CN112723307A - Liquid metal pyrolysis methane hydrogen production system - Google Patents
Liquid metal pyrolysis methane hydrogen production system Download PDFInfo
- Publication number
- CN112723307A CN112723307A CN202110242946.9A CN202110242946A CN112723307A CN 112723307 A CN112723307 A CN 112723307A CN 202110242946 A CN202110242946 A CN 202110242946A CN 112723307 A CN112723307 A CN 112723307A
- Authority
- CN
- China
- Prior art keywords
- pipe
- tank body
- gas
- electromagnetic pump
- heater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 38
- 239000001257 hydrogen Substances 0.000 title claims abstract description 38
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 229910001338 liquidmetal Inorganic materials 0.000 title claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 238000000197 pyrolysis Methods 0.000 title claims description 5
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 239000007789 gas Substances 0.000 claims abstract description 40
- 230000007704 transition Effects 0.000 claims abstract description 30
- 230000007246 mechanism Effects 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 15
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 238000003756 stirring Methods 0.000 claims abstract description 10
- 238000003860 storage Methods 0.000 claims abstract description 8
- 238000010438 heat treatment Methods 0.000 claims description 23
- 238000010992 reflux Methods 0.000 claims description 15
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 3
- 238000005336 cracking Methods 0.000 abstract description 7
- 238000009434 installation Methods 0.000 abstract 2
- 101100293261 Mus musculus Naa15 gene Proteins 0.000 abstract 1
- 238000004134 energy conservation Methods 0.000 abstract 1
- 239000006229 carbon black Substances 0.000 description 20
- 101150095744 tin-9.1 gene Proteins 0.000 description 20
- 239000000843 powder Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 239000012495 reaction gas Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000012774 insulation material Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000012827 research and development Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
- C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
- C09C1/44—Carbon
- C09C1/48—Carbon black
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
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 invention utilizes the characteristics of high thermal conductivity, fluidity and the like of the liquid metal to crack methane at high temperature, realizes continuous automatic production, achieves the aim of good energy conservation and can prepare high-purity hydrogen.
Description
Technical Field
The invention relates to the technical field of hydrogen preparation equipment, in particular to a system for preparing hydrogen by cracking methane at high temperature by using liquid metal.
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 defect of high cost in hydrogen production in the prior art, the invention provides a liquid metal high-temperature methane cracking hydrogen production system which utilizes the characteristics of high heat conductivity, fluidity and the like of liquid metal under the combined action of relevant equipment and mechanisms, cracks methane at the temperature of 1200 ℃, realizes continuous automatic production, achieves the good energy-saving purpose and can prepare high-purity hydrogen.
The technical scheme adopted by the invention for solving the technical problems is as follows:
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; 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 invention has the beneficial effects that: the method utilizes liquid metal (tin) to crack methane at high temperature to prepare hydrogen, has high purity and high cracking rate, can prepare high-purity hydrogen (the purity is more than 99.9 percent, and the cracking rate is more than 99.9 percent), does not generate carbon dioxide gas, and has the excellent characteristics of high purity, good thermal conductivity and the like of the byproduct carbon black, thereby having wider application. The invention adopts a distributor structure, and simultaneously combines the liquid metal electromagnetic pump A to drive the liquid tin, thereby realizing the convection flow of the liquid tin and reaction gas, enlarging the reaction interface and improving the 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 above, the invention has good application prospect.
Drawings
Fig. 1 is a schematic view of the overall structure of the present invention.
FIG. 2 is 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 top view of the flow guide groove of the present invention.
Fig. 5 is a schematic side view of the flow guide groove 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 view of the structure of the stirring vane 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; 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; 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.
While there have been shown and described what are at present considered the fundamental principles and essential features of the invention and its advantages, it will be apparent to those skilled in the art that the invention is not limited to the details of the foregoing exemplary embodiments, but is capable of other specific forms without departing from the spirit or essential characteristics thereof. 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; 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110242946.9A CN112723307A (en) | 2021-03-05 | 2021-03-05 | Liquid metal pyrolysis methane hydrogen production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110242946.9A CN112723307A (en) | 2021-03-05 | 2021-03-05 | Liquid metal pyrolysis methane hydrogen production system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112723307A true CN112723307A (en) | 2021-04-30 |
Family
ID=75595669
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110242946.9A Pending CN112723307A (en) | 2021-03-05 | 2021-03-05 | Liquid metal pyrolysis methane hydrogen production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112723307A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113264505A (en) * | 2021-05-19 | 2021-08-17 | 芶富均 | Liquid metal pyrolysis methane hydrogen production reactor |
| CN113304719A (en) * | 2021-06-10 | 2021-08-27 | 芶富均 | Carbon discharging mechanism for liquid metal high-temperature cracking methane hydrogen production equipment |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO984560D0 (en) * | 1998-09-30 | 1998-09-30 | Prototech As | Device and method for using carbon as catalyst in pyrolytic production of hydrogen and carbon |
| EP1018485A1 (en) * | 1999-01-05 | 2000-07-12 | Air Products And Chemicals, Inc. | Process and apparatus for the production of hydrogen by steam reforming of hydrocarbon |
| CN205917202U (en) * | 2016-04-21 | 2017-02-01 | 华东理工大学 | Preparation nanometer silver 3D inkjet conductive ink's device |
| CN107628589A (en) * | 2017-09-22 | 2018-01-26 | 中国矿业大学 | A kind of high temperature bubble type methane Direct Pyrolysis High Purity Hydrogen system and method for Photospot solar driving |
| US20180122519A1 (en) * | 2016-10-31 | 2018-05-03 | Georgia Tech Research Corporation | Thermal reactor systems and methods |
| CN109569473A (en) * | 2018-11-21 | 2019-04-05 | 太原理工大学 | A kind of device and method of liquid metal catalyzed hydrocarbon production hydrogen and carbon black |
| JP2019073411A (en) * | 2017-10-16 | 2019-05-16 | 国立研究開発法人産業技術総合研究所 | System for decomposing methane into carbon and hydrogen to produce hydrogen |
| CN209663273U (en) * | 2019-03-18 | 2019-11-22 | 东营宜达新材料有限责任公司 | A kind of cement water reducing agent reaction kettle |
| CN215161003U (en) * | 2021-03-05 | 2021-12-14 | 芶富均 | Liquid metal pyrolysis methane hydrogen production system |
-
2021
- 2021-03-05 CN CN202110242946.9A patent/CN112723307A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO984560D0 (en) * | 1998-09-30 | 1998-09-30 | Prototech As | Device and method for using carbon as catalyst in pyrolytic production of hydrogen and carbon |
| EP1018485A1 (en) * | 1999-01-05 | 2000-07-12 | Air Products And Chemicals, Inc. | Process and apparatus for the production of hydrogen by steam reforming of hydrocarbon |
| CN205917202U (en) * | 2016-04-21 | 2017-02-01 | 华东理工大学 | Preparation nanometer silver 3D inkjet conductive ink's device |
| US20180122519A1 (en) * | 2016-10-31 | 2018-05-03 | Georgia Tech Research Corporation | Thermal reactor systems and methods |
| CN107628589A (en) * | 2017-09-22 | 2018-01-26 | 中国矿业大学 | A kind of high temperature bubble type methane Direct Pyrolysis High Purity Hydrogen system and method for Photospot solar driving |
| JP2019073411A (en) * | 2017-10-16 | 2019-05-16 | 国立研究開発法人産業技術総合研究所 | System for decomposing methane into carbon and hydrogen to produce hydrogen |
| CN109569473A (en) * | 2018-11-21 | 2019-04-05 | 太原理工大学 | A kind of device and method of liquid metal catalyzed hydrocarbon production hydrogen and carbon black |
| CN209663273U (en) * | 2019-03-18 | 2019-11-22 | 东营宜达新材料有限责任公司 | A kind of cement water reducing agent reaction kettle |
| CN215161003U (en) * | 2021-03-05 | 2021-12-14 | 芶富均 | Liquid metal pyrolysis methane hydrogen production system |
Non-Patent Citations (1)
| Title |
|---|
| 李建雄;王振艳;: "甲烷催化裂解制氢气的研究", 河南机电高等专科学校学报, no. 01, 15 January 2008 (2008-01-15), pages 18 - 19 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113264505A (en) * | 2021-05-19 | 2021-08-17 | 芶富均 | Liquid metal pyrolysis methane hydrogen production reactor |
| CN113304719A (en) * | 2021-06-10 | 2021-08-27 | 芶富均 | Carbon discharging mechanism for liquid metal high-temperature cracking methane hydrogen production equipment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN215161003U (en) | Liquid metal pyrolysis methane hydrogen production system | |
| CN112723307A (en) | Liquid metal pyrolysis methane hydrogen production system | |
| WO2023231300A1 (en) | High-temperature heat exchange and heat storage unit, structure, and device | |
| CN203605506U (en) | U-shaped vacuum heat pipe type vacuum optical-heat and photoelectricity conversion glass tube | |
| CN221099372U (en) | Energy-saving vertical preheater for bauxite calcination | |
| CN214502182U (en) | Combined type phase change energy storage removes heat supply car | |
| CN108187598A (en) | Swirling eddy group structure solar heat chemical reactor device | |
| CN214881765U (en) | Splash type condensing equipment of pyrometallurgical zinc smelting system | |
| CN111416141B (en) | Molten hydroxide direct carbon fuel cell and power generation device including the same | |
| CN214863438U (en) | Coke oven gas desulfurization decarbonization compression synthesizer | |
| CN209383429U (en) | Electrothermic retorting device | |
| CN221601630U (en) | CO (carbon monoxide)2Trapping and methanol preparation integrated device | |
| CN220750424U (en) | Solar roof energy collecting system | |
| CN221201219U (en) | Fuel cell polar plate | |
| CN209607839U (en) | A kind of electrodeposit recyclable device of aluminium-air cell | |
| CN220689356U (en) | Heat pump with multi-medium mixed heating | |
| CN216513942U (en) | Spiral recovery furnace | |
| CN221548691U (en) | Solid oxide fuel cell energy supply system | |
| CN202101453U (en) | Plate core of flat plate collector | |
| CN212205113U (en) | Solar water heater water tank convenient to clearance | |
| CN211290518U (en) | Instant water heater device of fused salt | |
| CN102044685A (en) | Gas heating method for fuel cell system | |
| CN208932986U (en) | A kind of efficient processing unit (plant) of grapheme material | |
| CN211777668U (en) | Biogas generator set with waste heat recovery system | |
| CN201488328U (en) | Self-cleaning evacuated collector tube solar water heater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20230601 Address after: 610225 Industrial Concentration Zone of Shuangliu Southwest airport Economic Development Zone, Chengdu, Sichuan (West Airport Science and Technology Incubation Park) Applicant after: CHENGDU DAXINCHENG TECHNOLOGY Co.,Ltd. Address before: 550025 staff dormitory of North District of Guizhou University, Huaxi District, Guiyang City, Guizhou Province Applicant before: Pi Fujun |
|
| TA01 | Transfer of patent application right |