CN116845280A - Gas-liquid self-separating electricity-hydrogen cogeneration device - Google Patents
Gas-liquid self-separating electricity-hydrogen cogeneration device Download PDFInfo
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- CN116845280A CN116845280A CN202310921511.6A CN202310921511A CN116845280A CN 116845280 A CN116845280 A CN 116845280A CN 202310921511 A CN202310921511 A CN 202310921511A CN 116845280 A CN116845280 A CN 116845280A
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- 239000007788 liquid Substances 0.000 title claims abstract description 91
- 239000001257 hydrogen Substances 0.000 title claims abstract description 53
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 53
- 238000000926 separation method Methods 0.000 claims abstract description 109
- 238000006243 chemical reaction Methods 0.000 claims abstract description 54
- 238000004519 manufacturing process Methods 0.000 claims abstract description 22
- 239000003054 catalyst Substances 0.000 claims abstract description 9
- 239000012528 membrane Substances 0.000 claims abstract description 8
- 150000001768 cations Chemical class 0.000 claims abstract description 4
- 229910000510 noble metal Inorganic materials 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 28
- BDAGIHXWWSANSR-UHFFFAOYSA-M Formate Chemical compound [O-]C=O BDAGIHXWWSANSR-UHFFFAOYSA-M 0.000 claims description 19
- 239000012530 fluid Substances 0.000 claims description 18
- 238000004891 communication Methods 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 9
- 239000011230 binding agent Substances 0.000 claims description 8
- 239000000376 reactant Substances 0.000 claims description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 239000011865 Pt-based catalyst Substances 0.000 claims description 5
- 229910002804 graphite Inorganic materials 0.000 claims description 5
- 239000010439 graphite Substances 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 5
- 239000000758 substrate Substances 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 3
- 239000004280 Sodium formate Substances 0.000 claims description 3
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 3
- WFIZEGIEIOHZCP-UHFFFAOYSA-M potassium formate Chemical compound [K+].[O-]C=O WFIZEGIEIOHZCP-UHFFFAOYSA-M 0.000 claims description 3
- HLBBKKJFGFRGMU-UHFFFAOYSA-M sodium formate Chemical compound [Na+].[O-]C=O HLBBKKJFGFRGMU-UHFFFAOYSA-M 0.000 claims description 3
- 235000019254 sodium formate Nutrition 0.000 claims description 3
- 229920000557 Nafion® Polymers 0.000 claims description 2
- 238000013461 design Methods 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 7
- 238000005457 optimization Methods 0.000 abstract description 3
- 230000010354 integration Effects 0.000 abstract description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 37
- 238000003860 storage Methods 0.000 description 13
- 239000000126 substance Substances 0.000 description 10
- 239000012071 phase Substances 0.000 description 8
- 150000002431 hydrogen Chemical class 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- 125000002091 cationic group Chemical group 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- 238000004088 simulation Methods 0.000 description 3
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 2
- 238000003487 electrochemical reaction Methods 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- NPYPAHLBTDXSSS-UHFFFAOYSA-N Potassium ion Chemical compound [K+] NPYPAHLBTDXSSS-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- -1 hydrogen ions Chemical class 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229910001414 potassium ion Inorganic materials 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Fuel Cell (AREA)
Abstract
The invention discloses a gas-liquid self-separating electro-hydrogen co-production device, which comprises an anode flow field plate, a cathode gas-liquid self-separating flow field plate, an anode electrode and a cathode electrode which are loaded with noble metal catalysts, and a cation membrane for dividing the anode electrode and the cathode electrode; the cathode gas-liquid separation flow field plate is divided into a reaction zone and a separation zone by vertically arranged separation ribs, the reaction zone is communicated with the separation zone through flow channels above the separation ribs, and the reaction zone is internally provided with reaction zone flow channels; the cathode gas-liquid self-separation flow field plate is divided into a reaction area and a separation area, and the arrangement mode of the split area is adopted, so that the battery performance and the separation effect are designed and optimized independently, the high-performance of the battery in the reaction area and the high-efficiency separation of the separation area are guaranteed, the self-separation flow field design avoids an additional gas-liquid separation device, the integration level and usability of the electro-hydrogen co-production device are improved, the reliability of gas-liquid separation is improved, and the design difficulty of gas-liquid separation flow field optimization is reduced.
Description
Technical Field
The invention belongs to the technical field of fuel cells, and particularly relates to a gas-liquid self-separation electricity-hydrogen cogeneration device.
Background
The hydrogen energy is an ideal interconnection medium for promoting the clean and efficient utilization of the traditional fossil energy and supporting the large-scale development of renewable energy, and is the best choice for realizing large-scale deep decarburization in the fields of transportation, industry, construction and the like. However, the prior art is insufficient to support safe and effective operation of the entire hydrogen energy industry chain, and the large-scale utilization of hydrogen energy also faces some important challenges. For example, hydrogen has low volume energy density, is not easy to store, and has potential safety hazards; the technical admission threshold of hydrogen transportation is high, and the transportation cost even exceeds the production cost, and the problems seriously prevent the large-scale application of hydrogen energy.
At present, the storage and transportation modes of hydrogen mainly comprise three types of gaseous hydrogen storage, liquid hydrogen storage and solid hydrogen storage. Wherein gaseous hydrogen storage requires high pressure conditions, liquid hydrogen storage requires low temperature conditions, and solid hydrogen storage requires additional solid materials. In contrast, the adoption of liquid chemical hydrogen storage has the advantages of mild storage conditions, availability of the existing chemical storage and transportation equipment, high safety performance and the like. Formate is used as a liquid chemical hydrogen storage carrier, has extremely stable chemical properties, has no safety problems such as flammability, toxicity and the like, is favorable for long-term storage and long-distance transportation, and is therefore paid attention to researchers. The use of formate as a hydrogen carrier for distributed off-site hydrogen production is considered to be an effective solution to the current problems of hydrogen storage and transport.
Formate hydrogen-producing devices are important devices for producing hydrogen by formate decomposition. The design of the different plant structures can have a significant impact on the efficiency of formate decomposition. At present, formate hydrogen production equipment stays in a laboratory research stage, and mature integrated device designs are few. And more equipment and instruments are required to be connected in the laboratory for hydrogen production, and the gas-liquid separation steps of the product are more, so that the large-scale integrated production is not facilitated. In addition, most hydrogen production processes waste chemical energy of formate, reduce hydrogen production income and are not beneficial to further popularization and application of formate hydrogen production technology.
Therefore, a highly integrated formate decomposition hydrogen production device needs to be designed, the system usability is improved, high-efficiency gas-liquid separation is realized, meanwhile, the chemical energy of a reaction system is fully utilized, and high-efficiency, convenient, flexible and low-cost distributed hydrogen production is realized.
Disclosure of Invention
Aiming at the problems existing in the prior art, the invention aims to provide the gas-liquid self-separation electricity-hydrogen cogeneration device which can be highly integrated, realize gas-liquid separation in the device, is portable and easy to use and fully utilizes chemical energy.
In order to achieve the purpose, the invention is realized by adopting the following technical scheme:
a gas-liquid self-separating electro-hydrogen co-production device comprises an anode flow field plate, a cathode gas-liquid self-separating flow field plate, an anode electrode and a cathode electrode which are loaded with noble metal catalysts, and a cation membrane for dividing the anode electrode and the cathode electrode;
the cathode gas-liquid separation flow field plate is divided into a reaction zone and a separation zone by vertically arranged separation ribs, the reaction zone is communicated with the separation zone through flow channels above the separation ribs, reaction zone flow channels are arranged in the reaction zone, and the reaction zone flow channels are communicated with flow field inlets; the separation area is separated by a vertical partition plate into a separation cavity close to one side of the reaction area and a liquid cavity at the other side, the bottom of the separation cavity is connected with the liquid cavity through a communication port below the vertical partition plate, and the upper part of the liquid cavity is communicated with the liquid outlet; the baffle rib is arranged at the upper part of the separation cavity, the separation cavity is divided into a vertical flow channel and a gas flow channel, the vertical flow channel at one side close to the separation rib is communicated with the reaction zone flow channel of the reaction zone through the flow channel above the separation rib, and the gas flow channel is communicated with the gas outlet;
after the solution flows into the flow channel of the reaction zone from the flow field inlet to generate two-phase fluid, the mixed fluid flows into the separation cavity of the separation zone through the flow channel above the separation rib, the gas leaves the flow field from the gas outlet through the gas flow channel after the mixed fluid is layered under the action of gravity, and the liquid flows to the liquid cavity from the liquid outlet through the bottom communication port to leave the flow field.
Further, the reaction zone flow channel is a serpentine flow channel, a parallel flow channel, an interdigital flow channel or a lattice flow channel.
Further, the baffle ribs are rectangular, square, trapezoidal or triangular.
Further, the flow field inlet is arranged at the lower position of one side of the cathode gas-liquid self-separation flow field plate close to the reaction zone, and the gas outlet and the liquid outlet are respectively arranged at the upper position and the lower position of one side of the cathode gas-liquid self-separation flow field plate close to the separation zone.
Further, the cathode electrode adopts a Pt-based catalyst, and the Pt-based catalyst is supported on a three-dimensional graphite felt substrate layer through a Nafon binder.
Further, the anode electrode adopts a Pd-based catalyst, and the Pd-based catalyst is supported on a three-dimensional graphite felt substrate layer through a PTFE binder.
Further, the anode uses formate solution as a reactant and the cathode uses dilute acid solution as a reactant.
Further, the formate solution is sodium formate or potassium formate; the dilute acid solution is dilute sulfuric acid or dilute hydrochloric acid.
The technical scheme shows that the invention has the following advantages:
the cathode gas-liquid self-separation flow field plate is divided into a reaction area and a separation area by the vertically arranged separation ribs, and the arrangement mode of the separation area is adopted, so that the independent design optimization of the battery performance and the separation effect is facilitated, and the high-performance of the battery in the reaction area and the high-efficiency separation of the separation area are ensured. The reaction zone flow channel can be designed into a flow channel structure according to the requirement, so that the effect of high output power or high-speed hydrogen production is realized, and the separation zone can adjust the position of the outlet of the liquid cavity and the position of the baffle rib, so that the maximum outflow pressure of hydrogen, the liquid level height and the volume size of the separation zone are flexibly adjusted. The self-separating flow field design avoids an additional gas-liquid separation device, improves the integration level and usability of the electricity-hydrogen co-production device, and reduces the use cost; the partition design of the reaction area and the separation area ensures the performance and the efficiency of the device, improves the reliability of gas-liquid separation, and reduces the difficulty of optimizing the design of the gas-liquid separation flow field.
The cathode gas-liquid separation flow field plate is provided with a separation cavity and two fluid outlets, and gas-liquid layering is realized under the action of gravity. The design of the communication port at the lower position is matched, so that gas is ensured to be gathered at the upper layer of the separation cavity, and only can flow out through the gas outlet at the higher position, and liquid only can flow out through the fluid cavity outlet at the bottom.
The anode uses formate solution, and the hydrolysis reaction of formate ensures that the device does not need extra electrolyte, thereby reducing the use cost of the device. The formate solution and the dilute acid solution are used as reaction solutions, the theoretical potential of the reaction is up to 1.05V, and the device has the capability of outputting electric power externally, so that the device can realize the generation of electricity externally while generating hydrogen, and the chemical energy of reactants is fully utilized; the cathode uses dilute acid solution, and hydrogen is generated at the cathode along with the process of outputting electric power to the outside by the battery, so that zero-energy-consumption distributed high-efficiency hydrogen production is realized.
The electrochemical reaction and the hydrogen generation occur in the reaction zone, so that the fluid reaching the end point of the reaction zone becomes two-phase mixed fluid, the separation zone realizes gas-liquid layering under the action of gravity, so that gas and liquid respectively flow out of the flow field from different outlets, the gas-liquid self-separating electro-hydrogen cogeneration device can realize the simultaneous outward output of electric energy and hydrogen without adding extra electrolyte, the hydrogen production cost is reduced, and the system benefit is improved.
Drawings
FIG. 1 is a schematic elevational view of the present invention;
FIG. 2 is a schematic view of a cathode gas-liquid self-separating flow field plate of the present invention;
FIG. 3 is a graph of simulation results of a separation zone of a cathode gas-liquid separation flow field plate of the present invention;
in the figure: 1-an anode flow field plate; 2-an anode electrode; 3-cationic membrane; 4-cathode electrode; 5-cathode gas-liquid separation flow field plate; 6-dividing ribs; 7-a reaction zone flow channel; 8-a flow field inlet; 9-baffle ribs; 10-gas outlet; 11-vertical flow channels; 12-a liquid outlet; 13-a separation chamber; 14-a liquid chamber; 15-communicating port.
Detailed Description
The invention will be described in further detail with reference to the drawings and the specific examples.
Example 1:
as shown in fig. 1, the gas-liquid self-separating electro-hydrogen co-production device of the present invention comprises an anode flow field plate 1, a cathode gas-liquid self-separating flow field plate 5, an anode electrode 2 and a cathode electrode 4 carrying noble metal catalyst, and a cation membrane 3 dividing the cathode and the anode. The anode uses sodium formate solution, the cathode uses dilute acid solution as reactant, and the dilute acid solution is dilute sulfuric acid or dilute hydrochloric acid. The anode electrode 2 uses Pd-based catalyst, and the binder uses PTFE binder. The cathode electrode 4 uses a Pt-based catalyst, and the binder uses a Nafion binder. Both electrodes use three-dimensional graphite felt as electrode basal layer.
The theoretical external output voltage of the device can reach 1.05V, and in the operation process, the device can output electric energy from the cathode electrode and the anode electrode, and meanwhile, hydrogen is generated in the cathode electrode. Hydrogen gas may flow out of the device from the gas outlet 10 of the cathode gas-liquid separation flow field plate.
As shown in fig. 2, the cathode gas-liquid separation flow field plate 5 comprises a reaction zone I and a separation zone II. The two areas are separated by a separation rib 6, and only one runner is reserved at the top of the separation rib 6 to communicate the two areas of the reaction area I and the separation area II. The cathode gas-liquid self-separating flow field plate 5 is provided with two outlets and an inlet, the two outlets are arranged on the same side of the flow field plate, the outlet at the high position is a gas outlet 10, the outlet at the low position is a liquid outlet 12, and the inlet is arranged on the other side opposite to the outlet of the flow field plate. The flow field plate is provided with a flow field inlet 8 at the lower left position, the flow field inlet 8 is communicated with a reaction zone flow channel 7 of a reaction zone I, and the reaction zone flow channel 7 is a traditional serpentine, parallel, interdigital or lattice flow channel.
The separation zone II mainly comprises a separation cavity 13, a communication port 15 and a liquid cavity 14; the separation area II is divided into two cavities by a vertical partition board, one side cavity close to the reaction area I is a separation cavity 13 and the other side liquid cavity 14, the bottom of the separation cavity 13 is connected with the liquid cavity 14 through a communication port 15, and the upper part of the liquid cavity 14 is communicated with a liquid outlet 12 at the lower part of the flow field plate; the baffle rib 9 which is vertically arranged is arranged at the upper part of the separation cavity 13, the separation cavity 13 is divided into a vertical flow channel 11 and a gas flow channel, the vertical flow channel 11 which is close to one side of the separation rib 6 is communicated with the reaction zone flow channel 7 of the reaction zone I through the flow channel above the separation rib 6, and the gas flow channel is communicated with the gas outlet 10 at the high part of the flow field plate; the baffle ribs 9 are rectangular, square, trapezoidal or triangular in geometry, the baffle ribs 9 avoiding direct fluid impingement into the gas outlet 10.
After flowing in from the flow field inlet 8, the solution first flows through the reaction zone flow channels 7, generates two-phase fluid, and then passes over the zone separation ribs 6 to the separation zone II. After the mixed fluid flows into the separation chamber 13, gas-liquid stratification is achieved under the action of gravity. The layered liquid surface is higher than the bottom communication port 15, so that the gas can only leave the flow field from the upper gas outlet 10. The liquid then flows through the bottom communication port 15 to the liquid chamber 14 and eventually exits the flow field from the liquid outlet 12.
The cathode gas-liquid self-separation flow field plate 5 adopts an arrangement mode of electrochemical reaction and gas-liquid separation zone arrangement, which is convenient for carrying out independent design optimization on the cell performance and separation effect, and ensures the high performance of the cell in the reaction zone and the high-efficiency separation of the separation zone. The reaction zone flow channel can be designed into a serpentine, parallel and other flow channel structure according to the requirement, so that the effect of high output power or high-speed hydrogen production is realized. The separation area can adjust the outlet position of the liquid cavity and the position of the baffle rib, so as to realize flexible adjustment of the maximum outflow pressure of the hydrogen, the liquid level height and the volume of the separation area.
Example 2:
the flow channel 7 of the reaction zone of the cathode flow field plate is a parallel flow channel. The anode reactant solution was potassium formate and the cationic membrane 3 was a potassium ion conducting cationic membrane, otherwise constructed as in example 1.
The invention adopts formate solution and dilute acid solution as the reaction solution of the anode and the cathode of the device respectively, and the formate and the hydroxide are combined to generate oxidation reaction at the anode of the device to generate bicarbonate, water and electrons, and the reaction relation formula is as follows:
the hydroxyl in the formula is mainly generated by formate hydrolysis, so that electrolyte does not need to be added to the anode, and the hydrogen production cost is reduced. At the cathode of the device, electrons arriving through an external circuit combine with hydrogen ions of the cathode to generate hydrogen, the reaction relationship is as follows:
at the same time, the metal ions of the anode migrate through the cationic membrane to the cathode to maintain charge balance of the cathode and anode. The total theoretical potential of the reaction is up to 1.05V, and the device has the capability of outputting electric power externally, so that the device can realize the hydrogen production and simultaneously generate power externally, and the chemical energy of reactants is fully utilized.
Simulation is carried out on the flow channel of the separation area of the cathode flow field plate, which is used for verifying the separation effect of the separation area, and the simulation result obtained by using the phase field model is shown in figure 3. Dark areas in the figure are gas phase fluids and light areas are liquid phase fluids. The two-phase substances are simplified to flow in from different positions respectively, are mixed in the vertical flow channel 11, and form two-phase fluid which enters the separation cavity 13 together. The separation chamber 13 has a height of 5mm and a width of 6mm and is coupled to the liquid chamber 14 through a communication port 15 having a height of 1 mm. The figure can see that the gas-phase fluid leaves the flow field through the gas outlet 10, and the liquid-phase fluid leaves the flow field through the liquid outlet 12, so that the designed separation area of the cathode gas-liquid separation flow field plate has a good two-phase separation effect.
Claims (8)
1. A gas-liquid self-separating electricity-hydrogen co-production device is characterized in that: comprises an anode flow field plate (1), a cathode gas-liquid separation flow field plate (5), an anode electrode (2) and a cathode electrode (4) which are loaded with noble metal catalysts, and a cation membrane (3) for dividing the anode electrode (2) and the cathode electrode (4);
the cathode gas-liquid separation flow field plate (5) is divided into a reaction zone (I) and a separation zone (II) by a vertically arranged separation rib (6), the reaction zone (I) is communicated with the separation zone (II) through a flow channel above the separation rib (6), a reaction zone flow channel (7) is arranged in the reaction zone (I), and the reaction zone flow channel (7) is communicated with a flow field inlet (8); the separation zone (II) is separated by a vertical partition board into a separation cavity (13) close to one side of the reaction zone (I) and a liquid cavity (14) at the other side, the bottom of the separation cavity (13) is connected with the liquid cavity (14) through a communication port (15) below the vertical partition board, and the upper part of the liquid cavity (14) is communicated with the liquid outlet (12); the baffle rib (9) is arranged at the upper part of the separation cavity (13), the separation cavity (13) is divided into a vertical runner (11) and a gas runner, the vertical runner (11) close to one side of the separation rib (6) is communicated with the reaction zone runner (7) of the reaction zone (I) through a runner above the separation rib (6), and the gas runner is communicated with the gas outlet (10);
after the solution flows into the flow channel (7) of the reaction zone from the flow field inlet (8) to generate two-phase fluid, the mixed fluid flows into the separation cavity (13) of the separation zone (II) through the flow channel above the separation rib (6), the gas leaves the flow field from the gas outlet (10) through the gas flow channel after the mixed fluid is layered under the action of gravity, and the liquid flows into the liquid cavity (14) from the liquid outlet (12) through the bottom layer communication port (15) to leave the flow field.
2. The gas-liquid self-separating cogeneration apparatus of claim 1, wherein: the reaction zone flow channel (7) is a serpentine flow channel, a parallel flow channel, an interdigital flow channel or a lattice flow channel.
3. The gas-liquid self-separating cogeneration apparatus of claim 1, wherein: the baffle rib (9) is rectangular, square, trapezoid or triangular.
4. A gas-liquid self-separating cogeneration plant according to claim 2 or 3, wherein: the flow field inlet (8) is arranged at the lower position of one side of the cathode gas-liquid separation flow field plate (5) close to the reaction zone (I), and the gas outlet (10) and the liquid outlet (12) are respectively arranged at the upper position and the lower position of one side of the cathode gas-liquid separation flow field plate (5) close to the separation zone (II).
5. The gas-liquid self-separating cogeneration apparatus of claim 4, wherein: the cathode electrode (4) adopts a Pt-based catalyst, and the Pt-based catalyst is supported on a three-dimensional graphite felt substrate layer through a Nafion binder.
6. The gas-liquid self-separating cogeneration apparatus of claim 5, wherein: the anode electrode (2) adopts a Pd-based catalyst, and the Pd-based catalyst is supported on a three-dimensional graphite felt substrate layer through a PTFE binder.
7. The gas-liquid self-separating cogeneration apparatus of claim 4, wherein: the anode uses formate solution as a reactant and the cathode uses dilute acid solution as a reactant.
8. The gas-liquid self-separating cogeneration apparatus of claim 7, wherein: the formate solution is sodium formate or potassium formate; the dilute acid solution is dilute sulfuric acid or dilute hydrochloric acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310921511.6A CN116845280A (en) | 2023-07-26 | 2023-07-26 | Gas-liquid self-separating electricity-hydrogen cogeneration device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310921511.6A CN116845280A (en) | 2023-07-26 | 2023-07-26 | Gas-liquid self-separating electricity-hydrogen cogeneration device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116845280A true CN116845280A (en) | 2023-10-03 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310921511.6A Pending CN116845280A (en) | 2023-07-26 | 2023-07-26 | Gas-liquid self-separating electricity-hydrogen cogeneration device |
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| CN (1) | CN116845280A (en) |
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- 2023-07-26 CN CN202310921511.6A patent/CN116845280A/en active Pending
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