A dust removal and cooling device for high-dust, high-concentration, ultra-high-temperature hydrogen gas.

Abstract

This utility model discloses a dust removal and cooling device for high-dust, high-concentration, ultra-high-temperature hydrogen gas, used for dust removal and cooling of the cracked gas produced by methane cracking for hydrogen production. It includes a dust collector and a cooling device. The dust collector comprises a gravity dust collection box and a water tank, with the gravity dust collection box nested within the water tank. The gravity dust collection box is used to deposit carbon powder in the cracked gas and has an ash hopper at its bottom. The water tank cools the gas entering the gravity dust collection box by supplying circulating water. The cooling device cools the cracked gas after dust removal by supplying circulating water. This dust removal and cooling device effectively solves the technical problems existing in the current methane cracking for hydrogen production process, such as difficulty in carbon-hydrogen separation under high dust, high concentration, and ultra-high temperature conditions, carbon powder blockage during hydrogen cooling, and difficulty in collecting carbon powder after high-temperature dust removal. The cracked gas undergoes subsequent cooling treatment only after a large amount of carbon powder is removed and after initial cooling and deceleration, which reduces the risk of blockage in the cooler.

Description

Technical Field

[0001] This utility model relates to the field of methane cracking for hydrogen production technology, and in particular to a dust removal and cooling device for high-dust, high-concentration, ultra-high-temperature hydrogen. Background Technology

[0002] In current methane cracking for hydrogen production, high-temperature cracking is the mainstream method, with cracking temperatures typically between 800-1200℃. In this process, methane cracks under the combined action of a catalyst and high temperature to produce solid carbon powder and hydrogen. The produced hydrogen and carbon powder are discharged from the cracking unit in a mixed state. However, due to the properties of hydrogen and carbon powder, conventional dust removal and cooling systems are insufficient to meet the requirements of high-temperature dust removal and cooling. During the cooling process in the equipment, carbon powder easily adheres to pipes and bulkheads, causing blockages and leading to an increase in overall system pressure, posing a significant safety risk.

[0003] In addition, the temperature of the pyrolysis gas coming out of the pyrolysis equipment in the existing process can reach over 1000℃, the carbon powder concentration can reach over 50%, and there is also some adhesion between the carbon powders, which further exacerbates the difficulties in hydrocarbon separation, carbon powder blockage during hydrogen cooling, and difficulty in collecting carbon powder after high-temperature dust removal. For example, in the existing technology, there are the following problems: (1) In the conventional preheating recovery process, in order to ensure safety, the pyrolysis gas generally flows through the cooling system tube, but the existing process has carbon powder blockage, which leads to the problem of increased system pressure; (2) When a conventional dust removal system is added before the cooling system, the carbon powder is in a high-temperature state (up to over 1000℃) during collection, and the carbon powder will spontaneously combust when it comes into contact with air during the collection process, causing a safety accident; (3) Conventional materials will cause hydrogen embrittlement of metal materials during decarbonization and cooling, which will lead to hydrogen leakage and cause a safety accident; (4) (5) Because conventional cooling systems strictly control the amount of water to reduce the size of the equipment, the temperature of the pyrolysis gas is too high (it can reach more than 1000℃), which will evaporate the circulating water, resulting in increased pressure inside the equipment and posing a safety risk of explosion; (6) In the cavity of conventional dust collectors, the kinetic energy of the carbon powder inside does not disappear, resulting in most of the carbon powder being carried out of the dust collector by the pyrolysis gas; (7) The flue gas cooling efficiency in conventional high-temperature dust collectors is insufficient, resulting in excessively high flue gas flow rate and insufficient dust removal efficiency; (8) After the carbon powder settles down, it does not exchange heat with the circulating water in time, resulting in a high carbon powder temperature. Utility Model Content

[0004] The purpose of this invention is to solve the technical problems in the existing methane cracking hydrogen production process, such as the difficulty of separating carbon and hydrogen under high dust, high concentration and ultra-high temperature, carbon powder blockage during hydrogen cooling, and difficulty in collecting carbon powder after high temperature dust removal, and to provide a dust removal and cooling device for high dust, high concentration and ultra-high temperature hydrogen.

[0005] The technical solution adopted by this utility model to solve its technical problem is: a dust removal and cooling device for high dust, high concentration and ultra-high temperature hydrogen is provided for dust removal and cooling of cracked gas produced by methane cracking to produce hydrogen, which includes a dust collector and a cooling device arranged sequentially along the gas flow path.

[0006] The dust collector includes a gravity dust collection box and a water tank; the gravity dust collection box is nested inside the water tank. The gravity dust collection box is used to deposit carbon powder in the pyrolysis gas. It has an air inlet on one side, an air outlet on the other side, and an ash hopper at the bottom. The bottom of the ash hopper has an ash discharge port. The water tank cools the dust collection box by supplying circulating water.

[0007] The cooling device cools the pyrolysis gas after it has been dusted by the dust collector by supplying circulating water for heat exchange.

[0008] Furthermore, the cooling device includes a primary cooler and a secondary cooler;

[0009] The primary cooler includes a primary heat exchange tube bundle and a primary cooling box; the primary heat exchange tube bundle is disposed in the primary cooling box, and the air inlet of the primary heat exchange tube bundle is connected to the air outlet of the gravity dust collector; the primary cooling box exchanges primary heat with the pyrolysis gas in the primary heat exchange tube bundle by supplying circulating water.

[0010] The secondary cooler includes a secondary heat exchange tube bundle and a secondary cooling box; the secondary heat exchange tube bundle is disposed in the secondary cooling box, and the air inlet of the secondary heat exchange tube bundle is connected to the air outlet of the primary heat exchange tube bundle; the secondary cooling box exchanges heat with the cracked gas in the secondary heat exchange tube bundle by supplying circulating water.

[0011] Furthermore, there are multiple primary heat exchange tube bundles, and their inlet ends are respectively connected to the outlet ends of the primary flue gas distributor. The inlet end of the primary flue gas distributor is connected to the outlet of the gravity dust collector through a pipe.

[0012] The number of secondary heat exchange tube bundles is multiple, and their inlet ends are respectively connected to the outlet ends of the secondary flue gas distributor. The inlet end of the secondary flue gas distributor is connected to the outlet end of the primary heat exchange tube bundle through a pipe.

[0013] Furthermore, both the primary heat exchange tube bundle and the secondary heat exchange tube bundle are serpentine tube bundles.

[0014] Furthermore, the circulating water in the primary cooling tank submerges the top surface of the primary heat exchange tube bundle and the primary flue gas distributor, and the submersion height H2 is not less than 200mm;

[0015] The circulating water in the secondary cooling tank submerges the top surface of the secondary heat exchange tube bundle and the secondary flue gas distributor, and the submersion height H3 is not less than 200mm.

[0016] Furthermore, the water inlet of the water tank is located at its bottom, and the water outlet is located at its top.

[0017] Furthermore, the dust collector is also equipped with multiple horizontal pipes and multiple vertical pipes;

[0018] Multiple transverse pipes are arranged at intervals and extend horizontally through the gravity dust collector, with both ends connected to the water tank.

[0019] Multiple longitudinal pipes are arranged at intervals and run longitudinally through the gravity dust collector in the horizontal direction, while both ends are connected to the water tank.

[0020] Furthermore, the circulating water in the water tank submerges the top surface of the gravity dust collector, and the submersion height H1 is not less than 200mm.

[0021] Furthermore, a baffle is provided in the middle of the gravity dust collector, which extends downward from the top surface of the gravity dust collector by a predetermined distance, dividing the top of the gravity dust collector into two areas.

[0022] The air inlet and air outlet of the gravity dust collector are both located at the top of the gravity dust collector and on both sides of the baffle, respectively.

[0023] Furthermore, in both the dust collector and the cooling device, the parts in contact with the pyrolysis gas are made of SUS316 stainless steel. Specifically, the gravity dust collector is made of SUS316 stainless steel, the primary and secondary heat exchange tube bundles are made of SUS316 stainless steel, and the primary and secondary flue gas distributors are also made of SUS316 stainless steel.

[0024] Furthermore, the ash discharge port is equipped with an ash discharge valve.

[0025] The advantages of this utility model compared to the prior art are as follows:

[0026] (1) Solving the problem of carbon powder blockage: The dust collector of this utility model can deposit a large amount of carbon powder in the cracked gas before the cooler by gravity settling of the gravity dust collection box and water cooling heat exchange of the water tank. This can significantly reduce the blockage of the cooler caused by carbon powder, thereby avoiding the rise of system pressure and ensuring the stable operation of the system.

[0027] (2) Reduce the risk of spontaneous combustion of toner: By placing the ash hopper of the gravity dust collector in a water tank, the circulating water can be used to cool the toner in the ash hopper, so that the temperature of the toner is reduced to below the auto-ignition point (below 100℃) before collection, which can effectively avoid the risk of spontaneous combustion of toner when it comes into contact with air at high temperature.

[0028] (3) Preventing hydrogen embrittlement: This utility model uses SUS316 stainless steel, a hydrogen embrittlement resistant material, as the material of the parts that come into contact with hydrogen, which can ensure that hydrogen will not damage the equipment during dust removal and heat exchange, thereby avoiding hydrogen leakage and ensuring the safety of the system.

[0029] (4) Avoid increasing internal pressure: Both the dust collector and the cooler adopt a water immersion design, and the liquid level is more than 200mm higher than the contact part of the cracked gas. This design can effectively prevent the circulating water from being evaporated by the high temperature cracked gas, thereby maintaining the internal pressure of the equipment and avoiding the increase in internal pressure due to the evaporation of circulating water, thus reducing the risk of explosion.

[0030] (5) Improve carbon powder settling efficiency: The dust collector is equipped with baffles and staggered tube bundles. The cracked gas flows downward under the action of the baffles. The kinetic energy of the carbon powder decreases during the collision with the baffles and the horizontal and vertical tubes, which is conducive to the settling of the carbon powder. This design can significantly improve the settling efficiency of the carbon powder and reduce the possibility of the carbon powder being carried out of the dust collector by the cracked gas.

[0031] (6) Improve cooling efficiency: The water tank of the dust collector can cool the pyrolysis gas through circulating water. Combined with the cooling effect of the horizontal and vertical pipes in the gravity dust collector, it can effectively reduce the temperature of the pyrolysis gas, thereby reducing the flow rate of the pyrolysis gas and improving the dust removal efficiency of the carbon powder.

[0032] (7) Timely reduction of carbon powder temperature: The internal temperature of the cracked gas is reduced by using horizontal and vertical pipes. After the carbon powder settles down, it can quickly exchange heat with the circulating water, thus reducing the carbon powder temperature in time. This can avoid the problem of the temperature remaining too high after the carbon powder settles down due to untimely heat exchange. Attached Figure Description

[0033] Figure 1 This is an overall schematic diagram of the dust removal and cooling equipment for high-dust, high-concentration, ultra-high-temperature hydrogen provided by this utility model.

[0034] Figure 2 yes Figure 1 Schematic diagram of a medium-sized dust collector;

[0035] Figure 3 yes Figure 2 Side view;

[0036] Figure 4 yes Figure 1A schematic diagram of the structure of a primary or secondary cooler;

[0037] Figure 5 yes Figure 4 Top view;

[0038] In the accompanying drawings, solid arrows indicate the flow path of circulating water, hollow arrows indicate the flow path of pyrolysis gas, and dashed arrows indicate the flow path of toner. Detailed Implementation

[0039] The present invention will be further described in detail below with reference to specific embodiments, but the implementation of the present invention is not limited thereto.

[0040] like Figure 1 As shown, this utility model provides a dust removal and cooling device for high-dust, high-concentration, ultra-high-temperature hydrogen gas. The dust removal and cooling device includes a dust collector 100 and a cooling device 200 arranged sequentially along the gas flow path.

[0041] The structure of the dust collector 100 is as follows:

[0042] like Figure 2 and Figure 3 As shown, the dust collector 100 includes a gravity dust collection box 110 and a water tank 120. The gravity dust collection box 110 is nested within the water tank 120. The gravity dust collection box 110 is used to deposit carbon powder in the pyrolysis gas. It has an air inlet on one side, an air outlet on the other side, and an ash hopper 111 at the bottom. The bottom of the ash hopper 111 has an ash discharge port 111a, which is equipped with an ash discharge valve (not shown in the figure). The water tank 120 cools the pyrolysis gas entering the gravity dust collection box 110 by supplying circulating water.

[0043] Specifically, the dust collector 100 also includes multiple horizontal pipes 130 and multiple vertical pipes 140. The horizontal pipes 130 are arranged at intervals and pass horizontally through the gravity dust collector 110, with both ends connected to the water tank 120. The vertical pipes 140 are arranged at intervals and pass vertically through the gravity dust collector 110, with both ends connected to the water tank 120. See also... Figure 2 and Figure 3 The dust collector 110 has two layers of horizontal pipes 130 and two layers of vertical pipes 140 arranged alternately along its height. Each layer includes one or more horizontal pipes 130 or vertical pipes 140. These pipe bundles run through the dust collector 110, allowing circulating water from the water tank 120 to be introduced into the dust collector 110 for heat exchange with the pyrolysis gas in the dust collector 110. This reduces the overall volume of the pyrolysis gas by cooling it down. At the same time, the kinetic energy of carbon powder is reduced when it impacts the horizontal pipes 130 or the vertical pipes 140, which is beneficial for the deposition of carbon powder in the pyrolysis gas.

[0044] Specifically, a baffle 150 is provided in the middle of the gravity dust collector 110. The baffle 150 extends downwards from the top surface of the gravity dust collector 110 by a predetermined distance, dividing the top of the gravity dust collector 110 into two areas. The air inlet and outlet of the gravity dust collector 110 are both located at its top, on either side of the baffle 150. The baffle 150 guides the flow direction of the pyrolysis gas, causing it to form a deflection within the gravity dust collector 110. This increases the time the pyrolysis gas spends in the gravity dust collector 110, as well as the contact time and collision opportunities between the pyrolysis gas and the horizontal pipe 130 or the vertical pipe 140, thereby improving the cooling effect of the pyrolysis gas and the deposition efficiency of the carbon powder.

[0045] In addition, during operation, the circulating water in water tank 120 will submerge the top surface of gravity dust collector 110, with a submersion height H1 of not less than 200mm (see...). Figure 2 This design ensures that the circulating water does not evaporate, thus maintaining the internal pressure of the equipment.

[0046] The structure of the cooling device 200 is as follows:

[0047] like Figure 1 As shown, the cooling device 200 includes a primary cooler 210 and a secondary cooler 220. Both the primary cooler 210 and the secondary cooler 220 adopt a serpentine tube bundle design to increase the heat exchange area and heat exchange efficiency.

[0048] like Figure 4 and Figure 5 As shown, the primary cooler 210 includes a primary heat exchange tube bundle 211 and a primary cooling box 212. The primary heat exchange tube bundle 211 is disposed in the primary cooling box 212, and its inlet end is connected to the outlet of the gravity dust collector 110. The primary cooling box 212 exchanges primary heat with the pyrolysis gas in the primary heat exchange tube bundle 211 by supplying circulating water. There are multiple primary heat exchange tube bundles 211 (see...). Figure 5 (Top view), and the air inlets are respectively connected to the air outlets of the primary flue gas distributor 213, which in turn is connected to the air outlet of the gravity dust collector 110 via pipes. The primary flue gas distributor 213 ensures that the pyrolysis gas is evenly distributed to each primary heat exchange tube bundle 211 when entering the primary cooler 210, thereby improving cooling efficiency.

[0049] like Figure 4 and Figure 5As shown, the secondary cooler 220 includes a secondary heat exchange tube bundle 221 and a secondary cooling box 222. The secondary heat exchange tube bundle 221 is disposed in the secondary cooling box 222, and its inlet end is connected to the outlet end of the primary heat exchange tube bundle 211. The secondary cooling box 222 conducts secondary heat exchange with the cracked gas in the secondary heat exchange tube bundle 221 by supplying circulating water. There are multiple secondary heat exchange tube bundles 221, and their inlets are respectively connected to the outlet ends of the secondary flue gas distributor 223. The inlet end of the secondary flue gas distributor 223 is connected to the outlet end of the primary heat exchange tube bundle 211 through a pipe. Similarly, the arrangement of the secondary flue gas distributor 223 can ensure that the cracked gas is evenly distributed to each secondary heat exchange tube bundle 221 when entering the secondary cooler 220, thereby improving the cooling efficiency.

[0050] The aforementioned flue gas distributor is an existing device that can be purchased directly from the relevant manufacturers; therefore, this patent does not provide a specific description of its structure.

[0051] Additionally, see Figure 4 and Figure 5 Alternatively, a primary flue gas collector 214 can be installed in the primary cooler 210, with the outlet ends of each primary heat exchange tube bundle 211 connected to the inlet ends of the primary flue gas collector 214, allowing the pyrolysis gas after primary cooling to be collected together and then flow to the secondary cooler 220 through pipelines. Simultaneously, a secondary flue gas collector 224 can be installed in the secondary cooler 220, with the outlet ends of each secondary heat exchange tube bundle 221 connected to the inlet ends of the secondary flue gas collector 224, allowing the pyrolysis gas after secondary cooling to be collected together and then flow to the subsequent process through pipelines. The aforementioned flue gas collectors are existing devices and can be purchased directly from relevant manufacturers; therefore, this patent does not provide a detailed description of their structure.

[0052] The aforementioned primary heat exchanger tube bundle 211 and secondary heat exchanger tube bundle 221 are made of SUS316 stainless steel. The aforementioned primary flue gas distributor 213, secondary flue gas distributor 223, primary flue gas collector 214, and secondary flue gas collector 224 are also made of SUS316 stainless steel. The gravity dust collector 110 is also made of SUS316 stainless steel, and even the transverse tube 130 and longitudinal tube 140 can be made of SUS316 stainless steel.

[0053] Conventional metallic materials are prone to hydrogen embrittlement during decarbonization and cooling processes, leading to hydrogen leakage and potential safety accidents. However, this invention uses SUS316 stainless steel, a material resistant to hydrogen embrittlement, as the material in contact with hydrogen. This ensures that hydrogen will not damage the equipment during dust removal and heat exchange, thus preventing hydrogen leakage.

[0054] Furthermore, in this invention, the circulating water in the primary cooling tank 212 submerges the top surfaces of the primary heat exchange tube bundle 211 and the primary flue gas distributor 213, with a submersion height H2 of not less than 200 mm. Similarly, the circulating water in the secondary cooling tank 222 submerges the top surfaces of the secondary heat exchange tube bundle 221 and the secondary flue gas distributor 223, with a submersion height H3 of not less than 200 mm. This design ensures that the heat exchange tube bundle and flue gas distributor maintain full contact with the cooling water throughout the cooling process, improving cooling efficiency, while also preventing the circulating water from evaporating, thus maintaining the internal pressure of the equipment.

[0055] The aforementioned cooling device 200 adopts a design of two coolers of the same specification connected in series. After being distributed in the flue gas distributor, the pyrolysis gas enters the heat exchange tube bundle to exchange heat with the circulating water. After two stages of cooling, the temperature of the pyrolysis gas can be reduced to below 100°C and then directly enters the subsequent process section.

[0056] Additionally, in this utility model, see Figure 2 The water inlet of water tank 120 is located at its bottom, and the water outlet is located at its top. See also Figure 4 The inlets of the primary cooling tank 212 and the secondary cooling tank 222 are located at their bottoms, and their outlets are located at their tops. Thus, the dust collector 100, the primary cooler 210, and the secondary cooler 220 all adopt an overflow water outlet structure. This structure can ensure the internal circulating water volume of the equipment, maintain the cooling efficiency of the pyrolysis gas, and ensure operational safety.

[0057] The operation process of a specific embodiment of this utility model is as follows:

[0058] The cracking equipment for methane cracking to produce hydrogen uses a high-temperature liquid catalyst, with a cracking temperature of 1100℃ and an outlet pressure of 50KPa. The cracked gas consists of hydrogen, uncracked methane, and carbon powder.

[0059] See Figure 1After the pyrolysis gas is discharged from the pyrolysis equipment, it first enters the gravity dust collector 110 of the dust collector 100 through a pipeline. The residence time of the pyrolysis gas in the gravity dust collector 110 is more than 0.5 seconds. In the gravity dust collector 110, the circulating water in the water tank 120 exchanges heat with the pyrolysis gas, which can reduce the temperature of the pyrolysis gas by about 150°C and reduce its volume by about 10%. At the same time, the gravity dust collector 110 can be set with a large volume and cross-sectional area to reduce the wind speed of the pyrolysis gas. In addition, with the cooling effect and the collision effect of the pyrolysis gas with the horizontal pipe 130 and the vertical pipe 140, the wind speed of the pyrolysis gas can be reduced to below 1 m / s. Under the combined effect of reduced wind speed and reduced kinetic energy, a large amount of carbon powder in the pyrolysis gas is deposited (the dust removal efficiency of carbon powder can reach 40% to 60%), thereby greatly reducing the carbon powder concentration before the pyrolysis gas enters the cooler, thus reducing the risk of carbon powder blockage in the cooler. The carbon powder deposited in the ash hopper 111 is cooled by the circulating water in the water tank 120. After the temperature drops below 100℃ and the carbon powder level rises to 60%-80% of the ash hopper, the ash discharge valve can be opened to discharge the carbon powder and collect it in the carbon powder collection box.

[0060] After dust removal, the pyrolysis gas exits from the outlet of gravity dust collector 110 and enters the primary heat exchange tube bundle 211 of primary cooler 210. In primary heat exchange tube bundle 211, the pyrolysis gas exchanges heat with the circulating water in primary cooling tank 212, further reducing its temperature to approximately 300℃. After cooling by primary cooler 210, the pyrolysis gas enters the secondary heat exchange tube bundle 221 of secondary cooler 220, where it continues to exchange heat with the circulating water in secondary cooling tank 222. Ultimately, the temperature of the pyrolysis gas is reduced to below 100℃, meeting the process requirements of subsequent stages, and then exits from the outlet of secondary cooler 220 for later processing.

[0061] Therefore, the dust removal and cooling equipment of this invention can effectively solve the technical problems existing in the current methane cracking hydrogen production process, such as the difficulty of hydrocarbon separation under high dust concentration and ultra-high temperature, carbon powder blockage during hydrogen cooling, and difficulty in collecting carbon powder after high-temperature dust removal. Subsequent cooling treatment is carried out only after a large amount of carbon powder has been removed from the cracked gas and after preliminary cooling and speed reduction, which can reduce the risk of blockage in the cooler.

[0062] The above description is merely a preferred embodiment of this utility model and is not intended to limit the utility model. Various modifications and variations can be made to this utility model by those skilled in the art. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of this utility model should be included within the protection scope of this utility model.

Claims

1. A dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen, used for dust removal and cooling of pyrolysis gas generated by methane pyrolysis for hydrogen production, characterized in that, It includes a dust collector (100) and a cooling device (200) arranged sequentially along the gas flow path; The dust collector (100) includes a gravity dust collection box (110) and a water tank (120); the gravity dust collection box (110) is nested inside the water tank (120), and the gravity dust collection box (110) is used to deposit carbon powder in the pyrolysis gas. It has an air inlet on one side, an air outlet on the other side, and an ash hopper (111) at the bottom. The bottom of the ash hopper (111) has an ash discharge port (111a); the water tank (120) cools the water entering the gravity dust collection box (110) by supplying circulating water. The cooling device (200) cools the pyrolysis gas after it has been dusted by the dust collector (100) by supplying circulating water.

2. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen according to claim 1, characterized in that, The cooling device (200) includes a primary cooler (210) and a secondary cooler (220). The primary cooler (210) includes a primary heat exchange tube bundle (211) and a primary cooling box (212); the primary heat exchange tube bundle (211) is disposed in the primary cooling box (212), and the air inlet of the primary heat exchange tube bundle (211) is connected to the air outlet of the gravity dust collector (110); the primary cooling box (212) exchanges primary heat with the cracked gas in the primary heat exchange tube bundle (211) by supplying circulating water; The secondary cooler (220) includes a secondary heat exchange tube bundle (221) and a secondary cooling box (222); the secondary heat exchange tube bundle (221) is disposed in the secondary cooling box (222), and the air inlet of the secondary heat exchange tube bundle (221) is connected to the air outlet of the primary heat exchange tube bundle (211); the secondary cooling box (222) performs secondary heat exchange with the cracked gas in the secondary heat exchange tube bundle (221) by supplying circulating water.

3. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen according to claim 2, characterized in that, The number of the primary heat exchange tube bundles (211) is multiple and their inlet ends are respectively connected to the outlet ends of the primary flue gas distributor (213). The inlet end of the primary flue gas distributor (213) is connected to the outlet of the gravity dust collector (110) through a pipe. The number of the secondary heat exchange tube bundles (221) is multiple and their inlet ends are respectively connected to the outlet ends of the secondary flue gas distributor (223). The inlet end of the secondary flue gas distributor (223) is connected to the outlet end of the primary heat exchange tube bundle (211) through a pipe.

4. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen according to claim 3, characterized in that, Both the primary heat exchange tube bundle (211) and the secondary heat exchange tube bundle (221) are serpentine tube bundles.

5. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen gas according to claim 3 or 4, characterized in that, The circulating water in the primary cooling box (212) submerges the top surface of the primary heat exchange tube bundle (211) and the primary flue gas distributor (213), and the submersion height H2 is not less than 200mm. The circulating water in the secondary cooling box (222) submerges the top surface of the secondary heat exchange tube bundle (221) and the secondary flue gas distributor (223), and the submersion height H3 is not less than 200mm.

6. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen gas according to claim 1, characterized in that, The water tank (120) has its inlet located at its bottom and its outlet located at its top.

7. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen gas according to claim 6, characterized in that, The dust collector (100) is also provided with multiple horizontal pipes (130) and multiple vertical pipes (140). Multiple transverse pipes (130) are arranged at intervals and pass through the gravity dust collector (110) in a horizontal direction, while both ends are connected to the water tank (120); Multiple longitudinal pipes (140) are arranged at intervals and run longitudinally through the gravity dust collector (110) in the horizontal direction, while both ends are connected to the water tank (120).

8. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen gas according to claim 7, characterized in that, The circulating water in the water tank (120) submerges the top surface of the gravity dust collector (110), and the submersion height H1 is not less than 200mm.

9. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen gas according to claim 1, characterized in that, The gravity dust collector (110) is also provided with a baffle (150) in the middle. The baffle (150) extends downward from the top surface of the gravity dust collector (110) by a predetermined distance, dividing the top of the gravity dust collector (110) into two areas. The air inlet and air outlet of the gravity dust collector (110) are both located on the top of the gravity dust collector (110) and on both sides of the baffle (150).

10. The dust removal and cooling device for high-dust and high-concentration ultrahigh-temperature hydrogen gas according to claim 1, characterized in that, The parts of the dust collector (100) and the cooling device (200) that come into contact with the pyrolysis gas are both made of SUS316 stainless steel.

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