Coal gas decarburization hydrogen production device

Abstract

The application provides a coal gas decarburization hydrogen production device, which is improved on the original furnace body, reaction trays are arranged in a U-shaped structure for containing catalyst, and high-temperature gas directly flows into a U-shaped groove of the U-shaped structure through two arms of the U-shaped structure. Since the volume of the U-shaped groove is far less than the volume between the reaction cylinder body and the U-shaped groove, the high-temperature gas can fully contact the catalyst after diffusion in the U-shaped groove, and rapidly reacts with the catalyst, thereby avoiding the problem that the high-temperature gas cannot directly contact the catalyst after entering the space between the reaction cylinder body and the U-shaped groove and then gradually moving downward to the catalyst. Furthermore, since the decarburization expansion phenomenon occurs after the catalyst is contacted, the downward flowing gas cannot fully contact the catalyst after expansion after contacting the upper surface of the catalyst, the catalyst cannot fully react, and the hydrogen conversion rate is reduced.

Description

Technical Field

[0001] This invention relates to the field of decarbonization and hydrogen production technology, and particularly to a coalbed methane decarbonization and hydrogen production device. Background Technology

[0002] Existing hydrogen production methods mainly include water electrolysis, photocatalytic water splitting, carbon and hydrocarbon reforming to syngas, and catalytic cracking. With the large-scale development and utilization of natural gas, a clean production raw material has been provided for the production of carbon black and hydrogen. For example, Chinese patent (ZL89104111) provides a carbon black production method using natural gas as fuel and oxygen-enriched gas as a combustion aid. This method improves furnace temperature stability and ensures heating, but it does not effectively solve the problems of carbon black yield and quality, and it cannot simultaneously produce high-purity hydrogen. Chinese patent (ZL03152797.3) discloses a method for producing syngas by cracking and reforming methane-rich gas in a high-temperature carbon system. Methane is cracked and reformed in a partially gasified high-temperature carbon system (1150℃~1350℃) to produce syngas CO and H2. Chinese patent (ZL01118721.2) provides a microwave-excited methane conversion process for hydrogen production. These methods have problems such as high energy consumption, incomplete reaction, and emission of large amounts of greenhouse gas CO2. In addition, they require multiple subsequent processes such as carbon monoxide conversion, carbon dioxide removal and methanation to obtain hydrogen with high purity. The production cycle is long and high-quality carbon black cannot be produced at the same time.

[0003] Existing technologies also include methods for purifying hydrogen production by cracking methane and collecting carbon black. For example, a method for high-temperature methane cracking to co-produce carbon black and high-purity hydrogen, as described in application number 201010160179.9, uses low-calorific-value fuel gas (1300-1500 kcal / Nm3) as fuel and methane-containing gas as raw material. It employs a controlled oxygen supply to aid combustion and ensure complete combustion of the low-calorific-value fuel gas, alternating operation of the reactor for heat storage and exhaust of residual gas and methane cracking, creating an oxygen-free high-temperature methane cracking reaction environment. Specifically, this includes processes such as adjusting the combustion-supporting gas, heat storage and exhaust of residual gas in the reactor, methane cracking, carbon black collection, and hydrogen purification. This method can achieve increased production capacity and continuous, efficient production through multi-stage cascading of the cracking reactor. However, when high-temperature oxygen-free methane gas is introduced into the furnace, decarbonization and expansion occur upon contact with the catalyst, preventing sufficient contact between the gas and the catalyst. This results in untimely catalyst heating, thus limiting the improvement of hydrogen conversion rate. Summary of the Invention

[0004] The coal gas decarbonization and hydrogen production device provided by this invention achieves the technical objective of direct contact between high-temperature gas and catalyst based on the entry of high-temperature gas into the catalyst placement area.

[0005] This invention provides a coalbed methane decarbonization and hydrogen production device, comprising a reaction cylinder and a reaction tray placed inside the reaction cylinder. The reaction tray includes a U-shaped tray with an upward-facing U-shaped groove. Support arms extend outward from the ends of the two arms of the U-shaped groove, and the support arms are connected to the reaction cylinder. The open side of the U-shaped groove is a high-temperature reaction zone, and the other side is a high-temperature gas inlet zone. A thin layer of catalyst is laid on the bottom of the U-shaped groove. Secondary gas inlets are evenly distributed on both arms. A main gas inlet is opened on the side wall of the reaction cylinder located in the high-temperature gas inlet zone, and a gas outlet is opened on the side wall of the reaction cylinder located in the high-temperature reaction zone. The high-temperature gas inlet zone includes a first gas inlet zone corresponding to the bottom of the groove and a second gas inlet zone corresponding to the arms respectively. The first gas inlet zone and the second gas inlet zone are connected.

[0006] Preferably, the inner wall of the reaction cylinder is provided with an overlapping plate, and the support arm is placed on the overlapping plate.

[0007] Preferably, the support arm and the lap plate are provided with a male-female interlocking structure, which includes a protruding part and a recessed part that interlock.

[0008] Preferably, the end of the support arm is tightly fitted and connected to the inner wall of the reaction cylinder.

[0009] Preferably, the secondary air inlet is provided on the support arm.

[0010] Preferably, the angle between the support arm and the strut is a right angle.

[0011] Preferably, the connection between the support arm and the bottom of the groove is an arc structure, and the secondary air inlet is located above the arc structure.

[0012] Preferably, the connection between the support arm and the bottom of the groove is a chamfered structure, and the secondary air inlet is located above the chamfered structure.

[0013] Preferably, the main air intake is located in the middle of the first air intake zone.

[0014] Preferably, the volume of the high-temperature air intake zone is smaller than the volume of the high-temperature reaction zone.

[0015] Compared with the prior art, the beneficial effects of the present invention are:

[0016] 1. In this invention, the original furnace body is improved by setting the reaction tray as a U-shaped structure to hold the catalyst. The high-temperature gas flows directly into the U-shaped groove of the U-shaped structure through the two arms of the U-shaped structure. Since the volume of the U-shaped groove is much smaller than the volume between the reaction cylinder and the U-shaped groove, the high-temperature gas can fully contact the catalyst after diffusing in the U-shaped groove and quickly react with the catalyst. This avoids the problem in the prior art where the high-temperature gas enters the space between the reaction cylinder and the U-shaped groove, first fills the space, and then gradually moves downward to the catalyst, preventing the high-temperature gas from directly contacting the catalyst. Furthermore, since decarbonization and expansion occur after contacting the catalyst, the downward flowing gas expands after contacting the upper surface of the catalyst, which will prevent the downward flowing gas from fully contacting the catalyst. This will result in the catalyst not being able to react fully, reducing the hydrogen conversion rate.

[0017] Furthermore, a main air inlet is provided on the side wall of the reaction cylinder located in the high-temperature air inlet zone. This allows the high-temperature gas to first come into contact with the outer wall of the bottom of the U-shaped groove, preheating the outer wall of the groove, which in turn preheats the catalyst. This promotes the temperature rise of the catalyst and thus improves the reaction efficiency. Attached Figure Description

[0018] To more clearly illustrate the specific embodiments of the invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0019] Figure 1 This is a schematic diagram of the air intake and exhaust system using existing technology.

[0020] Figure 2 A schematic diagram of a coalbed methane decarbonization and hydrogen production unit (I);

[0021] Figure 3 Schematic diagram of a coalbed methane decarbonization and hydrogen production unit (II);

[0022] Figure 4 Schematic diagram of a coalbed methane decarbonization and hydrogen production unit (Part 3);

[0023] Among them, the reaction cylinder 1, U-shaped groove 3, support arm 4, support arm 5, groove bottom 6, high temperature reaction zone 7, high temperature air inlet zone 8, secondary air inlet 9, main air inlet 10, air outlet 11, overlapping plate 12, chamfered structure 13, arc structure 14, and heat-conducting fins 15. Detailed Implementation

[0024] The technical solution of the invention will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the invention, not all embodiments. Based on the embodiments of the invention, all other embodiments obtained by those skilled in the art without inventive effort are within the scope of protection of the invention.

[0025] In the description of the invention, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used solely for the convenience of describing the invention and for simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0026] In the description of the invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in the invention based on the specific circumstances.

[0027] like Figure 2-4As shown, this invention provides a coalbed methane decarbonization and hydrogen production device, including a reaction cylinder 1 for hydrogen production. The reaction cylinder 1 has an outlet for producing hydrogen gas. Inside the reaction cylinder 1 is a reaction tray. In the prior art, the reaction tray (i.e., the carrier holding the catalyst) is flat. High-temperature gas enters from above the reaction tray, with the entry point located at one end of the reaction cylinder 1. The outlet is located at the other end, also above the reaction tray. In this invention, the reaction tray includes a U-shaped tray with an upward-facing U-shaped groove 3. The U-shaped groove 3 provides a U-shaped reaction cavity. Support arms 5 extend outward from the ends of the two arms 4 of the U-shaped groove 3, and the support arms 5 are connected to the reaction cylinder 1. The connection method is not specified. Specifically, the space inside the reaction cylinder 1 can be divided into a high-temperature air intake zone 8 and a high-temperature reaction zone 7 from bottom to top. Specifically, the open side of the U-shaped groove 3 is the high-temperature reaction zone 7, and the other side is the high-temperature air intake zone 8. The high-temperature air intake zone 8 can be a sealed environment formed by the reaction tray, the reaction cylinder 1, and the caps at both ends of the reaction cylinder 1. Since forming a sealed environment is existing technology, it will not be elaborated here, but only illustrated by the following example: First, when an overlapping plate 12 is provided on the inner wall of the reaction cylinder 1, the support arm 5 is placed on the overlapping plate 12. A sealing structure is provided on the connecting surface between the support arm 5 and the overlapping plate 12. The sealing structure can be a high-temperature resistant sealing strip or a mechanical structure. The sealing, as a feasible mechanical seal structure, involves a male-female interlocking structure on the support arm 5 and the overlapping plate 12. This interlocking structure includes a protruding part and a recessed part for interlocking connection. It should be noted that the flow rate of high-temperature gas during this reaction process is not large, nor is the pressure particularly high, so there is no need to worry about the reaction tray being lifted by the gas. Secondly, when the end of the support arm 5 is tightly connected to the inner wall of the reaction cylinder 1, ensuring that the end (i.e., the outer edge) of the support arm 5 can adhere to the inner wall of the reaction cylinder 1 will prevent high-temperature gas from flowing out between the support arm 5 and the inner wall of the reaction cylinder 1. In this case, the high-temperature gas can only enter the high-temperature reaction zone 7 through the secondary inlet 9 described below. Thirdly... The connection between the two ends of the reaction tray and the cover can also refer to the two connection methods mentioned above, as long as the high-temperature air intake zone 8 is formed into a sealed environment; or it can be a non-sealed environment. In this case, when only the support arm 5 is set, a secondary air intake 9 is opened on the support arm 5, and some gas can enter the high-temperature reaction zone 7. When there is an overlap plate 12, a hole is also opened at the corresponding position of the overlap plate 12 to connect to the secondary air intake 9; the diameter of the secondary air intake 9 here can be smaller than the diameter on the support arm 4, or the number of them can be less than the number on the support arm; the connection between the two ends of the reaction tray and the cover here can still refer to the two connection methods mentioned above, forming a relatively sealed environment for the high-temperature air intake zone 8.

[0028] The high-temperature reaction zone 7 and the high-temperature intake zone 8 are respectively equipped with a first temperature sensor and a second temperature sensor. When the temperature difference between the first temperature sensor and the second temperature sensor is greater than a preset difference, it indicates that the temperature of the high-temperature intake zone 8 is too low and the gas temperature needs to be increased. It should be noted that the temperature value measured by the second temperature sensor cannot be used alone. The reason is that the high-temperature intake zone 8 preheats the catalyst and loses some heat. The second temperature sensor measures the local temperature of the high-temperature intake zone 8, which cannot fully indicate the overall temperature of the high-temperature intake zone 8. After the reaction, the heat of the mixed gas in the high-temperature reaction zone 7 is no longer lost. Therefore, the difference between the two can be used to accurately determine whether the overall temperature of the high-temperature intake zone 8 is too low.

[0029] Specifically, the bottom 6 of the U-shaped trough 3 is covered with a thin layer of catalyst, which is suitable for on-site construction, making full use of energy and taking into account gas production efficiency. The preferred size of the U-shaped trough 3 is 300*240*110 (length, width and height), but other sizes are not excluded. Secondary air inlets 9 are evenly distributed on the two arms 4. The main air inlet 10 is opened on the side wall of the reaction cylinder 1 located in the high-temperature air inlet zone 8, and the air outlet 11 is opened on the side wall of the reaction cylinder 1 located in the high-temperature reaction zone 7. The high-temperature air inlet zone 8 includes a first air inlet zone corresponding to the bottom 6 and a second air inlet zone corresponding to the arms 4 respectively. The first air inlet zone and the second air inlet zone are connected.

[0030] In summary, improvements were made to the existing furnace body by designing the reaction tray as a U-shaped structure to hold the catalyst. High-temperature gas flows directly into the U-shaped groove 3 through the two arms 4 of the U-shaped structure. Since the volume of the U-shaped groove 3 is much smaller than the volume between the reaction cylinder 1 and the U-shaped groove 3, the high-temperature gas can fully contact the catalyst after diffusing in the U-shaped groove 3 and rapidly react with it, avoiding the problems found in existing technologies (such as...). Figure 1 As shown, after the high-temperature gas enters the space between the reaction cylinder 1 and the U-shaped groove 3, it first fills the space and then gradually moves downwards to the catalyst. This causes the high-temperature gas to be unable to enter and directly contact the catalyst. Furthermore, since decarbonization and expansion will occur after contacting the catalyst, the downward-flowing gas will expand after contacting the upper surface of the catalyst. This will result in the downward-flowing gas not being able to fully contact the catalyst, which will cause the catalyst to not react fully and reduce the hydrogen conversion rate.

[0031] Furthermore, a main air inlet 10 is provided on the side wall of the reaction cylinder 1 located in the high-temperature air inlet zone 8, so that the high-temperature gas first contacts the outer wall of the bottom 6 of the U-shaped groove 3, preheating the outer wall of the bottom 6, which is to preheat the catalyst, thus promoting the temperature rise of the catalyst and improving the reaction efficiency.

[0032] As one specific implementation, the angle between the support arm 5 and the support arm 4 in this invention is a right angle, but it can also be other angles, as long as the support arm 5 can provide stable support.

[0033] As a specific implementation scheme, in order to avoid the expansion catalyst from hindering the flow of high-temperature gas, the connection between the support arm 4 and the bottom of the tank 6 in this invention is an arc structure 14 or a chamfer structure 13, and the secondary air inlet 9 is located above the arc structure 14, so that the catalyst cannot stay at the connection, that is, to ensure that there is a gap between the catalyst laying area and the secondary air inlet 9; on the other hand, the upward expansion characteristic of the catalyst is utilized here, and when there is a gap, the catalyst will not block the secondary air inlet 9.

[0034] As a specific implementation scheme, in order to ensure uniform ventilation, the main air inlet 10 is located in the middle of the first air inlet zone in this invention.

[0035] As a specific implementation scheme, in order to ensure the heating effect of the high-temperature air intake zone 8 and the space for the gas generated after the reaction in the high-temperature reaction zone 7, the volume of the high-temperature air intake zone 8 is smaller than the volume of the high-temperature reaction zone 7 in this invention.

[0036] As a specific implementation scheme, in order to ensure the preheating effect, a number of heat-conducting fins 15 are arranged on the outer wall of the tank bottom 6 in this invention.

[0037] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention in any way. It should be noted that those skilled in the art can make various improvements and modifications without departing from the principles of the present invention, and these improvements and modifications should also be considered within the scope of protection of the present invention.

Claims

1. A coal gas decarburization hydrogen production device, characterized by, The reaction device includes a reaction cylinder and a reaction tray placed inside the reaction cylinder. The reaction tray includes a U-shaped tray with an upward-facing U-shaped groove. Support arms extend outward from the ends of the two arms of the U-shaped groove and are connected to the reaction cylinder. The open side of the U-shaped groove is a high-temperature reaction zone, and the other side is a high-temperature gas inlet zone. A thin layer of catalyst is laid at the bottom of the U-shaped groove. Secondary gas inlets are evenly distributed on both arms. A main gas inlet is opened on the side wall of the reaction cylinder within the high-temperature gas inlet zone, and a gas outlet is opened on the side wall of the reaction cylinder within the high-temperature reaction zone. The high-temperature gas inlet zone includes a first gas inlet zone corresponding to the bottom of the groove and a second gas inlet zone corresponding to each arm. The first gas inlet zone and the second gas inlet zone are connected. The volume of the high-temperature air intake zone is smaller than the volume of the high-temperature reaction zone.

2. The coal gas decarbonization and hydrogen production apparatus according to claim 1, characterized in that, An overlapping plate is provided on the inner wall of the reaction cylinder, and the support arm is placed on the overlapping plate.

3. The coal gas decarburization hydrogen production device according to claim 2, characterized in that, The support arm and the lap plate are provided with a male and female interlocking structure, which includes a protruding part and a recessed part that interlock.

4. The coal gas decarburization hydrogen production device according to claim 1, characterized in that, The end of the support arm is tightly fitted and connected to the inner wall of the reaction cylinder.

5. The coal gas decarburization hydrogen production device according to claim 3 or 4, characterized in that, The support arm has a secondary air inlet.

6. The coal gas decarburization hydrogen production device according to claim 5, characterized in that, The angle between the support arm and the bracket arm is a right angle.

7. The coal gas decarburization hydrogen production device according to claim 1, characterized in that, The connection between the support arm and the bottom of the groove is an arc structure, and the secondary air inlet is located above the arc structure.

8. The coal gas decarbonization and hydrogen production apparatus according to claim 1, characterized in that, The connection between the support arm and the bottom of the groove is a chamfered structure, and the secondary air inlet is located above the chamfered structure.

9. The coal gas decarburization hydrogen production device according to claim 1, characterized in that, The main air intake is located in the middle of the first air intake zone.

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