Volatile organic exhaust gas treatment denitration system and method thereof

Abstract

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

Description

Technical Field

[0001] The present invention relates to a denitration system and method for treating volatile organic exhaust gas, and particularly to a system or similar device for treating volatile organic exhaust gas that can improve the efficiency of treating volatile organic exhaust gas and has the effect of reducing pollutant emissions, and is applicable to the semiconductor industry, optoelectronic industry or chemical-related industries. Background Art

[0002] At present, volatile organic gases (VOCs) are generated during the manufacturing process of the semiconductor industry or optoelectronic industry. The volatile organic gases (VOCs) contain compounds such as nitrogen oxides (NOx) and sulfur oxides (SOx), and 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 increasing strictness of environmental protection regulations, denitration equipment after combustion has gradually attracted 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 the reaction.

[0004] Therefore, in view of the above deficiencies, the inventor of the present invention hopes to propose a denitration system and method for treating volatile organic exhaust gas that has the effect of reducing pollutant emissions, and does not require injecting urea or ammonia as a reducing agent for the reaction, so that users can easily operate and assemble. Summary of the Invention

[0005] The main object of the present invention is to provide a denitration system and method for treating volatile organic exhaust gas. The treated tail gas containing at least one nitrogen oxide (NOx) is output from the outlet of the treatment device into the treatment output pipeline. The nitrogen oxide (NOx) includes nitric oxide, nitrogen dioxide, etc. At least a part of the adsorbed gas is transported to the treatment output pipeline through the clean gas discharge bypass pipeline, so that at least a part of the 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 efficiency of treating volatile organic exhaust gas can be improved, and the effect of reducing pollutant emissions can be achieved, thereby increasing the overall practicability.

[0006] The next object of the present invention is to provide a denitrification system and method for treating volatile organic exhaust gas. An ozone is generated by the ozone generator and conveyed to the ammonia-free catalyst device through the ozone conveying 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 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 generates a gas after the denitrification reaction, which is then output to the chimney through the ammonia-free catalyst output pipeline 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 object of the present invention is to provide a denitrification system and method for treating volatile organic exhaust gas. 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 to the treatment output pipeline through the outlet of the dust collector, so as to have the effect of dust removal and further increase the overall usability.

[0008] 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

[0009] Figure 1 It is a schematic diagram of the system architecture of the main implementation of the present invention.

[0010] Figure 2 It is a schematic diagram of the system architecture with a dust collector in the main implementation of the present invention.

[0011] Figure 3 It is a schematic diagram of the system architecture of another implementation of the present invention.

[0012] Figure 4 It is a schematic diagram of the system architecture with a dust collector in another implementation of the present invention.

[0013] Figure 5 It is a flowchart of the steps of the main implementation of the present invention.

[0014] Description of the Reference Numerals:

[0015] 10. Chimney 20. Heating device

[0016] 21. Heat exchanger

[0017] 30. Adsorption rotor 301. Adsorption zone

[0018] 302. Desorption zone 303. Cooling zone

[0019] 31. Inlet gas pipeline 32. Clean gas discharge pipeline

[0020] 321. Fan 33. Hot gas delivery pipeline

[0021] 34. Desorption concentrated gas pipeline 341. Fan

[0022] 35. Cooling gas inlet pipeline 36. Cooling gas delivery pipeline

[0023] 37. Inlet bypass pipeline 371. Inlet bypass control valve

[0024] 40. Treatment equipment 401. Inlet

[0025] 402. Outlet 403. Combustion chamber

[0026] 41. Treatment output pipeline 42. Air duct

[0027] 421. Air outlet 422. Air passage

[0028] 423. Heat insulation cotton 43. Burner head

[0029] 431. Channel 432. Burner head shield

[0030] 433. Gas fuel pipe 4331. Gas fuel inlet

[0031] 4332. First-stage gas port 4333. Second-stage gas port

[0032] 434. Combustion-supporting gas inlet 435. Combustion flame

[0033] 44. Enclosing shield 50. Chimney delivery pipeline

[0034] 60. Clean gas discharge bypass pipeline 601. Clean gas discharge bypass control valve

[0035] 61. Fan

[0036] 70. Ammonia-free catalyst device 701. Inlet

[0037] 702. Outlet 703. Ozone inlet

[0038] 71. Ammonia-free catalyst output pipeline 72. Ozone delivery pipeline

[0039] 73. Catalyst 74. Ozone generator

[0040] 80, Control valve 801, Chimney control valve

[0041] 802, Process output control valve 90, Dust collector

[0042] 901, Inlet 902, Outlet

[0043] S100, Input organic exhaust adsorption S110, Output desorbed and concentrated gas

[0044] S120, Process tail gas output treatment S130, Control valve to control flow direction

[0045] S140, Clean gas bypass transportation and mixing S150, Non-ammonia catalyst device for denitrification Specific implementation manner

[0046] Please refer to Figures 1 to 5 , which is a schematic diagram of an embodiment of the present invention. The best implementation manner of the volatile organic exhaust gas treatment and denitrification system and method 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 industries, mainly to improve the efficiency of volatile organic exhaust gas treatment and have the effect of reducing pollutant emissions.

[0047] The volatile organic exhaust gas treatment and denitrification system of the present invention mainly includes a combination design of a chimney 10, a heating device 20, an adsorption wheel 30, a processing device 40, a chimney conveying pipeline 50, a clean gas discharge bypass pipeline 60 and a non-ammonia catalyst device 70 (such as Figure 1 and Figure 2As shown, the adsorption rotor 30 is a zeolite concentration rotor or a concentration rotor made of other materials. The adsorption rotor 30 is provided with an adsorption zone 301 and a desorption zone 302. The adsorption rotor 30 is provided with an intake air pipeline 31, a clean air discharge pipeline 32, a hot air delivery pipeline 33 and a desorption concentrated gas pipeline 34. One end of the intake air pipeline 31 is connected to one side of the adsorption zone 301 of the adsorption rotor 30, and the other end of the intake air pipeline 31 is connected to a workplace (not shown in the figure) related to manufacturing sites, R & D sites, etc. in the semiconductor industry, optoelectronic industry or chemical-related industries, or an exhaust gas site generating volatile organic compounds (VOCs). To send an exhaust gas containing volatile organic compounds (VOCs) into one side of the adsorption zone 301 of the adsorption rotor 30 through the intake air pipeline 31, and the adsorption zone 301 adsorbs the volatile organic compounds (VOCs) to generate an adsorbed gas. In addition, one end of the clean air discharge pipeline 32 is connected to the other side of the adsorption zone 301 of the adsorption rotor 30, and the other end of the clean air discharge pipeline 32 is connected to the chimney 10 to transport the adsorbed gas to the chimney 10 for discharge through the clean air discharge pipeline 32. In addition, the clean air discharge pipeline 32 is provided with a fan 321 (as Figure 2 shown) to increase the flow rate of the adsorbed gas in the clean air discharge pipeline 32 to flow towards the chimney 10.

[0048] In addition, the heating device 20 outputs at least a part of hot air (as Figure 1 and Figure 2 shown). The heating device 20 is any one of a heater, a pipeline heater, and a heat exchanger 21. The heater 20 is any one of an electric heating wire, an electric heating tube, and an electric heating sheet (not shown in the figure). The pipeline heater uses any one of gas fuel or liquid fuel. One end of the hot air delivery pipeline 33 is connected to the other side of the desorption zone 302 of the adsorption rotor 30, and the other end of the hot air delivery pipeline 33 is connected to the heating device 20. And at least a part of the hot air of the heating device 20 is transmitted through the hot air delivery pipeline 33 to the other side of the desorption zone 302 of the adsorption rotor 30 to desorb the adsorbed volatile organic compounds (VOCs) on the adsorption rotor 30. Furthermore, one side of the desorption zone 302 of the adsorption rotor 30 is connected to one end of the desorption concentrated gas pipeline 34, and a desorption concentrated gas is output from one side of the desorption zone 302 of the adsorption rotor 30 to the desorption concentrated gas pipeline 34. The desorption concentrated gas pipeline 34 is provided with a fan 341 (as Figure 2 shown) to increase the flow rate of the desorption concentrated gas in the desorption concentrated gas pipeline 34.

[0049] In addition, in addition to the adsorption zone 301 and the desorption zone 302, the adsorption rotor 30 may also be provided with a cooling zone 303 (as Figures 2 to 4As shown, a cooling air inlet pipe 35 and a cooling air delivery pipe 36 are provided in the cooling zone 303 of the adsorption wheel 30. One end of the cooling air inlet pipe 35 is connected to one side of the cooling zone 303 of the adsorption wheel 30, and one end of the cooling air delivery pipe 36 is connected to the other side of the cooling zone 303 of the adsorption wheel 30. The other end of the cooling air delivery pipe 36 is connected to the heating device 20 (as Figure 2 shown). When the heating device 20 is a heat exchanger 21, a cooling gas output from the cooling zone 303 of the adsorption wheel 30 is delivered into the heat exchanger 21 for heat exchange (as Figure 3 and Figure 4 shown). There are two implementation manners for the cooling zone 303 of the adsorption wheel 30 described above. In the first implementation manner, the other end of the cooling air inlet pipe 35 connected to one side of the cooling zone 303 of the adsorption wheel 30 is for fresh air or outside air to enter (as Figure 3 shown), and the fresh air or outside air is used to cool down the cooling zone 303 of the adsorption wheel 30. In the second implementation manner, an intake bypass pipe 37 is provided in the intake pipe 31. One end of the intake bypass pipe 37 is connected to the intake pipe 31 (as Figure 2 and Figure 4 shown), and the other end of the intake bypass pipe 37 is connected to the other end of the cooling air inlet pipe 35, so that at least a part of the exhaust gas containing volatile organic compounds in the intake pipe 31 can be shunted and delivered into the cooling zone 303 of the adsorption wheel 30 for cooling. In addition, an intake bypass control valve 371 is provided in the intake bypass pipe 37 (as Figure 2 and Figure 4 shown) to control the air volume of the at least part of the exhaust gas containing volatile organic compounds delivered to the intake bypass pipe 71.

[0050] In addition, the treatment device 40 is provided with an inlet 401, an outlet 402 and a treatment output pipe 41, and the treatment device 40 is provided with at least one combustion chamber 403 (as Figure 1 and Figure 2 shown). The treatment device 40 is any one of a direct combustion incinerator (TO), a catalytic incinerator or a regenerative thermal oxidizer (RTO). When the treatment device 40 is a direct combustion incinerator (TO), at least two heat exchangers 21 or at least two or more heat exchangers 21 can be further provided in the direct combustion incinerator (TO) (as Figure 3 and Figure 4As shown, at least two heat exchangers 21 or more than two heat exchangers 21 can be used as the heating device 20, and at least a part of the hot gas is output from at least two heat exchangers 21 or more than two heat exchangers 21 in the direct-fired incinerator (TO) for use in the desorption zone 302 of the adsorption rotor 30. One end of the treatment output pipeline 41 is connected to the outlet 402 of the treatment device 40, and the inlet 401 of the treatment device 40 is connected to the other end of the desorption concentrated gas pipeline 34, so that the desorption concentrated gas output from one side of the desorption zone 302 of the adsorption rotor 30 can be transmitted through the desorption concentrated gas pipeline 34 to the inlet 401 of the treatment device 40, and then the desorption concentrated gas is subjected to high-temperature cracking treatment through the combustion chamber 403 of the treatment device 40. After the high-temperature cracking treatment, a treatment tail gas is generated, and the treatment tail gas contains at least one nitrogen oxide (NOx), and the treatment tail gas is output from the outlet 402 of the treatment device 40 into the treatment output pipeline 41. In addition, a fan 341 is provided in the desorption concentrated gas pipeline 34 (as shown in Figure 2 and Figure 4 shown) to push and pull the desorption concentrated gas into the inlet 401 of the treatment device 40.

[0051] One end of the chimney conveying pipeline 50 is connected to the treatment output pipeline 41, and the other end of the chimney conveying pipeline 50 is connected to the chimney 10. At least one control valve 80 is provided in either the chimney conveying pipeline 50 or the treatment output pipeline 41 (as shown in Figure 1 and Figure 3 shown) to control the flow direction of at least a part of the treatment tail gas in the treatment output pipeline 41. 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 50, the control valve 80 is the chimney control valve 801 to control the air volume of at least a part of the treatment tail gas in the treatment output pipeline 41 conveyed to the chimney 10. When the at least one control valve 80 is provided in the treatment output pipeline 41, the control valve 80 is the treatment output control valve 802 to control the air volume of at least a part of the treatment tail gas in the treatment output pipeline 41 conveyed to the ammonia-free catalyst device 70. In addition, when one control valve 80 is respectively provided on the treatment output pipeline 41 and the chimney conveying pipeline 50, the treatment output control valve 802 is on the treatment output pipeline 41 (as shown in Figure 2 and Figure 4 shown) to control the air volume of at least a part of the treatment tail gas in the treatment output pipeline 41 conveyed to the ammonia-free catalyst device 70, and the chimney control valve 801 is on the chimney conveying pipeline 50 (as shown in Figure 2 and Figure 4as shown in the figure), to control the amount of the treated tail gas in at least a part of the treatment output pipeline 41 delivered to the chimney 10.

[0052] One end of the clean gas discharge bypass pipeline 60 is connected to the clean gas discharge pipeline 32, and the other end of the clean gas discharge bypass pipeline 60 is connected to the treatment output pipeline 41. At least a part of the adsorbed gas in the clean gas discharge pipeline 32 is delivered into the treatment output pipeline 41 through the clean gas discharge bypass pipeline 60 (as Figures 1 to 4 shown in the figure), so that at least a part of the adsorbed gas can be mixed with at least a part of the treated tail gas in the treatment output pipeline 41 to reduce the temperature of at least a part of the treated tail gas in the treatment output pipeline 41. A clean gas discharge bypass control valve 601 is provided on the clean gas discharge bypass pipeline 60 (as Figures 1 to 4 shown in the figure), to control the amount of the adsorbed gas in at least a part delivered to the treatment output pipeline 41. A fan 61 is provided on the clean gas discharge bypass pipeline 60 (as Figure 3 and Figure 4 shown in the figure), to push and pull at least a part of the adsorbed gas into the treatment output pipeline 41. The main purpose of delivering at least a part of the adsorbed gas in the clean gas discharge pipeline 32 through the clean gas discharge bypass pipeline 60 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 treatment device 40 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 adsorbed gas in the clean gas discharge pipeline 32 for mixing and cooling to reach the 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.

[0053] 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 4As shown in the figure), 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 generates ozone by any one of the high-voltage discharge type, ultraviolet irradiation type, and electrolysis type. 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 inside or around the electric field to undergo an electrochemical reaction to produce ozone. The ozone generator 74 of the high-voltage discharge type can be divided into three types according to the high-voltage electrical 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 tubes, ceramic plates, ceramic tubes, glass tubes, and enamel tubes. It is possible to generate ozone through the ozone generator 74 and send it into the ozone inlet 703 of the ammonia-free catalyst device 70 via the ozone delivery pipeline 72. Additionally, the inlet 701 of the ammonia-free catalyst device 70 is connected to the other end of the treatment output pipeline 41. 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 via the treatment output pipeline 41, enabling at least a part of the treated tail gas after mixing to undergo a denitrification reaction with the ozone. That is, the ozone and the catalyst 73 are used to oxidize at least one nitrogen oxide (NOx) contained in at least a part of the treated tail 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 undergoes the denitrification reaction, the denitrification reaction gas is output via the outlet 702 of the ammonia-free catalyst device 70, that is, nitrogen (N 2 ). 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 10. In this way, the ammonia-free catalyst device 70 transports the reacted nitrogen (N 2 ) to the chimney 10 via the ammonia-free catalyst output pipeline 71 for emission, thereby improving the efficiency of removing nitrogen oxides (NOx) and achieving the effect of improving the emission of nitrogen oxides (NOx).

[0054] Another embodiment of the present invention is that a dust collector 90 is installed in the treatment output pipeline 41 (as Figure 2 and Figure 4As shown, the dust collector 90 is mainly located on the processing output pipeline 41 connected to the outlet 402 of the processing device 41, and is also at the front end where one end of the chimney conveying pipeline 50 is connected to the processing output pipeline 41. The dust collector 90 is provided with an inlet 901 and an outlet 902. When the processed exhaust gas output after the combustion of the processing device 40 contains particulate matter, which can also be called suspended particles (Particulate Matter), where 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 processed exhaust gas in the processing output pipeline 41 contains at least one particulate matter, at least a part of the processed exhaust gas in the processing output pipeline 41 enters the dust collector 90 through the inlet 901 of the dust collector 90 to collect the at least one particulate matter through the dust collector 90, so that at least a part of the processed exhaust gas in the processing output pipeline 41 can first collect the particulate matter to reduce the discharge of the particulate matter, and then be output from the outlet 902 of the dust collector 90 to the processing output pipeline 41, so as to achieve the effect of dust removal. Furthermore, when using the dust collector 90 to collect the particulate matter, the flow direction of at least a part of the processed exhaust gas in the processing output pipeline 41 can be controlled by at least one control valve 80 provided in any one of the chimney conveying pipeline 50 and the processing output pipeline 41 (such as Figure 2 and Figure 4 As shown, mainly most of the processed exhaust gas in at least a part of the processing output pipeline 41 flows to the chimney conveying pipeline 50 and is discharged through the chimney 10, and a small part of the processed exhaust gas in at least a part of the processing output pipeline 41 is first mixed with at least a part of the 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 volatile organic exhaust gas treatment can be improved, and the effect of reducing pollutant emissions can be achieved.

[0055] Furthermore, when the processing device 40 is a direct-fired incinerator (TO), the direct-fired incinerator (TO) is provided with an air duct 42, a burner head 43 and a surrounding shield 44. The air duct 42 is arranged inside the direct-fired incinerator (TO) (such as Figure 3 and Figure 4As shown, the burner head 43 is combined with the direct-fired incinerator (TO). The air duct 42 is connected to the inlet 401 of the direct-fired incinerator (TO). Additionally, the burner head 43 is provided with a channel 431, and the burner head 43 is provided with a burner head shield 432, a gaseous fuel pipe 433, and a combustion-supporting gas inlet 434. Among them, the combustion-supporting gas inlet 434 can be provided at one end or the side of the channel 431, and the combustion-supporting gas inlet 434 allows a combustion-supporting gas (not shown in the figure) to enter. Among them, the combustion-supporting gas is any one of air and oxygen. One end of the channel 431 can be provided with a fan (not shown in the figure) to increase the flow rate of the combustion-supporting gas and enable the combustion-supporting gas to enter the channel 431 of the burner head 43.

[0056] Additionally, the gaseous fuel pipe 433 has a gaseous fuel inlet 4331, at least one first-stage gas port 4332, and at least one second-stage gas port 4333. At least one first-stage gas port 4332 of the gaseous fuel pipe 433 is located within the channel 431 of the burner head 43, and the burner head shield 44 is located at the second-stage gas port 4333 of the gaseous fuel pipe 433 (as Figure 3 and Figure 4 shown). And the gaseous fuel inlet 4331 allows a gaseous fuel (not shown in the figure) to enter. Among them, the gaseous fuel is any one of natural gas and gas. The gaseous fuel is ejected from the first-stage gas port 4332 into the channel 431 of the burner head 43. Additionally, the gaseous fuel is ejected from the second-stage gas port 4333, and a combustion flame 435 is generated. Furthermore, the burner head shield 44 is provided with a mounting panel (not shown in the figure) and is installed on the direct-fired incinerator (TO) through the mounting panel, so that a part of the burner head 43 is exposed outside the direct-fired incinerator (TO). The gaseous fuel inlet 4331 of the gaseous fuel pipe 433 is provided outside the direct-fired incinerator (TO) to facilitate the entry of the gaseous fuel through the gaseous fuel inlet 4331. Additionally, the combustion-supporting gas inlet 434 is also provided outside the direct-fired incinerator (TO) to facilitate the entry of the combustion-supporting gas through the combustion-supporting gas inlet 434.

[0057] Additionally, at least one heat-insulating cotton 423 is provided between the air duct 42 and the direct-fired incinerator (TO) to form a barrier protection. The air duct 42 is made of a metal material, and the air duct 42 is connected to the inlet 401 of the direct-fired incinerator (TO) so that the desorption and concentration gas (such as a mixture containing one or more volatile organic compounds and air) can enter the air duct 42. The air duct 42 is provided with an air outlet 421. Additionally, a location of the air duct 42 is provided for installing the burner head shield 432 of the burner head 43 (as Figure 3 and Figure 4As shown in the figure, the burner shield 432 corresponds to the air outlet 421. Furthermore, the surrounding shield 44 is disposed inside the direct combustion incinerator (TO). The surrounding shield 44 is made of a metal material. The surrounding shield 44 is in the shape of any one of a cone, a conical body, a horn-shaped body, a square body, and a circular body, so as to be designed and implemented according to the actual situation. One end of the surrounding shield 44 is combined with the burner shield 432, and the other end of the surrounding shield 432 passes out of the air outlet 421 of the air duct 42. The air outlet 421 of the air duct 42 is larger than the surrounding shield 44, so that an air duct 422 is left between the air outlet 421 of the air duct 42 and the surrounding shield 44. When the gaseous fuel is ejected from the second-stage gas port 4333 and generates the combustion flame 435, the combustion flame 435 passes through the burner shield 432 of the burner 43 through the surrounding shield 44, and the combustion flame 435 can be prevented from being affected by the desorbed and concentrated gas (such as a mixture containing one or more volatile organic compounds and air) entering through the surrounding shield 44, so that the combustion flame 435 can be aggregated into a beam shape and has a concentrated effect.

[0058] The above-mentioned air duct 42 can directly transport the desorbed and concentrated gas to the air outlet 421, and the gas flows out through the air duct 422 left between the air outlet 421 and the surrounding shield 44 to the front end of the combustion flame 435 generated by the burner 43. Then, the combustion-supporting gas entering from the combustion-supporting gas inlet 434 of the burner 43 is lifted by more than 20% to 30% of the combustion equivalence ratio. When the combustion-supporting gas can enter the passage 431 of the burner 43, the combustion-supporting gas can be pre-mixed with a part of the gaseous fuel ejected from the first-stage gas port 4332 of the gaseous fuel pipe 433 in the passage 431 of the burner 43 first. The combustion-supporting gas mixed with a part of the gaseous fuel then flows to the second-stage gas port 4333 of the gaseous fuel pipe 433 and is re-mixed with the gaseous fuel ejected from the second-stage gas port 4333. Thus, through the two-stage injection of the gaseous fuel, the pre-mixing sequence and distribution of the generated combustion flame 435 can be more uniform, and the excess combustion-supporting gas can reduce the temperature of the combustion flame 435 generated by the burner 43, so that the desorbed and concentrated gas can reduce the generation of nitrogen oxides after passing through the generated combustion flame 435, and has the effect of reducing the generation of nitrogen oxides.

[0059] In addition, the denitration method for treating volatile organic exhaust gas of the present invention is mainly used for a volatile organic exhaust gas treatment and denitration system, and is provided with a combination design of a chimney 10, a heating device 20, an adsorption rotor 30, a treatment device 40, a chimney conveying pipeline 50, a clean gas discharge bypass pipeline 60, and a non-ammonia catalyst device 70 (as Figures 1 to 4 shown).

[0060] The main steps of the denitration method (asFigure 5 As shown in the figure, it includes: Step S100, input organic exhaust adsorption: An exhaust gas containing volatile organic compounds is sent into one side of the adsorption zone 301 of the adsorption wheel 30 through the intake pipeline 31. After being adsorbed by the adsorption zone 301, an adsorbed gas is output from the other side of the adsorption zone 301 of the adsorption wheel 30 to the clean gas discharge pipeline 32, and is transported to the chimney 10 through the clean gas discharge pipeline 32. After completing the above step S100, the next step S110 is carried out.

[0061] Among them, in the above step S100, the adsorption wheel 30 is a zeolite concentration wheel or a concentration wheel made of other materials. The adsorption wheel 30 is provided with an adsorption zone 301 and a desorption zone 302. The adsorption wheel 30 is provided with an intake pipeline 31, a clean gas discharge pipeline 32, a hot gas delivery pipeline 33 and a desorption concentrated gas pipeline 34. One end of the intake pipeline 31 is connected to one side of the adsorption zone 301 of the adsorption wheel 30, and the other end of the intake pipeline 31 is connected to relevant workplaces such as manufacturing sites and R & D sites in the semiconductor industry, optoelectronic industry or chemical related industries (not shown in the figure), or exhaust gas sites generating volatile organic compounds (VOCs). To send an exhaust gas containing volatile organic compounds (VOCs) into one side of the adsorption zone 301 of the adsorption wheel 30 through the intake pipeline 31, and the adsorption zone 301 adsorbs the volatile organic compounds (VOCs) to generate an adsorbed gas. In addition, one end of the clean gas discharge pipeline 32 is connected to the other side of the adsorption zone 301 of the adsorption wheel 30, and the other end of the clean gas discharge pipeline 32 is connected to the chimney 10 to transport the adsorbed gas to the chimney 10 for discharge through the clean gas discharge pipeline 32. In addition, the clean gas discharge pipeline 32 is provided with a fan 321 (as Figure 2 shown) to increase the flow rate of the adsorbed gas in the clean gas discharge pipeline 32 to flow towards the chimney 10.

[0062] In addition, the next step S110 outputs the desorption concentrated gas: The other side of the desorption zone 302 of the adsorption wheel 30 transports at least a part of the hot gas of the heating device 20 through the hot gas delivery pipeline 33 to desorb the volatile organic compounds adsorbed by the adsorption wheel 30, and then a desorption concentrated gas is output from one side of the desorption zone 302 of the adsorption wheel 30 to the desorption concentrated gas pipeline 34. After completing the above step S110, the next step S120 is carried out.

[0063] Among them, in the above step S110, the heating device 20 outputs at least a part of the hot gas (such as Figure 1 and Figure 2As shown in the figure, the heating device 20 can be any one of a heater, a pipeline heater, and a heat exchanger 21. The heater 20 can be any one of an electric heating wire, an electric heating tube, or an electric heating sheet (not shown in the figure). The pipeline heater can use either gaseous fuel or liquid fuel. One end of the hot gas delivery pipeline 33 is connected to the other side of the desorption zone 302 of the adsorption wheel 30, and the other end of the hot gas delivery pipeline 33 is connected to the heating device 20. At least a part of the hot gas from the heating device 20 is transmitted through the hot gas delivery pipeline 33 to the other side of the desorption zone 302 of the adsorption wheel 30 to desorb the volatile organic compounds (VOCs) adsorbed by the adsorption wheel 30.

[0064] Furthermore, one side of the desorption zone 302 of the adsorption wheel 30 is connected to one end of the desorption and concentration gas pipeline 34, and a desorption and concentration gas is output from one side of the desorption zone 302 of the adsorption wheel 30 to the desorption and concentration gas pipeline 34. A fan 341 is provided in the desorption and concentration gas pipeline 34 (as Figure 2 shown) to increase the flow rate of the desorption and concentration gas in the desorption and concentration gas pipeline 34.

[0065] In addition, in the next step S120, the tail gas output treatment is carried out: the desorption and concentration gas is transmitted through the desorption and concentration gas pipeline 34 to the inlet 401 of the treatment device 40, and the desorption and concentration gas is processed by the treatment device 40 to generate a tail gas containing at least one nitrogen oxide (NOx), and then the tail gas is output from the outlet 402 of the treatment device 40 to the treatment output pipeline 41. After completing the above step S120, the next step S130 is carried out.

[0066] In the above step S120, the treatment device 40 is provided with an inlet 401, an outlet 402, and a treatment output pipeline 41, and the treatment device 40 is provided with at least one combustion chamber 403 (as Figure 1 and Figure 2 shown). The treatment device 40 can be any one of a direct combustion incinerator (TO), a catalytic incinerator, or a regenerative thermal oxidizer (RTO). When the treatment device 40 is a direct combustion incinerator (TO), at least two heat exchangers 21 or more than two heat exchangers 21 can be further provided in the direct combustion incinerator (TO) (as Figure 3 and Figure 4 shown), and the at least two heat exchangers 21 or more than two heat exchangers 21 can be used as the heating device 20, and at least a part of the hot gas is output from the at least two heat exchangers 21 or more than two heat exchangers 21 in the direct combustion incinerator (TO) for use in the desorption zone 302 of the adsorption wheel 30.

[0067] One end of the processing output pipeline 41 is connected to the outlet 402 of the processing device 40, and the inlet 401 of the processing device 40 is connected to the other end of the desorption concentrated gas pipeline 34, so that the desorption concentrated gas output from one side of the desorption zone 302 of the adsorption wheel 30 can be transmitted to the inlet 401 of the processing device 40 through the desorption concentrated gas pipeline 34, and then the desorption concentrated gas is subjected to high-temperature cracking treatment through the combustion chamber 403 of the processing device 40. After the high-temperature cracking treatment, a processing tail gas is generated, and the processing tail gas contains at least one nitrogen oxide (NOx), and the processing tail gas is output from the outlet 402 of the processing device 40 to the processing output pipeline 41. In addition, a fan 341 is provided in the desorption concentrated gas pipeline 34 (as Figure 2 and Figure 4 shown), so as to push and pull the desorption concentrated gas into the inlet 401 of the processing device 40.

[0068] Furthermore, in addition to the adsorption zone 301 and the desorption zone 302, the adsorption wheel 30 can also be provided with a cooling zone 303 (as Figures 2 to 4 shown). A cooling gas inlet pipeline 35 and a cooling gas delivery pipeline 36 are provided in the cooling zone 303 of the adsorption wheel 30. One end of the cooling gas inlet pipeline 35 is connected to one side of the cooling zone 303 of the adsorption wheel 30, and one end of the cooling gas delivery pipeline 36 is connected to the other side of the cooling zone 303 of the adsorption wheel 30, and the other end of the cooling gas delivery pipeline 36 is connected to the heating device 20 (as Figure 2 shown). When the heating device 20 is a heat exchanger 21, a cooling gas output from the cooling zone 303 of the adsorption wheel 30 is delivered into the heat exchanger 21 for heat exchange (as Figure 3 and Figure 4 shown). There are two implementation manners for the cooling zone 303 of the adsorption wheel 30. The first implementation manner is that the other end of the cooling gas inlet pipeline 35 connected to one side of the cooling zone 303 of the adsorption wheel 30 is for fresh air or outside air to enter (as Figure 3 shown), and the fresh air or outside air is used to provide cooling for the cooling zone 303 of the adsorption wheel 30. In the second implementation manner, an intake bypass pipeline 37 is provided in the intake pipeline 31. One end of the intake bypass pipeline 37 is connected to the intake pipeline 31 (as Figure 2 and Figure 4 shown), and the other end of the intake bypass pipeline 37 is connected to the other end of the cooling gas inlet pipeline 35, so that at least a part of the exhaust gas containing volatile organic compounds in the intake pipeline 31 can be shunted and delivered into the cooling zone 303 of the adsorption wheel 30 for cooling use. In addition, an intake bypass control valve 371 is provided in the intake bypass pipeline 37 (as Figure 2 andFigure 4 as shown in the figure, to control the air volume of at least a part of the exhaust gas containing volatile organic compounds transported to the intake bypass pipeline 71.

[0069] In addition, in the next step S130, the control valve controls the flow direction: at least one control valve 80 is provided in either the chimney transport pipeline 50 or the treatment output pipeline 41 to control the flow direction of at least a part of the treated tail gas in the treatment output pipeline 41. After completing the above step S130, the next step S140 is carried out.

[0070] In the above step S130, one end of the chimney transport pipeline 50 is connected to the treatment output pipeline 41, and the other end of the chimney transport pipeline 50 is connected to the chimney 10, and at least one control valve 80 is provided in either the chimney transport pipeline 50 or the treatment output pipeline 41 (as Figure 1 and Figure 3 shown in the figure) to control the flow direction of at least a part of the treated tail gas in the treatment output pipeline 41. The control valve 80 can be any one of a two-way valve, a three-way valve, and an electric valve, mainly implemented in accordance with the design of the pipeline. When the at least one control valve 80 is provided in the chimney transport pipeline 50, 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 transported to the chimney 10 in the treatment output pipeline 41. When the at least one control valve 80 is provided in the treatment output pipeline 41, 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 transported to the ammonia-free catalyst device 70 in the treatment output pipeline 41. In addition, when one control valve 80 is respectively provided on the treatment output pipeline 41 and the chimney transport pipeline 50, the treatment output control valve 802 is provided on the treatment output pipeline 41 (as Figure 2 and Figure 4 shown in the figure) to control the air volume of at least a part of the treated tail gas transported to the ammonia-free catalyst device 70 in the treatment output pipeline 41, and the chimney control valve 801 is provided on the chimney transport pipeline 50 (as Figure 2 and Figure 4 shown in the figure) to control the air volume of at least a part of the treated tail gas transported to the chimney 10 in the treatment output pipeline 41.

[0071] In addition, in the next step S140, the purified gas bypass transport and mixing: at least a part of the adsorbed gas in the purified gas discharge pipeline 32 is transported to the treatment output pipeline 41 through the purified gas discharge bypass pipeline 60, so that at least a part of the adsorbed gas can be mixed with at least a part of the treated tail gas in the treatment output pipeline 41 to reduce the temperature of at least a part of the treated tail gas in the treatment output pipeline 41. After completing the above step S140, the next step S150 is carried out.

[0072] In the above step S140, one end of the clean gas discharge bypass pipeline 60 is connected to the clean gas discharge pipeline 32, and the other end of the clean gas discharge bypass pipeline 60 is connected to the treatment output pipeline 41. At least a part of the adsorbed gas in the clean gas discharge pipeline 32 is transported through the clean gas discharge bypass pipeline 60 into the treatment output pipeline 41 (as Figures 1 to 4 shown), so that at least a part of the adsorbed gas can be mixed with at least a part of the treated tail gas in the treatment output pipeline 41 to reduce the temperature of at least a part of the treated tail gas in the treatment output pipeline 41. 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 adsorbed gas transported to the treatment output pipeline 41. 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 adsorbed gas in the clean gas discharge pipeline 32 through the clean gas discharge bypass pipeline 60 is that the operating temperature of the ammonia-free catalyst device 70 needs to be lower than 200 °C. The treated tail gas generated after the high-temperature cracking treatment by the treatment device 40 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 adsorbed gas in the clean gas discharge pipeline 32 for mixing and cooling to reach a temperature that can enter the ammonia-free catalyst device 70 (such as lower than 200 °C), so as to achieve the effect of protecting the ammonia-free catalyst device 70.

[0073] In addition, in the next step S150, ammonia-free catalyst device denitrification: 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 41, 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 denitrification reaction gas is generated, and then is output through the ammonia-free catalyst output pipeline 71 to the chimney 10 for discharge.

[0074] In the above step S150, 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 4As shown in the figure), 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 generates ozone by any one of the high-voltage discharge method, ultraviolet irradiation method, and electrolysis method. Among them, the high-voltage discharge method (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 produce ozone. The ozone generator 74 of the high-voltage discharge method 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 tubes, ceramic plates, ceramic tubes, glass tubes, and enamel tubes. It is possible to generate ozone through the ozone generator 74 and send it into the ozone inlet 703 of the ammonia-free catalyst device 70 via the ozone delivery 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 41. The ammonia-free catalyst device 70 is provided with at least one catalyst 73 (as Figures 1 to 4 shown in the figure), 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 via the treatment output pipeline 41, enabling at least a part of the treated tail gas after mixing to undergo a denitrification reaction with the ozone. That is, the ozone and the catalyst 73 are used to oxidize at least one nitrogen oxide (NOx) contained in at least a part of the treated tail 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 undergoes the denitrification reaction, the denitrification reaction gas is output via the outlet 702 of the ammonia-free catalyst device 70, that is, nitrogen (N 2 ). 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 10. In this way, the nitrogen (N 2 ) after the reaction is transported to the chimney 10 via the ammonia-free catalyst output pipeline 71 by the ammonia-free catalyst device 70 for emission, thereby improving the efficiency of removing nitrogen oxides (NOx) and achieving the effect of improving the emission of nitrogen oxides (NOx).

[0075] In another embodiment of the present invention, a dust collector 90 is installed in the treatment output pipeline 41 (as Figure 2 and Figure 4As shown, the dust collector 90 is mainly located on the processing output pipeline 41 connected to the outlet 402 of the processing device 41, and is also at the front end where one end of the chimney conveying pipeline 50 is connected to the processing output pipeline 41. The dust collector 90 is provided with an inlet 901 and an outlet 902. When the processing exhaust gas output after the combustion of the processing device 40 contains particulate matter, which can also be called suspended particulate matter (Particulate Matter), where 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 processing exhaust gas in the processing output pipeline 41 contains at least one particulate matter, at least a part of the processing exhaust gas in the processing output pipeline 41 enters the dust collector 90 through the inlet 901 of the dust collector 90 to collect the at least one particulate matter through the dust collector 90, so that at least a part of the processing exhaust gas in the processing output pipeline 41 can first collect the particulate matter to reduce the discharge of the particulate matter, and then is output from the outlet 902 of the dust collector 90 to the processing output pipeline 41, so as to achieve the effect of dust removal. Furthermore, when using the dust collector 90 to collect the particulate matter, the flow direction of at least a part of the processing exhaust gas in the processing output pipeline 41 can be controlled by at least one control valve 80 provided in either the chimney conveying pipeline 50 or the processing output pipeline 41 (such as Figure 2 and Figure 4 As shown, mainly to make most of at least a part of the processing exhaust gas in the processing output pipeline 41 flow to the chimney conveying pipeline 50 and be discharged through the chimney 10, and to make a small part of at least a part of the processing exhaust gas in the processing output pipeline 41 first mix with at least a part of the adsorbed gas conveyed through the clean gas discharge bypass pipeline 60, and then flow 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 pollutant emissions can be achieved.

[0076] Furthermore, when the processing device 40 is a direct-fired incinerator (TO), the direct-fired incinerator (TO) is provided with an air duct 42, a burner head 43 and an enclosure shield 44. The air duct 42 is arranged inside the direct-fired incinerator (TO) (such as Figure 3 and Figure 4As shown, the burner head 43 is combined with the direct-fired incinerator (TO). The air duct 42 is connected to the inlet 401 of the direct-fired incinerator (TO). Additionally, the burner head 43 is provided with a channel 431, and the burner head 43 is provided with a burner head shield 432, a gaseous fuel pipe 433, and a combustion-supporting gas inlet 434. Among them, the combustion-supporting gas inlet 434 can be provided at one end or the side of the channel 431, and the combustion-supporting gas inlet 434 is for a combustion-supporting gas (not shown in the figure) to enter. Among them, the combustion-supporting gas is any one of air and oxygen. One end of the channel 431 can be provided with a fan (not shown in the figure) to increase the flow rate of the combustion-supporting gas and enable the combustion-supporting gas to enter the channel 431 of the burner head 43.

[0077] Additionally, the gaseous fuel pipe 433 has a gaseous fuel inlet 4331, at least one first-stage gas port 4332, and at least one second-stage gas port 4333. At least one first-stage gas port 4332 of the gaseous fuel pipe 433 is located in the channel 431 of the burner head 43, and the burner head shield 44 is located at the second-stage gas port 4333 of the gaseous fuel pipe 433 (as Figure 3 and Figure 4 shown). And the gaseous fuel inlet 4331 is for a gaseous fuel (not shown in the figure) to enter. Among them, the gaseous fuel is any one of natural gas and gas. The gaseous fuel is ejected from the first-stage gas port 4332 into the channel 431 of the burner head 43. Additionally, the gaseous fuel is ejected from the second-stage gas port 4333 and generates a combustion flame 435. Furthermore, the burner head shield 44 is provided with a mounting panel (not shown in the figure) and is installed on the direct-fired incinerator (TO) through the mounting panel, so that a part of the burner head 43 is exposed outside the direct-fired incinerator (TO). The gaseous fuel inlet 4331 of the gaseous fuel pipe 433 is provided outside the direct-fired incinerator (TO) to facilitate the entry of the gaseous fuel through the gaseous fuel inlet 4331. Additionally, the combustion-supporting gas inlet 434 is also provided outside the direct-fired incinerator (TO) to facilitate the entry of the combustion-supporting gas through the combustion-supporting gas inlet 434.

[0078] Additionally, at least one heat-insulating cotton 423 is provided between the air duct 42 and the direct-fired incinerator (TO) to form a barrier protection. The air duct 42 is made of a metal material, and the air duct 42 is connected to the inlet 401 of the direct-fired incinerator (TO) so that the desorption and concentration gas (such as a mixture containing more than one volatile organic compound and air) can enter the air duct 42. The air duct 42 is provided with an air outlet 421. Additionally, a place of the air duct 42 is for installing the burner head shield 432 of the burner head 43 (as Figure 3 and Figure 4As shown, the burner shield 432 corresponds to the air outlet 421. Furthermore, the surrounding shield 44 is disposed inside the direct-fired incinerator (TO). The surrounding shield 44 is made of a metal material. The surrounding shield 44 is in the shape of any one of a cone, a conical frustum, a trumpet, a cube, or a cylinder, so as to be designed and implemented according to the current situation. One end of the surrounding shield 44 is coupled to the burner shield 432, and the other end of the surrounding shield 432 passes through the air outlet 421 of the air duct 42. The air outlet 421 of the air duct 42 is larger than the surrounding shield 44, so that an air duct 422 is left between the air outlet 421 of the air duct 42 and the surrounding shield 44. When the gaseous fuel is ejected from the second-stage gas port 4333 and generates the combustion flame 435, the combustion flame 435 passes through the burner shield 432 of the burner 43 through the surrounding shield 44, and the surrounding shield 44 enables the combustion flame 435 to avoid being affected by the desorbed and concentrated gas (such as a mixture containing more than one volatile organic compound and air) entering, so that the combustion flame 435 can be aggregated into a bundle shape and has a concentrated effect.

[0079] The above-mentioned air duct 42 can directly convey the desorbed and concentrated gas to the air outlet 421, and the gas flows out through the air duct 422 left between the air outlet 421 and the surrounding shield 44 to the front end of the combustion flame 435 generated by the burner 43. Then, the combustion-supporting gas entering through the combustion-supporting gas inlet 434 of the burner 43 is increased by more than 20% to 30% of the combustion equivalence ratio. When the combustion-supporting gas enters the passage 431 of the burner 43, the combustion-supporting gas can be premixed with some of the gaseous fuel ejected from the first-stage gas port 4332 of the gaseous fuel pipe 433 in the passage 431 of the burner 43 first. The combustion-supporting gas mixed with some of the gaseous fuel then flows to the second-stage gas port 4333 of the gaseous fuel pipe 433 and is remixed with the gaseous fuel ejected from the second-stage gas port 4333. Thus, by injecting the gaseous fuel in two stages, the premixing sequence and distribution of the combustion flame 435 can be made more uniform, and the excess combustion-supporting gas can reduce the temperature of the combustion flame 435 generated by the burner 43, so that the desorbed and concentrated gas can reduce the generation of nitrogen oxides after passing through the generated combustion flame 435, and has the effect of reducing the generation of nitrogen oxides.

[0080] In the above-described specific embodiments, the object, technical solution, and beneficial effects of the present invention have been further described in detail. It should be understood that the above are only specific embodiments of the present invention and are not used 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. A volatile organic exhaust gas treatment and denitrification system, characterized in that: include: a chimney; a heating device that outputs at least a portion of the hot gas; An adsorption rotor, the adsorption rotor is provided with an adsorption zone and a desorption zone, the adsorption rotor is provided with an air intake pipeline, a clean gas discharge pipeline, a hot gas transmission pipeline and a desorption concentrated gas pipeline, an exhaust gas containing volatile organic compounds is sent into one side of the adsorption zone of the adsorption rotor through the air intake pipeline, and after being adsorbed by the adsorption zone, an adsorbed gas is output from the other side of the adsorption zone of the adsorption rotor to the clean gas discharge pipeline, and is transported to the chimney through the clean gas discharge pipeline, the other side of the desorption zone of the adsorption rotor transmits at least a part of the hot gas of the heating device through the hot gas transmission pipeline to desorb the volatile organic compounds adsorbed by the adsorption rotor, and a desorbed concentrated gas is output from one side of the desorption zone of the adsorption rotor to the desorption concentrated gas pipeline; A treatment device, the treatment device 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 treatment device, the desorbed concentrated gas is transmitted to the inlet of the treatment device through the desorbed concentrated gas pipeline, so that the desorbed concentrated gas is treated by the treatment device to generate a treated tail gas, the treated tail gas contains at least one nitrogen oxide (NOx), and then the treated tail gas is output from the outlet of the treatment device to the treatment output pipeline; 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 clean gas discharge pipeline, and the other end of which is connected to the treatment output pipeline, and at least a portion of the adsorbed gas in the 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 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 volatile organic gas exhaust treatment and denitration system 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 volatile organic gas exhaust treatment and denitrification system 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 volatile organic gas exhaust treatment and denitration system 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 volatile organic gas exhaust treatment and denitration system 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 volatile organic gas exhaust treatment and denitration system 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 volatile organic gas exhaust treatment and denitration system 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 adsorbed gas delivered to the treatment output pipeline.

8. The volatile organic gas exhaust treatment and denitration system according to claim 1, characterized in that: The heating device is further any one of a heater, a pipe heater, and a heat exchanger.

9. The volatile organic gas exhaust treatment and denitration system according to claim 1, characterized in that: The clean air discharge pipeline is further provided with a fan.

10. The volatile organic gas exhaust treatment and denitration system according to claim 1, characterized in that: The desorbed concentrated gas pipeline is further provided with a fan.

11. The volatile organic gas exhaust treatment and denitration system according to claim 1, characterized in that: The clean gas discharge bypass pipeline is further provided with a fan.

12. The volatile organic gas exhaust treatment and denitration system according to claim 1, characterized in that: The treatment equipment is further any one of a direct-fired incinerator (TO), a catalytic incinerator or a regenerative thermal incinerator (RTO).

13. The volatile organic gas exhaust treatment and denitration system according to claim 12, characterized in that: When the treatment equipment is a direct-fired incinerator (TO), at least two heat exchangers are further provided in the direct-fired incinerator (TO).

14. The volatile organic gas exhaust treatment and denitration system according to claim 12, characterized in that: When the processing equipment is a direct-fired incinerator (TO), it 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 channel, 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.

15. The volatile organic gas exhaust treatment and denitrification system according to claim 1, characterized in that: The adsorption wheel is further provided with a cooling zone, and the cooling zone of the adsorption wheel is provided with a cooling air inlet pipeline and a cooling air delivery pipeline, one end of the cooling air inlet pipeline is connected to one side of the cooling zone of the adsorption wheel, one end of the cooling air delivery pipeline is connected to the other side of the cooling zone of the adsorption wheel, and the other end of the cooling air delivery pipeline is connected to the heating device.

16. The volatile organic gas exhaust treatment and denitration system according to claim 15, characterized in that: The other end of the cooling air intake pipeline is further connected to an intake bypass pipeline, one end of the intake bypass pipeline is connected to the intake pipeline, and the other end of the intake bypass pipeline is connected to the cooling air intake pipeline.

17. The volatile organic gas exhaust treatment and denitration system according to claim 16, characterized in that: The air intake bypass pipeline is further provided with an air intake bypass control valve to control the air volume of the exhaust gas containing volatile organic compounds delivered to the air intake bypass pipeline.

18. The volatile organic gas exhaust treatment and denitration system according to claim 15, characterized in that: The other end of the cooling air intake pipeline is further used for the entry of either external air or fresh air.

19. A method for treating and denitrifying volatile organic exhaust gas, characterized in that: It is mainly used for volatile organic exhaust gas treatment and denitrification system, and is provided with a chimney, a heating device, an adsorption wheel, a treatment equipment, a chimney conveying pipeline, a clean gas emission bypass pipeline and an ammonia-free catalyst device. The heating device outputs at least a part of the hot gas. The adsorption wheel is provided with an adsorption area and a desorption area. The adsorption wheel is provided with an air intake pipeline, a clean gas emission pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline. The treatment equipment 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 treatment equipment, and one end of the chimney conveying pipeline is connected to the treatment output pipeline. The chimney conveying pipeline is provided with a heat treatment pipeline, a heat treatment pipeline and a desorption concentrated gas pipeline. The other end of the pipeline is connected to the chimney, one end of the clean gas emission bypass pipeline is connected to the clean gas emission pipeline, the other end of the 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 treatment denitration method include: Input organic exhaust gas adsorption: an exhaust gas containing volatile organic compounds is sent into one side of the adsorption zone of the adsorption wheel through the air inlet pipeline, and after being adsorbed by the adsorption zone, an adsorbed gas is output from the other side of the adsorption zone of the adsorption wheel to the clean gas discharge pipeline, and then transported to the chimney through the clean gas discharge pipeline; Outputting desorbed concentrated gas: the other side of the desorption zone of the adsorption wheel transmits at least a portion of the hot gas of the heating device through the hot gas transmission pipeline to desorb the volatile organic compounds adsorbed by the adsorption wheel, and then outputs a desorbed concentrated gas from one side of the desorption zone of the adsorption wheel to the desorbed concentrated gas pipeline; Treating tail gas output treatment: the desorbed concentrated gas is transmitted to the inlet of the treatment equipment through the desorbed concentrated gas pipeline, so that the desorbed concentrated gas is treated by the treatment equipment to produce a treated tail gas, the treated tail gas contains at least one nitrogen oxide (NOx), and then the treated tail gas is output from the outlet of the treatment equipment to the treatment output 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 adsorbed gas in the 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 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 and denitrifying volatile organic exhaust gas 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 and denitrifying volatile organic exhaust gas 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 and denitrifying volatile organic exhaust gas 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 and denitrifying volatile organic exhaust gas 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 and denitrifying volatile organic exhaust gas 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 and denitrifying volatile organic exhaust gas 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 adsorbed gas delivered to the treatment output pipeline.

26. The method for treating and denitrifying volatile organic gas according to claim 19, characterized in that: The heating device is further any one of a heater, a pipe heater, and a heat exchanger.

27. The method for treating and denitrifying volatile organic exhaust gas according to claim 19, characterized in that: The clean air discharge pipeline is further provided with a fan.

28. The method for treating and denitrifying volatile organic exhaust gas according to claim 19, characterized in that: The desorbed concentrated gas pipeline is further provided with a fan.

29. The method for treating and denitrifying volatile organic exhaust gas according to claim 19, characterized in that: The clean gas discharge bypass pipeline is further provided with a fan.

30. The method for treating and denitrifying volatile organic gas according to claim 19, characterized in that: The treatment equipment is further any one of a direct-fired incinerator (TO), a catalytic incinerator or a regenerative thermal incinerator (RTO).

31. The method for treating and denitrifying volatile organic gas according to claim 30, characterized in that: When the treatment equipment is a direct-fired incinerator (TO), at least two heat exchangers are further provided in the direct-fired incinerator (TO).

32. The method for treating and denitrifying volatile organic gas according to claim 30, characterized in that: When the processing equipment is a direct-fired incinerator (TO), it 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 channel, 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.

33. The method for treating and denitrifying volatile organic exhaust gas according to claim 19, characterized in that: The adsorption wheel is further provided with a cooling zone, and the cooling zone of the adsorption wheel is provided with a cooling air inlet pipeline and a cooling air delivery pipeline, one end of the cooling air inlet pipeline is connected to one side of the cooling zone of the adsorption wheel, one end of the cooling air delivery pipeline is connected to the other side of the cooling zone of the adsorption wheel, and the other end of the cooling air delivery pipeline is connected to the heating device.

34. The method for treating and denitrifying volatile organic gas according to claim 33, characterized in that: The other end of the cooling air intake pipeline is further connected to an intake bypass pipeline, one end of the intake bypass pipeline is connected to the intake pipeline, and the other end of the intake bypass pipeline is connected to the cooling air intake pipeline.

35. The method for treating and denitrifying volatile organic exhaust gas according to claim 34, characterized in that: The air intake bypass pipeline is further provided with an air intake bypass control valve to control the air volume of the exhaust gas containing volatile organic compounds delivered to the air intake bypass pipeline.

36. The method for treating and denitrifying volatile organic gas according to claim 33, characterized in that: The other end of the cooling air intake pipeline is further used for the entry of either external air or fresh air.

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