect of reducing nitrogen oxide emissions can be achieved.

[0088] In addition, the method for treating organic exhaust gas to reduce nitrogen oxides of the present invention is mainly used for an organic exhaust gas treatment system, and is provided with a combination design of a direct combustion 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 discharge bypass pipeline 60 and an ammonia-free catalyst device 70 (as Figures 1 to 4 shown).

[0089] The main steps of the organic exhaust gas treatment method include: Step S100 First adsorption rotor adsorption: An exhaust gas containing volatile organic compounds is sent into one side of the adsorption zone 301 of the first adsorption rotor 30 through the organic gas inlet pipeline 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 pipeline 32 on 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 carried out.

[0090] Among them, in the above step S100, 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 with an organic gas inlet pipeline 31, a first clean gas discharge pipeline 32, a first cooling gas inlet pipeline 33, a first cooling gas conveying pipeline 34, a first hot gas conveying pipeline 35 and a first desorption concentrated gas pipeline 36 (as Figures 1 to 4 shown). 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 with a second clean gas discharge pipeline 41, a second cooling gas inlet pipeline 42, a second cooling gas conveying pipeline 43, a second hot gas conveying pipeline 44 and a second desorption concentrated gas pipeline 45 (as Figures 1 to 4 shown). The first adsorption rotor 30 and the second adsorption rotor 40 are respectively a zeolite concentration rotor or a concentration rotor made of other materials.

[0091] One end of the organic gas inlet pipe 31 is connected to one side of the adsorption zone 301 of the first adsorption wheel 30, enabling an exhaust gas containing volatile organic compounds (VOCs) to be sent into one side of the adsorption zone 301 of the first adsorption wheel 30 through the organic gas inlet pipe 31 for adsorption. One end of the first clean gas discharge pipe 32 is connected to the other side of the adsorption zone 301 of the first adsorption wheel 30, and one end of the first clean gas discharge pipe 32 is connected to one side of the adsorption zone 401 of the second adsorption wheel 40 (as Figures 1 to 4 shown), so that after the exhaust gas containing volatile organic compounds (VOCs) is adsorbed by the adsorption zone 301 of the first adsorption wheel 30, the adsorbed gas is transported from the other side of the adsorption zone 301 of the first adsorption wheel 30 to the adsorption zone 401 of the second adsorption wheel 40 through the first clean gas discharge pipe 32.

[0092] Furthermore, after the step S100 of adsorption by the first adsorption wheel, the following step S101 of inputting the first cooling gas is provided: cooling gas is transported to the cooling zone 302 of the first adsorption wheel 30 through the other end of the first cooling gas inlet pipe 33, and then the cooling gas passing through the cooling zone 302 of the first adsorption wheel 30 is transported 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 transport pipe 34.

[0093] In the above step S101, one side of the cooling zone 302 of the first adsorption wheel 30 is connected to the first cooling gas inlet pipe 33 for transporting cooling gas to the cooling zone 302 of the first adsorption wheel 30 for cooling use. The other side of the cooling zone 302 of the first adsorption wheel 30 is connected to one end of the first cooling gas transport pipe 34, and the other end of the first cooling gas transport pipe 34 is connected to one end of the third cold side pipe 131 of the third heat exchanger 13 to transport the gas after entering the cooling zone 302 of the first adsorption wheel 30 into the third heat exchanger 13 for heat exchange (as Figures 1 to 4 shown).

[0094] There are two implementation manners for the cooling zone 302 of the first adsorption wheel 30. The first implementation manner is that the first cooling gas inlet pipe 33 connected to one side of the cooling zone 302 of the first adsorption wheel 30 is for fresh air or outside air to enter (as Figure 1 shown), and the fresh air or outside air is used to provide cooling for the cooling zone 303 of the first adsorption wheel 30. The second implementation manner is that the organic gas inlet pipe 31 is provided with an organic gas communication pipe 37, and the organic gas communication pipe 37 is connected to the first cooling gas inlet pipe 33 (as Figure 3As shown in the figure, at least a part of the exhaust gas containing volatile organic compounds (VOCs) in the organic gas inlet pipe 31 can be transported to the cooling zone 302 of the first adsorption wheel 30 through the organic gas connection pipe 37 for cooling use. In addition, an organic gas connection control valve 371 is provided on the organic gas connection pipe 37 (as Figure 3 shown) to control the air volume of the organic gas connection pipe 37.

[0095] In addition, in the next step S110, the first hot gas desorption is carried out: hot gas is transported to the desorption zone 303 of the first adsorption wheel 30 through the first hot gas transport pipe 35 connected to the third cold side pipe 131 of the third heat exchanger 13 for desorption, so as to desorb the volatile organic compounds adsorbed by the first adsorption wheel 30, and a desorbed and concentrated gas is output from one side of the desorption zone 303 of the first adsorption wheel 30 to the first desorbed and concentrated gas pipe 36, and then the desorbed and concentrated gas is transported into the first cold side pipe 111 of the first heat exchanger 11 through the first desorbed and concentrated gas pipe 36. After completing the above step S110, the next step S120 is carried out.

[0096] Among them, in the above step S110, one end of the first hot gas transport pipe 35 is connected to the other side of the desorption zone 303 of the first adsorption wheel 30, and the other end of the first hot gas transport 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 transported to the desorption zone 303 of the first adsorption wheel 30 through the first hot gas transport pipe 35 for desorption use (as Figures 1 to 4 shown)

[0097] In addition, in the next step S120, the desorbed and concentrated gas is transported: the desorbed and concentrated gas is transported to one end of the fourth cold side pipe 141 of the fourth heat exchanger 14 through the first cold side transport pipe 21 connected to the first cold side pipe 111 of the first heat exchanger 11, and then is transported to the inlet 103 of the direct combustion incinerator (TO) 10 through the fourth cold side transport pipe 22 connected to the other end of the fourth cold side pipe 141 of the fourth heat exchanger 14. After completing the above step S120, the next step S130 is carried out.

[0098] Among them, in the above step S120, one end of the first desorbed and concentrated gas pipe 36 is connected to one side of the desorption zone 303 of the first adsorption wheel 30, and the other end of the first desorbed and concentrated gas pipe 36 is connected to one end of the first cold side pipe 111 of the first heat exchanger 11 (as Figures 1 to 4As shown, 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 delivery pipeline 21, and the other end of the first cold-side delivery 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 pipeline 141 of the fourth heat exchanger 14 is connected to one end of the fourth cold-side delivery pipeline 22, and the other end of the fourth cold-side delivery pipeline 22 is connected to the inlet 103 of the direct-fired incinerator (TO) 10 (as Figures 1 to 4 shown), and passes through the desorption zone 303 of the first adsorption rotor 30 to desorb the volatile organic compound (VOCs) adsorbed by the first adsorption rotor 30, and outputs a desorbed and concentrated gas from one side of the desorption zone 303 of the first adsorption rotor 30 to the first desorbed and concentrated gas pipeline 36, and then transports the desorbed and concentrated gas into the first cold-side pipeline 111 of the first heat exchanger 11 through the first desorbed and concentrated gas pipeline 36. The desorbed and concentrated gas is transported to one end of the first cold-side delivery pipeline 21 through the other end of the first cold-side pipeline 111 of the first heat exchanger 11, and is transported to one end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14 through the other end of the first cold-side delivery pipeline 21, and then is transported to one end of the fourth cold-side delivery pipeline 22 through the other end of the fourth cold-side pipeline 141 of the fourth heat exchanger 14, and finally is transported to the inlet 103 of the direct-fired incinerator (TO) 10 through the other end of the fourth cold-side delivery pipeline 22, enabling the burner head 101 of the direct-fired incinerator (TO) 10 to perform high-temperature cracking to reduce volatile organic compounds (VOCs). In addition, a fan 361 is provided in the first desorbed and concentrated gas pipeline 36 (as Figure 3 and Figure 4 shown) to push and pull the desorbed and concentrated gas into one end of the first cold-side pipeline 111 of the first heat exchanger 11.

[0099] In the above step S120, the direct-fired incinerator (TO) 10 is provided with a burner head 101 and a furnace chamber 102. The burner head 101 communicates with the furnace chamber 102, and the first heat exchanger 11, the second heat exchanger 12, the third heat exchanger 13, and the fourth heat exchanger 14 are respectively arranged 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 output pipeline 15, an air duct 16, and a surrounding shield 17 (as Figures 1 to 4As shown, the inlet 103 is provided at the burner head 101, and the outlet 104 is provided at the furnace chamber 102. One end of the treatment output pipeline 15 is connected to the outlet 104 of the direct-fired incinerator (TO) 10. The direct-fired incinerator (TO) 10 generates a treatment tail gas, where the treatment tail gas contains at least one nitrogen oxide (NOx), and the treatment tail gas is output from the outlet 104 of the direct-fired incinerator (TO) 10 into the treatment output pipeline 15. The first heat exchanger 11 is provided with a first cold-side pipeline 111 and a first hot-side pipeline 112. The second heat exchanger 12 is provided with a second cold-side pipeline 121 and a second hot-side pipeline 122. The third heat exchanger 13 is provided with a third cold-side pipeline 131 and a third hot-side pipeline 132. The fourth heat exchanger 14 is provided with a fourth cold-side pipeline 141 and a fourth hot-side pipeline 142.

[0100] In addition, the air duct 16 is provided inside the direct-fired incinerator (TO) 10. The burner head 101 is combined with 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 shield 1012, a gaseous fuel pipe 1013, and a combustion-supporting gas inlet 1017 (as Figures 1 to 4 shown). The combustion-supporting gas inlet 1017 can be provided at one end or the side of the channel 1011, and the combustion-supporting gas inlet 1017 allows a combustion-supporting gas (not shown in the figure) to enter. The combustion-supporting gas is any one of air and oxygen. A fan (not shown in the figure) 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.

[0101] In addition, the gas fuel pipe 1013 has a gas fuel inlet 1014, at least one first-stage gas port 1015, and at least one second-stage gas port 1016. At least one first-stage gas port 1015 of the gas fuel pipe 1013 is located in the passage 1011 of the burner head 101, and the burner head shield 1012 is located at the second-stage gas port 1016 of the gas fuel pipe 1013. The gas fuel inlet 1014 allows a gas fuel (not shown in the figure) to enter. The gas fuel is any one of natural gas and gas. The gas fuel is ejected from the first-stage gas port 1015 into the passage 1011 of the burner head 101. In addition, the gas fuel is ejected from the second-stage gas port 1016 to generate a combustion flame 1018. Furthermore, the burner head shield 1012 is provided with a mounting panel (not shown in the figure) and is mounted on the direct-fired incinerator (TO) 10 through the mounting panel, so that a 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 provided outside the direct-fired incinerator (TO) 10 to facilitate the entry of the gas fuel through the gas fuel inlet 1014. In addition, the combustion-supporting gas inlet 1017 is also provided outside the direct-fired incinerator (TO) 10 to facilitate the entry of the combustion-supporting gas through the combustion-supporting gas inlet 1017.

[0102] In addition, 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 a metal material and is connected to the inlet 103 of the direct-fired incinerator (TO) 10, so that the desorption concentrated gas (such as a mixture containing more than one volatile organic compound and air) can enter the air duct 16. The air duct 16 is provided with an air outlet 161. In addition, a burner shield 1012 for setting the burner 101 is provided at a place of the air duct 16, and the burner shield 1012 corresponds to the air outlet 161. Furthermore, the surrounding shield 17 is arranged inside the direct-fired incinerator (TO) 10 and is made of a metal material. The surrounding shield 17 is any one of a cone, a conical body, a trumpet-shaped body, a square body, and a circular body, and is designed and implemented according to the actual situation. One end of the surrounding shield 17 is combined with the burner shield 1012, and the other end of the surrounding shield 17 passes out of the air outlet 161 of the air duct 16. The air outlet 161 of the air duct 16 is larger than the surrounding shield 17, so that an air duct 162 is left between the air outlet 160 of the air duct 16 and the surrounding shield 17. When the gaseous fuel is ejected from the second-stage gas port 1016 and generates the combustion flame 1018, the combustion flame 1018 passes through the burner shield 1012 of the burner 101, passes through the surrounding shield 17, and through the surrounding shield 17, the combustion flame 1018 can be prevented from being affected by the desorption concentrated gas (such as a mixture containing more than one volatile organic compound and air) entering and affecting the ejection direction of the combustion flame 1018, so that the combustion flame 1018 can be gathered into a beam shape and has a concentrated effect.

[0103] The above-mentioned air duct 16 can directly transport the desorption concentrated gas to the air outlet 161, and flow out through the air duct 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 101. Then, when the combustion-supporting gas 1 entering from the combustion-supporting gas inlet 1017 of the burner 101 is increased by more than 20% to 30% of the combustion equivalence ratio and can enter the passage 1011 of the burner 101 through the combustion-supporting gas 1, the combustion-supporting gas can first be premixed with a part of the gaseous fuel ejected from the first-stage gas port 1015 of the gaseous fuel pipe 1013 in the passage 1011 of the burner 101. The combustion-supporting gas mixed with the part of the gaseous fuel then flows to the second-stage gas port 1016 of the gaseous fuel pipe 1013 and is remixed with the gaseous fuel ejected from the second-stage gas port 1016. Thus, through the two-stage injection of the gaseous fuel, the premixing sequence and distribution of the generated combustion flame 1018 can be more uniform, and the excess combustion-supporting gas can reduce the temperature of the combustion flame 1018 generated by the burner 101, so that the desorption concentrated gas can reduce the generation of nitrogen oxides after passing through the generated combustion flame 1018, and has the effect of reducing the generation of nitrogen oxides.

[0104] In addition, in the next step S130, the tail gas output treatment is carried out: the direct-fired incinerator (TO) 10 treats the desorbed and concentrated gas to generate a treated tail gas containing at least one nitrogen oxide (NOx), and then outputs the treated tail gas from the outlet 104 of the direct-fired incinerator (TO) 10 into the treatment output pipeline 15. After completing the above step S130, the next step S140 is carried out.

[0105] In the above step S130, the treated tail gas in the direct-fired incinerator (TO) 10 is first transported to one side of the fourth heat side pipeline 142 of the fourth heat exchanger 14 for heat exchange, and then transported from the other side of the fourth heat side pipeline 142 of the fourth heat exchanger 14 to one side of the third heat side pipeline 132 of the third heat exchanger 13 for heat exchange, and then transported from the other side of the third heat side pipeline 132 of the third heat exchanger 13 to one side of the second heat side pipeline 122 of the second heat exchanger 12 for heat exchange, and then transported from the other side of the second heat side pipeline 122 of the second heat exchanger 12 to one side of the first heat side pipeline 112 of the first heat exchanger 11 for heat exchange, and finally transported from the other side of the first heat side pipeline 112 of the first heat exchanger 11 to the outlet 104 of the direct-fired incinerator (TO) 10 (as Figures 1 to 4 shown).

[0106] In addition, in the next step S140, the second adsorption wheel adsorption is carried out: the adsorbed gas in the first clean gas discharge pipeline 32 is transported to one side of the adsorption zone 401 of the second adsorption wheel 40 for adsorption, and the second adsorbed gas is generated through the adsorption zone 401 of the second adsorption wheel 40, and then the second adsorbed gas is output from the other side of the adsorption zone 401 of the second adsorption wheel 40 to the chimney 50 for discharge through the second clean gas discharge pipeline 41. After completing the above step S140, the next step S150 is carried out.

[0107] In the above step S140, the other side of the adsorption zone 401 of the second adsorption wheel 40 is connected to the second clean gas discharge pipeline 41, and the other end of the second clean gas discharge pipeline 41 is connected to the chimney 50 to transport the adsorbed gas in the first clean gas discharge pipeline 32 to one side of the adsorption zone 401 of the second adsorption wheel 40 for adsorption (as Figures 1 to 4 shown), and the second adsorbed gas is generated through the adsorption zone 401 of the second adsorption wheel 40, and then the second adsorbed gas is output from the other side of the adsorption zone 401 of the second adsorption wheel 40 to the chimney 50 for discharge through the second clean gas discharge pipeline 41. In addition, a fan 411 is provided on the second clean gas discharge pipeline 41 (as Figure 3 and Figure 4As shown, the blower 411 is enabled to push and pull the gas after the second adsorption in the second clean gas discharge pipeline 41 into the chimney 50 for discharge.

[0108] Furthermore, after the step S140 of the second adsorption wheel adsorption, the following step S141 of inputting the second cooling gas is provided: Cooling gas is transported to the cooling area 402 of the second adsorption wheel 40 through the other end of the second cooling gas inlet pipeline 42 for cooling, and then the cooling gas that has passed through the cooling area 402 of the second adsorption wheel 40 is transported to one end of the second cold side pipeline 121 of the second heat exchanger 12 through the other end of the second cooling gas transport pipeline 43.

[0109] In the above step S141, one side of the cooling area 402 of the second adsorption wheel 40 is connected to the second cooling gas inlet pipeline 42 for transporting cooling gas to the cooling area 402 of the second adsorption wheel 40 for cooling use, and the other side of the cooling area 402 of the second adsorption wheel 40 is connected to one end of the second cooling gas transport pipeline 43. The other end of the second cooling gas transport pipeline 43 is connected to one end of the second cold side pipeline 121 of the second heat exchanger 12 to transport the gas after entering the cooling area 402 of the second adsorption wheel 40 into the second heat exchanger 12 for heat exchange (as Figures 1 to 4 shown).

[0110] The cooling area 402 of the above second adsorption wheel 40 has two implementation modes. The first implementation mode is that the second cooling gas inlet pipeline 42 connected to one side of the cooling area 402 of the second adsorption wheel 40 is for fresh air or outside air to enter (as Figure 2 shown), and the fresh air or outside air is used to provide cooling for the cooling area 402 of the second adsorption wheel 40. In the second implementation mode, the first clean gas discharge pipeline 32 is provided with a first clean gas connection pipeline 38, and the other end of the first clean gas connection pipeline 38 is connected to the second cooling gas inlet pipeline 42 (as Figure 3 and Figure 4 shown), so that at least a part of the adsorbed gas in the first clean gas discharge pipeline 32 can be transported to the cooling area 402 of the second adsorption wheel 40 for cooling use through the first clean gas connection pipeline 38. In addition, the first clean gas connection pipeline 38 is provided with a first clean gas connection control valve 381 (as Figure 3 and Figure 4 shown) to control the air volume of the first clean gas connection pipeline 38.

[0111] In addition, in the next step S150, second hot gas desorption is performed: hot gas is transported through the second hot gas transport pipeline 44 connected to the second cold-side pipeline 121 of the second heat exchanger 12 to the desorption zone 403 of the second adsorption wheel 40 for desorption, so as to desorb the volatile organic compound adsorbed by the second adsorption wheel 40, and a desorbed and concentrated gas is output from one side of the desorption zone 403 of the second adsorption wheel 40 to the second desorbed and concentrated gas pipeline 45, and then output through the second desorbed and concentrated gas pipeline 45. After completing the above step S150, the next step S160 is carried out.

[0112] In the above step S150, one end of the second hot gas transport pipeline 44 is connected to the other side of the desorption zone 403 of the second adsorption wheel 40, and the other end of the second hot gas transport pipeline 44 is connected to the other end of the second cold-side pipeline 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 transported through the second hot gas transport pipeline 44 to the desorption zone 403 of the second adsorption wheel 40 for desorption use (as Figures 1 to 4 shown).

[0113] In addition, one end of the second desorbed and concentrated gas pipeline 45 is connected to one side of the desorption zone 403 of the second adsorption wheel 40, and hot gas is transported through the second hot gas transport pipeline 44 connected to the second cold-side pipeline 121 of the second heat exchanger 12 to the desorption zone 403 of the second adsorption wheel 40 for desorption (as Figures 1 to 4 shown), and the volatile organic compound (VOCs) adsorbed by the second adsorption wheel 40 is desorbed through the desorption zone 403 of the second adsorption wheel 40, and a desorbed and concentrated gas is output from one side of the desorption zone 403 of the second adsorption wheel 40 to the second desorbed and concentrated gas pipeline 45, and then output through the second desorbed and concentrated gas pipeline 45. The other end of the second desorbed and concentrated gas pipeline 45 has two implementation manners. The first implementation manner is that the other end of the second desorbed and concentrated gas pipeline 45 is connected to the organic gas inlet pipeline 31 (as Figure 1 and Figure 3 shown), so that the desorbed and concentrated gas can enter the adsorption zone 301 of the first adsorption wheel 30 again through the organic gas inlet pipeline 31 for re-adsorption. The second implementation manner is that the other end of the second desorbed and concentrated gas pipeline 45 is connected to the first cooling gas inlet pipeline 33 (as Figure 2 and Figure 4 shown), so that the desorbed and concentrated gas can enter the cooling zone 302 of the first adsorption wheel 30 again through the first cooling gas inlet pipeline 33 for cooling use. Furthermore, a fan 45 is provided on the second desorbed and concentrated gas pipeline 45 (as Figure 3 andFigure 4 As shown, it can push and pull the re-desorbed concentrated gas into the organic gas inlet pipeline 31 or the first cooling gas inlet pipeline 33, so that the re-desorbed concentrated gas generated by the desorption zone 403 of the second adsorption rotor 40 can enter the adsorption zone 301 or the cooling zone 302 of the first adsorption rotor 30 for recycling.

[0114] In addition, in the next step S160, the control valve controls the flow direction: at least one control valve 80 is provided in any one of the chimney conveying pipeline 51 and the treatment output pipeline 15 to control the flow direction of at least a part of the treated tail gas in the treatment output pipeline 15. After completing the above step S160, the next step S170 is carried out.

[0115] One end of the chimney conveying pipeline 51 is connected to the treatment output pipeline 15 in the above step S160, and the other end of the chimney conveying pipeline 51 is connected to the chimney 50 (as Figures 1 to 4 shown), and at least one control valve 80 is provided in any one of the chimney conveying pipeline 51 and the treatment output pipeline 15 (as Figure 1 and Figure 3 shown) to control the flow direction of at least a part of the treated tail gas in the treatment output pipeline 15. The control valve 80 can be any one of a two-way valve, a three-way valve, and an electric valve, mainly implemented in cooperation with the pipeline design. When the at least one control valve 80 is provided in the chimney conveying pipeline 51, the control valve 80 is the chimney control valve 801 to control the air volume of at least a part of the treated tail gas in the treatment output pipeline 15 conveyed to the chimney 50. When the at least one control valve 80 is provided in the treatment output pipeline 15, the control valve 80 is the treatment output control valve 802 to control the air volume of at least a part of the treated tail gas in the treatment output pipeline 15 conveyed to the ammonia-free catalyst device 70. In addition, when one control valve 80 is respectively provided on the treatment output pipeline 15 and the chimney conveying pipeline 51 (as Figure 2 and Figure 4 shown), the treatment output control valve 802 is provided on the treatment output pipeline 15 to control the air volume of at least a part of the treated tail gas in the treatment output pipeline 15 conveyed to the ammonia-free catalyst device 70, and the chimney control valve 801 is provided on the chimney conveying pipeline 51 to control the air volume of at least a part of the treated tail gas in the treatment output pipeline 15 conveyed to the chimney 50.

[0116] In addition, in the next step S170, clean gas bypass transportation and mixing are carried out: At least a part of the gas after the second adsorption in the second clean gas discharge pipeline 41 is transported through the clean gas discharge bypass pipeline 60 into the treatment output pipeline 15, so that at least a part of the gas after the second adsorption can be mixed with at least a part of the treated tail gas in the treatment output pipeline 15 to reduce the temperature of at least a part of the treated tail gas in the treatment output pipeline 15. After completing the above step S170, the next step S180 is carried out.

[0117] In the above step S170, one end of the clean gas discharge bypass pipeline 60 is connected to the second clean gas discharge pipeline 41, and the other end of the clean gas discharge bypass pipeline 60 is connected to the treatment output pipeline 15 (as Figures 1 to 4 shown), and at least a part of the gas after the second adsorption in the second clean gas discharge pipeline 41 is transported through the clean gas discharge bypass pipeline 60 into the treatment output pipeline 15, so that at least a part of the gas after the second adsorption can be mixed with at least a part of the treated tail gas in the treatment output pipeline 15 to reduce the temperature of at least a part of the treated tail gas in the treatment output pipeline 15. The clean gas discharge bypass pipeline 60 is provided with a clean gas discharge bypass control valve 601 (as Figures 1 to 4 shown) to control the air volume of at least a part of the gas after the second adsorption transported to the treatment output pipeline 15. In addition, the clean gas discharge bypass pipeline 60 is provided with a fan 61 (as Figure 3 and Figure 4 shown) to push and pull at least a part of the adsorbed gas into the treatment output pipeline 41. The main purpose of transporting at least a part of the gas after the second adsorption in the second clean gas discharge pipeline 41 through the clean gas discharge bypass pipeline 601 is that the operating temperature of the ammonia-free catalyst device 70 needs to be lower than 200 °C, and the treated tail gas generated after the high-temperature cracking treatment by the direct-fired incinerator (TO) 10 may be higher than 200 °C (such as 220 °C or 250 °C, etc.), which may damage the ammonia-free catalyst device 70. Therefore, it is necessary to introduce at least a part of the gas after the second adsorption in the second clean gas discharge pipeline 41 for mixing and cooling to reach the temperature that can enter the ammonia-free catalyst device 70 (such as lower than 200 °C) to achieve the effect of protecting the ammonia-free catalyst device 70.

[0118] In addition, in step S180 to be performed next, denitrification is carried out by an ammonia-free catalyst device: the ozone generator 74 generates ozone, which is transported through the ozone transport pipeline 72 into the ammonia-free catalyst device 70. The inlet 701 of the ammonia-free catalyst device 70 is connected to the other end of the treatment output pipeline 15, so that at least a part of the treated tail gas after mixing enters the ammonia-free catalyst device 70 for denitrification reaction, and a gas after the denitrification reaction is generated, and then is output through the ammonia-free catalyst output pipeline 71 to the chimney 50 for emission.

[0119] In step S180 above, the ammonia-free catalyst device 70 is provided with an inlet 701, an outlet 702, an ozone inlet 703, an ammonia-free catalyst output pipeline 71 and an ozone transport pipeline 72 (as Figures 1 to 4 shown). One end of the ozone transport pipeline 72 is connected to the ozone inlet 703 of the ammonia-free catalyst device 70, and the other end of the ozone transport pipeline 72 is connected to an ozone generator 74. The ozone generator 74 uses any one of the high-voltage discharge type, ultraviolet irradiation type, and electrolytic type to generate ozone. Among them, the high-voltage discharge type (not shown in the figure) uses a high-voltage current of a certain frequency to create a high-voltage electric field, so that oxygen molecules in or around the electric field undergo an electrochemical reaction to generate ozone. The ozone generator 74 of the high-voltage discharge type can be divided into three types according to the high-voltage electric frequency: low frequency (50 - 60 Hz), medium frequency (400 - 1000 Hz), and high frequency (greater than 1000 Hz), can be divided into oxygen type and air type according to the gas raw material used, can be divided into water-cooled type and air-cooled type according to the cooling method, and can be divided into several types such as quartz tube, ceramic plate, ceramic tube, glass tube, and enamel tube according to the dielectric material. Ozone can be generated by the ozone generator 74 and sent into the ozone inlet 703 of the ammonia-free catalyst device 70 through the ozone transport pipeline 72. In addition, 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 provided with at least one catalyst 73 (as Figures 1 to 4 shown), so that at least a part of the treated tail gas after mixing can enter the inlet 701 of the ammonia-free catalyst device 70 through the treatment output pipeline 15, so that at least a part of the treated tail gas after mixing can react with the ozone for denitrification, that is, at least one nitrogen oxide (NOx) in at least a part of the treated tail gas after mixing is oxidized by the ozone and the catalyst 73. The nitrogen oxide (NOx) includes nitric oxide and nitrogen dioxide, etc., and a gas after the denitrification reaction is generated. When the ammonia-free catalyst device 70 undergoes a denitrification reaction, the gas after the denitrification reaction is output through the outlet 702 of the ammonia-free catalyst device 70, that is, nitrogen (N 2), wherein 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, so as to convey the nitrogen gas (N 2 ) after the reaction to the chimney 50 for discharge through the ammonia-free catalyst device 70, thereby improving the efficiency of removing nitrogen oxides (NOx) and achieving the effect of improving the emission of nitrogen oxides (NOx).

[0120] In another embodiment of the present invention, a dust collector 90 (as shown in Figure 2 and Figure 4 ) is installed on the treatment output pipeline 15. The dust collector 90 is mainly located on the treatment output pipeline 15 connected to the outlet 104 of the direct combustion incinerator (TO) 10, and is also at the front end where one end of the chimney conveying pipeline 51 is connected to the treatment output pipeline 15. The dust collector 90 is provided with an inlet 901 and an outlet 902. When the particulate matter, which can also be called suspended particulate matter (Particulate Matter), is contained in the treatment tail gas output after the combustion of the direct combustion incinerator (TO) 10, the particulate matter refers to a mixture of solid particles and liquid droplets in the gas, and some particulate matter is large enough to be regarded as dust or dirt. When at least a part of the treatment tail gas in the treatment output pipeline 15 contains at least one particulate matter, at least a part of the treatment tail gas in the treatment output pipeline 15 enters the dust collector 90 through the inlet 901 of the dust collector 90, so as to collect the at least one particulate matter through the dust collector 90, enabling at least a part of the treatment tail gas in the treatment output pipeline 15 to collect the particulate matter first to reduce the discharge of the particulate matter, and then being output to the treatment output pipeline 15 through the outlet 902 of the dust collector 90, thus having the effect of dust removal. Furthermore, when using the dust collector 90 to collect the particulate matter, the flow direction of at least a part of the treatment tail 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 Figure 2 and Figure 4 ). Mainly, most of at least a part of the treatment tail gas in the treatment output pipeline 15 flows to the chimney conveying pipeline 51 and is discharged through the chimney 50, while a small part of at least a part of the treatment tail gas in the treatment output pipeline 15 is first mixed with at least a part of the second adsorbed gas conveyed through the clean gas discharge bypass pipeline 60, and then flows into the ammonia-free catalyst device 70 for denitrification reaction. Thereby, the efficiency of treating volatile organic tail gas can be improved, and the effect of reducing nitrogen oxide emissions can be achieved.

[0121] The specific embodiments described above further elaborate on the object, technical solution, and beneficial effects of the present invention. It should be understood that the above are only specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. An organic tail gas treatment system for reducing nitrogen oxides, characterized in that: include: A direct-fired incinerator (TO), 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), the direct-fired incinerator (TO) produces a treated tail gas, the treated tail gas contains at least one nitrogen oxide (NOx), and the treated tail gas is output to the treatment output pipeline through the outlet of the direct-fired incinerator (TO); A first heat exchanger, the first heat exchanger is arranged in the direct-fired incinerator (TO), and the first heat exchanger is provided with a first cold side pipeline and a first hot side pipeline; a second heat exchanger, the second heat exchanger being arranged in the direct-fired incinerator (TO), the second heat exchanger being provided with a second cold-side pipeline and a second hot-side pipeline; a third heat exchanger, the third heat exchanger being arranged in the direct-fired incinerator (TO), the third heat exchanger being provided with a third cold-side pipeline and a third hot-side pipeline; a fourth heat exchanger, the fourth heat exchanger being arranged in the direct-fired incinerator (TO), the fourth heat exchanger being provided with a fourth cold-side pipeline and a fourth hot-side pipeline; a first cold-side transport pipeline, one end of which is connected to the other end of the first cold-side pipeline, and the other end of which is connected to one end of the fourth cold-side pipeline; a fourth cold side delivery pipeline, one end of which is connected to the other end of the fourth cold side pipeline, and the other end of which is connected to the inlet of the direct-fired incinerator (TO); A first adsorption rotor, the first adsorption rotor is provided with an adsorption zone, a cooling zone and a desorption zone, the first adsorption rotor is connected with an organic gas intake pipeline, a first clean gas exhaust pipeline, a first cooling gas intake pipeline, a first cooling gas delivery pipeline, a first hot gas delivery pipeline and a first desorption concentrated gas pipeline, one end of the organic gas intake pipeline is connected to one side of the adsorption zone of the first adsorption rotor, one end of the first clean gas exhaust pipeline is connected to the other side of the adsorption zone of the first adsorption rotor, one end of the first cooling gas intake pipeline is connected to one side of the cooling zone of the first adsorption rotor, and the One end of the first cooling gas delivery pipeline is connected to the other side of the cooling zone of the first adsorption rotor, the other end of the first cooling gas delivery pipeline is connected to one end of the third cold side pipeline of the third heat exchanger, one end of the first hot gas delivery pipeline is connected to the other side of the desorption zone of the first adsorption rotor, the other end of the first hot gas delivery pipeline is connected to the other end of the third cold side pipeline of the third heat exchanger, one end of the first desorption concentrated gas pipeline is connected to one side of the desorption zone of the first adsorption rotor, and the other end of the first desorption concentrated gas pipeline is connected to one end of the first cold side pipeline of the first heat exchanger; a second adsorption rotor, the second adsorption rotor being provided with an adsorption zone, a cooling zone and a desorption zone, the second adsorption rotor being connected with a second clean gas discharge pipeline, a second cooling gas intake pipeline, a second cooling gas delivery pipeline, a second hot gas delivery pipeline and a second desorption concentrated gas pipeline, one end of the first clean gas discharge pipeline being connected to one side of the adsorption zone of the second adsorption rotor, one end of the second clean gas discharge pipeline being connected to the other side of the adsorption zone of the second adsorption rotor, one end of the second cooling gas intake pipeline being connected to the second adsorption rotor, and one end of the second adsorption rotor being connected to the second adsorption rotor. One end of the second cooling gas delivery pipeline is connected to one side of the cooling zone of the second adsorption rotor, 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 second hot gas 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 desorption concentrated gas pipeline is connected to one side of the desorption zone of the second adsorption rotor; a chimney, to which the other end of the second clean gas discharge pipeline is connected; a chimney delivery pipeline, one end of which is connected to the treatment output pipeline, and the other end of which is connected to the chimney, and either the chimney delivery pipeline or the treatment output pipeline is provided with at least one control valve to control the flow direction of at least a portion of the treated tail gas in the treatment output pipeline; a clean gas discharge bypass pipeline, one end of which is connected to the second clean gas discharge pipeline, and the other end of which is connected to the treatment output pipeline, and at least a portion of the second adsorbed gas in the second clean gas discharge pipeline is transported to the treatment output pipeline through the clean gas discharge bypass pipeline, so that the at least a portion of the second adsorbed gas can be mixed with at least a portion of the treated tail gas in the treatment output pipeline to reduce the temperature of at least a portion of the treated tail gas in the treatment output pipeline; as well as An ammonia-free catalyst device is provided 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 ozone generator generates ozone and delivers it to the ammonia-free catalyst device through the ozone delivery pipeline. The inlet of the ammonia-free catalyst device is connected to the other end of the treatment output pipeline, so that at least a part of the treated exhaust gas after mixing enters the ammonia-free catalyst device for denitration reaction and generates a denitration reaction gas, which is then output to the chimney for discharge through the ammonia-free catalyst output pipeline.

2. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The ammonia-free catalyst device is further provided with at least one catalyst. The denitration reaction of the ammonia-free catalyst device utilizes the ozone and the catalyst to oxidize at least one nitrogen oxide (NOx) contained in the treated tail gas.

3. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The treatment output pipeline is further provided 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, 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 is output to the treatment output pipeline through the outlet of the dust collector.

4. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: When the at least one control valve is further arranged on 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 tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: When the at least one control valve is further arranged 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 tail gas in the treatment output pipeline delivered to the ammonia-free catalyst device.

6. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: When the at least one control valve is further provided on the treatment output pipeline and the chimney delivery pipeline, respectively, the treatment output control valve is provided on the treatment output pipeline 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 delivery pipeline is provided on the 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 tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: 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 delivered to the treatment output pipeline.

8. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The first cooling air intake pipeline is further used for fresh air or external air to enter.

9. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The second cooling air intake pipeline is further used for fresh air or external air to enter.

10. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The organic gas intake pipeline is further provided with an organic gas connecting pipeline, and the organic gas connecting pipeline is connected to the first cooling gas intake pipeline. The organic gas connecting pipeline is further provided with an organic gas connecting control valve to control the air volume of the organic gas connecting pipeline.

11. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The first clean air discharge pipeline is further provided with a first clean air connecting pipeline, and the first clean air connecting pipeline is connected to the second cooling air intake pipeline. The first clean air connecting pipeline is further provided with a first clean air connecting control valve to control the air volume of the first clean air connecting pipeline.

12. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The first desorbed concentrated gas pipeline is further provided with a fan.

13. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The second desorbed concentrated gas pipeline is further provided with a fan.

14. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The second clean air discharge pipeline is further provided with a fan.

15. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The clean gas discharge bypass pipeline is further provided with a fan.

16. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The other end of the second desorption concentrated gas pipeline is further connected to the organic gas inlet pipeline.

17. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The other end of the second desorbed concentrated gas pipeline is further connected to the first cooling gas intake pipeline.

18. The organic tail gas treatment system for reducing nitrogen oxides according to claim 1, characterized in that: The direct-fired incinerator (TO) is further provided with an air duct, a burner head and an enclosing shield. The air duct is arranged in the direct-fired incinerator (TO), the burner head is combined with the direct-fired incinerator (TO), the air duct is connected to the inlet of the direct-fired incinerator (TO), the air duct is provided with an air outlet, the burner head is provided with a passage, the burner head is provided with 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 inlet and at least one second gas inlet, the burner head shield is located at the second gas inlet of the gas fuel pipe, one end of the enclosing shield is combined with the burner head shield, and the other end of the enclosing shield passes through the air outlet of the air duct, the air outlet of the air duct is larger than the enclosing shield, so that an air duct is left between the air outlet of the air duct and the enclosing shield.

19. A method for treating organic tail gas to reduce nitrogen oxides, characterized in that: It is mainly used for organic tail gas treatment system and is provided with 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 delivery pipeline, a fourth cold side delivery pipeline, a first adsorption rotor, a second adsorption rotor, a chimney, a chimney delivery 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), and one end of the chimney delivery pipeline is connected to the treatment output pipeline. The other end of the chimney delivery pipeline is connected to the chimney, the first heat exchanger is provided with a first cold side pipeline and a first hot side pipeline, the second heat exchanger is provided with a second cold side pipeline and a second hot side pipeline, the third heat exchanger is provided with a third cold side pipeline and a third hot side pipeline, the fourth heat exchanger is provided with a fourth cold side pipeline and a fourth hot side pipeline, one end of the first cold side delivery pipeline is connected to the other end of the first cold side pipeline, the other end of the first cold side delivery pipeline is connected to one end of the fourth cold side pipeline, one end of the fourth cold side delivery pipeline is connected to the other end of the fourth cold side pipeline, and the other end of the fourth cold side delivery pipeline The first adsorption rotor is connected to the inlet of the direct-fired incinerator (TO), the first adsorption rotor is provided with an adsorption zone, a cooling zone and a desorption zone, the first adsorption rotor is connected with an organic gas intake pipeline, a first clean gas exhaust pipeline, a first cooling gas intake pipeline, a first cooling gas delivery pipeline, a first hot gas delivery pipeline and a first desorption concentrated gas pipeline, the second adsorption rotor is provided with an adsorption zone, a cooling zone and a desorption zone, the second adsorption rotor is connected with a second clean gas exhaust pipeline, a second cooling gas intake pipeline, a second cooling gas delivery pipeline, a second hot gas delivery pipeline and a second desorption concentrated gas pipeline , one end of the clean gas emission bypass pipeline is connected to the second clean gas emission pipeline, the other end of the second clean gas emission bypass pipeline is connected to the treatment output pipeline, the ammonia-free catalyst device is provided 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, 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, and the main steps of the organic tail gas treatment method include: Adsorption by the first adsorption wheel: an exhaust gas containing volatile organic compounds is sent to one side of the adsorption zone of the first adsorption wheel through the organic gas intake pipeline for adsorption, and the adsorbed gas is output from the other side of the adsorption zone of the first adsorption wheel through the first clean gas discharge pipeline to the adsorption zone of the second adsorption wheel; Desorption of the first hot gas: Desorption of the hot gas to the desorption zone of the first adsorption rotor through the first hot gas delivery pipeline connected to the third cold side pipeline of the third heat exchanger, so as to desorb the volatile organic compounds adsorbed by the first adsorption rotor, and output a desorbed concentrated gas from one side of the desorption zone of the first adsorption rotor to the first desorption concentrated gas pipeline, and then the desorbed concentrated gas is transported to the first cold side pipeline of the first heat exchanger through the first desorption concentrated gas pipeline; Desorbed concentrated gas transportation: the desorbed concentrated gas is transported to one end of the fourth cold side pipeline of the fourth heat exchanger through the first cold side transportation pipeline connected to the first cold side pipeline of the first heat exchanger, and then transported to the inlet of the direct-fired incinerator (TO) through the fourth cold side transportation pipeline connected to the other end of the fourth cold side pipeline of the fourth heat exchanger; Treating tail gas output: The direct-fired incinerator (TO) treats the desorbed concentrated gas and produces a treated tail gas, the treated tail gas containing at least one nitrogen oxide (NOx), and then outputs the treated tail gas from the outlet of the direct-fired incinerator (TO) to the treated output pipeline; Adsorption by the second adsorption wheel: the adsorbed gas in the first clean gas discharge pipeline is transported to one side of the adsorption zone of the second adsorption wheel for adsorption, and the second adsorbed gas is generated through the adsorption zone of the second adsorption wheel, and then the second adsorbed gas is output to the chimney through the second clean gas discharge pipeline from the other side of the adsorption zone of the second adsorption wheel for discharge; Transporting the second hot gas for desorption: transporting the hot gas to the desorption zone of the second adsorption rotor for desorption through the second hot gas transport pipeline connected to the second cold side pipeline of the second heat exchanger, so as to desorb the volatile organic compounds adsorbed by the second adsorption rotor, and outputting a desorbed concentrated gas from one side of the desorption zone of the second adsorption rotor to the second desorption concentrated gas pipeline, and then outputting it through the second desorption concentrated gas pipeline; Control valve controls flow direction: at least one control valve is provided in either the chimney delivery pipeline or the treatment output pipeline to control the flow direction of at least a portion of the treated tail gas in the treatment output pipeline; Clean gas bypass delivery and mixing: at least a portion of the second adsorbed gas in the second clean gas discharge pipeline is delivered to the treatment output pipeline through the clean gas discharge bypass pipeline, so that the at least a portion of the second adsorbed gas can be mixed with at least a portion of the treated tail gas in the treatment output pipeline to reduce the temperature of at least a portion of the treated tail gas in the treatment output pipeline; and Denitrification by ammonia-free catalyst device: The ozone generator generates ozone, which is transported to the ammonia-free catalyst device via the ozone transport pipeline. The inlet of the ammonia-free catalyst device is connected to the other end of the treatment output pipeline, so that at least a portion of the treated exhaust gas after mixing enters the ammonia-free catalyst device for denitrification reaction, and generates a denitrification reaction gas, which is then output to the chimney for discharge via the ammonia-free catalyst output pipeline.

20. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The ammonia-free catalyst device is further provided with at least one catalyst. The denitration reaction of the ammonia-free catalyst device utilizes the ozone and the catalyst to oxidize at least one nitrogen oxide (NOx) contained in the treated tail gas.

21. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The treatment output pipeline is further provided 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, 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 is output to the treatment output pipeline through the outlet of the dust collector.

22. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: When the at least one control valve is further arranged on 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.

23. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: When the at least one control valve is further arranged 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 tail gas in the treatment output pipeline delivered to the ammonia-free catalyst device.

24. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: When the at least one control valve is further arranged on the treatment output pipeline and the chimney delivery pipeline respectively, the treatment output pipeline is a treatment output control valve to control the air volume of at least a part of the treated exhaust gas in the treatment output pipeline delivered to the ammonia-free catalyst device, and the chimney delivery pipeline is a chimney control valve to control the air volume of at least a part of the treated exhaust gas in the treatment output pipeline delivered to the chimney.

25. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: 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 delivered to the treatment output pipeline.

26. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: After the first adsorption wheel adsorption step, the following steps are further provided: Input the first cooling gas: transport the cooling gas to the cooling zone of the first adsorption wheel for cooling through the other end of the first cooling gas inlet pipeline, and then transport the cooling gas passing through the cooling zone of the first adsorption wheel to one end of the third cold side pipeline of the third heat exchanger through the other end of the first cooling gas transport pipeline.

27. The method for treating organic tail gas to reduce nitrogen oxides according to claim 26, characterized in that: The first cooling air intake pipeline is further used for fresh air or external air to enter.

28. The method for treating organic tail gas to reduce nitrogen oxides according to claim 26, characterized in that: The first cooling air intake pipeline is further connected to an organic gas connecting pipeline, and the organic gas connecting pipeline is connected to the organic gas intake pipeline. The organic gas connecting pipeline is further provided with an organic gas connecting control valve to control the air volume of the organic gas connecting pipeline.

29. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: After the step of adsorption by the second adsorption wheel, the following steps are further provided: Input the second cooling gas: transport the cooling gas to the cooling zone of the second adsorption rotor for cooling through the other end of the second cooling gas inlet pipeline, and then transport the cooling gas passing through the cooling zone of the second adsorption rotor to one end of the second cold side pipeline of the second heat exchanger through the other end of the second cooling gas transport pipeline.

30. The method for treating organic tail gas to reduce nitrogen oxides according to claim 29, characterized in that: The second cooling air intake pipeline is further used for fresh air or external air to enter.

31. The method for treating organic tail gas to reduce nitrogen oxides according to claim 29, characterized in that: The second cooling air intake pipeline is further connected to a first clean air connecting pipeline, the first clean air connecting pipeline is connected to the first clean air exhaust pipeline, and the first clean air connecting pipeline is further provided with a first clean air connecting control valve to control the air volume of the first clean air connecting pipeline.

32. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The first desorbed concentrated gas pipeline is further provided with a fan.

33. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The second desorbed concentrated gas pipeline is further provided with a fan.

34. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The second clean air discharge pipeline is further provided with a fan.

35. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The clean gas discharge bypass pipeline is further provided with a fan.

36. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The second desorbed concentrated gas pipeline is further connected to the organic gas inlet pipeline.

37. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The second desorbed concentrated gas pipeline is further connected to the first cooling gas intake pipeline.

38. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: In the step of treating the exhaust gas output, the treated exhaust gas is further transported to the third hot side pipe of the third heat exchanger via the fourth hot side pipe of the fourth heat exchanger, and transported to the second hot side pipe of the second heat exchanger via the third hot side pipe of the third heat exchanger, and then transported to the first hot side pipe of the first heat exchanger via the second hot side pipe of the second heat exchanger, and finally transported to the outlet of the direct-fired incinerator (TO) from the other end of the first hot side pipe of the first heat exchanger.

39. The method for treating organic tail gas to reduce nitrogen oxides according to claim 19, characterized in that: The direct-fired incinerator (TO) is further provided with an air duct, a burner head and an enclosing shield. The air duct is arranged in the direct-fired incinerator (TO), the burner head is combined with the direct-fired incinerator (TO), the air duct is connected to the inlet of the direct-fired incinerator (TO), the air duct is provided with an air outlet, the burner head is provided with a passage, the burner head is provided with 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 inlet and at least one second gas inlet, the burner head shield is located at the second gas inlet of the gas fuel pipe, one end of the enclosing shield is combined with the burner head shield, and the other end of the enclosing shield passes through the air outlet of the air duct, the air outlet of the air duct is larger than the enclosing shield, so that an air duct is left between the air outlet of the air duct and the enclosing shield.

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