CN220926680U - System for preparing liquid fuel by complementation of biogas and green hydrogen - Google Patents
System for preparing liquid fuel by complementation of biogas and green hydrogen Download PDFInfo
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- CN220926680U CN220926680U CN202322549685.2U CN202322549685U CN220926680U CN 220926680 U CN220926680 U CN 220926680U CN 202322549685 U CN202322549685 U CN 202322549685U CN 220926680 U CN220926680 U CN 220926680U
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- pipeline
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- liquid fuel
- methane
- gas
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 58
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 58
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 239000000446 fuel Substances 0.000 title claims abstract description 46
- 239000007788 liquid Substances 0.000 title claims abstract description 41
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 88
- 239000007789 gas Substances 0.000 claims abstract description 87
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 43
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 238000002485 combustion reaction Methods 0.000 claims abstract description 39
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 claims abstract description 22
- 238000002407 reforming Methods 0.000 claims abstract description 22
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 239000001301 oxygen Substances 0.000 claims description 15
- 229910052760 oxygen Inorganic materials 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 37
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 19
- 239000001569 carbon dioxide Substances 0.000 abstract description 18
- 238000006243 chemical reaction Methods 0.000 abstract description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 10
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 10
- 229910052799 carbon Inorganic materials 0.000 abstract description 9
- 238000006057 reforming reaction Methods 0.000 abstract description 9
- 150000002431 hydrogen Chemical class 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 7
- 239000013589 supplement Substances 0.000 abstract description 7
- 230000009286 beneficial effect Effects 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 5
- KDRIEERWEFJUSB-UHFFFAOYSA-N carbon dioxide;methane Chemical compound C.O=C=O KDRIEERWEFJUSB-UHFFFAOYSA-N 0.000 abstract description 4
- 239000012071 phase Substances 0.000 description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Hydrogen, Water And Hydrids (AREA)
Abstract
The utility model relates to a system for preparing liquid fuel by complementation of marsh gas and green hydrogen, belonging to the technical field of low-carbon utilization of energy. The system comprises a first mixer, a reforming reactor, a heat exchanger, a steam-water separator, a second mixer, an electrolyzed water hydrogen production device, a Fischer-Tropsch synthesis reactor, a liquid fuel collector, a three-phase separator and a combustion furnace. The system provided by the utility model has the advantages that the air inlet of the first mixer is connected with the tail gas outlet of the combustion furnace through the pipeline, the air inlet of the first mixer is connected with the methane supply pipeline, the tail gas discharged by the combustion furnace and methane are input into the first mixer through the pipeline for mixing, and methane and carbon dioxide are not required to be separated in advance, so that methane and sufficient carbon dioxide are subjected to methane-carbon dioxide reforming reaction; the utility model supplements hydrogen to the Fischer-Tropsch synthesis reactor in time through the water electrolysis hydrogen production device to participate in the Fischer-Tropsch synthesis reaction, thereby being beneficial to improving the conversion rate of carbon monoxide in the reaction.
Description
Technical Field
The utility model relates to the technical field of low-carbon utilization of energy, in particular to a system for preparing liquid fuel by complementation of biogas and green hydrogen.
Background
Compared with the traditional fossil energy, the biogas is used as a renewable biomass energy source, can obviously reduce carbon emission, and has the main components of 50-70% of methane and 30-40% of carbon dioxide, and also contains a small amount of hydrogen sulfide and hydrogen. The traditional biogas utilization mode mainly comprises the steps of burning, heating, generating electricity, purifying, separating, injecting into a natural gas pipe network, compressing and liquefying for transportation, wherein the value of the biogas utilization mode is relatively low, and carbon dioxide serving as impurity gas is discharged into the atmosphere, so that a strong greenhouse effect is brought.
The main components of the synthesis gas generated by the methane carbon dioxide reforming reaction are hydrogen and carbon monoxide, which are important ways for reducing the emission of greenhouse gases in the biogas utilization process. The prior patent proposes a system for preparing liquid fuel, which takes methane as a single raw material, after the methane enters a reforming reactor, methane and carbon dioxide in the methane undergo reforming reaction under the catalysis of a catalyst to generate synthetic gas, and the system mainly comprises the following reactions: CH 4+CO2＝2CO+2H2; because the molar ratio of methane to carbon dioxide in the biogas is far greater than 1 and the stoichiometric ratio of methane to carbon dioxide in the reforming reaction is large, the conversion rate of methane is low, and part of unreacted methane needs to be separated from the synthesis gas and returned to the reforming reactor for circulation, so that the running cost and the operation difficulty of the system are increased; after the synthesis gas enters the Fischer-Tropsch synthesis reactor, the conversion rate of carbon monoxide is lower because the amount of hydrogen in the synthesis gas is relatively insufficient, unreacted carbon monoxide is required to be separated from products, and the unreacted carbon monoxide is circularly introduced into the Fischer-Tropsch synthesis reactor, so that the hydrogen-carbon ratio in the Fischer-Tropsch reactant is further reduced, and the product distribution of the Fischer-Tropsch synthesis is seriously influenced.
Therefore, it is necessary to design a system for preparing liquid fuel by complementing methane and green hydrogen, which can supplement carbon dioxide to participate in methane carbon dioxide reforming reaction and supplement hydrogen to participate in Fischer-Tropsch synthesis reaction in time.
Disclosure of utility model
The utility model aims to overcome the defects of the prior art and provide a system for preparing liquid fuel by complementing methane and green hydrogen, which inputs tail gas discharged by a combustion furnace and methane into a first mixer through a pipeline to be mixed so that methane and sufficient carbon dioxide perform methane-carbon dioxide reforming reaction, and can timely supplement hydrogen to a Fischer-Tropsch synthesis reactor through a water electrolysis hydrogen production device to participate in the Fischer-Tropsch synthesis reaction.
In order to achieve the above purpose, the technical scheme adopted by the utility model is as follows:
A system for preparing liquid fuel by complementation of marsh gas and green hydrogen comprises a first mixer, a reforming reactor, a heat exchanger, a steam-water separator, a second mixer, an electrolyzed water hydrogen production device, a Fischer-Tropsch synthesis reactor, a liquid fuel collector, a three-phase separator and a combustion furnace; the gas inlet of the first mixer is connected with the tail gas outlet of the combustion furnace through a pipeline, and the gas inlet of the first mixer is also connected with a methane supply pipeline; the heat exchanger is provided with a first flow path through the mixture and a second flow path through the synthesis gas; the gas outlet of the first mixer is connected with the inlet of the first flow passage through a pipeline, the outlet of the first flow passage is connected with the gas inlet of the reforming reactor through a pipeline, the gas outlet of the reforming reactor is connected with the inlet of the second flow passage, the outlet of the second flow passage is connected with the gas inlet of the steam-water separator through a pipeline, the gas outlet of the steam-water separator is connected with the gas inlet of the second mixer through a pipeline, the gas outlet of the second mixer is connected with the gas inlet of the Fischer-Tropsch synthesis reactor through a pipeline, the hydrogen outlet of the electrolyzed water hydrogen production device is connected with the gas inlet of the second mixer through a pipeline, the liquid fuel outlet of the Fischer-Tropsch synthesis reactor is connected with the fuel inlet of the liquid fuel collector through a pipeline, the gas phase outlet of the Fischer-Tropsch synthesis reactor is connected with the inlet of the three-phase separator through a pipeline, and the gas phase outlet of the three-phase separator is connected with the inlet of the combustion furnace through a pipeline.
The system of the utility model connects the air inlet of the first mixer with the tail gas outlet of the combustion furnace through the pipeline, connects the air inlet of the first mixer with the methane supply pipeline, inputs the tail gas discharged by the combustion furnace and methane into the first mixer through the pipeline for mixing, not only does not need to separate methane and carbon dioxide in advance, but also does not need to acquire carbon dioxide in the tail gas through carbon capture, can flexibly adjust the proportion of reactants in the reforming reactor, improves the conversion rate of methane in the methane, reduces the generation of carbon deposition in the reaction process, avoids the greenhouse effect caused by direct discharge of the tail gas, and has high economic benefit;
The utility model supplements hydrogen to the Fischer-Tropsch synthesis reactor in time through the water electrolysis hydrogen production device to participate in the Fischer-Tropsch synthesis reaction, thereby being beneficial to improving the conversion rate of carbon monoxide in the reaction.
As a preferred embodiment of the utility model, the oxygen outlet of the electrolytic water hydrogen production device is connected with the oxygen inlet of the combustion furnace through a pipeline.
As a preferred embodiment of the utility model, the water electrolysis hydrogen production device is powered by a wind generating set or a photovoltaic power supply.
The utility model utilizes renewable energy sources to carry out water electrolysis to generate oxygen and hydrogen, the oxygen is used as a combustion improver for tail gas combustion, and combustion products are used as raw materials of synthesis gas, thereby realizing effective utilization of the oxygen and being beneficial to improving the economic benefit of system operation.
As a preferred embodiment of the utility model, the liquid fuel outlet of the three-phase separator is connected to the fuel inlet of the liquid fuel collector by a pipe.
As a preferred embodiment of the present utility model, the reforming reactor is a fixed bed reactor, a heat transfer pipe is provided in the reforming reactor, and a heat supply port of the combustion furnace is connected with an inlet of the heat transfer pipe through a pipe.
As a preferred embodiment of the present utility model, a flow meter and a control valve are provided on each pipe.
Compared with the prior art, the utility model has the beneficial effects that:
The system of the utility model connects the air inlet of the first mixer with the tail gas outlet of the combustion furnace through the pipeline, connects the air inlet of the first mixer with the methane supply pipeline, inputs the tail gas discharged by the combustion furnace and methane into the first mixer through the pipeline for mixing, not only does not need to separate methane and carbon dioxide in advance, but also does not need to capture carbon dioxide in the tail gas through carbon, and is convenient and flexible to adjust the proportion of reactants in the reforming reactor, improves the conversion rate of methane in the methane, reduces the generation of carbon deposition in the reaction process, avoids the greenhouse effect caused by direct discharge of the tail gas, and has high economic benefit;
the utility model can timely supplement hydrogen to the Fischer-Tropsch synthesis reactor through the water electrolysis hydrogen production device to participate in the Fischer-Tropsch synthesis reaction, thereby being beneficial to improving the conversion rate of carbon monoxide in the reaction.
Drawings
FIG. 1 is a schematic diagram of a system for producing liquid fuel by complementing biogas and green hydrogen.
In the figure, a 1-first mixer, a 2-reforming reactor, a 3-heat exchanger, a 4-steam-water separator, a 5-second mixer, a 6-water electrolysis hydrogen production device, a 7-Fischer-Tropsch synthesis reactor, an 8-liquid fuel collector, a 9-three-phase separator and a 10-combustion furnace are arranged.
Detailed Description
For a better description of the objects, technical solutions and advantages of the present utility model, the present utility model will be further described with reference to the following specific examples.
Referring to fig. 1, an embodiment of the present utility model provides a system for preparing liquid fuel by complementing biogas and green hydrogen, which comprises a first mixer 1, a reforming reactor 2, a heat exchanger 3, a steam-water separator 4, a second mixer 5, an electrolyzed water hydrogen production device 6, a fischer-tropsch synthesis reactor 7, a liquid fuel collector 8, a three-phase separator 9 and a combustion furnace 10.
The heat exchanger 3 is equipped with a first flow path through the mixture and a second flow path through the synthesis gas.
The air inlet of the first mixer 1 is connected with the tail gas outlet of the combustion furnace 10 through a pipeline, and the air inlet of the first mixer 1 is also connected with a biogas supply pipeline.
The gas outlet of the first mixer 1 is connected with the inlet of the first flow passage through a pipeline, the outlet of the first flow passage is connected with the gas inlet of the reforming reactor 2 through a pipeline, the gas outlet of the reforming reactor 2 is connected with the inlet of the second flow passage, the outlet of the second flow passage is connected with the gas inlet of the steam-water separator 4 through a pipeline, the gas outlet of the steam-water separator 4 is connected with one gas inlet of the second mixer 5 through a pipeline, the gas outlet of the second mixer 5 is connected with the gas inlet of the Fischer-Tropsch synthesis reactor 7 through a pipeline, the liquid fuel outlet of the Fischer-Tropsch synthesis reactor 7 is connected with the fuel inlet of the liquid fuel collector through a pipeline, the gas outlet of the Fischer-Tropsch synthesis reactor 7 is connected with the inlet of the three-phase separator 9 through a pipeline, the gas phase outlet of the three-phase separator 9 is connected with the inlet of the combustion furnace 10 through a pipeline, and the liquid fuel outlet of the three-phase separator 9 is connected with the fuel inlet of the liquid fuel collector 8 through a pipeline.
The hydrogen outlet of the electrolytic water hydrogen production device 6 is connected with the other air inlet of the second mixer 5 through a pipeline, and the oxygen outlet of the electrolytic water hydrogen production device 6 is connected with the oxygen inlet of the combustion furnace 10 through a pipeline.
In this embodiment, a flowmeter and a control valve are provided in each pipe.
In this embodiment, the working principle of the system for preparing liquid fuel by complementation of biogas and green hydrogen is as follows:
The biogas is conveyed to the first mixer 1 through a pipeline, and meanwhile, combustion products (the main component is carbon dioxide gas) discharged by the combustion furnace 10 are conveyed to the first mixer 1 through a pipeline, and the biogas and the tail gas are mixed into mixed gas in the first mixer 1, so that the adjustment of the proportion between the methane and the carbon dioxide is realized; the biogas can be biogas (the main component is methane gas) generated by anaerobic fermentation of biomass and subjected to desulfurization and impurity removal treatment.
The mixed gas enters a first flow passage of a heat exchanger 3, and enters a reforming reactor 2 after heat exchange and temperature rise, methane and carbon dioxide in the mixed gas are subjected to reforming reaction under the catalysis of a catalyst in the reforming reactor 2 to generate hydrogen and carbon monoxide, and the synthetic gas discharged from the reforming reactor 2 mainly comprises hydrogen, carbon monoxide, a small amount of water vapor and other substances; the synthesis gas enters a second flow passage of the heat exchanger 3 through a pipe, enters a steam-water separator 4 after heat exchange and temperature reduction, and water vapor contained in a reaction product is condensed into liquid water and is separated and discharged out of the system;
The synthesis gas after steam-water separation enters the second mixer 5 through a pipeline, the hydrogen discharged by the electrolytic water hydrogen production device 6 enters the second mixer 5, the synthesis gas and the hydrogen are mixed in the second mixer 5, the mixing proportion of the synthesis gas and the hydrogen can be adjusted by adjusting the opening of a valve on a corresponding pipeline, and the mixed gas enters the Fischer-Tropsch synthesis reactor 7 to synthesize hydrocarbon or alcohol fuel under the action of a catalyst.
The product discharged from the Fischer-Tropsch synthesis reactor 7 has two phases of gas and liquid, wherein the gas phase contains uncondensed light hydrocarbon and unreacted synthesis gas, and the liquid phase is liquid fuel;
The liquid fuel enters the liquid fuel collector 8 to be collected, the gas phase enters the three-phase separator 9 to be subjected to phase separation, the liquid fuel (the main component is light hydrocarbon) is separated, the water phase and the tail gas are collected in the liquid fuel collector 8, the water phase is discharged from the system, the tail gas enters the combustion furnace 10 through a pipeline, the oxygen discharged by the electrolyzed water hydrogen production device 6 enters the combustion furnace 10, the oxygen is used as a combustion improver in the combustion furnace 10, the heat is released through combustion, the tail gas is generated, and the carbon dioxide content in the tail gas is high.
The embodiment provides the combustion tail gas through the combustion furnace 10, and the mixing proportion of the tail gas and the methane can be adjusted by controlling the opening of the valve on the corresponding pipeline, so that the tail gas and the methane are mixed for preparing the reforming reaction raw gas, the carbon source in the methane is fully utilized, methane and carbon dioxide are not required to be separated, air pollution caused by direct discharge of the combustion tail gas is avoided, and the economic benefit is high. The utility model supplements hydrogen to the Fischer-Tropsch synthesis reactor in time through the water electrolysis hydrogen production device to participate in the Fischer-Tropsch synthesis reaction, thereby being beneficial to improving the conversion rate of carbon monoxide in the reaction.
In this embodiment, the reforming reactor 2 is a fixed bed reactor in which a heat transfer pipe is provided, and a heat supply port of the burner 10 is connected to an inlet of the heat transfer pipe through a pipe.
In the process of producing hydrogen by utilizing the electrolytic water hydrogen production device to produce the electrolytic water, oxygen is often discharged into the atmosphere as a byproduct. In this embodiment, the electrolytic water hydrogen production device 6 is powered by a wind power generator set or a photovoltaic power source, and utilizes renewable energy sources to perform water electrolysis to generate oxygen and hydrogen, wherein the oxygen is used as a combustion improver in a combustion furnace, and further tail gas generated by combustion is used as a raw material for reforming reaction, so that effective utilization of the oxygen is realized, and the economic benefit of system operation is improved.
It should be understood that, in the description of the present utility model, the terms "upper," "lower," and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the device or element in question must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
Finally, it should be noted that the above embodiments are only for illustrating the technical solution of the present utility model and not for limiting the scope of the present utility model, and although the present utility model has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present utility model may be modified or substituted equally without departing from the spirit and scope of the technical solution of the present utility model.
Claims (6)
1. The system for preparing the liquid fuel by complementation of methane and green hydrogen is characterized by comprising a first mixer, a reforming reactor, a heat exchanger, a steam-water separator, a second mixer, an electrolyzed water hydrogen production device, a Fischer-Tropsch synthesis reactor, a liquid fuel collector, a three-phase separator and a combustion furnace; the gas inlet of the first mixer is connected with the tail gas outlet of the combustion furnace through a pipeline, and the gas inlet of the first mixer is also connected with a methane supply pipeline; the heat exchanger is provided with a first flow path through the mixture and a second flow path through the synthesis gas; the gas outlet of the first mixer is connected with the inlet of the first flow passage through a pipeline, the outlet of the first flow passage is connected with the gas inlet of the reforming reactor through a pipeline, the gas outlet of the reforming reactor is connected with the inlet of the second flow passage, the outlet of the second flow passage is connected with the gas inlet of the steam-water separator through a pipeline, the gas outlet of the steam-water separator is connected with the gas inlet of the second mixer through a pipeline, the gas outlet of the second mixer is connected with the gas inlet of the Fischer-Tropsch synthesis reactor through a pipeline, the hydrogen outlet of the electrolyzed water hydrogen production device is connected with the gas inlet of the second mixer through a pipeline, the liquid fuel outlet of the Fischer-Tropsch synthesis reactor is connected with the fuel inlet of the liquid fuel collector through a pipeline, the gas phase outlet of the Fischer-Tropsch synthesis reactor is connected with the inlet of the three-phase separator through a pipeline, and the gas phase outlet of the three-phase separator is connected with the inlet of the combustion furnace through a pipeline.
2. The system for producing liquid fuel by complementing methane and green hydrogen as claimed in claim 1, wherein the oxygen outlet of the electrolytic water hydrogen production device is connected with the oxygen inlet of the combustion furnace through a pipeline.
3. The system for producing liquid fuel by complementing methane and green hydrogen as claimed in claim 1, wherein the water electrolysis hydrogen production device is powered by a wind power generator set or a photovoltaic power source.
4. The system for producing liquid fuel by complementing biogas and green hydrogen according to claim 1, wherein the liquid fuel outlet of the three-phase separator is connected with the fuel inlet of the liquid fuel collector through a pipeline.
5. The system for preparing liquid fuel by complementation of methane and green hydrogen according to claim 1, wherein the reforming reactor is a fixed bed reactor, a heat transfer pipe is arranged in the fixed bed reactor, and a heat supply port of the combustion furnace is connected with an inlet of the heat transfer pipe through a pipeline.
6. A system for producing liquid fuel by complementing methane and green hydrogen as claimed in claim 1, wherein a flowmeter and a control valve are provided on each pipeline.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322549685.2U CN220926680U (en) | 2023-09-20 | 2023-09-20 | System for preparing liquid fuel by complementation of biogas and green hydrogen |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202322549685.2U CN220926680U (en) | 2023-09-20 | 2023-09-20 | System for preparing liquid fuel by complementation of biogas and green hydrogen |
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| CN220926680U true CN220926680U (en) | 2024-05-10 |
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| CN202322549685.2U Active CN220926680U (en) | 2023-09-20 | 2023-09-20 | System for preparing liquid fuel by complementation of biogas and green hydrogen |
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- 2023-09-20 CN CN202322549685.2U patent/CN220926680U/en active Active
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