CN116742080A - Hydrogen fuel cell water separation method and system - Google Patents
Hydrogen fuel cell water separation method and system Download PDFInfo
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- CN116742080A CN116742080A CN202310884627.7A CN202310884627A CN116742080A CN 116742080 A CN116742080 A CN 116742080A CN 202310884627 A CN202310884627 A CN 202310884627A CN 116742080 A CN116742080 A CN 116742080A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 270
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 239000001257 hydrogen Substances 0.000 title claims abstract description 104
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 104
- 239000000446 fuel Substances 0.000 title claims abstract description 102
- 238000000926 separation method Methods 0.000 title claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 105
- 239000007789 gas Substances 0.000 claims abstract description 99
- 239000012495 reaction gas Substances 0.000 claims abstract description 54
- 238000000034 method Methods 0.000 claims abstract description 29
- 238000003487 electrochemical reaction Methods 0.000 claims abstract description 13
- 230000008569 process Effects 0.000 claims abstract description 13
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 230000036647 reaction Effects 0.000 claims abstract description 10
- 230000000694 effects Effects 0.000 claims description 32
- 239000012528 membrane Substances 0.000 claims description 32
- 230000008859 change Effects 0.000 claims description 19
- 238000009792 diffusion process Methods 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 11
- 238000003860 storage Methods 0.000 claims description 9
- 239000012071 phase Substances 0.000 claims description 8
- 239000000376 reactant Substances 0.000 claims description 8
- 238000005273 aeration Methods 0.000 claims description 7
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- 239000000306 component Substances 0.000 description 8
- 238000009826 distribution Methods 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 238000009833 condensation Methods 0.000 description 6
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- 229910052760 oxygen Inorganic materials 0.000 description 6
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- 230000001276 controlling effect Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000005259 measurement Methods 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 3
- 229910001882 dioxygen Inorganic materials 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
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- 238000012544 monitoring process Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000000470 constituent Substances 0.000 description 1
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- 239000008358 core component Substances 0.000 description 1
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- 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
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
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Abstract
The present disclosure provides a method and a system for separating water from a hydrogen fuel cell, comprising controlling the electrochemical reaction of the reaction gas in a reaction chamber according to an anode flow channel, a cathode flow channel and a pre-constructed gas flow model in the hydrogen fuel cell, and determining a first vapor generated by the chemical reaction of the reaction gas of the hydrogen fuel cell; determining second water vapor generated in the reaction chamber during the inflation process based on the temperature value of a condenser in the reaction chamber of the hydrogen fuel cell during inflation and the pressure variation values of the reaction chamber before and after inflation; and adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by taking the highest water vapor recovery rate as a constraint condition through a preset water vapor separation boundary condition, and carrying out water conveying treatment on the first water vapor and the second water vapor. The method disclosed by the application can effectively separate the moisture generated in the hydrogen fuel cell and improve the working performance of the hydrogen fuel cell.
Description
Technical Field
The disclosure relates to the technical field of new energy, in particular to a hydrogen fuel cell water separation method and system.
Background
Fuel cells will produce water while operating, while releasing a significant amount of heat. If water generated by the electrochemical reaction cannot be removed from the battery in time, water accumulation in the battery can be caused. The slight water accumulation can cause insufficient local air supply and uneven current distribution in the battery, so as to lead to uneven performance attenuation; and the battery can be seriously reversed, so that the degradation of the battery performance is accelerated, and the service life of the battery is shortened.
How to provide a solution to the above technical problems is a problem that needs to be solved by those skilled in the art.
Disclosure of Invention
The embodiment of the disclosure provides a method and a system for separating water from a hydrogen fuel cell, which can at least solve part of problems in the prior art, namely the problem that the prior art cannot timely discharge water vapor in the cell.
In a first aspect of embodiments of the present disclosure,
there is provided a hydrogen fuel cell water separation method including:
controlling the reaction gas to perform electrochemical reaction in a reaction chamber according to an anode runner, a cathode runner and a pre-constructed gas flow model in the hydrogen fuel cell, and determining first vapor generated by the chemical reaction of the reaction gas of the hydrogen fuel cell;
the determining the first water vapor generated by the chemical reaction of the reactant gases of the hydrogen fuel cell includes:
determining an anode current according to a gas flow rate of a reaction gas flowing into an anode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the anode flow channel, and a volume of the anode flow channel;
determining a cathode current according to a gas flow rate of a reaction gas flowing into a cathode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the cathode flow channel, and a volume of the cathode flow channel;
determining the first water vapor based on the correspondence between the battery current and water vapor according to the anode current and the cathode current;
determining second water vapor generated in the reaction chamber during the inflation process based on the temperature value of a condenser in the reaction chamber of the hydrogen fuel cell during inflation and the pressure variation values of the reaction chamber before and after inflation;
the determining the second water vapor generated in the reaction chamber during the inflation process based on the temperature value of the condenser in the reaction chamber of the hydrogen fuel cell during the inflation and the pressure variation values of the reaction chamber before and after the inflation comprises:
determining water saturation information based on a temperature value of a condenser in a reaction chamber of the hydrogen fuel cell during inflation and a water attribute parameter corresponding to humidified gas during inflation;
determining the second water vapor according to the pressure change values of the reaction chambers before and after inflation, the gas-liquid attribute information of the proton exchange membrane in the hydrogen fuel cell and the mass change rate between the gas phase and the liquid phase and the water saturation information;
and adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by taking the highest water vapor recovery rate as a constraint condition through a preset water vapor separation boundary condition, and carrying out water conveying treatment on the first water vapor and the second water vapor.
In an alternative embodiment of the present application,
the determining the first water vapor based on the correspondence between the battery current and the water vapor according to the anode current and the cathode current includes:
determining the anode water vapor activity corresponding to the anode current according to the corresponding relation between the anode current and the battery current and the water vapor;
determining cathode water vapor activity corresponding to the cathode current according to the corresponding relation between the cathode current and the battery current and the water vapor;
the first water vapor is determined based on the anode water vapor activity, the cathode water vapor activity, and a cell current determined from the anode current and the cathode current in combination with attribute information of the hydrogen fuel cell.
In an alternative embodiment of the present application,
the determining the first water vapor is as follows:
wherein W is 1 Represents a first water vapor, M w Represents the molar mass of water, A fc Represents the cross-sectional area of the proton exchange membrane of the hydrogen fuel cell, A m Represents the thickness of the proton exchange membrane, n represents the number of single-chip cells of the hydrogen fuel cell, I D A battery current representing the composition of the anode current and the cathode current, M representing a current density, D w Represents the water diffusion coefficient, r 1 、r 2 Respectively represent the weight coefficient corresponding to the water vapor activity of the anode and the weight coefficient corresponding to the water vapor activity of the cathode, L A 、L C The anode water vapor activity and the cathode water vapor activity are shown, respectively.
In an alternative embodiment of the present application,
the determining the second water vapor is as follows:
wherein W is 2 Represents a second water vapor, M w Represents the molar mass of water, D w Represents the water diffusion coefficient, r represents the dissolved water content, T represents the temperature value of the condenser during aeration, p v Represents the density, K of the proton exchange membrane r Represents the relative permeability, u v Represents the dynamic viscosity of the liquid, ΔP represents the pressure difference before and after aeration, S gd Representing the rate of mass change between the gas and liquid phases.
In an alternative embodiment of the present application,
the step of adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by using the preset water vapor separation boundary condition and taking the highest water vapor recovery rate as a constraint condition, and carrying out water conveying treatment on the first water vapor and the second water vapor comprises the following steps:
the water transport treatment was performed according to the following formula:
wherein Tran w Represents the control amount of the water transport treatment, α represents the heat transfer coefficient between the water surface and the gas, ε represents the porosity of the porous medium, s represents the porosity, K D Represents the diffusion coefficient of water vapor through the gas, T F Indicating the temperature of the reaction chamber, K q Represents the air permeability of the proton exchange membrane, W 1 Represents a first water vapor, W 2 Represents the second water vapor, and Δp represents the pressure difference before and after inflation.
In a second aspect of the embodiments of the present disclosure,
there is provided a hydrogen fuel cell water separation system comprising:
the first unit is used for controlling the reaction gas to perform electrochemical reaction in the reaction chamber according to an anode runner, a cathode runner and a pre-constructed gas flow model in the hydrogen fuel cell, and determining first steam generated by the chemical reaction of the reaction gas of the hydrogen fuel cell;
the first unit is further configured to determine an anode current according to a gas flow rate of a reaction gas flowing into an anode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the anode flow channel, and a volume of the anode flow channel;
determining a cathode current according to a gas flow rate of a reaction gas flowing into a cathode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the cathode flow channel, and a volume of the cathode flow channel;
determining the first water vapor based on the correspondence between the battery current and water vapor according to the anode current and the cathode current;
a second unit for determining a second water vapor generated in the reaction chamber during the inflation based on a temperature value of a condenser in the reaction chamber of the hydrogen fuel cell at the time of inflation and a pressure variation value of the reaction chamber before and after inflation;
the second unit is further used for determining water saturation information based on a temperature value of a condenser in a reaction chamber of the hydrogen fuel cell when the hydrogen fuel cell is inflated and water attribute parameters corresponding to humidified gas when the hydrogen fuel cell is inflated;
determining the second water vapor according to the pressure change values of the reaction chambers before and after inflation, the gas-liquid attribute information of the proton exchange membrane in the hydrogen fuel cell and the mass change rate between the gas phase and the liquid phase and the water saturation information;
and the third unit is used for adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by taking the highest water vapor recovery rate as a constraint condition through a preset water vapor separation boundary condition, and carrying out water management on the first water vapor and the second water vapor.
In a third aspect of the embodiments of the present disclosure,
there is provided an electronic device including:
a processor;
a memory for storing processor-executable instructions;
wherein the processor is configured to invoke the instructions stored in the memory to perform the method described previously.
In a fourth aspect of embodiments of the present disclosure,
there is provided a computer readable storage medium having stored thereon computer program instructions which, when executed by a processor, implement the method as described above.
According to the hydrogen fuel cell water separation method, the water vapor generated by the chemical reaction and the water vapor generated by the condenser in the inflation process of the reaction chamber can be determined according to the electrochemical reaction of the reaction gas in the reaction chamber, so that the water conveying treatment can be ensured to the greatest extent; and the boundary condition of water vapor separation and the highest water vapor recovery rate are set as constraint conditions, and water is conveyed and treated by adjusting the temperature and the pressure value, so that water is drained as much as possible.
Drawings
FIG. 1 is a schematic flow diagram of a hydrogen fuel cell water separation method according to an embodiment of the present disclosure;
FIG. 2 is a schematic diagram of a temperature profile of a hydrogen fuel cell according to an embodiment of the present disclosure;
fig. 3 is a schematic structural diagram of a hydrogen fuel cell water separation system according to an embodiment of the present disclosure.
Detailed Description
For the purposes of making the objects, technical solutions and advantages of the embodiments of the present disclosure more apparent, the technical solutions of the embodiments of the present disclosure will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present disclosure, and it is apparent that the described embodiments are only some embodiments of the present disclosure, not all embodiments. Based on the embodiments in this disclosure, all other embodiments that a person of ordinary skill in the art would obtain without making any inventive effort are within the scope of protection of this disclosure.
The technical scheme of the present disclosure is described in detail below with specific examples. The following embodiments may be combined with each other, and some embodiments may not be repeated for the same or similar concepts or processes.
Fig. 1 is a schematic flow chart of a water separation method of a hydrogen fuel cell according to an embodiment of the disclosure, as shown in fig. 1, the method includes:
s101, controlling the reaction gas to perform electrochemical reaction in a reaction chamber according to an anode runner, a cathode runner and a pre-constructed gas flow model in a hydrogen fuel cell, and determining first vapor generated by the chemical reaction of the reaction gas of the hydrogen fuel cell;
when the hydrogen fuel cell is operated, the cathode reaction gas oxygen is introduced into the cathode flow channel, and the anode reaction gas hydrogen is introduced into the anode flow channel. After the reaction gas is introduced into the cell, the gas is distributed to an active area in the cell by a flow channel, in the active area, hydrogen gas reaches the surface of an anode catalytic layer through a gas diffusion layer (Gas Diffusion Layer, GDL), and is dissociated into protons and electrons under the action of a catalyst, the protons pass through a proton exchange membrane which is a core component of the fuel cell, reach a cathode of the cell, and the electrons are collected by a current collecting plate to apply work to an external circuit: oxygen reaches the surface of the cathode catalytic layer through the GDL, and under the action of the catalyst, the oxygen combines with protons passing through the proton exchange membrane and external circuit electrons to generate water, and a large amount of heat is released.
Fuel cells produce water while operating and emit a large amount of heat, and attention should be paid to heat management and water management in the cells to prevent local cell performance degradation due to heat and water, thereby creating a performance shortboard.
In an alternative embodiment of the present application,
the determining the first water vapor generated by the chemical reaction of the reactant gases of the hydrogen fuel cell includes:
determining an anode current according to a gas flow rate of a reaction gas flowing into an anode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the anode flow channel, and a volume of the anode flow channel;
determining a cathode current according to a gas flow rate of a reaction gas flowing into a cathode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the cathode flow channel, and a volume of the cathode flow channel;
and determining the first water vapor based on the corresponding relation between the battery current and the water vapor according to the anode current and the cathode current.
Illustratively, the first water vapor of the present application refers to water vapor that is generated when an electrochemical reaction is performed in the reaction chamber of a hydrogen fuel cell. Alternatively, a flow meter or other gas measuring device may be used to monitor the gas flow of the reactant gas flowing into the anode flow channels of the reaction chamber in real time.
Determining anode current according to a first gas flow rate of the reaction gas flowing into the anode flow channel, a consumption amount of the reaction gas consumed by the anode flow channel, a water flow rate of a proton exchange membrane passing through the anode flow channel, a pressure sum of each component gas of the reaction gas in the anode flow channel and a volume of the anode flow channel, which are determined by the gas flow channel model;
determining a total pressure (Pa) of the reaction gas and partial pressures (P1, P2, P3,) of the respective component gases from measurement data (Qa) of a first gas flow rate of the reaction gas flowing into the anode flow channel and measurement data of a sum of pressures of the respective component gases of the reaction gas in the anode flow channel;
from the measurement data (Ca) of the consumption of the reaction gas consumed by the anode flow channels, the water flow rate (Mw) of the proton exchange membrane passing through the anode flow channels is determined by a gas flow channel model. The gas flow channel model considers factors such as physical characteristics, flow speed and transmission characteristics of the proton exchange membrane of the gas; determining a net volume of the anode flow channels from measurement data (Va) of the volume of the anode flow channels; the molar amount (Na) of the reaction gas is calculated from the total pressure (Pa) of the reaction gas and the partial pressures (P1, P2, P3,) of the respective component gases, and the net volume (Va) of the anode flow channel using an ideal gas state equation (for example, ideal gas law).
Illustratively, the anode in the embodiments of the present disclosure is dead ended, so the drain items are all zero. However, to avoid flooding and inert gas accumulation problems, embodiments of the present disclosure periodically/aperiodically open the valve of the vent valve to vent excess moisture or gas.
Illustratively, the cathode current is determined from the second gas flow rate of the reactant gas flowing into the cathode flow channels, the third gas flow rate of the reactant gas flowing out of the cathode flow channels, the mass fractions of the components in the reactant gas determined by the gas flow model, and the gas constants of the components in the reactant gas and the volume of the cathode flow channels.
Further, the method for determining the battery current from the anode current and the cathode current is as follows:
wherein I is D The current of the electric pile is represented by n, the number of single batteries in the electric pile is represented by a, the bias coefficient corresponding to the anode current is represented by A, the bias coefficient corresponding to the cathode current is represented by B, I S Represents anode current, I n Representing the cathode current.
In an alternative embodiment of the present application,
the determining the first water vapor based on the correspondence between the battery current and the water vapor according to the anode current and the cathode current includes:
determining the anode water vapor activity corresponding to the anode current according to the corresponding relation between the anode current and the battery current and the water vapor;
determining cathode water vapor activity corresponding to the cathode current according to the corresponding relation between the cathode current and the battery current and the water vapor;
the first water vapor is determined based on the anode water vapor activity, the cathode water vapor activity, and a cell current determined from the anode current and the cathode current in combination with attribute information of the hydrogen fuel cell.
Wherein, the water vapor activity is used for indicating the diffusion degree of the water vapor in the closed space.
Illustratively, according to specific data and experimental results, a corresponding relation model of battery current and water vapor generation is established, which can be determined by experimentally measuring the water vapor generation amounts under different battery currents and then fitting or establishing a mathematical model. And determining the anode water vapor activity corresponding to the anode current according to the anode current and a corresponding relation model of the battery current and water vapor, and obtaining a water vapor activity value corresponding to the anode current by interpolating or calculating the known battery current and the corresponding water vapor generation amount. And similarly, determining the cathode water vapor activity corresponding to the cathode current according to the corresponding relation model of the cathode current and the battery current and the water vapor, and obtaining the water vapor activity value corresponding to the cathode current by interpolating or calculating the known battery current and the corresponding water vapor generation amount.
Determining the amount or mole fraction of the first water vapor based on the anode water vapor activity, the cathode water vapor activity, and a cell current determined from the anode current and the cathode current in combination with attribute information of the hydrogen fuel cell.
In an alternative embodiment of the present application,
the determining the first water vapor is as follows:
wherein W is 1 Represents a first water vapor, M w Represents the molar mass of water, A fc Represents the cross-sectional area of the proton exchange membrane of the hydrogen fuel cell, A m Represents the thickness of the proton exchange membrane, n represents the number of single-chip cells of the hydrogen fuel cell, I D A battery current representing the composition of the anode current and the cathode current, M representing a current density, D w Represents the water diffusion coefficient, r 1 、r 2 Respectively represent the weight coefficient corresponding to the water vapor activity of the anode and the weight coefficient corresponding to the water vapor activity of the cathode, L A 、L C The anode water vapor activity and the cathode water vapor activity are shown, respectively.
By determining the current of the anode and the cathode according to the gas flow, consumption and volume of the anode and the cathode channels, the operating state of the battery can be precisely known and basic data can be provided for subsequent steam generation.
By monitoring the gas flow of the reaction gas flowing into the anode flow channel and the cathode flow channel of the reaction chamber and calculating the consumption of the reaction gas consumed in the anode flow channel and the cathode flow channel, the accurate control of the reaction gas flow can be realized, the stability and uniformity of the gas supply in the reaction chamber can be ensured, and the efficiency and consistency of the electrochemical reaction can be improved.
S102, determining second vapor generated in the process of inflation of the reaction chamber based on a temperature value of a condenser in the reaction chamber of the hydrogen fuel cell during inflation and pressure variation values of the reaction chamber before and after inflation;
in an alternative embodiment of the present application,
the determining the second water vapor generated in the reaction chamber during the inflation process based on the temperature value of the condenser in the reaction chamber of the hydrogen fuel cell during the inflation and the pressure variation values of the reaction chamber before and after the inflation comprises:
determining water saturation information based on a temperature value of a condenser in a reaction chamber of the hydrogen fuel cell during inflation and a water attribute parameter corresponding to humidified gas during inflation;
and determining the second water vapor according to the pressure change values of the reaction chambers before and after the inflation, the gas-liquid property information of the proton exchange membrane in the hydrogen fuel cell and the mass change rate between the gas phase and the liquid phase and the water saturation information.
According to the temperature value of the condenser when the condenser is inflated, the water saturation information is determined by combining the water attribute parameters corresponding to the humidified gas when the condenser is inflated, and the saturated steam pressure or the mole fraction of the saturated steam at a given temperature can be determined by consulting a corresponding relation table of the saturated steam pressure and the temperature of water or using tools such as a water steam meter. And determining the generation amount or mole fraction of the second water vapor according to the pressure change value of the reaction chamber before and after the inflation, the gas-liquid property information of the proton exchange membrane in the hydrogen fuel cell and the mass change rate between the gas phase and the liquid phase and combining the water saturation information. Firstly, calculating the mass variation of hydrogen and oxygen in the process of inflation according to the pressure variation values of the reaction chambers before and after inflation and the gas-liquid attribute information of the proton exchange membrane, wherein the mass variation can be calculated based on factors such as a gas diffusion theory, characteristic parameters of the proton exchange membrane, inflation time and the like; the molar amount of the second water vapor generated by the reaction of hydrogen and oxygen with water vapor during the aeration process can be calculated from the mass change rate between the gas phase and the liquid phase, which can be calculated based on the theory of chemical reaction equations, reaction kinetics, and the like.
The generation condition of the water vapor in the reaction chamber can be known in real time by monitoring the temperature and pressure change of the condenser, and the reaction condition can be regulated according to the requirement, so that the generation amount of the second water vapor can be accurately controlled; by determining the saturation information of water and the attribute of the proton exchange membrane, the reaction condition can be optimized, so that the water vapor is fully utilized in the reaction chamber, and the generation efficiency of the water vapor is improved; the production of the second water vapor is accurately controlled, so that the working state of the hydrogen fuel cell can be optimized, the energy conversion efficiency is improved, and the output performance of the hydrogen fuel cell is more stable and efficient. Enhancing the stability and reliability of hydrogen fuel cells: by accurately controlling the amount of water vapor produced, the risk of too high or too low humidity in the hydrogen fuel cell can be reduced, and a suitable working environment can be maintained, thereby enhancing the stability and reliability of the hydrogen fuel cell.
In an alternative embodiment of the present application,
the determining the second water vapor is as follows:
wherein W is 2 Represents a second water vapor, M w Represents the molar mass of water, D w Represents the water diffusion coefficient, r represents the dissolved water content, T represents the temperature value of the condenser during aeration, p v Represents the density, K of the proton exchange membrane r Represents the relative permeability, u v Represents the dynamic viscosity of the liquid, ΔP represents the pressure difference before and after aeration, S gd Representing the rate of mass change between the gas and liquid phases.
S103, adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by taking the highest water vapor recovery rate as a constraint condition through a preset water vapor separation boundary condition, and carrying out water conveying treatment on the first water vapor and the second water vapor.
When the hydrogen fuel cell is operated, a great amount of heat is generated, the proton exchange membrane is dehydrated due to the excessive cell temperature, the proton conductivity is reduced, and even the cell is irreversibly damaged in severe cases. If the local temperature is too low, the catalyst in the battery does not reach the optimal active point, resulting in low battery performance. The heat generated by the operation of the battery can lead to uneven temperature distribution in the battery, overlarge temperature difference at each point in the electric pile, uneven heating of the membrane electrode and reduced uniformity of the battery. Meanwhile, the uneven temperature distribution of the battery reduces the safety and life of the hydrogen fuel cell, and it is difficult to precisely control the operating temperature of the battery. Therefore, in order to operate the cell at an optimal temperature and to improve the uniformity within the cell, the temperature distribution within the fuel cell needs to be determined.
The present application can achieve the highest water vapor recovery rate by adjusting the temperature and pressure values of the reaction chamber of the hydrogen fuel cell, these two factors affecting the water discharge, and, in particular,
the hydrogen and oxygen gas generated by the water electrolysis accords with the wet gas in engineering thermodynamics, and the water content of the gas is shown in the following formula:
wherein W is d Represents the water content of the gas, M w 、M g Represents the molar mass of water and the molar mass of gas, P s (T) represents saturated water vapor pressure at the current temperature, P represents total gas pressure, X d Indicating the relative humidity parameter.
After the electrolytic hydrogen and oxygen gas are centrifuged to separate liquid water, the relative humidity is considered to be 100% at this time, that is, the hydrogen and oxygen gas carry saturated water vapor. The gas moisture content is only related to two parameters: total gas pressure and saturated vapor pressure at the current temperature. Where the total gas pressure is an operating parameter and the saturated water vapor pressure is a function of the current temperature.
In order to determine the amount of water precipitated by condensation, in the process of inflating the gas storage tank, under the condition that the volume of the gas storage tank and the inflation mass flow rate are fixed, the pressure of gas in the bottle is in direct proportion to time:
wherein m is w Representing the water quantity entering in the process of inflating the gas storage tank, M w Represents the molar mass of water, P s (T) represents the saturated water vapor pressure at the present temperature, deltat represents the inflation time, P 2 、P 1 Respectively indicates the internal pressure of the air charging storage tank to stop and the internal pressure of the air charging storage tank to start.
When the water content in the hydrogen fuel cell is too high, flooding occurs with high probability, and liquid water occupies gas transmission pores and reaction sites, so that voltage oscillation is caused, and even the cell is directly shut down. When the water content is too low, the mass transfer rate and the electrochemical reaction rate on the membrane are significantly slowed down, and membrane dehydration or dry cracking occurs, which seriously affects the durability of the fuel cell. Therefore, the application meets the requirements that the liquid water keeps the membrane moist and simultaneously blocks the pores of the porous material of the gas diffusion layer by adjusting the temperature and the pressure value of the reaction chamber of the hydrogen fuel cell, thereby slowing down the gas diffusion and the hydrogen oxygen reaction rate.
Condensation of water vapor in the inlet gas stream and evaporation of liquid water in the form of droplets or films in the flow channels form a heat source and a heat sink, respectively. Wherein evaporation occurs only when liquid water is present in the inlet air stream and gas unsaturation occurs simultaneously. Condensation occurs only when the gas is fully saturated and the gas temperature drops. In addition, when the constituent components of the intake gas undergo an electrochemical reaction to be consumed, a condensation phenomenon also occurs in the catalyst layer.
In an alternative embodiment of the present application,
the step of adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by using the preset water vapor separation boundary condition and taking the highest water vapor recovery rate as a constraint condition, and carrying out water conveying treatment on the first water vapor and the second water vapor comprises the following steps:
the water transport treatment was performed according to the following formula:
wherein Tran w Represents the control amount of the water transport treatment, α represents the heat transfer coefficient between the water surface and the gas, ε represents the porosity of the porous medium, s represents the porosity, K D Represents the diffusion coefficient of water vapor through the gas, T F Indicating the temperature of the reaction chamber, K q Represents the air permeability of the proton exchange membrane, W 1 Represents a first water vapor, W 2 Represents the second water vapor, and Δp represents the pressure difference before and after inflation.
Illustratively, the water vapor separation boundary conditions of the present application may include:
when modeling a hydrogen fuel cell, a one-dimensional model can determine the components distribution, pressure drop, potential drop, and overall potential drop. The two-dimensional model may reflect cell performance along or through the flow channels, primarily studying the effects of the electrolyte assembly, porous diffusion layer, and gas transport in the flow channels. The three-dimensional model can comprehensively analyze all the phenomena, and the differential equation is applied in three directions, so that the boundary condition must be applied in three dimensions. Boundary conditions of the present application may include:
the condensation rate is the largest at the air inlet of the runner, and the corresponding formula is:
wherein N is H2O Represents the condensation rate, s represents the porosity, c r Representing the rate constant, p wv 、p sat Respectively, water vapor pressure and saturated vapor pressure, and RT represents liquid water saturation.
The catalyst layer should exhibit electrical neutrality and the sum of the fluxes of current and water in the solid phase at the interface of the gas diffusion layer and the catalyst layer is at least one of continuous and zero ion current.
FIG. 2 shows a temperature distribution curve of the unit cells in the stack at an air flow rate of 500L/min, a cooling water flow rate of 45L/min, and an operating current density of 500 mAom. As can be seen from the graph, the temperature at each point in the battery increases as the battery operates. The highest temperatures in the 4 monitored single cells are TC8, TC7, TC6 and TC5 respectively, and the positions of the highest temperatures are all at the middle outlet of the bottom of the single cell stack. Wherein TC6 is the highest temperature of the galvanic pile; the lowest temperature is at the inlet and outlet of the two ends of the pile, which are respectively the test point TC1 and test point TC6 of the 1 st single cell. In the electric pile, the maximum temperature difference in the single cells is between 4.5 and 5 ℃ in the 3 rd single cell positioned in the middle of the electric pile; the minimum temperature difference is between the 1 st single cell and the 6 th single cell at the two ends of the pile, and the temperature difference is within 1 ℃; the temperature difference of the single cell 1 is between 2 and 2.5 ℃. Therefore, the temperature difference value in the single cell is related to the position of the single cell in the electric pile, the temperature difference is maximum when the single cell is in the middle position, and the temperature difference of the single cells at the two ends of the electric pile is smaller. The temperature distribution at an operating current density of 700 mA.cm was similar to the temperature distribution characteristics of the single cell at an operating current density of 500 mA.cm.
In a second aspect of the embodiments of the present disclosure,
fig. 3 is a schematic structural diagram of a hydrogen fuel cell water separation system according to an embodiment of the disclosure, including:
the first unit is used for controlling the reaction gas to perform electrochemical reaction in the reaction chamber according to an anode runner, a cathode runner and a pre-constructed gas flow model in the hydrogen fuel cell, and determining first steam generated by the chemical reaction of the reaction gas of the hydrogen fuel cell;
the first unit is further configured to determine an anode current according to a gas flow rate of a reaction gas flowing into an anode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the anode flow channel, and a volume of the anode flow channel;
determining a cathode current according to a gas flow rate of a reaction gas flowing into a cathode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the cathode flow channel, and a volume of the cathode flow channel;
determining the first water vapor based on the correspondence between the battery current and water vapor according to the anode current and the cathode current;
a second unit for determining a second water vapor generated in the reaction chamber during the inflation based on a temperature value of a condenser in the reaction chamber of the hydrogen fuel cell at the time of inflation and a pressure variation value of the reaction chamber before and after inflation;
the second unit is further used for determining water saturation information based on a temperature value of a condenser in a reaction chamber of the hydrogen fuel cell when the hydrogen fuel cell is inflated and water attribute parameters corresponding to humidified gas when the hydrogen fuel cell is inflated;
determining the second water vapor according to the pressure change values of the reaction chambers before and after inflation, the gas-liquid attribute information of the proton exchange membrane in the hydrogen fuel cell and the mass change rate between the gas phase and the liquid phase and the water saturation information;
and the third unit is used for adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by taking the highest water vapor recovery rate as a constraint condition through a preset water vapor separation boundary condition, and carrying out water management on the first water vapor and the second water vapor.
In a third aspect of the embodiments of the present disclosure,
there is provided an electronic device including:
a processor;
a memory for storing processor-executable instructions;
wherein the processor is configured to invoke the instructions stored in the memory to perform the method described previously.
In a fourth aspect of embodiments of the present disclosure,
there is provided a computer readable storage medium having stored thereon computer program instructions which, when executed by a processor, implement the method as described above.
The present application may be a method, apparatus, system, and/or computer program product. The computer program product may include a computer readable storage medium having computer readable program instructions embodied thereon for performing various aspects of the present application.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present disclosure, and not for limiting the same; although the present disclosure has been described in detail with reference to the foregoing embodiments, it should be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the corresponding technical solutions from the scope of the technical solutions of the embodiments of the present disclosure.
Claims (8)
1. A hydrogen fuel cell water separation method, characterized by comprising:
controlling the reaction gas to perform electrochemical reaction in a reaction chamber according to an anode runner, a cathode runner and a pre-constructed gas flow model in the hydrogen fuel cell, and determining first vapor generated by the chemical reaction of the reaction gas of the hydrogen fuel cell;
the determining the first water vapor generated by the chemical reaction of the reactant gases of the hydrogen fuel cell includes:
determining an anode current according to a gas flow rate of a reaction gas flowing into an anode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the anode flow channel, and a volume of the anode flow channel;
determining a cathode current according to a gas flow rate of a reaction gas flowing into a cathode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the cathode flow channel, and a volume of the cathode flow channel;
determining the first water vapor based on the correspondence between the battery current and water vapor according to the anode current and the cathode current;
determining second water vapor generated in the reaction chamber during the inflation process based on the temperature value of a condenser in the reaction chamber of the hydrogen fuel cell during inflation and the pressure variation values of the reaction chamber before and after inflation;
the determining the second water vapor generated in the reaction chamber during the inflation process based on the temperature value of the condenser in the reaction chamber of the hydrogen fuel cell during the inflation and the pressure variation values of the reaction chamber before and after the inflation comprises:
determining water saturation information based on a temperature value of a condenser in a reaction chamber of the hydrogen fuel cell during inflation and a water attribute parameter corresponding to humidified gas during inflation;
determining the second water vapor according to the pressure change values of the reaction chambers before and after inflation, the gas-liquid attribute information of the proton exchange membrane in the hydrogen fuel cell and the mass change rate between the gas phase and the liquid phase and the water saturation information;
and adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by taking the highest water vapor recovery rate as a constraint condition through a preset water vapor separation boundary condition, and carrying out water conveying treatment on the first water vapor and the second water vapor.
2. The method of claim 1, wherein the determining the first water vapor based on the correspondence of the battery current and water vapor from the anode current and the cathode current comprises:
determining the anode water vapor activity corresponding to the anode current according to the corresponding relation between the anode current and the battery current and the water vapor;
determining cathode water vapor activity corresponding to the cathode current according to the corresponding relation between the cathode current and the battery current and the water vapor;
the first water vapor is determined based on the anode water vapor activity, the cathode water vapor activity, and a cell current determined from the anode current and the cathode current in combination with attribute information of the hydrogen fuel cell.
3. The method of claim 2, wherein the step of determining the position of the substrate comprises,
the determining the first water vapor is as follows:
wherein W is 1 Represents a first water vapor, M w Represents the molar mass of water, A fc Represents the cross-sectional area of the proton exchange membrane of the hydrogen fuel cell, A m Represents the thickness of the proton exchange membrane, n represents the number of single-chip cells of the hydrogen fuel cell, I D A battery current representing the composition of the anode current and the cathode current, M representing a current density, D w Represents the water diffusion coefficient, r 1 、r 2 Respectively represent the weight coefficient corresponding to the water vapor activity of the anode and the weight coefficient corresponding to the water vapor activity of the cathode, L A 、L C The anode water vapor activity and the cathode water vapor activity are shown, respectively.
4. The method of claim 1, wherein the step of determining the position of the substrate comprises,
the determining the second water vapor is as follows:
wherein W is 2 Represents a second water vapor, M w Represents the molar mass of water, D w Represents the water diffusion coefficient, r represents the dissolved water content, T represents the temperature value of the condenser during aeration, p v Represents the density, K of the proton exchange membrane r Represents the relative permeability, u v Represents the dynamic viscosity of the liquid, ΔP represents the pressure difference before and after aeration, S gd Representing the rate of mass change between the gas and liquid phases.
5. The method of claim 1, wherein adjusting the temperature and pressure values of the hydrogen fuel cell reaction chamber with the highest water vapor recovery rate as a constraint by the preset water vapor separation boundary conditions, comprises:
the water transport treatment was performed according to the following formula:
wherein Tran w Represents the control amount of the water transport treatment, α represents the heat transfer coefficient between the water surface and the gas, ε represents the porosity of the porous medium, s represents the porosity, K D Represents the diffusion coefficient of water vapor through the gas, T F Indicating the temperature of the reaction chamber, K q Represents the air permeability of the proton exchange membrane, W 1 Represents a first water vapor, W 2 Represents the second water vapor, and Δp represents the pressure difference before and after inflation.
6. A hydrogen fuel cell water separation system, comprising:
the first unit is used for controlling the reaction gas to perform electrochemical reaction in the reaction chamber according to an anode runner, a cathode runner and a pre-constructed gas flow model in the hydrogen fuel cell, and determining first steam generated by the chemical reaction of the reaction gas of the hydrogen fuel cell;
the first unit is further configured to determine an anode current according to a gas flow rate of a reaction gas flowing into an anode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the anode flow channel, and a volume of the anode flow channel;
determining a cathode current according to a gas flow rate of a reaction gas flowing into a cathode flow channel of the reaction chamber, a consumption amount of the reaction gas consumed by the cathode flow channel, and a volume of the cathode flow channel;
determining the first water vapor based on the correspondence between the battery current and water vapor according to the anode current and the cathode current;
a second unit for determining a second water vapor generated in the reaction chamber during the inflation based on a temperature value of a condenser in the reaction chamber of the hydrogen fuel cell at the time of inflation and a pressure variation value of the reaction chamber before and after inflation;
the second unit is further used for determining water saturation information based on a temperature value of a condenser in a reaction chamber of the hydrogen fuel cell when the hydrogen fuel cell is inflated and water attribute parameters corresponding to humidified gas when the hydrogen fuel cell is inflated;
determining the second water vapor according to the pressure change values of the reaction chambers before and after inflation, the gas-liquid attribute information of the proton exchange membrane in the hydrogen fuel cell and the mass change rate between the gas phase and the liquid phase and the water saturation information;
and the third unit is used for adjusting the temperature and pressure value of the hydrogen fuel cell reaction chamber by taking the highest water vapor recovery rate as a constraint condition through a preset water vapor separation boundary condition, and carrying out water management on the first water vapor and the second water vapor.
7. A hydrogen fuel cell water separation apparatus, characterized by comprising:
a processor;
a memory for storing processor-executable instructions;
wherein the processor is configured to invoke the instructions stored in the memory to perform the method of any of claims 1 to 5.
8. A computer readable storage medium having stored thereon computer program instructions, which when executed by a processor, implement the method of any of claims 1 to 5.
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