Enameled wire tail gas treatment device and method
By setting up a pre-denitrification catalytic layer and a flue gas reheating layer in the enameled wire exhaust gas treatment device and combining it with oxygen-rich ion washing technology, the problems of catalyst blockage and incomplete purification were solved, and stable operation and deep purification effects were achieved.
Patent Information
- Application Number
- CN202510871447.4
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-06-26
- Publication Date
- 2025-10-10
AI Technical Summary
The existing enameled wire exhaust gas purification system has problems such as catalyst blockage and incomplete pollutant purification. In particular, the salts and volatile solvents generated during catalytic combustion are prone to condensation during the cooling process, causing the denitrification catalyst to become blocked. In addition, the concentrations of acidic gases and low-molecular solvents in the exhaust gas are high, and the emissions do not meet the standards.
A pre-denitrification catalytic layer and a flue gas reheating layer are set up in front of the denitrification device, and the waste heat is used to reheat the exhaust gas to prevent the condensation of salt and volatile solvents in the denitrification catalytic layer. After denitrification, a washing device is added to use oxygen-rich ions for deep purification, and alkaline washing liquid is used to wash the acidic gas and low molecular solvents.
It achieves long-term stable operation of the catalyst and deep purification of the tail gas, avoids catalyst blockage, ensures the complete removal of acid gases and low-molecular solvents in the tail gas, and meets environmental emission standards.
Smart Images
Figure CN120754695A_ABST
Abstract
Description
Technical Field
[0001] The present application relates to the field of industrial tail gas treatment, and specifically to an enameled wire tail gas treatment device and method. Background Art
[0002] During the enameled wire production process, the precision and quality requirements for manufacturing are constantly increasing, coating technology is constantly innovating, and at the same time, a large amount of volatile solvents are used. As a result, the coating and drying processes of the enameled wire generate a large amount of VOCs waste gas, and the types are diverse. This VOC waste gas treatment poses a daunting challenge.
[0003] Catalytic combustion technology is primarily used for the initial treatment of enameled wire exhaust gases. This process utilizes organic solvents (such as cresol and xylene) volatilized from the insulating varnish and oxygen from the air, creating a complete oxidation reaction (i.e., combustion) under the action of a catalyst. The catalytic combustion of the solvent exhaust gases can raise their temperature to 600°C. The heat released from the combustion reaction is recovered by a waste heat recovery device and fed back into the enameling machine as a heat source for wire coating and drying. This heats the entire enameling furnace, eliminating the need for energy-intensive electric heating devices for wire preheating, volatilization, and curing. This eliminates the pungent odor caused by solvent volatilization and reduces energy consumption and emissions. Nitrogen oxides primarily originate from the thermal decomposition of nitrogen-containing organic compounds in the insulating varnish and nitrogen oxidation reactions during the combustion process. For example, some insulating varnishes contain nitrogen-containing compounds such as amines and amides. These compounds decompose to produce nitrogen oxides during the high-temperature drying process. Currently, reducing agents (such as ammonia and urea) are primarily used to reduce nitrogen oxides in the exhaust gas to nitrogen and water.
[0004] However, the current enameled wire exhaust purification system has the problems of being unable to operate stably for a long time and incomplete purification of pollutants. Summary of the Invention
[0005] In response to the problems existing in the existing treatment process, this application analyzes the existing enameled wire tail gas purification system and finds that the main reasons for the above problems are: (1) In order to reduce the energy consumption of the enameled wire device, it is usually necessary to reduce the exhaust temperature of the enameled wire tail gas after the waste heat recovery is completed to below 200°C. The salts generated during the catalytic combustion process and the volatile solvents that are not burned are very likely to condense at the inlet of the denitrification catalyst during the cooling process, blocking the catalyst; (2) The concentration of acidic gases and low-molecular organic solvents generated during the catalytic combustion process in the exhaust gas of the enameled wire is relatively high, resulting in a high concentration of VOC in the exhaust gas and the emission of pollutants in the exhaust gas of the enameled wire does not meet the standards.
[0006] Therefore, solving the blockage of the denitrification catalyst of the enameled wire exhaust and carrying out deep purification of the enameled wire exhaust with acidic gases and low molecular weight solvents are the technical difficulties currently faced by the deep purification of the enameled wire exhaust.
[0007] The present application provides an enameled wire tail gas treatment device and method. It has been verified in practice that the device can operate stably for a long period of time and achieve deep purification of acidic gases and organic low-molecular substances in the tail gas.
[0008] On the one hand, the present application sets up two pre-denitrification catalytic layers, two denitrification catalytic layers and one flue gas reheating layer in the denitrification device. The enameled wire exhaust gas (exhaust gas at about 200°C) after the waste heat recovery is first reacted in the flue gas pre-denitrification catalytic layer to remove a small amount of nitrogen oxides. At the same time, a small amount of salt and volatile solvent generated in the catalytic combustion process condense at the inlet of the pre-denitrification catalytic layer. The flue gas after pre-denitrification is reheated in the flue gas reheating layer and the temperature rises by 10~15°C. The exhaust gas temperature rises to 210~220°C, and then enters the denitrification catalytic layer, so that the condensable components are removed in the pre-denitrification catalytic layer, and will not condense and clog again in the denitrification catalytic layer.
[0009] On the other hand, this application adds a scrubbing device after the denitrification device, which has two internal scrubbing layers. A scrubbing pump delivers alkaline scrubbing liquid to the scrubbing tower to scrub the flue gas after denitrification, purifying the acidic gases and low-molecular solvents in the flue gas. An oxygen enrichment generator is also provided and connected to the output pipeline of the scrubbing pump. It uses a plasma process to convert oxygen in the air into a large amount of oxygen-rich ions with strong oxidizing ability, which are delivered to the scrubbing pump delivery pipeline for emulsification. The large amount of oxygen-rich ions enter the scrubbing tower along with the alkaline scrubbing liquid, oxidizing the low-molecular escaped solvents, thereby achieving deep purification of the enameled wire exhaust gas.
[0010] An enameled wire tail gas treatment device comprises a catalytic combustion unit and a waste heat recovery unit, wherein the waste heat recovery unit is used to recover waste heat from the tail gas of the catalytic combustion unit; a denitrification unit and an oxidation washing unit are sequentially arranged downstream of the waste heat recovery unit; The denitration unit comprises: A denitrification tower, the denitrification tower having an air inlet and an exhaust port, the air inlet being connected to the exhaust port of the waste heat recovery unit through a flue, and the tail gas from the waste heat recovery unit flowing from the air inlet to the exhaust port in the denitrification tower; A pre-denitrification catalytic layer, a flue gas reheating layer, and a denitrification catalytic layer are sequentially arranged in the denitrification tower along the exhaust gas flow path. The pre-denitrification catalytic layer is detachably installed and has a thickness smaller than the denitrification catalytic layer. The heat source of the flue gas reheating layer comes from the waste heat recovery unit. The oxidation washing unit comprises: A scrubbing tower, the scrubbing tower having an air inlet and an exhaust port, the air inlet being connected to the exhaust port of the denitrification tower via a flue, and a scrubbing layer being arranged in the scrubbing tower; a washing pump connected to the washing liquid storage tank and the washing layer, and used for delivering alkaline washing liquid to the washing layer; The oxygen-enriched generator has an output end connected to the connection pipeline of the washing pump and the washing layer through a pipeline, and is used to transport oxygen-enriched ions into the alkaline washing liquid.
[0011] Several optional methods are also provided below, but they do not serve as additional limitations on the above-mentioned overall solution. They are merely further supplements or optimizations. Under the premise that there are no technical or logical contradictions, each optional method can be combined separately for the above-mentioned overall solution, and can also be a combination of multiple optional methods.
[0012] The catalytic combustion unit is an existing combustion furnace or RCO (regenerative catalytic incinerator).
[0013] The waste heat recovery unit is an existing thermal oil pipe heat exchanger.
[0014] Optionally, the height of the single-layer pre-denitrification catalytic layer is 10-20 cm.
[0015] Optionally, the pre-denitrification catalytic layer is installed in a drawer style.
[0016] Optionally, the pre-denitration catalytic layer is provided in 1 to 3 layers, and the spacing between adjacent pre-denitration catalytic layers is 30 to 50 cm. Further preferably, the pre-denitration catalytic layer is provided in 2 layers, and the height of a single pre-denitration catalytic layer is 10 to 20 cm.
[0017] Optionally, the pre-denitration catalytic layer is provided with two layers; the height of each layer is 10-20 cm; and the distance between the two pre-denitration catalytic layers is 30-50 cm.
[0018] Optionally, each pre-denitrification catalyst layer is independently configured with a pressure sensor for real-time monitoring of the operating resistance of the corresponding pre-denitrification catalyst layer. When the flue gas operating resistance of a single pre-denitrification catalyst layer increases by more than 30Pa, the corresponding pre-denitrification catalyst layer is replaced.
[0019] Optionally, the catalyst of the pre-denitrification catalytic layer can be an iron-based medium-low temperature catalyst, and an iron-based catalyst with an optimal denitrification temperature window of 180-210° C. is selected, and the denitrification catalyst is prepared into a catalyst layer block of 10-20 cm.
[0020] Optionally, the flue gas reheat layer utilizes a tubular heat exchanger, with high-temperature thermal oil from the waste heat recovery unit flowing through the heat exchange tubes. The flue gas reheat layer utilizes some of the high-temperature thermal oil from the waste heat recovery unit to reheat the pre-denitrified flue gas. The reheated flue gas temperature is raised by 10-15°C by controlling the flow of the thermal oil.
[0021] Optionally, a branch is led out from the high-temperature thermal oil pipeline of the waste heat recovery unit, and an oil pump and a corresponding flow regulating valve are provided on the branch. The high-temperature thermal oil flows through the flue gas reheating layer, exchanges heat with the exhaust gas after pre-denitrification, and then flows into the high-temperature thermal oil pipeline of the waste heat recovery unit to form a reheating circuit.
[0022] Optionally, two denitration catalytic layers are provided, and the height of each layer is 100-120 cm; and the distance between adjacent denitration catalytic layers is 30-60 cm.
[0023] Optionally, the catalyst of the denitration catalytic layer may be a medium-low temperature manganese-based catalyst, and a denitration catalyst having an optimal catalytic denitration temperature of 200-230° C. is selected, and the denitration catalyst is prepared into a catalyst layer block with a thickness of 100-120 cm.
[0024] Optionally, the washing layer adopts a spray mechanism and is provided with 2 to 3 layers.
[0025] The present application also provides a method for treating enameled wire tail gas, which is performed using the enameled wire tail gas treatment device, comprising: After being treated in the catalytic combustion unit and cooled to 195-205°C in the preheat recovery unit, the enameled wire tail gas enters the denitrification tower and flows through the pre-denitrification catalytic layer, the flue gas reheat layer, and the denitrification catalytic layer in sequence. The salts generated during the catalytic combustion and the volatile solvents that are not burned are condensed at the inlet of the pre-denitrification catalytic layer. The flue gas reheat layer uses the recovered waste heat from the waste heat recovery unit to reheat the pre-denitrification tail gas by 10-15°C. After reheating, the tail gas temperature rises to 210-220°C and enters the denitrification catalytic layer. The tail gas after treatment in the denitrification tower enters the oxidation scrubber, where it comes into reverse contact with the alkaline absorption liquid rich in oxygen ions to purify the acidic gases and low-molecular organic solvents in the flue gas. Optionally, the oxygen-rich ion concentration in the alkaline absorption liquid is 50-300 mg / L; the liquid-gas ratio of the single-layer washing layer is 1-3 L / m 3 .
[0026] Optionally, when the flue gas operation resistance of a single-layer pre-denitrification catalytic layer increases by more than 30 Pa, the corresponding pre-denitrification catalytic layer is replaced.
[0027] Compared with the prior art, this application has the following beneficial effects: In solving the problem of catalyst clogging: the temperature of the enameled wire tail gas after being treated by the catalytic combustion unit and completing the waste heat recovery is about 200℃. The salts generated during the catalytic combustion process and the volatile solvents that cannot be burned can easily clog the denitrification catalyst. To solve this problem, on the one hand, the present application adds a pre-denitrification catalytic layer at the front end of the denitrification catalytic layer. The main purpose of the pre-denitrification catalytic layer is to enrich the condensable components in the tail gas, and at the same time it also has a certain pre-removal effect on nitrogen oxides. The pre-denitrification catalytic layer is detachably installed and its thickness is controlled to be significantly smaller than the denitrification catalytic layer. When the flue gas running resistance of the single-layer pre-denitrification catalytic layer increases to a certain extent, the pre-denitrification catalytic layer is directly replaced, and the denitrification catalytic layer will no longer be clogged. On the other hand, the waste heat recovered by the front-end catalytic combustion unit is used to heat the tail gas to 210~220℃ before entering the denitrification catalytic layer. The heated tail gas then enters the denitrification catalytic layer, thereby improving the denitrification efficiency.
[0028] In solving the problem of deep purification of tail gas to meet emission standards: an oxygen-enriched generator is set up and connected to the output pipeline of the washing pump. It uses a plasma process to convert the oxygen in the air into a large number of oxygen-rich ions with strong oxidizing ability, which are sent to the washing pump delivery pipeline and emulsified. A large number of oxygen-rich ions enter the washing tower with the alkaline washing liquid to oxidize the low-molecular escape solvent, thereby achieving deep purification of the enameled wire tail gas. BRIEF DESCRIPTION OF THE DRAWINGS
[0029] Figure 1 This is the processing device and process flow chart of this application. The reference numerals shown in the figures are as follows: 10. Catalytic combustion unit; 20. Waste heat recovery unit; 30. Denitration unit: 31. Denitration tower, 32. Pre-denitration catalytic layer, 33. Flue gas reheating layer, 34. Denitration catalytic layer; 40. Oxidation washing unit: 41. Scrubbing tower, 42. Scrubbing layer, 43. Scrubbing pump, 44. Oxygen enrichment generator; 50. Exhaust gas preheating unit. DETAILED DESCRIPTION
[0030] The following will be combined with the drawings in the embodiments of this application to clearly and completely describe the technical solutions in the embodiments of this application. Obviously, the embodiments described are only part of the embodiments of this application, not all of the embodiments. Based on the embodiments in this application, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of this application.
[0031] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used in the description herein is for describing particular embodiments only and is not intended to be limiting of the application.
[0032] An enameled wire tail gas treatment device, as shown in the figure, comprises a catalytic combustion unit 10, a waste heat recovery unit 20, a denitration unit 30 and an oxidation washing unit 40. The catalytic combustion unit 10 and the waste heat recovery unit 20 are both existing treatment devices, in an embodiment, the catalytic combustion unit adopts RCO, the waste heat recovery unit adopts a heat conduction oil pipe heat exchanger, the waste heat recovery unit 20 is used for recovering the waste heat of the catalytic combustion unit, and the denitration unit 30 and the oxidation washing unit 40 are sequentially arranged downstream of the waste heat recovery unit 20. Figure 1
[0033] The denitration unit 30 comprises a denitration tower 31, the denitration tower 31 has an air inlet and an air outlet, the air inlet of the denitration tower 31 is connected to the air outlet of the waste heat recovery unit 20 through a flue, and the tail gas from the waste heat recovery unit 20 flows in the denitration tower 31 from the air inlet to the air outlet. In some embodiments, the air inlet is arranged at a side wall close to the bottom of the denitration tower, the air outlet is arranged at the top of the denitration tower, a pre-denitration catalytic layer 32, a flue gas reheating layer 33 and a denitration catalytic layer 34 are sequentially arranged in the denitration tower from bottom to top (along the tail gas flow path), the pre-denitration catalytic layer 32 is detachably installed in the denitration tower 31, the thickness of the pre-denitration catalytic layer is smaller than that of the denitration catalytic layer, and the pre-denitration catalytic layer is mainly used for enriching condensable substances in the tail gas, and the flue gas reheating layer 33 is used for heating the tail gas before entering the denitration catalytic layer by using part of the waste heat recovered by the waste heat recovery unit.
[0034] In some embodiments, the pre-denitration catalytic layer 32 is provided with two layers, the thickness of each layer is 10-20 cm, and the spacing between the two layers of the pre-denitration catalytic layer is 30-50 cm, which can meet the pre-treatment requirements and also facilitate replacement.
[0035] The pre-denitration catalytic layer 32 is detachably installed in the denitration tower 31; each pre-denitration catalytic layer 32 is independently provided with a pressure sensor (not shown in the figure) for monitoring the running resistance of the corresponding pre-denitration catalytic layer in real time. When the flue gas running resistance of a single pre-denitration catalytic layer increases by more than 30 Pa, the corresponding pre-denitration catalytic layer is replaced. The catalyst of the pre-denitration catalytic layer adopts an iron-based low-temperature catalyst, the optimal denitration temperature window of which is 180-210℃, and the denitration catalyst is prepared into a 10-20 cm catalyst layer block.
[0036] As a specific implementation method of detachable installation, an opening and a sealing baffle door that adapts to each other are provided on the side wall of the denitrification tower and at a corresponding position above the air inlet. The pre-denitrification catalytic layer can be installed in the denitrification tower in a drawer style to facilitate the replacement of the pre-denitrification catalytic layer.
[0037] In some embodiments, the flue gas reheat layer uses a tubular heat exchanger, and heat transfer oil from the waste heat recovery unit flows through the heat exchange tubes. The flue gas reheat layer uses part of the high-temperature medium of the waste heat recovery unit to reheat the flue gas and raise its temperature. By controlling the flow rate of the heat transfer oil fed into the heat exchanger, the flue gas temperature is raised by 10-15°C. After reheating, the exhaust gas temperature is raised to 210-220°C. A temperature sensor (not shown in the figure) is provided above the flue gas reheat layer.
[0038] Part of the waste heat recovered by the waste heat recovery unit 20 is used to preheat the exhaust gas before it enters the catalytic combustion unit 10, and part is used to reheat the pre-denitrified exhaust gas in the denitrification tower. The front end of the catalytic combustion unit 10 is equipped with an exhaust gas preheating unit 50. This exhaust gas preheating unit 50 also uses a thermal oil tubular heat exchanger, forming a thermal oil circulation loop with the thermal oil tubular heat exchanger of the waste heat recovery unit 20. This thermal oil circulation loop is equipped with an oil pump and a flow valve (not shown). A branch line is drawn from the high-temperature thermal oil pipeline flowing from the waste heat recovery unit 20 to the exhaust gas preheating unit 50. This branch line is equipped with an oil pump and a corresponding flow control valve (not shown). The high-temperature thermal oil flows through the flue gas reheat layer, exchanges heat with the pre-denitrified exhaust gas, and then rejoins the high-temperature thermal oil pipeline of the waste heat recovery unit, forming a reheat loop.
[0039] In some embodiments, the denitration catalytic layer is provided in two layers, each layer having a height of 100 to 120 cm; and the distance between adjacent denitration catalytic layers is 30 to 60 cm.
[0040] The catalyst of the nitrate catalytic layer adopts a medium-low temperature manganese-based catalyst, the optimal catalytic denitrification temperature of which is 200~230℃, and the denitrification catalyst is prepared into a catalyst layer block with a thickness of 100~120cm.
[0041] The method of delivering the reducing agent (ammonia or urea) into the denitrification tower is still carried out according to the current treatment process (not shown in the figure). For example, the reducing agent can be sprayed into the inlet flue of the denitrification tower, mixed with the exhaust gas and then enter the denitrification tower.
[0042] The oxidation scrubbing unit 40 comprises a scrubbing tower 41, a scrubbing pump 43, and an oxygen-enriched generator 44. The scrubbing tower 41 has an air inlet and an exhaust port, the air inlet connected to the exhaust port of the denitrification tower 31 via a flue. Within the scrubbing tower 41 are scrubbing layers 42, which utilize a spraying mechanism and are arranged in two to three layers. The scrubbing pump 43 connects a scrubbing liquid storage tank (not shown) to the scrubbing layers 41, delivering alkaline scrubbing liquid to the scrubbing layers. The output of the oxygen-enriched generator 44 is connected to the connecting pipeline between the scrubbing pump 43 and the scrubbing layers 42 via a pipeline. The oxygen-enriched generator 44 utilizes a plasma process to convert oxygen from the air into a large amount of highly oxidizing nutrient-rich ions, which are then emulsified and transported to the scrubbing pump delivery pipeline. These nutrient-rich ions enter the scrubbing tower along with the alkaline scrubbing liquid, oxidizing low-molecular-weight escaped solvents, thereby achieving deep purification of the enameled wire exhaust. The slurry within the scrubbing tower can be directly discharged via a discharge pump or fed to the scrubbing layers via a circulation pump for circulated spraying.
[0043] The power for the enameled wire exhaust gas to flow between the exhaust preheating unit 50, the catalytic combustion unit 10, the waste heat recovery unit 20, the denitrification unit 30 and the washing unit 40 comes from the fan. The fan can be set according to the current process, or an exhaust fan can be added at the exhaust port of the denitrification tower and the washing tower.
[0044] An implementation method for treating enameled wire tail gas using the above-mentioned enameled wire tail gas treatment device: The temperature of the enameled wire tail gas after being treated by the catalytic combustion unit and cooled by the waste heat recovery unit is about 200℃. After entering the denitrification tower, it first contacts and reacts with the pre-denitrification catalytic layer. The salts generated during the catalytic combustion and the volatile solvents that cannot be burned and other condensable components condense at the inlet of the pre-denitrification catalytic layer. The tail gas after pre-denitrification enters the flue gas reheating layer. The flue gas reheating layer uses the recovered waste heat of the catalytic combustion unit to reheat the tail gas after pre-denitrification and raise its temperature by 10~15℃. The tail gas temperature after reheating rises to 210~220℃ and then enters the denitrification catalytic layer.
[0045] The tail gas after treatment in the denitrification tower enters the scrubber 41 and contacts with the alkaline absorption liquid rich in oxygen ions in reverse order to purify the acidic gas and low molecular organic solvent in the flue gas; the concentration of oxygen ions in the alkaline absorption liquid is 50~300mg / L; the liquid-gas ratio of the single-layer scrubbing layer is 1~3L / m 3 .
[0046] When the flue gas operation resistance of a single-layer pre-denitrification catalytic layer increases by more than 30Pa, the corresponding pre-denitrification catalytic layer should be replaced.
[0047] The above-described embodiments merely represent several implementation methods of the present application. While the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the present invention. It should be noted that a person skilled in the art could make various modifications and improvements without departing from the spirit of the present application, all of which fall within the scope of protection of the present application. Therefore, the scope of protection of the present patent application shall be determined by the appended claims.
Claims
1. An enameled wire tail gas treatment device, comprising a catalytic combustion unit and a waste heat recovery unit, wherein the waste heat recovery unit is used to recover the waste heat of the tail gas of the catalytic combustion unit; characterized in that: A denitration unit and an oxidation washing unit are sequentially arranged downstream of the waste heat recovery unit; The denitration unit comprises: A denitrification tower, the denitrification tower having an air inlet and an exhaust port, the air inlet being connected to the exhaust port of the waste heat recovery unit through a flue, and the tail gas from the waste heat recovery unit flowing from the air inlet to the exhaust port in the denitrification tower; A pre-denitrification catalytic layer, a flue gas reheating layer, and a denitrification catalytic layer are sequentially arranged in the denitrification tower along the exhaust gas flow path. The pre-denitrification catalytic layer is detachably installed and has a thickness smaller than the denitrification catalytic layer. The heat source of the flue gas reheating layer comes from the waste heat recovery unit. The oxidation washing unit comprises: A scrubbing tower, the scrubbing tower having an air inlet and an exhaust port, the air inlet being connected to the exhaust port of the denitrification tower via a flue, and a scrubbing layer being arranged in the scrubbing tower; a washing pump connected to the washing liquid storage tank and the washing layer, and used for delivering alkaline washing liquid to the washing layer; The oxygen-enriched generator has an output end connected to the connection pipeline of the washing pump and the washing layer through a pipeline, and is used to transport oxygen-enriched ions into the alkaline washing liquid.
2. The enameled wire tail gas treatment device according to claim 1, characterized in that: The height of the single-layer pre-denitrification catalytic layer is 10~20cm.
3. The enameled wire tail gas treatment device according to claim 1, characterized in that: The pre-denitration catalytic layer is provided with 1 to 3 layers; the distance between adjacent pre-denitration catalytic layers is 30 to 50 cm.
4. The enameled wire tail gas treatment device according to claim 1, characterized in that: Each pre-denitrification catalytic layer is independently configured with a pressure sensor for real-time monitoring of the operating resistance of the corresponding pre-denitrification catalytic layer.
5. The enameled wire tail gas treatment device according to claim 1, characterized in that: The flue gas reheat layer adopts a tubular heat exchanger, and the high-temperature medium from the waste heat recovery unit flows through the heat exchange tubes; temperature sensors are arranged above and below the flue gas reheat layer.
6. The enameled wire tail gas treatment device according to claim 1, characterized in that: The denitration catalytic layer is provided in two layers, and the height of each layer is 100-120 cm; the distance between adjacent denitration catalytic layers is 30-60 cm.
7. The enameled wire tail gas treatment device according to claim 1, characterized in that: The washing layer adopts a spray mechanism and is provided with 2 to 3 layers.
8. A method for treating enameled wire tail gas, characterized in that: The enameled wire tail gas treatment device according to claim 1 is used, comprising: the enameled wire tail gas treated by the catalytic combustion unit and cooled to 195-205°C by the preheat recovery unit enters the denitrification tower, flows through the pre-denitrification catalytic layer, the flue gas reheating layer and the denitrification catalytic layer in sequence, the salts generated during the catalytic combustion and the volatile solvents that cannot be burned are condensed at the inlet of the pre-denitrification catalytic layer, the flue gas reheating layer uses the recovered waste heat from the waste heat recovery unit to reheat the pre-denitrified tail gas by 10-15°C, and the tail gas temperature after reheating is increased to 210-220°C, and enters the denitrification catalytic layer; the tail gas treated by the denitrification tower enters the oxidation washing tower, and is in reverse contact with the alkaline absorption liquid rich in oxygen ions to purify the acidic gases and low-molecular organic solvents in the flue gas.
9. The method for treating enameled wire tail gas according to claim 8, characterized in that: The concentration of oxygen-rich ions in the alkaline absorption liquid is 50~300mg / L; the liquid-gas ratio of the single-layer washing layer is 1~3L / m 3 .
10. The method for treating enameled wire tail gas according to claim 8, characterized in that: When the flue gas operation resistance of a single-layer pre-denitrification catalytic layer increases by more than 30Pa, the corresponding pre-denitrification catalytic layer should be replaced.