Plasma hydrogen production, oxygen and natural gas mixed combustion system

Abstract

The invention relates to the technical field of hydrogen fuel application, in particular to a plasma hydrogen production and oxygen and natural gas mixed combustion system which is mainly composed of a natural gas reaction device, a heat exchange device, a carbon powder taking device, a natural gas combustion device, a first gas mixing device, a second gas mixing device and an oxygen production device. Firstly, hydrogen is prepared and generated through the natural gas reaction device, then oxygen is prepared through the oxygen generation device, the hydrogen and the oxygen are mixed into natural gas through the gas mixing device, then combustion is conducted through the natural gas combustion device, the combustion efficiency of the natural gas can be greatly improved, and the natural gas is saved by 40% or above; a large amount of carbon powder can be recycled; and the emission of carbon dioxide is greatly reduced.

Description

Technical Field

[0001] The present application relates to the technical field of methane cracking hydrogen production, and in particular to a plasma hydrogen production and oxygen and natural gas mixed combustion system. Background Art

[0002] As national emission regulations become increasingly stringent, many factories have dismantled coal-fired boilers and upgraded them to natural gas boilers. At the same time, the world's energy is increasingly scarce, and people are increasingly in-depth in the search for alternative energy sources. The main alternative fuels currently used are natural gas, combustible ice, shale gas, coal gas, hydrogen, alcohol ether fuel and biomass fuel. However, due to the shortage of supply and seasonal gas shortages in some areas where natural gas resources are scarce, the production of enterprises and the lives of residents have been seriously affected. At the same time, many chemical plants' production equipment produces hydrogen as a by-product, but its supply is not enough to support the boiler system that burns hydrogen alone. There is no sufficient scale benefit for purifying and compressing such hydrogen sources, resulting in the fact that many factories have failed to effectively utilize hydrogen, and it is discharged into the atmosphere in vain, resulting in a waste of this clean and high-quality energy. Blending these precious clean energy with existing natural gas is a reasonable and effective way to turn waste into treasure without increasing the environmental load.

[0003] The natural gas combustion system in the prior art generally uses a single natural gas as fuel, which has low combustion efficiency and produces a large amount of carbon dioxide. For example, when using an existing natural gas stove, 3m 3 The heat generated by natural gas combustion is 21,000 kcal, the combustion efficiency of natural gas is about 80%, and the carbon dioxide emissions are 5,500 grams. It can be seen that using a single natural gas fuel to pass through the natural gas combustion system will have the disadvantages of low natural gas combustion efficiency and high carbon dioxide emissions. Summary of the invention

[0004] In view of this, the purpose of this application is to provide a plasma hydrogen production and oxygen and natural gas mixed combustion system, so as to improve the combustion efficiency of natural gas and save more than 40% of natural gas; and to recover a large amount of carbon powder; and to greatly reduce the emission of carbon dioxide.

[0005] The first aspect of the embodiment of the present application discloses a plasma hydrogen production and oxygen and natural gas mixed combustion system, including a natural gas combustion device, and also including:

[0006] A natural gas reaction device, wherein the natural gas reaction device performs electrolysis and cracking reactions on natural gas;

[0007] a heat exchange device, the heat exchange device being connected to the natural gas reaction device and cooling the product of the natural gas reaction device;

[0008] A carbon powder taking device, the carbon powder taking device is connected to the heat exchange device and performs gas-solid separation on the product of the heat exchange device;

[0009] An oxygen generator, wherein the oxygen generator generates oxygen according to the required oxygen concentration;

[0010] a second gas mixing device, the second gas mixing device being in communication with the oxygen production device and mixing a product of the oxygen production device with natural gas;

[0011] The first gas mixing device is connected to the carbon powder taking device, the natural gas combustion device and the second gas mixing device respectively, and mixes the gas product of the carbon powder taking device and the product of the second gas mixing device and then sends them to the natural gas combustion device.

[0012] In one embodiment, the natural gas reaction device includes: a plasma generator, the air inlet end of the plasma generator is connected to a natural gas source; a first cracking chamber, the injection end of the plasma generator is arranged inside the first cracking chamber; a second cracking chamber, the second cracking chamber is connected to the first cracking chamber, the air inlet end and the air outlet end of the second cracking chamber are respectively provided with baffles, and the baffles are provided with vents.

[0013] In one embodiment, the natural gas reaction device further comprises: a first thermal insulation layer, which is wrapped around the outside of the first cracking chamber; and a second thermal insulation layer, which is wrapped around the outside of the second cracking chamber.

[0014] In one embodiment, the temperature of the arc generated by the plasma generator is 800-2000°C, and the spray range of the arc covers the space inside the first cracking chamber; the length of the first cracking chamber is 25-45cm and the diameter is 5-8cm; the length of the second cracking chamber is greater than or equal to the length of the first cracking chamber, and the diameter of the second cracking chamber is 6-12cm and greater than the diameter of the first cracking chamber; the diameter of the baffle is 3-8cm, and the baffle is provided with 18-36 ventilation holes, and the aperture of the ventilation holes is 0.4-1㎜.

[0015] In one embodiment, the temperature of the arc generated by the plasma generator is 2000°C, and the spray range of the arc covers the space in the first cracking chamber; the length of the first cracking chamber is 30 cm and the diameter is 6 cm; the length of the second cracking chamber is 30 cm and the diameter is 8 cm; the diameter of the baffle is 6 cm, and 24 ventilation holes are provided on the baffle, and the aperture of the ventilation holes is 0.8 mm.

[0016] In one embodiment, the carbon powder removal device includes: a collection chamber; a mounting frame, the mounting frame is arranged in the collection chamber, and the surface of the mounting frame has a separation membrane; a transmission part, the mounting frame is movably cooperated with the collection chamber through the transmission part; and a driving part, the driving part is connected to the transmission part.

[0017] In one embodiment, the transmission part includes a rotating shaft, both ends of which are movably connected to the collecting chamber respectively, and the mounting frame is arranged on the rotating shaft; the driving part includes a first motor, and the output end of the first motor is connected to the end of the rotating shaft.

[0018] In one embodiment, the transmission part includes a screw and a screw nut that cooperate with each other in transmission, the two ends of the screw are respectively movably connected to the collecting chamber, and the mounting frame is arranged on the screw nut; the driving part includes a second motor, and the output end of the second motor is connected to the end of the screw.

[0019] In one embodiment, it also includes a catalytic device, which is connected to the carbon powder taking device and the first gas mixing device respectively, and the catalytic device includes: a catalytic chamber; a net bag, which is arranged in the catalytic chamber; and a heating component, which is arranged outside the catalytic chamber.

[0020] In one embodiment, the heating assembly includes a heating tube wrapped around the outside of the catalytic chamber, the inlet end of the heating tube is connected to the first inlet of the heat exchange device, and the outlet end of the heating tube is connected to the first outlet of the heat exchange device.

[0021] The present application adopts a combustion system consisting of a natural gas reaction device, a heat exchange device, a carbon powder extraction device, a natural gas combustion device, a first gas mixing device, a second gas mixing device and an oxygen production device, and through the design of a gas loop, firstly prepares hydrogen through the natural gas reaction device, then prepares oxygen through the oxygen production device, and mixes hydrogen and oxygen into natural gas through the gas mixing device, and then burns through the natural gas combustion device, which can greatly improve the combustion efficiency of natural gas and save more than 40% of natural gas; and can also recover a large amount of carbon powder; and greatly reduce the emission of carbon dioxide. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0023] Figure 1It is a structural schematic diagram of a plasma hydrogen production and oxygen and natural gas mixed combustion system from a first perspective disclosed in the first embodiment of the present application;

[0024] Figure 2 yes Figure 1 Schematic diagram of the structure of the natural gas reaction device;

[0025] Figure 3 yes Figure 1 A schematic diagram of the structure of the heat exchange device;

[0026] Figure 4 yes Figure 1 A schematic structural diagram of a first embodiment of a device for extracting carbon powder;

[0027] Figure 5 yes Figure 1 A schematic structural diagram of a second embodiment of a device for extracting carbon powder;

[0028] Reference numerals:

[0029] 1-natural gas reaction device, 11-plasma generator, 12-first cracking chamber, 13-second cracking chamber, 14-blocking net, 15-vent, 16-first insulation layer, 17-second insulation layer;

[0030] 2-heat exchange device, 21-first inlet, 22-second inlet, 23-second outlet, 24-second outlet;

[0031] 3-carbon powder taking device, 31-collecting chamber, 32-third outlet, 33-rotating shaft, 331′-screw, 332′-screw slider, 34-first motor, 34′-second motor, 35-fourth outlet, 36-metal ion membrane, 37-mounting frame, 38-third inlet;

[0032] 4-catalytic device, 41-heating component, 42-net bag;

[0033] 5-Natural gas combustion device

[0034] 6-first gas mixing device, 61-fifth outlet, 62-fourth inlet, 63-fifth inlet;

[0035] 7-second gas mixing device, 71-sixth outlet, 72-sixth inlet, 73-seventh inlet;

[0036] 8-Oxygen Generator

[0037] 100 - first pipeline, 110 - second pipeline, 120 - third pipeline, 130 - fourth pipeline, 140 - fifth pipeline, 150 - sixth pipeline, 160 - seventh pipeline, 170 - eighth pipeline, 180 - ninth pipeline, 190 - tenth pipeline;

[0038] 200 - first refrigerant pipeline, 210 - second refrigerant pipeline. DETAILED DESCRIPTION

[0039] The following will be combined with the drawings in the embodiments of the present application to clearly and completely describe the technical solutions in the embodiments of the present application. Obviously, the described embodiments are only part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of this application.

[0040] In the present invention, the directions or positional relationships indicated by "upper", "lower", "outer", etc. are based on the directions or positional relationships shown in the drawings. These terms are mainly used to better describe the present invention and its embodiments, and are not used to limit the indicated devices, elements or components to have a specific direction, or to be constructed and operated in a specific direction.

[0041] In addition, some of the above terms may be used to express other meanings in addition to indicating orientation or positional relationship. For example, the term "on" may also be used to express a certain dependency or connection relationship in some cases. For those skilled in the art, the specific meanings of these terms in the present invention can be understood according to specific circumstances.

[0042] In addition, the terms "installed", "set", "provided with", and "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral structure; it can be a mechanical connection, or an electrical connection; it can be a direct connection, or an indirect connection through an intermediate medium, or it can be an internal connection between two devices, elements, or components. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0043] In addition, the terms "first", "second", etc. are mainly used to distinguish different devices, elements or components (the specific types and structures may be the same or different), and are not used to indicate or imply the relative importance and quantity of the indicated devices, elements or components. Unless otherwise specified, "plurality" means two or more.

[0044] The inventive concept of the present invention is that the natural gas combustion system in the prior art only uses a single natural gas as fuel, and the combustion efficiency is low and a large amount of carbon dioxide will be generated during the combustion process. It can be seen that the technical problem to be solved by the present invention is how to improve the combustion efficiency of natural gas and reduce the emission of carbon dioxide. In order to solve the above technical problems, the present invention provides a plasma hydrogen production and oxygen and natural gas mixed combustion system, which is mainly composed of a natural gas reaction device 1, a heat exchange device 2, a carbon powder extraction device 3, an oxygen production device 8, a first gas mixing device 6, a second gas mixing device 7 and a natural gas combustion device 5. The specific structure is as follows:

[0045] Example 1

[0046] like Figure 1 The plasma hydrogen production and oxygen and natural gas mixed combustion system shown includes a natural gas combustion device 5. The specific natural gas combustion device 5 includes a natural gas stove, a boiler burner, a dryer, etc. used by the user terminal.

[0047] The system further comprises: a natural gas reaction device 1, which performs electrolysis and cracking reaction on natural gas. Specifically, the natural gas reaction device 1 is directly connected to a natural gas source through a first pipeline 100. The natural gas source can be residential pipeline natural gas, wherein the methane content is more than 98%;

[0048] The heat exchange device 2 is connected to the natural gas reaction device 1, and the heat exchange device 2 cools down the product of the natural gas reaction device 1. The specific heat exchange device 2 can be a shell and tube heat exchanger, and the second inlet 22 of the shell and tube heat exchanger is connected to the natural gas reaction device 1 through the second pipeline 110;

[0049] A carbon powder taking device 3 is connected to the heat exchange device 2, and the carbon powder taking device 3 performs gas-solid separation on the product of the heat exchange device 2. Specifically, the second outlet 23 of the shell and tube heat exchanger is connected to the carbon powder taking device 3 through the third pipeline 120;

[0050] The oxygen generator 8 generates oxygen according to the required oxygen concentration. Specifically, the oxygen generator 8 may be a molecular sieve oxygen generator. The air inlet end of the molecular sieve oxygen generator is connected to the air source through the tenth pipeline 190.

[0051] The second gas mixing device 7 is connected to the oxygen making device 8. The second gas mixing device 7 mixes the product of the oxygen making device 8 with natural gas. Specifically, the second gas mixing device 7 can be a gas mixer B. The gas mixer B has a sixth outlet 71, a fifth inlet 72 and a sixth inlet 73. The gas outlet of the molecular sieve oxygen making machine is connected to the seventh inlet 73 of the gas mixer B through a ninth pipeline 180. The sixth inlet 72 of the gas mixer B is connected to a natural gas source through an eighth pipeline 170. The natural gas source can be a residential pipeline natural gas, wherein the methane content is more than 98%;

[0052] The first gas mixing device 6 is connected with the carbon powder taking device 3, the natural gas combustion device 5 and the second gas mixing device 7 respectively, and mixes the gas product of the carbon powder taking device 3 and the product of the second gas mixing device 7 and then sends them to the natural gas combustion device 5. The specific first gas mixing device 6 can adopt a gas mixer A, and the gas mixer A has a fifth outlet 61, a fourth inlet 62 and a fifth inlet 63. The fourth inlet 62 of the gas mixer A is connected with the carbon powder taking device 3 through the fifth pipeline 140, and the fifth outlet 61 of the gas mixer A is connected with the natural gas combustion device 5 through the sixth pipeline 150. The fifth inlet 63 of the gas mixer A is connected with the sixth outlet 71 of the gas mixer B through the ninth pipeline 180. At the same time, the gas mixer A can also be connected with the air source through the eleventh pipeline.

[0053] In order to facilitate the control of the flow rate of fluid in each pipeline, pipeline solenoid valves are respectively provided in the first pipeline 100, the second pipeline 110, the third pipeline 120, the fourth pipeline 130, the fifth pipeline 140, the sixth pipeline 150, the seventh pipeline 160, the eighth pipeline 170, the ninth pipeline 180, the tenth pipeline 190 and the eleventh pipeline.

[0054] The working principle of this system is as follows (for example, the mixed air, oxygen, hydrogen, and natural gas are passed into the natural gas combustion device for combustion):

[0055] First, natural gas provided by a natural gas source (for example, 3 cubic meters of natural gas is introduced into the first pipeline 100 and the eighth pipeline 170 in total) is partially introduced into the natural gas reaction device 1 through the first pipeline 100. The natural gas reaction device 1 generates an electric field to electrolyze the methane component in the natural gas introduced therein, ionizing the methane into active ions such as carbon ions and hydrogen ions. Secondly, under the action of the electric field, the carbon ions and hydrogen ions move and collide, generating a high-temperature arc, and the high-temperature arc causes the methane to be cracked under high-temperature conditions to generate The products are hydrogen (e.g., 6 cubic meters of hydrogen) and nano-scale carbon powder (e.g., 1500 grams of carbon powder), and the products (hydrogen and nano-scale carbon powder) generated by the reaction are sent to the heat exchange device 2 through the second pipeline 110. The heat exchange device 2 cools the above products (hydrogen and nano-scale carbon powder), usually from 800°C to 40-60°C (e.g., specifically from 800°C to room temperature). The heat exchange device 2 sends the cooled products to the carbon powder taking device 3 through the third pipeline 120. The carbon powder taking device 3 performs gas-solid separation on the above products. After the treatment, the hydrogen and the nano-scale carbon powder are separated (for example, 6 cubic meters of hydrogen and 1500 grams of carbon powder are obtained after the gas-solid separation treatment), and the hydrogen generated by the gas-solid separation treatment is sent to the first gas mixing device 6 through the fifth pipeline 140; secondly, the air provided by the air source (for example, 6 cubic meters of air) is sent to the oxygen generator 8 through the tenth pipeline 190, and the oxygen generator 8 uses the pressurized adsorption and atmospheric pressure desorption (HP) method to treat the air to generate oxygen (for example, 3 cubic meters of oxygen), and the prepared oxygen is sent to the first gas mixing device 6 through the ninth pipeline 180. The second gas mixing device 7 is provided with another part of natural gas provided by the natural gas source, and is sent to the second gas mixing device 7 through the eighth pipeline 170. The second gas mixing device 7 mixes oxygen and natural gas, and sends the treated mixed gas to the first gas mixing device 6 through the seventh pipeline 160. 3 cubic meters of air are introduced into the first gas mixing device 6 through the eleventh pipeline. After the first gas mixing device 6 mixes the air, oxygen, hydrogen and natural gas, it is sent to the natural gas combustion device 5 through the sixth pipeline 150 for combustion.

[0056] The combustion system provided in this embodiment mainly consists of a natural gas reaction device 1, a heat exchange device 2, a carbon powder taking device 3, an oxygen production device 8, a first gas mixing device 6, a second gas mixing device 7 and a natural gas combustion device 5. First, the natural gas reaction device 1 generates an electric field to electrolyze the methane component in the natural gas introduced therein, and ionizes the methane into active ions such as carbon ions and hydrogen ions. Secondly, under the action of the electric field, the carbon ions and hydrogen ions move and collide to generate a high-temperature arc, and the methane is cracked under high temperature conditions through the high-temperature arc to generate products of hydrogen and nano-scale carbon powder. Since the product after the cracking reaction has a very high temperature, in order to avoid the high-temperature product from damaging the subsequent process equipment, thereby making the entire process unable to continue, it is necessary to set a heat exchange device 2 connected to the natural gas reaction device 1, so that the product after the cracking of the natural gas reaction device 1 is cooled by the heat exchange device 2. Secondly, the carbon powder taking device 3 performs gas-solid separation on the cooled product to obtain a gas product (hydrogen), and the carbon powder taking device 3 is connected to the first gas mixing device 6 to allow the gas product (hydrogen) to be passed into the first gas mixing device 6;

[0057] An oxygen generator 8 is provided again to generate oxygen according to the required oxygen concentration, and the oxygen generator 8 is connected to the second gas mixing device 7, so that the prepared oxygen is passed into the second gas mixing device 7, the second gas mixing device 7 mixes the oxygen and the natural gas, and the second gas mixing device 7 is connected to the first gas mixing device 6, so that the mixed oxygen and the natural gas are passed into the first gas mixing device 6 together, and the oxygen, hydrogen and the natural gas are mixed by the first gas mixing device 6 and then passed into the natural gas combustion device 5 together for combustion;

[0058] Therefore, the above system can greatly improve the combustion efficiency of natural gas and save more than 40% of natural gas (for example, as shown in Table 1, when natural gas is directly used as a single fuel to be passed into a natural gas combustion device for combustion, 21,000 kcal of heat is generated, and 3 m 3 The natural gas combustion efficiency is 82.35%. When the above system is used to generate 20,000 kcal of heat, only 1.5 m 3 natural gas, the natural gas combustion efficiency is about 160%); and a large amount of carbon powder can be recovered; and the emission of carbon dioxide is greatly reduced (for example, as shown in Table 2, when natural gas is directly used as a single fuel to pass into the natural gas combustion device for combustion, 21,000 kcal of heat is generated, and 3 m 3 of natural gas, producing 5500 grams of carbon dioxide emissions, while the above system only consumes 1.5m 3 of natural gas, producing 275 grams of carbon dioxide emissions).

[0059] Table 1 Comparison of natural gas combustion efficiency

[0060]

[0061]

[0062] The specific calculation of natural gas combustion efficiency is as follows:

[0063] First, the calorific value of natural gas is about 8500-9100 kcal / m3 (here we take the common value of 8500 kcal / m3);

[0064] Secondly, the intake volume is known to be V = 3 cubic meters. The heat that should be generated theoretically is Qtheoretical = 8500*3 = 25500 kcal, and the actual heat generated is Qactual = 21000;

[0065] The final calculated combustion efficiency = Qactual / Qtheoretical*100%=21000 / 25500*100%=82.35%.

[0066] Table 2 Comparison of carbon dioxide emissions

[0067]

[0068]

[0069] In order to improve the cracking efficiency of methane in natural gas, in this example, the natural gas reaction device 1 preferably includes: a plasma generator 11, the air inlet end of the plasma generator 11 is connected to the natural gas source; a first cracking chamber 12, the injection end of the plasma generator 11 is arranged inside the first cracking chamber 12; a second cracking chamber 13, the second cracking chamber 13 is connected to the first cracking chamber 12, and the air inlet end and the air outlet end of the second cracking chamber 13 are respectively provided with a baffle 14, and the baffle 14 is provided with a vent 15.

[0070] In this embodiment, a plasma generator 11 is first provided. Specifically, the plasma generator 11 may be a high current plasma generator as disclosed in the prior art CN216057599U. Figure 1The specific structure includes an arc main pole, an arc main body with a cathode connection end, and an anode installed in the installation hole. First, the arc main pole and the anode are energized respectively to generate an electric field between the cathode and the anode. The electric field ionizes methane into carbon ions and hydrogen ions, that is, high-energy electrons ionize methane into active ions such as carbon ions and hydrogen ions through inelastic collisions with methane molecules. The carbon ions and hydrogen ions are then moved and collided by the electric field to generate a high-temperature arc. The high-temperature arc causes the methane gas to undergo a cracking reaction under high temperature conditions. At the same time, the fluidity of natural gas under high temperature and high pressure is affected by temperature and pressure. Studies have shown that the fluidity of natural gas increases with increasing temperature. This is because under high temperature conditions, the movement speed of natural gas molecules is accelerated, making them easier to flow and diffuse. In order to effectively ensure the residence time of natural gas in a high temperature environment, a first cracking chamber 12 and a second cracking chamber 13 are arranged to be interconnected. During the first cracking of methane in the natural gas by the plasma generator 11 in the first cracking chamber 12, the generated products (hydrogen and nano-scale carbon powder) will have a very high temperature. After the high-temperature gas continues to flow to the second cracking chamber 13, the second cracking chamber 13 will have a certain temperature (even if the methane in the natural gas that has not been cracked in the first cracking chamber 12 continues to undergo a second cracking). Therefore, by designing two cracking chambers, the high-temperature environment covers a larger area, thereby increasing the residence time of natural gas in a high-temperature environment. At the same time, since the density of hydrogen is smaller than that of natural gas, the weight of hydrogen of the same volume is lighter than that of natural gas. Therefore, in the same temperature environment, the flow rate of hydrogen is faster than that of natural gas. Based on the above principle, by respectively placing the first cracking chamber 12 in the second cracking chamber 13, the second cracking chamber 13 will have a certain temperature (even if the methane in the natural gas that has not been cracked in the first cracking chamber 12 continues to undergo a second cracking). The air inlet and air outlet of the second cracking chamber 13 are provided with a baffle 14, and the baffle 14 is provided with an air vent 15. Since the hydrogen in the first cracking chamber 12 flows faster, it can drive part of the natural gas to flow to the air vent 15 provided on the baffle 14 at the air inlet of the second cracking chamber 13, so that a gas wall can be formed at the air vent 15, so that the unreacted natural gas in the first cracking chamber 12 hits the gas wall driven by the hydrogen and then flows back to the first cracking chamber 12 for cracking reaction. Similarly, the second cracking chamber 1 Since the hydrogen in the first cracking chamber 12 flows faster, it can drive part of the natural gas to flow to the vent 15 provided on the baffle 14 at the gas outlet of the second cracking chamber 13, so that a gas wall can be formed at the vent 15, so that the unreacted natural gas in the second cracking chamber 13 hits the gas wall driven by the hydrogen and then flows back to the second cracking chamber 13 for cracking reaction. The baffle 14 is respectively provided at the gas inlet and gas outlet of the second cracking chamber 13, so that the residence time of the natural gas in the high temperature environment is further increased. In summary, the structure composed of the first cracking chamber 12, the second cracking chamber 13 and the baffle 14 with the vent 15 can effectively increase the residence time of the natural gas in the high temperature environment, thereby increasing the efficiency of methane cracking in the natural gas.

[0071] In order to effectively maintain a high-temperature environment for cracking methane in natural gas, in this example, the natural gas f reaction device 1 preferably also includes: a first insulation layer 16, the first insulation layer 16 is wrapped around the outside of the first cracking chamber 12; specifically, when the shape of the first cracking chamber 12 is a cylinder, the shape of the first insulation layer 16 is also a cylinder, and the first insulation layer 16 is wrapped around the outer surface of the first cracking chamber 12 by a sleeve manner; a second insulation layer 17, the second insulation layer 17 is wrapped around the outside of the second cracking chamber 13, specifically when the shape of the second cracking chamber 13 is a cylinder, the shape of the second insulation layer 17 is also a cylinder, and the second insulation layer 17 is wrapped around the outer surface of the second cracking chamber 13 by a sleeve manner.

[0072] In this embodiment, the first cracking chamber 12 is wrapped with a first insulation layer 16 that matches its shape, and the second cracking chamber 13 is wrapped with a second insulation layer 17 that matches its shape. Through the respective actions of the first insulation layer 16 and the second insulation layer 17, the heat in the first cracking chamber 12 and the second cracking chamber 13 is less likely to diffuse to the outside, thereby effectively maintaining a high temperature environment for methane cracking in natural gas.

[0073] In order to further improve the cracking efficiency of methane in natural gas, the preferred plasma generator 11 of this example has an arc temperature of 800-2000°C, and the arc spray range covers the space inside the first cracking chamber 12; the length of the first cracking chamber 12 is 25-45cm, and the diameter is 5-8cm; the length of the second cracking chamber 13 is greater than or equal to the length of the first cracking chamber 12, and the diameter of the second cracking chamber 13 is 6-12cm and greater than the diameter of the first cracking chamber 12; the baffle 14 The diameter is 3-8cm, 18-36 ventilation holes 15 are provided on the blocking net 14, and the aperture of the ventilation holes 15 is 0.4-1㎜. Further preferably, the temperature of the arc generated by the plasma generator 11 is 2000℃; the length of the first cracking chamber 12 is 30cm and the diameter is 6cm; the length of the second cracking chamber 13 is 30cm and the diameter is 8cm; the diameter of the blocking net 14 is 6cm, and 24 ventilation holes 15 are provided on the blocking net 14, and the aperture of the ventilation holes 15 is 0.8㎜.

[0074] Specifically, when the shape of the first cracking chamber 12 is a cylinder, and the length of the first cracking chamber 12 is 30 cm and the diameter is 6 cm, the shape of the arc generated by the plasma generator 11 can be made cylindrical by controlling parameters such as the power of the plasma generator 11. At the same time, the length of the arc generated by the plasma generator 11 is made 30 cm, and the diameter of the cross section (i.e., circular) is made 6 cm, so that the spray range of the arc covers the space inside the first cracking chamber 12.

[0075] In this embodiment, by setting the above parameters, the cracking efficiency of methane is further improved, that is, the hydrogen production and the production of nano-scale carbon powder are higher, as shown in Table 1 (S1-9 in Table 1 correspond to Examples 1-9, D1-6 correspond to Comparative Examples 1-6, and in order to reflect the differences, the same points between Examples 2-9 and Comparative Examples 1-6 and Example 1 are not filled in):

[0076] Table 1

[0077]

[0078]

[0079] In order to effectively realize the gas-solid separation of hydrogen and nano-carbon powder, the present embodiment preferably comprises a carbon powder taking device 3 including: a collecting chamber 31. Specifically, in order to facilitate the collection of nano-carbon powder, the collecting chamber 31 has a third outlet 32, a third inlet 38 and a fourth outlet 35. The collecting chamber 31 is connected to the third pipeline 120 through the third inlet 38, and the collecting chamber 31 is connected to the fourth pipeline 130 through the fourth outlet 35. The outer wall of the lower half of the collecting chamber 31 is inclined toward the fourth outlet 35, that is, the diameter of the upper part of the lower half of the collecting chamber 31 is larger than the diameter of the third outlet 32 ​​arranged below the lower half of the collecting chamber. First, by setting the fourth outlet 35, it is convenient to The separated hydrogen enters the next process through the fourth outlet 35, and secondly, by setting an inclined outer wall and a third outlet 32, the inclined outer wall facilitates guiding the split nano-scale carbon powder to the third outlet 32; a mounting frame 37, the mounting frame 37 is arranged in the collection chamber 31, and a separation membrane is provided on the surface of the mounting frame 37. Specifically, in order to facilitate the adsorption of nano-scale carbon powder, since the carbon powder carries ions under high temperature environment and the particle size of the carbon powder is less than 100nm, the separation membrane can be a metal ion membrane with a pore size greater than or equal to 100nm; a transmission part, the mounting frame 37 is movably matched with the collection chamber 31 through the transmission part; a driving part, the driving part is connected to the transmission part.

[0080] In this example, a metal ion membrane is first used as the separation membrane. Since the pore size of the metal ion membrane is larger than the particle size of the carbon powder, and the carbon powder carries ions under high temperature environment, the charged carbon powder can be adsorbed on the metal ion membrane made of metal material through electrostatic effect. That is, when a charged object approaches a metal object, electrostatic induction will occur inside the metal object, causing the free electrons in the object to move to the surface, making the surface charged. Therefore, the potential generated by electrostatic induction and the static electricity of the charged object attract each other under the action of Coulomb force, so that adsorption occurs. Therefore, the charged carbon powder can be adsorbed first through the metal ion membrane. When the charged carbon powder completely blocks the through holes of the metal ion membrane, the nano-scale carbon powder will fall into the collection chamber 31 under the obstruction of the metal ion membrane, thereby completing the gas-solid separation of hydrogen and nano-scale carbon powder. Secondly, the metal ion membrane is installed on the mounting frame 37, and the mounting frame 37 is movably matched with the collection chamber 31 through the transmission part, and the transmission part is connected to the driving part, that is, the driving part can drive the transmission part to drive the mounting frame 37 to move, such as rotate or reciprocate, so that the nano-scale carbon powder initially adsorbed on the metal ion membrane on the mounting frame 37 is shaken off through the movement of the mounting frame 37, thereby completing the collection of nano-scale carbon powder.

[0081] In order to realize regular rotation of the separation membrane, in this embodiment, preferably, the transmission part includes a rotating shaft 33, both ends of the rotating shaft 33 are respectively movably connected to the collecting chamber 31, and the mounting frame 37 is arranged on the rotating shaft 33; the driving part includes a first motor 34, and the output end of the first motor 34 is connected to the end of the rotating shaft 33.

[0082] In this example, the mounting bracket 37 is arranged on the rotating shaft 33, and the output end of the first motor 34 is connected to the end of the rotating shaft 33. The specific first motor 34 can be a servo motor. Since the speed and position accuracy of the servo motor are very accurate, the driving force can be transmitted to the rotating shaft 33 by controlling the forward or reverse rotation of the servo motor, thereby driving the rotating shaft 33 to rotate forward or reverse regularly. Since the mounting bracket 37 is arranged on the rotating shaft 33, the rotating shaft 33 can drive the mounting bracket 37 to move regularly (i.e., forward or reverse), thereby making it easier to shake off the nano-scale carbon powder adsorbed on the metal ion membrane.

[0083] In order to realize regular reciprocating movement of the separation membrane, in this embodiment, preferably, the transmission part includes a screw rod 331′ and a screw nut 332′ that cooperate with each other, the two ends of the screw rod 331′ are respectively movably connected to the collection chamber 31, and the mounting bracket 37 is arranged on the screw nut 332′; the driving part includes a second motor 34′, and the output end of the second motor 34′ is connected to the end of the screw rod 331′.

[0084] In this example, the mounting bracket 37 is arranged on the screw nut 332′, and the output end of the second motor 34′ is connected to the end of the screw 331′. The specific second motor 34′ can be a servo motor. Since the speed and position accuracy of the servo motor are very accurate, the driving force can be transmitted to the screw 331′ by controlling the forward or reverse rotation of the servo motor, thereby driving the screw 331′ to rotate forward or reverse regularly. Since the screw nut 332′ and the screw 331′ are transmission-matched, i.e., threaded-matched, the screw nut 332′ can be driven to reciprocate on the screw 331′ along the direction of the screw 331′ through the screw 331′. Since the mounting bracket 37 is arranged on the screw nut 332′, the mounting bracket 37 can be driven to move regularly (i.e., reciprocate), thereby making it easier to shake off the nano-scale carbon powder adsorbed on the metal ion membrane.

[0085] In order to further improve the purity of the gas product in the carbon powder device (i.e., the purity of hydrogen), the present embodiment further comprises a plasma hydrogen production and oxygen and natural gas mixed combustion system further comprising a catalytic device 4, which is respectively connected to the carbon powder taking device 3 and the first gas mixing device 6, and the catalytic device 4 comprises: a catalytic chamber 43; a net bag 42, which is arranged in the catalytic chamber 43; and a heating component 41, which is arranged outside the catalytic chamber 43.

[0086] In order to further provide the temperature for the catalytic reaction, the preferred heating assembly 41 of this embodiment includes a heating tube wrapped around the outside of the catalytic chamber 43, the inlet end of the heating tube is connected to the first inlet 21 of the heat exchange device 2 through the first refrigerant pipeline 200, and the outlet end of the heating tube is connected to the first outlet 24 of the heat exchange device 2 through the second refrigerant pipeline 210.

[0087] In this example, the first outlet 24 of the heat exchange device 2 is connected to the outlet end of the heating tube through the second refrigerant pipeline 210, and the first inlet 21 of the heat exchange device 2 is connected to the inlet end of the heating tube through the first refrigerant pipeline 200. Thus, through the process of refrigerant heat exchange, the heat generated by the refrigerant is transferred to the heating tube, so that the catalytic chamber 43 is heated by the heating tube, thereby providing the temperature for the catalytic reaction.

[0088] Each embodiment in this specification is described in a progressive manner, and the same and similar parts between the embodiments can be referred to each other, and each embodiment focuses on the differences from other embodiments. The above are only embodiments of the present application and are not intended to limit the present application. For those skilled in the art, the present application may have various changes and variations. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present application should be included in the rights of the present application.

Claims

1. A plasma hydrogen production and oxygen and natural gas mixed combustion system, comprising a natural gas combustion device (5), characterized in that: Also includes: A natural gas reaction device (1), wherein the natural gas reaction device (1) performs electrolysis and cracking reactions on natural gas; A heat exchange device (2), the heat exchange device (2) being connected to the natural gas reaction device (1) and cooling the product of the natural gas reaction device (1); A carbon powder taking device (3), wherein the carbon powder taking device (3) is connected to the heat exchange device (2) and performs gas-solid separation on the product of the heat exchange device (2); An oxygen production device (8), wherein the oxygen production device (8) produces oxygen according to a required oxygen concentration; a second gas mixing device (7), the second gas mixing device (7) being connected to the oxygen production device (8) and mixing the product of the oxygen production device (8) with natural gas; A first gas mixing device (6), wherein the first gas mixing device (6) is respectively connected to the carbon powder extracting device (3), the natural gas combustion device (5) and the second gas mixing device (7), and mixes the gas product of the carbon powder extracting device (3) and the product of the second gas mixing device (7) and then feeds the mixed products into the natural gas combustion device (5).

2. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 1 is characterized in that: The natural gas reaction device (1) comprises: A plasma generator (11), wherein an air inlet end of the plasma generator (11) is connected to a natural gas source; A first cracking chamber (12), wherein the injection end of the plasma generator (11) is arranged inside the first cracking chamber (12); A second cracking chamber (13), wherein the second cracking chamber (13) is communicated with the first cracking chamber (12), and a baffle (14) is respectively provided at the air inlet end and the air outlet end of the second cracking chamber (13), and a vent hole (15) is provided on the baffle (14).

3. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 2 is characterized in that: The natural gas reaction device (1) further comprises: A first thermal insulation layer (16), wherein the first thermal insulation layer (16) is wrapped around the outside of the first cracking chamber (12); A second thermal insulation layer (17), wherein the second thermal insulation layer (17) is wrapped around the outside of the second cracking chamber (13).

4. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 2 or 3, characterized in that: The temperature of the arc generated by the plasma generator (11) is 800-2000° C., and the spray range of the arc covers the space inside the first cracking chamber (12); The first lysis chamber (12) has a length of 25-45 cm and a diameter of 5-8 cm; The length of the second lysis chamber (13) is greater than or equal to the length of the first lysis chamber (12), and the diameter of the second lysis chamber (13) is 6-12 cm and greater than the diameter of the first lysis chamber (12); The diameter of the blocking net (14) is 3-8 cm, and 18-36 ventilation holes (15) are arranged on the blocking net (14), and the aperture of the ventilation holes (15) is 0.4-1 mm.

5. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 2 or 3, characterized in that : The temperature of the arc generated by the plasma generator (11) is 2000° C., and the spray range of the arc covers the space inside the first cracking chamber (12); The first cracking chamber (12) has a length of 30 cm and a diameter of 6 cm; The second cracking chamber (13) has a length of 30 cm and a diameter of 8 cm; The diameter of the blocking net (14) is 6 cm, and 24 ventilation holes (15) are arranged on the blocking net (14), and the aperture of the ventilation holes (15) is 0.8 mm.

6. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 1 is characterized in that: The carbon powder taking device (3) comprises: A collecting chamber (31); A mounting frame (37), the mounting frame (37) being arranged in the collecting chamber (31), and a separation membrane being provided on a surface of the mounting frame (37); a transmission part, through which the mounting frame (37) movably cooperates with the collecting chamber (31); A driving part is connected to the transmission part.

7. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 6 is characterized in that: The transmission part comprises a rotating shaft (33), both ends of the rotating shaft (33) are movably connected to the collecting chamber (31), and the mounting frame (37) is arranged on the rotating shaft (33); The driving unit comprises a first motor (34), and an output end of the first motor (34) is connected to an end of the rotating shaft (33).

8. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 6 is characterized in that: The transmission part comprises a screw rod (331′) and a screw rod nut (332′) which are mutually transmission-coordinated, two ends of the screw rod (331′) are respectively movably connected to the collection chamber (31), and the mounting frame (37) is arranged on the screw rod nut (332′); The driving part comprises a second motor (34'), and an output end of the second motor (34') is connected to an end of the lead screw (331').

9. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 1 is characterized in that: The device further comprises a catalytic device (4), wherein the catalytic device (4) is connected to the carbon powder taking device (3) and the first gas mixing device (6) respectively, and the catalytic device (4) comprises: Catalytic chamber (43); A net bag (42), wherein the net bag (42) is arranged in the catalytic chamber (43); A heating component (41), wherein the heating component (41) is arranged outside the catalytic chamber (43).

10. The plasma hydrogen production and oxygen and natural gas mixed combustion system according to claim 9, characterized in that: The heating assembly (41) comprises a heating tube wrapped around the outside of the catalytic chamber (43), the inlet end of the heating tube being connected to the first inlet (21) of the heat exchange device (2), and the outlet end of the heating tube being connected to the first outlet (24) of the heat exchange device (2).

Images