Dry quenching system

Abstract

The utility model discloses a dry quenching system which comprises a dry quenching furnace, a heat pipe heat exchanger, a primary dust remover, a secondary dust remover and a dry quenching boiler, the dry quenching furnace is connected with a first nitrogen inlet pipeline and an air inlet pipeline, and a second nitrogen inlet pipeline is arranged between the secondary dust remover and the dry quenching boiler. A third nitrogen inlet pipeline is arranged between the dry quenching furnace and the heat pipe heat exchanger, the first nitrogen inlet pipeline and the third nitrogen inlet pipeline are arranged to be used for introducing nitrogen into the dry quenching furnace, and the second nitrogen inlet pipeline is arranged to be used for introducing nitrogen into the secondary dust remover. According to the dry quenching system disclosed by the utility model, the temperature of circulating gas and the content of oxygen and carbon dioxide can be directly reduced by introducing nitrogen behind the demineralized water heat pipe heat exchanger, so that the temperature cooling efficiency of red coke is improved, and the burning loss of the red coke is reduced; nitrogen is introduced into the middle bolt to be mixed with air, and the concentration of oxygen introduced into the air is reduced, so that the burning loss of coke powder is reduced, and the burning loss rate of coke is powerfully reduced.

Description

Technical Field

[0001] This utility model belongs to the technical field of coke quenching systems, specifically, it relates to a dry coke quenching system. Background Technology

[0002] Dry quenching technology in coking plants is an environmentally friendly and efficient quenching technology. It cools red-hot coke through the circulation of inert gas (such as nitrogen) while recovering heat energy. Its gas circulation system is the core component, mainly including gas flow, heat transfer, dust treatment, and gas composition control. Coke (approximately 1000–1100°C) is transported from the coke oven to the dry quenching hoist by coke carts. It is then lifted by a hoist and fed into the top of the dry quenching furnace. From there, it is loaded into the pre-storage chamber and then enters the lower cooling chamber. In the cooling chamber below the pre-storage chamber, the coke exchanges heat with the inert gas, cooling to below 200°C before being discharged through a coke discharge device. The coke is then conveyed to the coke screening device via a heat-resistant coke conveyor belt at the bottom of the dry quenching furnace. A rotary sealing device is installed at the coke discharge device to prevent gas leakage from the dry quenching furnace. The circulating gas (120–140°C) enters from the bottom of the dry quenching furnace, flows upwards, and comes into countercurrent contact with the red-hot coke, absorbing heat and rising to 880–980°C. After leaving the dry quenching furnace, the high-temperature circulating gas first passes through a primary dust collector (gravity settling or multi-stage cyclone dust collector) to remove large particles of dust (coke powder). The dust-removed high-temperature circulating gas then enters the waste heat boiler, where it exchanges heat with demineralized water to generate high-pressure steam (used for power generation or heating), reducing the circulating gas temperature to 160–200°C. The gas then passes through a secondary dust collector (such as a cyclone dust collector or a porous ceramic filter) to further remove fine dust, ensuring the cleanliness of the circulating gas. The cooled gas is pressurized by a circulating fan, cooled by a demineralized water heat exchanger (generally a heat pipe heat exchanger), and then reintroduced into the bottom of the dry quenching furnace to complete the cycle. In the dry quenching (CDQ) process, the traditional direct injection of nitrogen (N2) has a significant impact on system safety, thermal efficiency, energy consumption, and equipment lifespan.

[0003] Dry quenching, a widely used coke quenching technology, offers significant advantages over wet quenching. However, a certain degree of coke loss occurs during the dry quenching process. This is primarily due to the presence of carbon dioxide and oxygen in the atmosphere of the dry quenching system, which react with the coke, leading to mass loss. Based on industry experience from companies like Baosteel and Ansteel, this loss rate is approximately 2-2.5%.

[0004] As the steel industry continues to demand higher standards for coke quality and cost control, the problem of excessively high dry quenching coke loss rate is receiving increasing attention. A high loss rate increases coke consumption and can also affect the normal operation of dry quenching units and the stability of subsequent steel production. Therefore, reducing the dry quenching coke loss rate is becoming increasingly important to the industry.

[0005] In terms of cost control: reducing the burn-off rate directly reduces the additional consumption of coke. Coke accounts for a high proportion of costs in steel production, and reducing the burn-off rate can effectively reduce production costs and improve the economic efficiency of enterprises.

[0006] In terms of quality assurance: reducing coke burn-off helps stabilize coke quality. Because burn-off changes the particle size distribution, strength, and other performance indicators of coke, stable coke quality is crucial for the smooth operation of blast furnace ironmaking. For example, it can ensure good blast furnace permeability, which is conducive to the stability of furnace conditions.

[0007] In terms of environmental protection, energy conservation, and carbon reduction: reducing the burn loss rate means increasing the effective utilization rate of coke, which is a manifestation of energy conservation from a resource utilization perspective. At the same time, reducing emissions such as waste gas generated by burn loss also has positive significance for environmental protection and carbon emission reduction.

[0008] Currently, the coking industry is employing various methods to reduce the burn-off rate of dry quenching coke. Some coking plants are increasing the CO concentration in the circulating gas to reduce the carbon dissolution reaction within the dry quenching furnace (CO2 + C = 2CO), thereby reducing coke burn-off. However, excessively high CO concentrations can lead to an increase in combustible gas levels, posing a risk of explosion in the dry quenching coke circulation system. Therefore, the highest CO concentration currently generally does not exceed 8%. This approach has limited effectiveness in reducing the burn-off rate of dry quenching coke.

[0009] Some coking plants reduce the concentration of combustible gases in the circulating gas by introducing nitrogen into the dry quenching furnace, while simultaneously releasing some of the circulating gas. However, this method also has the problems of excessive nitrogen introduction and high costs. In addition, when red-hot coke enters the dry quenching furnace, the concentration of combustible gases may exceed the standard for a short period of time, and some air still needs to be introduced to burn off the combustible gases. Therefore, introducing nitrogen into the furnace cannot completely solve the problem of coke burn-off in dry quenching.

[0010] Chinese patent application number 201310577013.0 discloses a dry quenching system, which includes a dry quenching bin, a track, and a wet coke car traveling on it. The quenching bin is located beside the track and is positioned below it. A coke loading port is opened on the upper side wall of the quenching bin near the track. A coke loading chute leading to the opening is provided between the track and the quenching bin. The end of the coke loading chute near the track is higher, and the end near the quenching bin is lower. However, this system does not solve the problem of coke burn-off in dry quenching.

[0011] The aim is to provide an improved dry quenching system, particularly regarding how to effectively reduce coke burn-off rate and improve nitrogen utilization. Utility Model Content

[0012] This invention aims to solve at least one of the technical problems existing in the prior art. To this end, this invention provides a dry quenching system for reducing coke burn-off rate.

[0013] To achieve the above objectives, the technical solution adopted by this utility model is as follows: a dry quenching system, including a dry quenching furnace, a heat pipe heat exchanger, a primary dust collector, a secondary dust collector, and a dry quenching boiler. The dry quenching furnace is connected to a first nitrogen inlet pipeline and an air inlet pipeline. A second nitrogen inlet pipeline is provided between the secondary dust collector and the dry quenching boiler. A third nitrogen inlet pipeline is provided between the dry quenching furnace and the heat pipe heat exchanger. The first and third nitrogen inlet pipelines are configured to introduce nitrogen into the dry quenching furnace, and the second nitrogen inlet pipeline is configured to introduce nitrogen into the secondary dust collector.

[0014] The first nitrogen inlet pipe and the air inlet pipe are connected to the middle plug of the dry quenching furnace, and the third nitrogen inlet pipe is connected to the bottom of the dry quenching furnace.

[0015] A pressurizing fan is installed in the third nitrogen inlet pipeline.

[0016] A circulating fan is installed between the secondary dust collector and the heat pipe heat exchanger, and the circulating fan is connected to the emergency nitrogen inlet pipeline.

[0017] The primary dust collector is located between the dry quenching furnace and the dry quenching coke boiler.

[0018] A regulating valve is installed in the first nitrogen inlet pipeline, the second nitrogen inlet pipeline, and the third nitrogen inlet pipeline.

[0019] The heat pipe heat exchanger is connected to the demineralized water inlet pipe and the demineralized water outlet pipe, which are connected by a bypass pipe.

[0020] The dry quenching system of this invention directly reduces the temperature of the circulating gas by introducing nitrogen after the demineralized water heat pipe heat exchanger, thereby reducing the oxygen and carbon dioxide content, improving the cooling efficiency of red-hot coke, and reducing red-hot coke burn-off. By introducing nitrogen into the middle vent and mixing it with air, the oxygen concentration in the introduced air is reduced, thereby reducing the burn-off of coke powder and significantly reducing the coke burn-off rate. Attached Figure Description

[0021] This manual includes the following figures, which illustrate the following:

[0022] Figure 1 This is a schematic diagram of the dry coke quenching system of this utility model;

[0023] The following are marked in the diagram: 1. Dry quenching furnace; 2. Heat pipe heat exchanger; 3. Primary dust collector; 4. Secondary dust collector; 5. Dry quenching coke boiler; 6. First nitrogen inlet pipeline; 7. Air inlet pipeline; 8. Second nitrogen inlet pipeline; 9. Third nitrogen inlet pipeline; 10. Pressurizing fan; 11. Circulating fan; 12. Vent pipe; 13. Demineralized water inlet pipe; 14. Demineralized water outlet pipe; 15. Bypass pipeline; 16. Flow meter; 17. Central plug. Detailed Implementation

[0024] The specific embodiments of this utility model will be further described in detail below with reference to the accompanying drawings, in order to help those skilled in the art to have a more complete, accurate and in-depth understanding of the concept and technical solution of this utility model, and to facilitate its implementation.

[0025] It should be noted that in the following embodiments, the terms "first," "second," and "third" do not represent an absolute distinction in structure and / or function, nor do they represent the order of execution; they are merely for the convenience of description.

[0026] like Figure 1 As shown, this utility model provides a dry quenching system, including a dry quenching furnace 1, a heat pipe heat exchanger 2, a circulating fan 11, a primary dust collector 3, a secondary dust collector 4, and a dry quenching boiler 5. The dry quenching furnace 1 is connected to a first nitrogen inlet pipe 6 and an air inlet pipe 7. A second nitrogen inlet pipe 8 is provided between the secondary dust collector 4 and the dry quenching boiler 5. A third nitrogen inlet pipe 9 is provided between the dry quenching furnace 1 and the heat pipe heat exchanger 2. The first nitrogen inlet pipe 6 and the third nitrogen inlet pipe 9 are configured to introduce nitrogen into the dry quenching furnace 1, and the second nitrogen inlet pipe 8 is configured to introduce nitrogen into the secondary dust collector 4.

[0027] Specifically, such as Figure 1 As shown, the first nitrogen inlet pipe 6 and the air inlet pipe 7 are connected to the central plug 17 of the dry quenching furnace 1. A regulating valve and a flow meter 16 are installed in the first nitrogen inlet pipe 6 and the air inlet pipe 7. The opening of the regulating valve is adjustable, and the nitrogen and air inlet volumes are adjusted accordingly. A nitrogen inlet A and an air inlet pipe are installed at the central plug 17 of the dry quenching furnace. The regulating valve is controlled according to the inlet gas flow rate to control the nitrogen and air inlet ratio, ensuring that the air-to-nitrogen ratio entering the dry quenching furnace 1 is 1:1.5 to 1:6. This is to burn off the combustible gases produced by the red-hot coke, maintaining the carbon monoxide and hydrogen concentrations in the circulating gas to no more than 9% and 3% respectively, while minimizing coke powder loss before the primary dust collector 3.

[0028] Based on the existing gas composition detection data for dry quenching, the regulating valves for air and nitrogen introduced into the dry quenching vent 17 are adjusted to provide an appropriate air-to-nitrogen ratio. When the CO and H2 content is high, i.e., the CO+H2 concentration is between 9% and 12%, the air-to-nitrogen ratio entering the dry quenching vent can be increased to 1:1.5 to 1:3. When the CO+H2 concentration is between 6% and 9%, the air-to-nitrogen ratio entering the dry quenching vent can be adjusted to 1:3 to 1:6 to reduce the introduction of air and reduce coke burn-off.

[0029] like Figure 1 As shown, the outlet of the dry quenching coke boiler 5 is connected to the inlet of the secondary dust collector 4 through the first connecting pipe. The first connecting pipe is connected to the second nitrogen inlet pipe 8. The second nitrogen inlet pipe 8 is set between the dry quenching coke boiler 5 and the secondary dust collector 4. Nitrogen is introduced through the second nitrogen inlet pipe 8 to reduce the content of combustible gas components in the circulating gas. At the same time, it avoids all room temperature nitrogen from entering through the dry quenching furnace 1 through the shunt 17, so as not to reduce the temperature of the circulating gas T6 entering the dry quenching coke boiler 5 (the temperature of T6 is generally required to be stable at 880-980℃), thereby reducing the heat exchange efficiency of the dry quenching coke boiler 5.

[0030] By introducing nitrogen into the circulating gas pipeline after the dry quenching coke boiler 5, the combustible gas components in the circulating gas are diluted. At the same time, the composition of the circulating gas at this point is detected to ensure that the oxygen concentration in the circulating gas does not exceed 1.0% (based on the existing detection instruments for dry quenching coke) and the carbon dioxide concentration does not exceed 6.0-7.0%, so as to control the oxygen and carbon dioxide components in the circulating gas to prevent them from being excessive.

[0031] like Figure 1 As shown, the outlet of the heat pipe heat exchanger 2 is connected to the bottom of the dry quenching furnace 1 via a second connecting pipe. The third nitrogen inlet pipe 9 is connected to the second connecting pipe. A regulating valve, a flow meter 16, and a pressurizing fan 10 are installed in the third nitrogen inlet pipe 9. Nitrogen gas is introduced after the heat pipe heat exchanger 2 and before entering the bottom of the dry quenching furnace 1. Because the circulating gas is in a positive pressure zone here, generally between 2 and 6 kPa, it is necessary to pressurize the relatively inexpensive low-pressure nitrogen gas using the pressurizing fan 10. If the low-pressure nitrogen gas itself has a high pressure, the pressurizing fan 10 may not be required.

[0032] Introducing nitrogen C after the heat pipe heat exchanger 2 and before it enters the bottom of the dry quenching furnace 1 can quickly reduce the temperature of the circulating gas, reduce the content of combustible gas components, carbon dioxide gas that can cause carbon dissolution reaction, and corrosive gases such as sulfur dioxide in the circulating gas, improve the cooling efficiency of red coke, reduce the dry quenching coke burn-off rate, and reduce the corrosion rate of the equipment.

[0033] like Figure 1As shown, the heat pipe heat exchanger 2 is connected to a demineralized water inlet pipe 13 and a demineralized water outlet pipe 14. The demineralized water inlet pipe 13 is used to send demineralized water into the heat pipe heat exchanger 2, and the demineralized water in the heat pipe heat exchanger 2 is discharged through the demineralized water outlet pipe 14. The demineralized water inlet pipe 13 and the demineralized water outlet pipe 14 are connected by a bypass pipe 15. A bypass pipe 15 is added between the demineralized water inlet and outlet pipes of the heat pipe heat exchanger 2. A regulating valve is installed in the bypass pipe 15 to regulate the amount of demineralized water exchanged, thereby regulating the temperature of the circulating gas after the heat pipe heat exchanger 2 and preventing the circulating gas temperature from being too low, which could cause dew point corrosion from acidic gases such as sulfur trioxide.

[0034] like Figure 1 As shown, a circulating fan 11 is installed between the secondary dust collector 4 and the heat pipe heat exchanger 2. The circulating fan 11 is connected to the secondary dust collector 4 and the heat pipe heat exchanger 2. The circulating fan 11 is also connected to the emergency nitrogen inlet pipe, which facilitates the rapid introduction of emergency nitrogen in the event of an accident, thereby ensuring the safety of the dry quenching system.

[0035] like Figure 1 As shown, the primary dust collector 3 is installed between the dry quenching furnace 1 and the dry quenching coke boiler 5, and the primary dust collector 3 is connected to the dry quenching furnace 1 and the dry quenching coke boiler 5.

[0036] like Figure 1 As shown, the nitrogen introduced at vent 17 in the dry quenching furnace 1, mixed with air, is called nitrogen introduction A; the nitrogen introduced between the dry quenching coke boiler 5 and the secondary dust collector 4 is called nitrogen introduction B; and the nitrogen introduced between the heat pipe heat exchanger 2 and the bottom of the dry quenching furnace 1 is called nitrogen introduction C. Nitrogen introduction B and nitrogen introduction C are backups for each other. When using them, it must be ensured that the carbon dioxide content in the circulating gas system is less than 6%. If it is less than 6%, nitrogen introduction B is used; if it is higher than 6%, nitrogen introduction C is turned on, and nitrogen introduction B is stopped.

[0037] Furthermore, the ratio of introduced nitrogen A to introduced nitrogen B (or introduced nitrogen C) can be 5:5 to 9:1. Under normal circumstances, introduced nitrogen A is the main component.

[0038] like Figure 1 As shown, the heat pipe heat exchanger 2 is connected to the vent pipe 12. Excess circulating gas is released through the vent pipe 12 after the heat pipe heat exchanger 2. Nitrogen C is then introduced into the main circulating gas pipe after the vent pipe 12, which can effectively reduce the concentration of combustible gases, acidic gases such as sulfur dioxide, carbon dioxide, and water vapor in the circulating gas. This can reduce system corrosion, carbon dissolution reaction, and water-gas reaction, thereby mitigating corrosion and reducing coke burn-off rate. At the same time, because nitrogen is introduced into a small amount of circulating gas after venting, the waste of nitrogen can be reduced.

[0039] The dry quenching system described above has the following advantages:

[0040] 1. Reduce the generation of harmful gases and lower production costs.

[0041] By introducing air, some harmful flammable gases can be burned off, effectively reducing the difficulty of waste gas treatment. Simultaneously, the generated waste gas can participate in the dry quenching system's circulation, reducing nitrogen usage and lowering production costs.

[0042] 2. Reduce dry quenching coke loss rate

[0043] By introducing nitrogen gas after the heat pipe heat exchanger 2, the temperature of the circulating gas can be directly reduced, and the oxygen and carbon dioxide content can be reduced, thereby improving the cooling efficiency of the red coke temperature and reducing the burning loss of the red coke. By introducing nitrogen gas into the middle plug 17 and mixing it with air, the oxygen concentration in the introduced air is reduced, thereby reducing the burning loss of coke powder and thus effectively reducing the coke burning rate.

[0044] 3. It helps maintain the overall pressure stability of the dry quenching system.

[0045] By introducing nitrogen at three different locations, introducing air at the middle plug 17, and adjusting the amount of circulating gas released according to the system pressure, airflow disturbance can be effectively reduced, interference with the dry quenching operation can be minimized, and the pressure of the dry quenching system can be kept stable.

[0046] 4. It helps reduce dew point corrosion.

[0047] The nitrogen inlet B is placed before the secondary dust collector 4 because the circulating gas temperature here is relatively high, reaching approximately 160°C. This helps reduce the risk of localized dew point corrosion in the circulating gas after nitrogen is introduced into the dry quenching system, which could be caused by excessive temperature drop. Although the circulating gas temperature is already lower after the heat pipe heat exchanger 2, the dew point corrosion can still be reduced by adjusting the demineralized water bypass opening to ensure the circulating gas temperature remains above 122–128°C.

[0048] 5. Facilitates rapid control of gas composition

[0049] By rapidly controlling the concentrations of combustible gases, carbon dioxide, water vapor, and corrosive gases in the circulating gas, excess gas is released through the vent pipe 12 after the heat pipe heat exchanger 2. After venting, nitrogen C is introduced, which can effectively reduce the concentrations of combustible gases, acidic gases such as sulfur dioxide, carbon dioxide, and water vapor in the circulating gas. This can reduce system corrosion, carbon dissolution reaction, and water-gas reaction, thereby mitigating corrosion and reducing coke burn-off rate.

[0050] 6. Ensure that dry quenching has good thermal efficiency.

[0051] By introducing nitrogen C after the heat pipe heat exchanger 2, the temperature of the circulating gas entering the dry quenching furnace 1 can be moderately reduced without causing dew point corrosion. This reduces the coke discharge temperature of the dry quenching furnace, improves heat exchange efficiency, and increases the boiler steam production.

[0052] 7. Ensure the long-term, trouble-free, and stable operation of the circulating fan 11.

[0053] This utility model retains the emergency nitrogen charging pipeline in front of the circulating fan 11, but does not add a nitrogen inlet pipeline in front of the circulating fan 11. This ensures that nitrogen can be charged in time during an accident, and also avoids the possibility that introducing nitrogen at room temperature during normal operation may cause the local temperature of the circulating gas flowing through the circulating fan 11 to be lower than the acid dew point, thus leading to corrosion of the circulating fan 11.

[0054] 8. It can reduce the waste of nitrogen gas.

[0055] Excess circulating gas is released through the vent pipe 12 after the heat pipe heat exchanger. Nitrogen C is then introduced into the main circulating gas pipe after the vent pipe 12. This effectively reduces the concentration of combustible gases, acidic gases such as sulfur dioxide, carbon dioxide, and water vapor in the circulating gas. This reduces system corrosion, carbon dissolution reactions, and water-gas reactions, thereby mitigating corrosion and lowering the coke burn-off rate. Furthermore, introducing nitrogen after venting effectively reduces nitrogen waste.

[0056] Example

[0057] In this embodiment, the first nitrogen inlet pipe 6 and the air inlet pipe 7 are connected in parallel. The pressure of nitrogen A introduced into the first nitrogen inlet pipe 6 is 4 kPa. After the nitrogen and air are fully mixed, the nitrogen is introduced into the middle plug 17 of the dry quenching furnace 1. The ratio of nitrogen to air is 3.5:1, and the air input is 4000 m3 / h.

[0058] A third nitrogen inlet pipe 9 is added after the heat pipe heat exchanger 2, and a small pressurizing fan 10 is installed in the third nitrogen inlet pipe 9 for pressurization. The fan flow rate is 6000 m³ / s. 3 / h, with a total pressure of 8 kPa, which can easily provide a pressure greater than the 3 kPa pressure of the circulating gas here; at the same time, the flow rate of nitrogen C introduced through the third nitrogen inlet pipeline 9 is 3000 m³ / h. 3 / h.

[0059] Nitrogen B is introduced through the second nitrogen inlet pipe 8 on the circulating gas pipeline between the dry quenching coke boiler 5 and the secondary dust collector 4. The pressure here is -1.5KPa, so there is no need to pressurize. You can simply connect the low-pressure nitrogen at 4KPa directly.

[0060] The vent pipe 12 after heat pipe heat exchanger 2 releases excess circulating gas at a flow rate of 25000 m³ / s.3 / h, the circulating gas volume before venting is 250,000 m³ / h. 3 / h, the amount of recirculated gas after venting is 250000-25000=225000m³ 3 After introducing nitrogen C at a rate of / h, the proportion of nitrogen introduced can reach 3000 / 225000 = 1.33%. However, when nitrogen B is introduced before the secondary dust collector 4 before venting, the proportion of nitrogen introduced is only 3000 / 250000 = 1.2% for the same amount. Therefore, introducing nitrogen B can increase the actual proportion of nitrogen introduced and reduce the proportion of combustible gas components and harmful components such as carbon dioxide and sulfur dioxide.

[0061] The present invention has been described above by way of example with reference to the accompanying drawings. Obviously, the specific implementation of the present invention is not limited to the above-described manner. Any non-substantial improvements made using the inventive concept and technical solution of the present invention; or the direct application of the inventive concept and technical solution to other situations without modification, are all within the protection scope of the present invention.

Claims

1. A dry quenching system comprising a dry quenching furnace, a heat pipe exchanger, a primary dust collector, a secondary dust collector and a dry quenching boiler, characterized in that: The dry quenching furnace is connected with a first nitrogen inlet pipeline and an air inlet pipeline, a second nitrogen inlet pipeline is arranged between the secondary dust collector and the dry quenching furnace boiler, a third nitrogen inlet pipeline is arranged between the dry quenching furnace and the heat pipe heat exchanger, the first nitrogen inlet pipeline and the third nitrogen inlet pipeline are arranged to introduce nitrogen into the dry quenching furnace, and the second nitrogen inlet pipeline is arranged to introduce nitrogen into the secondary dust collector.

2. The dry quenching system of claim 1, wherein: The first nitrogen inlet pipeline and the air inlet pipeline are connected with the middle plug of the dry quenching furnace, and the third nitrogen inlet pipeline is connected with the bottom of the dry quenching furnace.

3. The dry quenching system of claim 1, wherein: A pressurized fan is arranged in the third nitrogen inlet pipeline.

4. The dry quenching system according to any one of claims 1 to 3, characterized in that: A circulating fan is arranged between the secondary dust collector and the heat pipe heat exchanger, and the circulating fan is connected with an accident nitrogen inlet pipeline.

5. The dry quenching system according to any one of claims 1 to 3, characterized in that: The primary dust collector is arranged between the dry quenching furnace and the dry quenching furnace boiler.

6. The dry quenching system according to any one of claims 1 to 3, characterized in that: Adjusting valves are arranged in the first nitrogen inlet pipeline, the second nitrogen inlet pipeline and the third nitrogen inlet pipeline.

7. The dry quenching system according to any one of claims 1 to 3, characterized in that: The heat pipe heat exchanger is connected with a desalted water inlet pipeline and a desalted water outlet pipeline, and the desalted water inlet pipeline and the desalted water outlet pipeline are connected through a bypass pipeline.

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