CN215161003U - Liquid metal pyrolysis methane hydrogen production system - Google Patents
Liquid metal pyrolysis methane hydrogen production system Download PDFInfo
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- CN215161003U CN215161003U CN202120474576.7U CN202120474576U CN215161003U CN 215161003 U CN215161003 U CN 215161003U CN 202120474576 U CN202120474576 U CN 202120474576U CN 215161003 U CN215161003 U CN 215161003U
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Abstract
A liquid metal high-temperature cracking methane hydrogen production system comprises a reaction mechanism, a filter, a gas separator and a treatment mechanism; the reaction mechanism is including the jar body of installation together, the blending tank, the gas-supply pipe, electromagnetic pump A, heater A, the heater strip, the distributor, liquid tin, the guiding gutter, convection tube down, upward convection tube and backward flow groove, the blast pipe of jar body and filter inlet end are connected, the exhaust end of filter and gas separator's inlet end are connected, gas separator's exhaust end and blending tank are connected, gas separator's blast pipe and the intake-tube connection of hydrogen gas jar, processing mechanism is including the transition cavity of installation together, collect the cavity, the storage chamber, electromagnetic pump B, the valve, including a motor, stirring vane, heater B, lower back flow, go up the back flow, liquid tin is located the jar internally. The novel liquid metal high-thermal conductivity and fluidity and other characteristics are utilized, methane is cracked at high temperature, continuous automatic production is realized, the purpose of good energy conservation is achieved, and high-purity hydrogen can be prepared.
Description
Technical Field
The utility model relates to a hydrogen preparation equipment technical field, especially a liquid metal pyrolysis methane hydrogen manufacturing system.
Background
Since global energy demand is rapidly increasing, non-renewable energy sources such as fossil fuels face a risk of depletion, and the influence of fossil fuels on the environment is not negligible, development and utilization of new energy sources are becoming more and more urgent. Among many new energy fuels, hydrogen is attracting more and more attention as an energy fuel, which is considered to be an ideal clean high-energy fuel. However, in the prior art, because the preparation cost of the hydrogen is high, the great use of hydrogen energy in life and production has certain difficulty. Therefore, research and development of more advanced new hydrogen production process technology is an important guarantee for solving the problem of cheap hydrogen source, and the new process technology has obvious breakthrough in the aspects of reducing the investment of production devices and reducing the production cost.
The method for producing hydrogen by using methane has the advantages of low cost, obvious scale effect and the like, and is high in production purity and production efficiency. However, in the prior art, no equipment for effectively utilizing methane to prepare hydrogen exists, so that research and development of more advanced new process technology and equipment for preparing hydrogen from methane are important guarantees for solving the problem of cheap hydrogen source.
Disclosure of Invention
In order to overcome the drawback that hydrogen manufacturing has with high costs among the prior art, the utility model provides an under relevant equipment and mechanism combined action, utilize characteristics such as liquid metal high thermal conductivity and mobility, pyrolysis methane when temperature 1200 ℃ realizes continuous automated production, has reached good energy-conserving purpose, can prepare out a liquid metal pyrolysis methane hydrogen manufacturing system of high-purity hydrogen.
The utility model provides a technical scheme that its technical problem adopted is:
a liquid metal pyrolysis methane hydrogen production system is characterized by comprising a reaction mechanism, a filter, a gas separator and a treatment mechanism; the reaction mechanism comprises a tank body, a mixing tank, a gas pipe, an electromagnetic pump A, a heater A, a heating wire, a distributor, liquid tin, a diversion trench, a lower convection pipe, an upper convection pipe and a reflux trench, wherein the left part, the right part and the upper part of the mixing tank are respectively provided with a connecting pipe; the upper end of the gas pipe is arranged at the lower part in the tank body, and the distributor is arranged at the upper end of the gas pipe; the heaters A are annularly distributed and installed on the outer side of the tank body, the left part of the lower convection pipe is installed at the right lower end of the tank body, the right part of the lower convection pipe is connected with the liquid inlet end of the electromagnetic pump A, the liquid outlet end of the electromagnetic pump A is connected with one end of the upper convection pipe, the other end of the upper convection pipe is installed at the right upper part of the tank body, and the heating wires are wound on the outer side of the middle part of the upper convection pipe; the guide groove and the reflux groove are respectively arranged at the left upper part of the tank body from top to bottom and the right part of the tank body, the upper end of the tank body is provided with an exhaust pipe, the other end of the exhaust pipe is connected with the air inlet end of the filter, the exhaust end of the filter is connected with the air inlet end of the gas separator, the exhaust end of the gas separator is connected with the connecting pipe at the right part of the mixing tank, and the exhaust pipe of the gas separator is connected with the air inlet pipe of the hydrogen tank; the treatment mechanism comprises a transition chamber, a collection chamber, a storage chamber, an electromagnetic pump B, a valve, a motor, a stirring blade, a heater B, a lower return pipe and an upper return pipe, wherein the collection chamber is arranged at the left end of the transition chamber; one end of the lower backflow pipe is arranged at the lower end of the transition chamber, the other end of the lower backflow pipe is connected with the liquid inlet end of the electromagnetic pump B, one end of the upper backflow pipe is connected with the liquid outlet end of the electromagnetic pump B, and the other end of the upper backflow pipe is connected with the left lower end of the backflow groove; the heater B surrounds the outer end of the transition chamber, and the liquid tin is located in the tank body.
Furthermore, the left end of the diversion trench and the left end of the reflux trench are low in height, and the right end of the diversion trench and the reflux trench are high in height.
Furthermore, the left end of the diversion trench is communicated with the transition chamber, and the left end of the reflux trench is of a closed structure.
Furthermore, a distance is reserved between the upper end and the lower end of the stirring blade and the upper end and the lower end of the middle opening of the partition plate.
Furthermore, the distributor is a conical hollow structure, the interior of the distributor is communicated with the inside of the gas transmission pipe, and the upper surface of the distributor is provided with a plurality of openings at intervals.
Further, the heater A adopts a sectional heating mode, wherein the upper heating temperature is 1200 ℃, the middle heating temperature is 800 ℃, and the bottom heating temperature is 350 ℃.
Furthermore, fin-shaped blades are respectively arranged on two sides in the guide groove.
The utility model has the advantages that: the utility model discloses utilize liquid metal (tin) pyrolysis methane hydrogen manufacturing, purity is high, the schizolysis rate is high, can prepare high-purity hydrogen (purity > 99.9%, the schizolysis rate > 99.9%), and do not have carbon dioxide gas and produce, and its accessory substance carbon black has excellent characteristics such as purity height, good thermal conductivity simultaneously, has more extensive usage. The utility model discloses a distributor structure combines liquid metal electromagnetic pump A drive liquid tin simultaneously, can realize that liquid tin and reaction gas convection current flow, and increase reaction interface has improved reaction efficiency. The diversion trench structure is adopted to form turbulence to better realize the separation of carbon black and liquid tin, and meanwhile, the reflux trench and the diversion trench are combined into a heat exchange structure, so that the aim of saving energy is fulfilled well. The carbon black is automatically discharged through stirring, the carbon black is better collected, and meanwhile, the continuous automatic production is realized. Based on the foregoing, the utility model discloses good application prospect has.
Drawings
Fig. 1 is a schematic view of the overall structure of the present invention.
Fig. 2 is a schematic diagram of a side view of the dispenser of the present invention.
Fig. 3 is a schematic top view of the dispenser of the present invention.
Fig. 4 is a schematic view of the structure of the diversion trench in a top view.
Fig. 5 is a schematic side view of the diversion trench of the present invention.
Fig. 6 is a schematic view of the structure of the rotating shaft of the motor of the present invention.
Fig. 7 is a schematic structural view of the stirring blade of the present invention.
Detailed Description
As shown in fig. 1, 2, 3, 4, 5, 6, and 7, a system for producing hydrogen by pyrolysis of methane with liquid metal comprises a reaction mechanism, a filter 1, a gas separator 2, and a treatment mechanism; the reaction mechanism comprises a tank body 3, a mixing tank 4, a gas pipe 5, an electromagnetic pump A6, a heater A13, a heating wire 7, a distributor 8, liquid tin 9, a diversion trench 10, a lower convection pipe 11, a reflux trench 12 and an upper convection pipe 14, wherein the left part, the right part and the upper part of the mixing tank 4 are respectively provided with a connecting pipe, the left connecting pipe of the mixing tank 4 is connected with an exhaust valve 29 of a methane tank through a pipeline joint, and the lower end of the gas pipe 5 is connected with the connecting pipe on the upper part of the mixing tank 4 through a pipeline joint; the upper part of the gas pipe 5 is arranged at the lower part in the tank body 3, and the distributor 8 is arranged at the upper end of the gas pipe 5 and is positioned at the lower part in the tank body 3; the heaters A13 are annularly arranged on the outer side of the tank body 3, the left part of the lower convection pipe 11 is arranged at the right lower end of the tank body 3 and communicated with the inside of the tank body 3, the right part of the lower convection pipe 11 is connected with the liquid inlet end of the electromagnetic pump A6 through a pipeline, the liquid outlet end of the electromagnetic pump A6 is connected with one end of the upper convection pipe 14 through a pipeline, the other end of the upper convection pipe 14 is arranged at the right upper part of the tank body 3 and communicated with the inside of the tank body 3, and the heating wires 7 are annularly arranged and surrounded on the outer side of the middle part of the upper convection pipe 14; the guide groove 10 and the reflux groove 12 are respectively arranged at the upper left part of the tank body 3 from top to bottom and communicated with the left end in the tank body 3, the upper end of the tank body 3 is provided with an exhaust pipe 15 communicated with the inside of the tank body 3, the other end of the exhaust pipe 15 is connected with the air inlet end of the filter 1 through a pipeline, the exhaust end of the filter 1 is connected with the air inlet end of the gas separator 2 through a pipeline, the exhaust end of the gas separator 2 is connected with the right connecting pipe of the mixing tank 4 through a pipeline joint, and the exhaust pipe of the gas separator 2 is connected with the air inlet pipe of the hydrogen tank through a pipeline; the treatment mechanism comprises a transition chamber 16, a collection chamber 17, a storage chamber 18, an electromagnetic pump B19, a valve 20, a motor 21, a stirring blade 22, a heater B23, a lower return pipe 24 and an upper return pipe 25, wherein the collection chamber 17 is arranged at the left end of the transition chamber 16, an opening 26 is arranged in the middle of a partition plate between the collection chamber 17 and the transition chamber 16, the motor is arranged in the middle of the upper end of the transition chamber 16, the stirring blade 22 is arranged at the lower end of a rotating shaft of the motor 21 and is positioned between the openings of the upper ends in the transition chamber 16 and the collection chamber 17, one end of the valve 20 is arranged in the middle of the lower end of the collection chamber, the other end of the valve 20 is arranged at the upper end of the storage chamber 18, and the lower end of the storage chamber 18 is provided with an opening as a discharge port 27; one end of the lower return pipe 24 is arranged in the middle of the lower end of the transition chamber 16 and communicated with the interior of the transition chamber 16, the other end of the lower return pipe 24 is connected with the liquid inlet end of the electromagnetic pump B19 through a pipeline, one end of the upper return pipe 25 is connected with the liquid outlet end of the electromagnetic pump B19 through a pipeline, and the other end of the upper return pipe 25 is connected with the left lower end of the return tank 12 and communicated with the interior of the return tank 12; the heaters B23 are distributed around the outer end of the transition chamber 16, and the liquid tin 9 is positioned in the tank 3.
As shown in fig. 1, 2, 3, 4, 5, 6 and 7, the height of the left end of the guide groove 10 and the height of the right end of the reflux groove 12 are low and high. The left end of the diversion trench 10 is communicated with the transition chamber 16, and the left end of the reflux trench 12 is of a closed structure. The upper and lower ends of the stirring vanes 22 are spaced from the upper and lower ends of the baffle plate central opening 26. The distributor 8 is a conical hollow structure, the interior of the distributor 8 is communicated with the interior of the gas transmission pipe 5, and the upper surface is provided with a plurality of holes at certain intervals. The heater A13 adopts a sectional heating mode, wherein the upper heating temperature is 1200 ℃, the middle heating temperature is 800 ℃, and the bottom heating temperature is 350 ℃. The inner two sides of the guiding gutter 10 are respectively provided with a fin-shaped blade 101. The reaction gas methane enters the mixing tank 4 through the methane tank exhaust valve 29, enters the distributor 8 along the gas pipe 5, is guided into the tank body 3 through the distributor 8, fully contacts with the high-temperature liquid tin 9 in the tank body 3, and is cracked into hydrogen and carbon black. Hydrogen, unreacted methane and part of carbon black powder carried by the methane enter the filter 1 and the gas separator 2 in sequence through the exhaust pipe 15, and the carbon black powder and the methane can be separated by the filter 1 and the gas separator 2, so that high-purity hydrogen is obtained. The carbon black 102 cracked in the tank body 3 floats on the surface of the liquid tin 9 and flows into the transition chamber 16 along the flow guide groove 10 along with the liquid tin 9, and after being accumulated on the surface of the liquid tin 9, the carbon black 102 is pushed to the collecting chamber 17 by the blades 22 and then enters the storage chamber 18 through the collecting chamber 17, so that centralized collection is facilitated.
As shown in fig. 1, 2, 3, 4, 5, 6 and 7, a heater a13 is installed outside a tank body 3, a thermal insulation material is arranged outside a heater a13 to prevent heat loss, metal tin 9 is filled inside the tank body 3, the metal tin is heated to 1200 ℃ under the action of a heater a13 to form molten liquid metal tin, the heater a adopts a sectional heating mode, the upper heating temperature is 1200 ℃, the middle heating temperature is 800 ℃ and the bottom heating temperature is 350 ℃, so that the cracking condition of methane is ensured, the operation at an overhigh temperature is avoided, and the requirement on the selection of the liquid metal electromagnetic pump a6 is reduced. The reaction gas methane comes from an external gas storage tank, enters the tank body 3 through the methane tank exhaust valve 29, enters the distributor 8 along the gas conveying pipe 5 together with the methane gas from the separator 2, and is provided with uniformly distributed gas holes 81, so that the methane gas can enter the tank body 3, is diffused in the rising process and fully contacts with the liquid tin 9, the reaction interface is enlarged, and the methane gas is cracked into hydrogen and carbon black. The side surface of the tank body 3 is connected with a liquid metal electromagnetic pump A6 (model: R240L 350), the inlet end of the liquid metal electromagnetic pump A6 is connected with the lower convection pipe 11, the outlet end of the liquid metal electromagnetic pump A6 is connected with the upper convection pipe 14, so that liquid tin 9 in the tank body 3 can circularly flow, the outer part of the upper convection pipe 14 is provided with a heating wire 7, the liquid tin 9 in the pipeline can be heated to 1200 ℃ and flows into the tank body 3, the reaction gas methane and the liquid tin 9 can flow in a convection manner, and the cracking efficiency is improved. Hydrogen, unreacted methane and part of carbon black powder carried by the methane enter the filter 1 and the separator 2 in sequence through the exhaust pipe 15, and the carbon black powder and the methane can be separated, so that high-purity hydrogen is obtained. The carbon black powder of separation can directly collect, and the methane gas of separation gets into blending tank 4 along the connecting pipe, gets into distributor 2 through gas-supply pipe 5, and the leading-in jar of body 3 of distributor 2 is internal further to react again, has improved the utilization ratio of methane. The carbon black (102) cracked in the tank body 3 floats on the surface of the liquid tin 9 and flows into the transition chamber 16 along the flow guide groove 10 along with the liquid tin 9, after the carbon black is accumulated on the surface of the liquid tin 9, the blade 22 (the blade 22 is arranged at a position 30mm away from the surface of the liquid tin 9.) is driven by the motor 21, and the carbon black is pushed and swept into the collection chamber 17 through the opening 26 between the transition chamber 16 and the collection chamber 17. The carbon black is collected centrally by the collection chamber 17 into the storage chamber 18 and is sucked out by vacuum through the outlet 27. The valve 20 is closed during discharging to avoid the fluctuation of the air flow in the tank 3. After the discharge is completed, the valve 20 is opened to ensure that the carbon black smoothly enters the storage chamber 18. The fins 101 are arranged inside the flow guide groove 10, and the fins 101 can enable the liquid tin 9 to form turbulence in the flow guide groove 10, so that carbon black is separated out as much as possible and floats on the surface of the liquid tin 9, and the collection of the carbon black in the later period is facilitated. The transition chamber 16 is equipped with a heater B23 to maintain the temperature of the liquid metallic tin in the transition chamber 16 at about 350 ℃ all the time, so that the liquid metallic tin has good fluidity. The heater B23 is externally provided with a heat insulation material which can prevent heat loss. The liquid metal electromagnetic pump B19 is connected to the bottom of the transition chamber 16, and can drive the liquid tin 9 in the transition chamber 16 to the tank body 3 through the reflow tank 12, so as to realize recycling. The reflux groove 12 and the diversion groove 10 can realize convection heat exchange, namely the temperature of the liquid tin 9 flowing into the transition chamber 16 from the tank body 3 can be reduced, the transition chamber 16 can work in a low-temperature state, and the requirements on materials and structures are greatly reduced; but also can increase the temperature of the liquid tin 9 flowing into the reactor 3 from the transition chamber 16, thereby achieving the purpose of good energy saving.
The basic principles and essential features of the invention and the advantages of the invention have been shown and described above, it will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, but is capable of being embodied in other specific forms without departing from the spirit or essential characteristics of the invention. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.
Furthermore, it should be understood that although the present description refers to embodiments, the embodiments do not include only one independent technical solution, and such description is only for clarity, and those skilled in the art should take the description as a whole, and the technical solutions in the embodiments may be appropriately combined to form other embodiments that can be understood by those skilled in the art.
Claims (7)
1. A liquid metal pyrolysis methane hydrogen production system is characterized by comprising a reaction mechanism, a filter, a gas separator and a treatment mechanism; the reaction mechanism comprises a tank body, a mixing tank, a gas pipe, an electromagnetic pump A, a heater A, a heating wire, a distributor, liquid tin, a diversion trench, a lower convection pipe, an upper convection pipe and a reflux trench, wherein the left part, the right part and the upper part of the mixing tank are respectively provided with a connecting pipe; the upper end of the gas pipe is arranged at the lower part in the tank body, and the distributor is arranged at the upper end of the gas pipe; the heaters A are annularly distributed and installed on the outer side of the tank body, the left part of the lower convection pipe is installed at the right lower end of the tank body, the right part of the lower convection pipe is connected with the liquid inlet end of the electromagnetic pump A, the liquid outlet end of the electromagnetic pump A is connected with one end of the upper convection pipe, the other end of the upper convection pipe is installed at the right upper part of the tank body, and the heating wires are wound on the outer side of the middle part of the upper convection pipe; the guide groove and the reflux groove are respectively arranged at the left upper part of the tank body from top to bottom and the right part of the tank body, the upper end of the tank body is provided with an exhaust pipe, the other end of the exhaust pipe is connected with the air inlet end of the filter, the exhaust end of the filter is connected with the air inlet end of the gas separator, the exhaust end of the gas separator is connected with the connecting pipe at the right part of the mixing tank, and the exhaust pipe of the gas separator is connected with the air inlet pipe of the hydrogen tank; the treatment mechanism comprises a transition chamber, a collection chamber, a storage chamber, an electromagnetic pump B, a valve, a motor, a stirring blade, a heater B, a lower return pipe and an upper return pipe, wherein the collection chamber is arranged at the left end of the transition chamber; one end of the lower backflow pipe is arranged at the lower end of the transition chamber, the other end of the lower backflow pipe is connected with the liquid inlet end of the electromagnetic pump B, one end of the upper backflow pipe is connected with the liquid outlet end of the electromagnetic pump B, and the other end of the upper backflow pipe is connected with the left lower end of the backflow groove; the heater B surrounds the outer end of the transition chamber, and the liquid tin is located in the tank body.
2. The system for producing hydrogen by pyrolyzing methane according to claim 1, wherein the diversion trench and the reflux trench are low in height at the left end and high in height at the right end.
3. The system for producing hydrogen by pyrolyzing methane according to claim 1, wherein the left end of the diversion trench is communicated with the transition chamber, and the left end of the reflux trench has a closed structure.
4. The system for producing hydrogen by pyrolyzing methane according to claim 1, wherein the upper and lower ends of the stirring blade are spaced apart from the upper and lower ends of the opening in the middle of the partition plate.
5. The system for producing hydrogen by pyrolyzing methane according to claim 1, wherein the distributor is a tapered hollow structure, the interior of the distributor is communicated with the gas transmission pipe, and the upper surface of the distributor is provided with a plurality of openings at intervals.
6. The system for producing hydrogen by pyrolyzing methane according to claim 1, wherein the heater A adopts a sectional heating mode, and has an upper heating temperature of 1200 ℃, a middle heating temperature of 800 ℃ and a bottom heating temperature of 350 ℃.
7. The system for producing hydrogen by pyrolyzing methane according to claim 1, wherein the guide groove is provided with fin-shaped blades at both sides thereof.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202120474576.7U CN215161003U (en) | 2021-03-05 | 2021-03-05 | Liquid metal pyrolysis methane hydrogen production system |
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| CN202120474576.7U CN215161003U (en) | 2021-03-05 | 2021-03-05 | Liquid metal pyrolysis methane hydrogen production system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112723307A (en) * | 2021-03-05 | 2021-04-30 | 芶富均 | Liquid metal pyrolysis methane hydrogen production system |
| CN115477279A (en) * | 2022-09-15 | 2022-12-16 | 山东建筑大学 | Cyclone reactor for producing hydrogen by solar-driven methane thermal cracking |
-
2021
- 2021-03-05 CN CN202120474576.7U patent/CN215161003U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112723307A (en) * | 2021-03-05 | 2021-04-30 | 芶富均 | Liquid metal pyrolysis methane hydrogen production system |
| CN115477279A (en) * | 2022-09-15 | 2022-12-16 | 山东建筑大学 | Cyclone reactor for producing hydrogen by solar-driven methane thermal cracking |
| CN115477279B (en) * | 2022-09-15 | 2023-11-28 | 山东建筑大学 | Rotational flow reactor for preparing hydrogen by thermally cracking methane driven by solar energy |
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Effective date of registration: 20230802 Address after: 610000 Industrial Concentration Zone (West Airport Science and Technology Incubation Park), Southwest Airport Economic Development Zone, Shuangliu, Chengdu, Sichuan Province Patentee after: CHENGDU DAXINCHENG TECHNOLOGY Co.,Ltd. Address before: 550025 staff dormitory of North District of Guizhou University, Huaxi District, Guiyang City, Guizhou Province Patentee before: Pi Fujun |
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