CN111900442A - Fuel cell gas flow distribution device and control method - Google Patents

Fuel cell gas flow distribution device and control method Download PDF

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CN111900442A
CN111900442A CN202010554439.4A CN202010554439A CN111900442A CN 111900442 A CN111900442 A CN 111900442A CN 202010554439 A CN202010554439 A CN 202010554439A CN 111900442 A CN111900442 A CN 111900442A
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fuel cell
gas
stage
cell stack
target
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CN111900442B (en
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张擘
刘佰博
齐洪峰
李明高
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CRRC Industry Institute Co Ltd
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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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04746—Pressure; Flow
    • H01M8/04753—Pressure; Flow of fuel cell reactants
    • 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
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04992—Processes for controlling fuel cells or fuel cell systems characterised by the implementation of mathematical or computational algorithms, e.g. feedback control loops, fuzzy logic, neural networks or artificial intelligence
    • 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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  • Life Sciences & Earth Sciences (AREA)
  • Fuel Cell (AREA)
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Abstract

The embodiment of the invention provides a fuel cell gas flow distribution device and a control method, wherein the fuel cell gas flow distribution device comprises a mass flow meter, a mass flow meter and a control device, wherein the mass flow meter is used for measuring the actual mass flow of reaction gas in a gas inlet main pipe; the pressurization module is used for increasing the pressure of the reaction gas in the gas inlet main pipe so as to enable the reaction gas to enter the flow distribution module; the master controller is used for sending a preset signal to the flow distribution module; and the flow distribution module is used for determining a corresponding preset control strategy according to the preset signal, so that the flow distribution module is communicated with only one target air inlet branch pipe at each time and circularly charges air to each air inlet branch pipe in a reciprocating manner. The embodiment of the invention alternately provides reaction gas for each fuel cell stack through the flow distribution module, thereby realizing the function of simultaneously providing the reaction gas for a plurality of fuel cell stacks through one compressor, and reducing the auxiliary power consumption and the cost of the fuel cell power system; the problems of energy loss and waste are solved, and the efficiency of the fuel cell power system is improved.

Description

Fuel cell gas flow distribution device and control method
Technical Field
The invention relates to the technical field of batteries, in particular to a fuel cell gas flow distribution device and a control method.
Background
In recent years, fuel cell technologies, particularly, stack technologies, electrode plate technologies, catalyst technologies, and the like, have been rapidly developed. The power of the electric pile is gradually increased, and the power density is increased. In the aspect of a system, the volume of a fuel cell power system is gradually reduced, and the integration level of the system is greatly improved. Therefore, the fuel cell power system has wide application prospect in the field of traffic vehicles.
With the rapid increase in fuel cell power, the air demand on the cathode side of the stack also increases substantially. In order to ensure the normal and efficient operation of the electrochemical reaction in the electric pile, the current high-power fuel cell needs to be equipped with an air supercharging device so as to ensure the sufficient gas concentration at the cathode side of the electric pile. At present, the power grade of a single galvanic pile can break through 120kW, and the net output power of the system is about 100 kW. The continuous increase of system power requires a plurality of stacks, and a plurality of fuel cell system modules are connected in parallel to provide output power, which results in a large increase of cost, and the reliability and safety of the system are obviously affected. One of the main reasons that the power of the single-cell stack fuel cell system is difficult to be further increased is limited by the auxiliary components of the system. The technology of the electric air compressor for the vehicle is one of bottlenecks, and the air flow demand of a high-power electric pile is difficult to meet by the prior art under the condition of comprehensively considering the size, the weight and the noise.
However, when the fuel cell stack is operated at a low power, the gas excess coefficient of the cathode side of the stack can reach 5 or more due to a decrease in the electrochemical reaction rate. The excess factor is also between 1.5 and 2.5 at rated power operation. This shows that about 50% -80% of the gas is discharged by the system without participating in the electrochemical reaction during the power generation process of the fuel cell. The purpose of this is to ensure the sufficient supply of the gas participating in the electrochemical reaction in the stack, but will cause a large amount of energy waste, and also make the power increase of the fuel cell system be restricted by the factors such as the power consumption increase of the auxiliary components such as the air compressor, etc., and the volume and weight increase by times.
Disclosure of Invention
In order to solve the above problems, embodiments of the present invention provide a fuel cell gas flow distribution device and a control method.
In a first aspect, an embodiment of the present invention provides a fuel cell gas flow distribution device, including:
intake manifold, a plurality of air inlet branch pipe, mass flow meter, pressure boost module, flow distribution module and total controller, wherein, intake manifold's one end and target compressor are connected, mass flow meter the pressure boost module with flow distribution module installs in proper order on the intake manifold, flow distribution module's exit end is connected with the one end of each air inlet branch pipe, and the other end and each fuel cell pile of each air inlet branch pipe are connected, wherein:
the mass flow meter is used for measuring the actual mass flow of the reaction gas in the gas inlet main pipe;
the pressurization module is used for increasing the pressure of the reaction gas in the gas inlet main pipe so that the reaction gas enters the flow distribution module;
the master controller is used for sending a preset signal to the flow distribution module;
the flow distribution module is used for determining a corresponding preset control strategy according to the preset signal, so that the flow distribution module is only communicated with one target air inlet branch pipe at a time, when the target fuel cell stack enters a stage T2, reactant gas is not required to be continuously provided for the target fuel cell stack, the reactant gas is distributed to any other fuel cell stack, any other fuel cell stack enters a stage T1, after the target fuel cell stack enters a stage T3, the reactant gas is supplemented for the target fuel cell stack, the target fuel cell stack enters a stage T1 again, the reaction of each fuel cell stack is divided into a stage T1, a stage T2 and a stage T3 according to the time sequence, and the stage T1 represents the process that the reactant gas passes through the target air inlet branch pipe to the target fuel cell stack, the stage T2 represents the process of the reactant gas filling the working volume in the target fuel cell stack, the stage T3 represents the process of the reactant gas completing the electrochemical reaction at the working volume, and the duration of the stage T1 is determined according to the actual mass flow.
Preferably, the flow distribution module includes: the gas flow control device comprises a rotating blade, a driving motor, a rotating shaft, a rotating limiting groove, a gas flow distribution mechanism body and a gas flow control unit, wherein the rotating blade is arranged on the rotating shaft;
the driving motor is connected with the rotating shaft, the rotating shaft is also connected with the rotating blades, and the rotating limiting grooves are positioned on the outer sides of the rotating blades;
the rotating blade includes a hollow portion and a solid portion;
the gas flow distribution mechanism body comprises a plurality of gas distribution ports, each gas distribution port corresponds to each gas inlet branch pipe, and the gas distribution ports corresponding to the gas inlet branch pipes which are not communicated are sealed;
the gas flow control unit is used for controlling the driving motor according to the preset signal and driving a motor in the fuel cell gas flow distribution mechanism body so as to adjust the rotating speed and the stop position of the rotating blade, so that the flow distribution module is communicated with only one target gas inlet branch pipe at each time.
Preferably, the length of each inlet branch pipe is the same, and the number of times the pipe is bent is the same as the bending angle.
In a second aspect, an embodiment of the present invention provides a control method for a fuel cell gas flow distribution device, including:
measuring an actual mass flow of reactant gas in the inlet manifold by the mass flow meter;
increasing the pressure of the reaction gas in the gas inlet manifold through the pressurization module so that the reaction gas enters the flow distribution module;
sending a preset signal to the flow distribution module through the master controller;
determining a corresponding preset control strategy by the flow distribution module according to the preset signal, so that the flow distribution module is communicated with only one target air inlet branch pipe at a time, when the target fuel cell stack enters a stage T2, reactant gas is not required to be continuously provided for the target fuel cell stack, the reactant gas is distributed to any other fuel cell stack, any other fuel cell stack enters a stage T1, after the target fuel cell stack enters a stage T3, the target fuel cell stack is supplemented with reactant gas flow according to the time of the stage T1 or the time of the stage T2, the target fuel cell stack enters a stage T1 again, the reaction of each fuel cell stack is divided into a stage T1, a stage T2 and a stage T3 according to the time sequence, the stage T1 represents the process of the reactant gas passing through the target air inlet branch pipe to the target fuel cell stack, the stage T2 represents the process required for the reactant gas to fill the working volume within the target fuel cell stack, the stage T3 represents the process required for the reactant gas to complete the electrochemical reaction at the working volume, and the duration of the stage T1 is determined based on the actual mass flow rate.
Preferably, the preset control strategy includes:
if the preset signal is a starting signal, the rotating blade rotates at a constant speed at a first speed, and the first speed is determined according to the opening size of the rotating blade and the duration of the T2 stage;
if the preset signal is that the master controller sends a power demand signal and the equivalent time is longer than the duration of the stage T1, the rotating blades rotate at a second speed at a constant speed;
if the preset signal is that the master controller sends a power demand signal, and the equivalent time is less than the duration of a T1 stage, the rotating blades rotate at a third speed at a constant speed, wherein the equivalent time is determined according to the T2 stage time, the T2 equivalent time, the duration of the T3 stage and gamma, the gamma represents an equivalent coefficient for simultaneously performing gas diffusion and electrochemical reaction, the equivalent time is determined by the length of a flow channel on a fuel cell stack plate, the outlet pressure of the fuel cell stack, the pressure at the inlet of the fuel cell stack and the flow rate of reactant gas at the inlet of the fuel cell stack, the second speed is determined according to the opening size of the rotating blades and the equivalent time, and the third speed is determined according to the opening size of the rotating blades and the duration of the T1 stage;
and if the preset signal is a stop signal, the rotating blade rotates at the first speed at a constant speed.
Preferably, when the master controller sends the power demand signal, the preset signal is that the rotating blades rotate between any two intake branch pipes at a fourth speed, the fourth speed is determined according to an angle between any two branch pipes and a gas distribution frequency of the target compressor at the maximum flow rate, and the gas distribution frequency of the target compressor at the maximum flow rate is determined according to the equivalent time and the duration of the T1 stage.
Preferably, for the target intake manifold, the duration of the T1 phase is determined by:
T1＝LAIM_1/S1*α，
S1＝f1/(π*r2)，
wherein, T1Denotes the duration, L, of the T1 phaseAIM_1Indicates the length of the target intake manifold, S1Denotes the flow rate of the reaction gas, f1Representing an actual volume flow of the target fuel cell stack, r being a radius of the target intake manifold;
the duration of stage T2 is determined by:
T2＝V2/f2*β，
wherein, T2Denotes the duration, V, of the T2 phase2Representing the working volume of reactant gas in the target fuel cell stack, f2Representing an actual volumetric flow rate of the target fuel cell stack, β representing a diffusion coefficient of the target fuel cell stack;
the duration of stage T3 is determined by:
T3＝tv-tLim，
wherein, T3Denotes the duration, T, of the stage T3vIndicates the time at which the target fuel cell stack starts to emit the rated voltage, tLimIndicating electrificationThe voltage fluctuates after the slow rate of the chemical reaction until the time of reaching the limited voltage value.
Preferably, the first speed is determined in particular according to the following formula:
R1＝θ1/(T2*6)，
wherein R is1Representing said first speed, θ1Denotes the size of the opening, T, of the rotating blade2Indicating the duration of the T2 phase.
Preferably, the second speed and the third speed are determined according to the following formulas:
R2＝θ1/(T23*6)，
T23＝[(T2-T2′)+T3]*γ，
T2′＝l*Pout/S2*Pin，
S2＝f1/(w*h)，
wherein R is2Representing said second speed, T1Denotes the duration of the stage T1, T23Represents said equivalent time, T2Denotes the duration of the stage T2, T3The duration of the T3 stage is shown, gamma is the equivalent coefficient of simultaneous gas diffusion and electrochemical reaction, l is the length of the flow channel on the target fuel cell stack plate, and P isoutIs the target fuel cell stack outlet pressure, PinRepresents the target fuel cell stack inlet pressure, S2Representing the target fuel cell stack inlet reactant gas flow rate, f1Representing the actual volume flow of the target fuel cell stack, w representing the width of a flow channel on the target fuel cell stack polar plate, and h representing the depth of the flow channel on the target fuel cell stack polar plate;
the third speed is specifically determined according to the following formula:
R2′＝θ1/(T1*6)，
wherein R is2′Representing the third speed.
Preferably, the fourth speed is determined by the following formula:
R3＝θ2*HCP/6，
HCP＝1/Δ(T23-T1)，
wherein R is3Representing said fourth speed, θ2Representing the angle, T, between two adjacent inlet manifolds23Represents said equivalent time, T1Indicating the duration of the T1 phase.
In a third aspect, an embodiment of the present invention provides an electronic device, which includes a memory, a processor, and a computer program stored in the memory and executable on the processor, where the processor executes the computer program to implement the steps of the method for controlling a fuel cell gas flow distribution device according to the first aspect of the present invention.
In a fourth aspect, an embodiment of the present invention provides a non-transitory computer-readable storage medium, on which a computer program is stored, which when executed by a processor, implements the steps of the control method of a fuel cell gas flow distribution apparatus provided in the first aspect of the present invention.
The embodiment of the invention provides a fuel cell gas flow distribution device and a control method, wherein reaction gas is alternately provided for each fuel cell stack through a flow distribution module, so that the function of simultaneously providing the reaction gas for a plurality of fuel cell stacks through one compressor is realized, the auxiliary power consumption and the cost of a fuel cell power system are reduced, and the system integration level is further improved; and the problems of energy loss and waste caused by high excess coefficient of reaction gas on the cathode side of the conventional fuel cell stack are solved, and the efficiency of a fuel cell power system is improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and those skilled in the art can also obtain other drawings according to the drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a fuel cell gas flow distribution device according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a traffic distribution module according to an embodiment of the present invention;
FIG. 3 is a front view of a traffic distribution module in an embodiment of the present invention;
FIG. 4 is a top view of a flow distribution module in an embodiment of the present invention;
FIG. 5 is a right side view of a traffic distribution module in an embodiment of the present invention;
FIG. 6 is a schematic structural view of three different forms of a rotary vane in an embodiment of the present invention;
fig. 7 is a flowchart of a control method of a fuel cell gas flow distribution device according to an embodiment of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the prior art, the power requirement of a certain fuel cell power system is 400kW, the maximum power of a configurable single electric pile is 100kW, and if the electric pile is used, the gas flow requirement of the cathode side is calculated to be 135 g/s. After the inquiry, only a few superchargers can meet the flow demand. However, to achieve the output requirement of 400kW system power, 4 superchargers are required to be equipped simultaneously, and 4 sets of 100kW fuel cell modules are formed to meet the requirement.
According to the technical scheme, the cost and the structural complexity of the 4 sets of 100kW fuel cell modules are greatly improved, and the control difficulty is increased. Although currently on passenger or light commercial vehicles, a fuel cell module of 100kW maximum power can meet the basic requirements for a 1-pack fuel cell module. However, the use of more powerful fuel cell power systems in other vehicles, rail traffic or marine vessels is greatly limited for future developments. Moreover, the power consumption of the selectable compressor models in the scheme reaches 22kW, 17kW and 26.5kW respectively, and the noise grades are 106db, 95db and 88db respectively from the perspective of the compressor. There are significant drawbacks to a power system consisting of 4 sets of 100kW fuel cell modules, both from noise level and compressor power consumption. And the maximum efficiency of the fuel cell system can be greatly reduced by the excessive power consumption of the auxiliary device, so that the characteristics of cleanness and high efficiency of the fuel cell can not be fully exerted.
The embodiment of the invention provides a fuel cell gas flow distribution device, which reasonably distributes the gas flow by measuring the time required by the gas entering a galvanic pile to participate in electrochemical reaction under the unit volume, so that a single compressor can simultaneously provide the gas flow for a plurality of fuel cell galvanic piles, thereby reducing the auxiliary power consumption of the fuel cell and improving the system efficiency.
Fig. 1 is a schematic structural diagram of a fuel cell gas flow distribution device according to an embodiment of the present invention, as shown in fig. 1, the device includes: intake manifold, a plurality of air inlet branch pipe, mass flow meter, pressure boost module, flow distribution device and total controller, wherein, intake manifold's one end and target compressor are connected, mass flow meter the pressure boost module with flow distribution device installs in proper order on the intake manifold, flow distribution device's exit end is connected with the one end of each air inlet branch pipe, and the other end and each fuel cell pile of each air inlet branch pipe are connected, wherein:
the mass flow meter is used for measuring the actual mass flow of the reaction gas in the gas inlet main pipe;
the pressurization module is used for increasing the pressure of the reaction gas in the gas inlet manifold so that the reaction gas enters the flow distribution device;
the master controller is used for sending a preset signal to the flow distribution device according to the reaction condition of each fuel cell stack;
the flow distribution device is used for determining a corresponding preset control strategy according to the preset signal, enabling the flow distribution device to be communicated with only one target air inlet branch pipe at a time, enabling the target fuel cell stack to enter a T2 stage without continuously providing reaction gas for the target fuel cell stack, distributing the reaction gas to any other fuel cell stack, enabling any other fuel cell stack to enter a T1 stage, supplementing the target fuel cell stack with the flow of the reaction gas according to the time of the T1 stage or the time of the T2 stage after the target fuel cell stack enters the T3 stage, enabling the target fuel cell stack to enter a T1 stage again, enabling the reaction of each fuel cell stack to be divided into a T1 stage, a T2 stage and a T3 stage according to the time sequence, wherein the T1 stage represents the process of the reaction gas passing through the target air inlet branch pipe to the target fuel cell stack, the stage T2 represents the process of the reactant gas filling the working volume in the target fuel cell stack, the stage T3 represents the process of the reactant gas completing the electrochemical reaction at the working volume, and the duration of the stage T1 is determined according to the actual mass flow.
Specifically, the fuel cell gas flow distribution device comprises an air inlet manifold, a plurality of air inlet branch pipes, a mass flow meter, a pressurization module, a flow distribution device and a master controller, wherein one end of the air inlet manifold is connected with a target compressor, the mass flow meter, the pressurization module and the flow distribution module are sequentially installed at the other end of the air inlet manifold, the outlet end of the flow distribution module is connected with one end of each air inlet branch pipe, and the tail end of each air inlet branch pipe is connected with a fuel cell stack.
In the figure, FCs _1, FCs _2, and FCs _ n denote fuel cell stacks, ACMm denotes a boost module, ACMc denotes a controller of the boost module, AFMm denotes a mass flow meter, ASMm denotes a gas flow distribution mechanism body, ASMc denotes a gas flow control unit, FCc denotes a total controller, AIT denotes an intake manifold, AIM _1, AIM _2, and AIM _ n denote intake branch pipes, and tps (x) denotes a temperature and pressure integrated sensor.
Specifically, the number of the fuel cell stacks is determined according to the power of the fuel cell power system and the power of a single fuel cell stack, the fuel cell stacks can be PEMFC, SOFC, MFC and other types of stacks, and the reaction gas can be hydrogen, oxygen, air and other gaseous substances. The fuel cell stacks in the embodiment of the invention are the stacks with the same stack type, power, volume, mass and reaction gas flow, the number of the air inlet branch pipes is the same as that of the fuel cell stacks, and one air inlet branch pipe corresponds to one fuel cell stack.
Specifically, the fuel cell stacks should be arranged in a manner that the distance between the reactant gas inlet of each fuel cell stack and the flow distribution module is consistent as much as possible, so that the moving time of the reactant gas in the gas inlet branch pipe is similar.
The target compressor compresses reaction gas to enter a main gas inlet pipe, and the reaction gas passes through a mass flow meter which measures the actual mass flow of the reaction gas in the gas inlet main pipe.
The function of the boost module is to increase the pressure in the intake manifold so that the reactant gas has sufficient pressure to enter the flow distribution module. The pressurizing module in the embodiment of the invention is an electrically driven centrifugal pressurizing device, has the characteristics of high pressure ratio and large flow, and can provide reaction gas for a plurality of fuel cell electric piles in the embodiment of the invention.
The master controller is used for monitoring the reaction condition of each fuel cell stack and sending a preset signal to the flow distribution module.
The flow distribution module determines corresponding preset control strategies according to the preset signals, the corresponding preset control strategies of different preset signals are different, but generally speaking, the purpose of the preset control strategies is to enable the flow distribution module to be communicated with only one air inlet branch pipe at each time, and the communicated air inlet branch pipe is called as a target air inlet branch pipe. The period of filling each fuel cell stack with the reactant gas consists of three stages, namely a stage T1, a stage T2 and a stage T3, wherein the stage T1 represents the process of the reactant gas passing through a target air inlet branch pipe to the target fuel cell stack, the stage T2 represents the process of filling the working volume in the fuel cell stack with the reactant gas, the stage T3 represents the process of completing the electrochemical reaction of the reactant gas under the working volume, and the duration of the stage T1 is determined according to the actual mass flow.
The principle of the whole flow distribution module is as follows: when the target fuel cell is filled with the reactant gas through the target intake manifold, the reactant gas first passes through the target intake manifold, that is, the T1 stage is passed, and when the target fuel cell enters the T2 stage, the reactant gas in the intake manifold enters the target fuel cell stack, and there is no need to continuously supply the reactant gas to the target fuel cell stack, and the reactant gas is distributed to any other fuel cell stack, so that any other fuel cell stack enters the T1 stage. When the target fuel cell stack enters the stage T3, the target fuel cell stack is replenished with reaction gas so that the target fuel cell re-enters the stage T1. The circulation is repeated, so that the use efficiency of the compressor is improved.
In summary, the embodiment of the invention alternately provides the reaction gas to each fuel cell stack through the flow distribution module, thereby realizing the function of simultaneously providing the reaction gas to a plurality of fuel cell stacks through one compressor, reducing the auxiliary power consumption and the cost of the fuel cell power system, and further improving the system integration level; and the problems of energy loss and waste caused by high excess coefficient of reaction gas on the cathode side of the conventional fuel cell stack are solved, and the efficiency of a fuel cell power system is improved.
The fuel cell gas flow distribution device also comprises a controller of the pressurization module, one end of the controller of the pressurization module is connected with the pressurization module, the other end of the controller of the pressurization module is connected with the master controller, and the controller of the pressurization module is used for receiving a control instruction sent by the master controller and controlling the pressurization module to be opened or closed according to the control instruction.
On the basis of the foregoing embodiments, preferably, fig. 2 is a schematic structural diagram of a flow distribution module provided in an embodiment of the present invention, fig. 3 is a front view of the flow distribution module in the embodiment of the present invention, fig. 4 is a top view of the flow distribution module in the embodiment of the present invention, fig. 5 is a right view of the flow distribution module in the embodiment of the present invention, and as shown in fig. 2 to fig. 5, the flow distribution module includes: the gas flow control device comprises a rotating blade, a driving motor, a rotating shaft, a rotating limiting groove, a gas flow distribution mechanism body and a gas flow control unit, wherein the rotating blade is arranged on the rotating shaft;
in the figure, CP denotes a rotary blade, M denotes a drive motor and a rotary shaft, ML denotes a rotation restricting groove, ASMm denotes a gas flow rate distribution mechanism body, ASMc denotes a gas flow rate control unit, AITs denotes a housing of the gas flow rate distribution mechanism body, and AIMa denotes a gas intake manifold joint.
Specifically, fig. 6 is a schematic structural view of three different forms of a rotary vane in an embodiment of the present invention, and as shown in fig. 6, CP1, CP2, and CP3 denote three structures of the rotary vane, where black denotes a solid portion and white denotes a hollow portion. The rotary blades can be of various structural forms and materials, the size of each blade can be determined according to the size of the air inlet main pipe, the thickness of each blade is 0.5mm, and the shape, the size and the number of the openings of the blades can be determined according to the number and the form of the air inlet branch pipes.
The driving motor is connected with the rotating shaft, the rotating shaft is also connected with the rotating blades, and the rotating limiting grooves are positioned on the outer sides of the rotating blades;
the driving motor is connected with the rotating shaft, the rotating shaft and the rotating blade are positioned and connected through splines, and the end part of the rotating shaft is fastened through a locknut. The driving motor is driven by the gas flow control unit, and the direct current rotating speed is adjustable.
The rotation limiting groove is located the rotating vane outside, and width 0.6mm, degree of depth 0.2mm, and its effect is that the vibrations of rotating vane at level and vertical direction are restricted, prevents simultaneously that rotating vane from taking place to interfere with air intake manifold in rotating, and then causes the blade card to die, damage and to the damage of air intake manifold inner wall.
The rotary blade is circular and comprises a hollow part and a solid part;
the gas flow distribution mechanism body comprises a plurality of gas distribution ports, each gas distribution port corresponds to each gas inlet branch pipe, and the gas distribution ports which are not connected with the gas inlet branch pipes are sealed;
the gas flow distribution mechanism body is of a cylindrical structure and consists of three parts, namely a gas inlet main pipe connecting part, a gas distribution part and a gas inlet branch pipe connecting part. The gas distribution part can process corresponding number of gas distribution ports according to the actual number of the galvanic piles, or the gas distribution ports which are not connected with pipelines are sealed during actual use, so that waste of reaction gas is avoided.
The gas flow control unit is used for controlling the driving motor according to the preset signal and driving a motor in the fuel cell gas flow distribution mechanism body so as to adjust the rotating speed and the stop position of the rotating blade.
The gas flow control unit is responsible for driving a motor in the fuel cell gas flow distribution mechanism body, adjusting the rotating speed, the stopping position and the like of the motor, receiving a preset signal from the master controller, and simultaneously sending a state signal of the flow distribution module to the master controller.
Reaction gas inlet manifold connects and gas flow distribution mechanism body shell, and formula structure as an organic whole recommends to adopt the aluminum alloy material to process, and other types of metal and nonmetal material also can use under the condition of satisfying intensity and weight requirement. The housing size may be determined based on the intake manifold size. The joint and the main pipe are connected and fastened by a clamp.
The reaction gas inlet branch pipe joint is arranged on the inner side of the inlet main pipe, one end of the reaction gas inlet branch pipe joint is connected with a gas distribution port in the flow distribution module, and the reaction gas inlet branch pipe joint is provided with a sealing gasket and is fastened and sealed through screws. The other end of the air inlet branch pipe is connected and fastened with each air inlet branch pipe through a hoop, and the installation quantity of the joints is the same as that of the galvanic piles.
The fuel cell power system control unit FCc collects the AFMm signal, ACMm signal, ASMm signal and tps (x) signals, transmits them to the ASMc, and obtains the ASMc execution feedback signal, so as to realize the closed-loop control of the device. FCc also sends power-up and power-down signals to each actuator and receives actuator fault signals.
The reaction gas inlet manifold is generally made of soft silica gel, is easy to connect and has good sealing property and corrosion resistance. The diameter of the main pipe is determined according to the required flow and the pressure of the reaction gas of the fuel cell, and the surface of the inner wall of the main pipe is required to be smooth as much as possible so as to reduce the on-way resistance loss.
The reaction gas inlet branch pipes are silica gel hoses with diameters smaller than that of the inlet main pipe, the extension lengths of the inlet branch pipes connected to the inlet of the electric pile need to be measured accurately, and data are input into the flow distribution module to be used for calculating the movement time of the reaction gas in the branch pipes.
As shown in fig. 1, the extension lengths of the air inlet branch pipes are consistent, and the bending times and the bending angles of the pipelines are also consistent, so that the pressure drop in the air inlet branch pipes is consistent.
Preferably, the intake manifold and each intake branch pipe are respectively provided with: the integrated sensor comprises an ASM inlet temperature and pressure sensor TPs _ i, an AIM _1 inlet temperature and pressure sensor TPs _1, an FCs _1 inlet temperature and pressure sensor TPs _11, an AIM _2 inlet temperature and pressure sensor TPs _2, an FCs _2 inlet temperature and pressure sensor TPs _21, an AIM _ n inlet temperature and pressure sensor TPs _ n, and an FCs _ n inlet temperature and pressure sensor TPs _ n 1. Each sensor is used for monitoring the reaction condition of each module in the fuel cell gas flow distribution device and transmitting a signal to the master controller, so that the master controller monitors the fuel cell gas flow distribution device.
The cooling cycle in the above-described structure and apparatus is not included in the scope of the embodiments of the present invention. The electric energy of the fuel cell power system control unit, the fuel cell gas flow distribution mechanism control unit and the electric drive device is supplied by an external power supply.
As described above, the embodiment of the present invention is significantly different from the structure of the conventional fuel cell power system, and can realize the capability of a single compressor to simultaneously supply reactant gases to a plurality of fuel cells. The specific implementation mode is as follows:
(1) under the condition that the power supply of the external power supply is stable and the hydrogen supply pressure of the fuel cell is normal, FCc is activated, the control unit of the fuel cell power system (namely, a general controller) starts to work, and FCc controls the AFMm power supply, the ACMc power supply and the ASMc power supply.
(2) After the ASMc is electrified, the position of the rotating blade CP in the ASMm is judged firstly, and if the rotating blade CP is at the preset position, no reaction gas residue exists in the fuel cell stack and in the pipeline of the gas inlet branch pipe. After confirming that the line is in the closed position, ASMc drives ASMm to start, CP starts to rotate at the lowest speed, and the vane opening first passes AIM _1 to supply the reactant gas to FCs _ 1. After a certain time, the blades rotate to AIM _2 inlet, where gas is supplied in FCs _2, FCs _ n.
(3) FCc sends a signal to ACMc after receiving the normal operation command of ASMc, ACMc controls ACMm to operate, and after ACMm establishes the operating pressure and flow, the reaction gas starts to enter ASM. Because the CP rotating speed is low, in order to ensure the smooth start of the galvanic pile, the ACMm is kept to continuously rotate at a high speed, and sufficient reaction gas sequentially enters each galvanic pile. At this time, FCc keeps the fuel cell hydrogen supply off and the stack does not generate electricity.
(4) And detecting signals TPs _11, TPs _21 and TPs _ n1, and if the TPs _11 reaches the working pressure of FCs _1, namely the reactor is full of reaction gas, FCc controls FCs _1 to supply hydrogen to be started. FCs _2 and FCs _ n then reach operating conditions, FCc control hydrogen supply on, respectively.
(5) Based on the above operation steps, the electrochemical reaction process of each cell stack is continuously performed in sequence, i.e., the cycle of FCs _1 → FCs _2 → FCs _ n → FCs _1 is continuously performed.
(6) After each galvanic pile works for a period of time, the internal electrochemical reaction rate of each galvanic pile is slowed down along with the reduction of the concentration of the reaction gas, at the moment, the current and the voltage output by the galvanic pile fluctuate, and in order to avoid the damage to the galvanic pile caused by the lack of the reaction gas, FCc needs to monitor the power generation condition of each galvanic pile in real time. At a given voltage and current, FCc sends signals to ACMc and ASMc based on the reactant gas consumption time, causing ACMc control ACMm to increase the reactant gas flow rate, and causing ASMc control ASMm to increase the reactant gas distribution frequency.
(7) At FCc, when the fuel cell power system is required to output at rated power, the operation of the rotating blades CP is controlled by ASMc, which ensures both adequate flow of reactant gas to a single stack and reactant gas distribution frequency between multiple stacks. Thus, the rotation process of the CP can be roughly described as: when the CP opening part rotates to a certain AIM inlet, the speed is reduced; after the opening part completely passes through the AIM inlet, performing accelerated motion; until the CP opening part reaches the next AIM inlet, decelerating again; the acceleration and deceleration processes are carried out in a circulating and reciprocating mode, the flow of reaction gas entering the galvanic pile is sufficient when the reaction gas passes through the AIM inlet, meanwhile, the time that the CP does not distribute the reaction gas, namely the CP opening sweeps over the AIM inlet is shortened, and the distribution frequency of the reaction gas is improved.
(8) Step (7) is a CP rotating process executed based on a circular opening rotating vane form, various rotating vane opening forms are involved, and other forms of CP rotating process control principles are consistent with step (7), but the specific action process can be adjusted through a control program in the ASMc.
(9) The adjustment and determination of the CP rotational speed are based on pressure, time, flow, calculated from ASMc, detailed control method and calculation based on the control method portion of the fuel cell gas flow distribution device.
(10) When FCc receives that the power output demand of the fuel cell power system is 0, the shutdown program is started to execute, signals are sent to ACMc and ASMc, the supercharger is controlled to reduce the rotating speed and the flow, the CP rotation action is controlled, the action process is carried out by acceleration and deceleration reciprocating, and the transition is gradually carried out to the uniform rotation until the state of the steps (4) and (5) is recovered.
(11) FCc controlling the hydrogen supply of fuel cell to be closed, and continuously operating ACMm and CP for a certain time, at this time, the AIT manifold is connected with inert gas or non-reactive gas to purge the residual reactive gas in each electric pile.
(12) FCc, detecting whether each pile meets the requirements of current and voltage, after each pile discharges, FCc sends a stop state command to ASMc, and the ASMc controls CP to rotate to a stop position, which can totally close all AIM inlets. At this point, the fuel cell reactant gas flow distribution process is fully completed.
In summary, the fuel cell gas flow distribution device provided by the embodiment of the present invention has a rotating blade, a motor driving mechanism, and a split-flow pipeline structure, and is obviously different from the prior art. By using the rotating blades, the reaction gases are distributed to a plurality of electric piles in sequence or in groups, so that the power consumption of auxiliary components of the fuel cell is reduced, and the system efficiency is improved.
The embodiment of the invention also provides a control method of the device, which is obviously different from the existing scheme. The control method of the device is based on the flow, the flow speed and the electrochemical reaction rate of the actual reaction gas. The dynamic control of the working states of the high-low power and different numbers of the galvanic piles is realized by adjusting the rotating speed of the rotating blades or replacing the blades with different sizes.
Fig. 7 is a flowchart of a control method of a fuel cell gas flow distribution device according to an embodiment of the present invention, and as shown in fig. 7, the method includes:
measuring an actual mass flow of reactant gas in the inlet manifold by the mass flow meter;
increasing the pressure of the reaction gas in the gas inlet manifold through the pressurization module so that the reaction gas enters the flow distribution module;
sending a preset signal to the flow distribution module through the master controller;
determining, by the flow distribution module, a corresponding preset control strategy according to the preset signal, so that the flow distribution module is communicated with only one target intake manifold at a time, and so that when the target fuel cell stack enters the stage T2, reactant gas is not required to be continuously provided to the target fuel cell stack, distributing the reactant gas to any other fuel cell stack, and making any other fuel cell stack enter the stage T1, and after the target fuel cell stack enters the stage T3, supplementing a reactant gas flow to the target fuel cell stack according to a time of the stage T1 or a time of the stage T2, making the target fuel cell stack reenter the stage T1, wherein a reaction time required by each fuel cell stack is composed of the stages T1, T2, and T3, and the stage T1 represents a process in which the reactant gas passes through each intake manifold to the fuel cell stack corresponding to the first intake manifold, the stage T2 represents the process required for the reactant gas to fill the working volume in the fuel cell stack, the stage T3 represents the process required for the reactant gas to complete the electrochemical reaction at the working volume, and the duration of the stage T1 is determined according to the actual mass flow.
The present embodiment is a method embodiment corresponding to the above device embodiment, and please refer to the above device embodiment for details, which is not described herein again.
Specifically, for the target intake manifold, the duration of the T1 phase is determined by:
T1＝LAIM_1/S1*α，
S1＝f1/(π*r2)，
wherein, T1Denotes the duration, L, of the T1 phaseAIM_1Indicates the length of the target intake manifold, S1Denotes the flow rate of the reaction gas, f1Representing an actual volume flow of the target fuel cell stack, r being a radius of the target intake manifold;
the duration of stage T2 is determined by:
T2＝V2/f2*β，
wherein, T2Denotes the duration, V, of the T2 phase2Representing the working volume of reactant gas in the target fuel cell stack, f2Representing an actual volumetric flow rate of the target fuel cell stack, β representing a diffusion coefficient of the target fuel cell stack;
the duration of stage T3 is determined by:
T3＝tv-tLim，
wherein, T3Denotes the duration, T, of the stage T3vIndicates the time at which the target fuel cell stack starts to emit the rated voltage, tLimIndicating the time when the voltage fluctuates after the electrochemical reaction rate is slowed down until the limited voltage value is reached.
Taking the target intake manifold as an example, the fuel cell stack connected to the target intake manifold is referred to as a target fuel cell stackThe duration of the T1 stage of the target fuel cell stack, where the diffusion coefficient is selected based on the flow channel cross-section, resistance, and pressure drop within the stack, can be determined according to the above equation1The total time required for the reaction gas to complete the reaction at the flow rate is TT＝T1+T2+T3The same applies to other fuel cell stacks, which also have the same total reaction time.
On the basis of the foregoing embodiment, preferably, the preset control strategy includes:
if the preset signal is a starting signal, the rotating blade rotates at a constant speed at a first speed, and the first speed is determined according to the opening size of the rotating blade and the duration of the T2 stage;
if the preset signal is that the master controller sends a power demand signal, if the equivalent time is longer than the duration of a T1 stage, the rotating blade rotates at a second speed at a constant speed, otherwise, the rotating blade rotates at a third speed at a constant speed, wherein the equivalent time is determined according to the T2 stage time, the T2 equivalent time, the duration of a T3 stage and gamma, the gamma represents an equivalent coefficient for simultaneously performing gas diffusion and electrochemical reaction, the T2 equivalent time is determined by the length of a flow channel on a pile electrode plate, the pile outlet pressure, the pile inlet pressure and the flow rate of reaction gas at the pile inlet, the second speed is determined according to the opening size of the rotating blade and the equivalent time, and the third speed is determined according to the opening size of the rotating blade and the duration of the T1 stage;
and if the preset signal is a stop signal, the rotating blade rotates at the first speed at a constant speed.
Specifically, in the embodiment of the present invention, a control strategy corresponding to the preset signal is selected according to different types of the preset signal. And when the preset signal is the starting signal, controlling the rotating blade to rotate at a constant speed at a first speed, wherein the first speed is determined according to the opening size of the rotating blade and the duration of the T2 stage.
Specifically, the calculation formula of the first speed is as follows:
R1＝θ1/(T2*6)，
wherein R is1Representing said first speed, θ1Denotes the size of the opening, T, of the rotating blade2Indicating the duration of the T2 phase.
Preferably, the flow distribution control unit first checks whether the rotary vanes are in the preset positions before controlling the rotary vanes to rotate after receiving the preset signal, and in general, if the rotary vanes are in the preset positions, it indicates that no reactant gas remains in the fuel cell stack, and then may control the rotary vanes to rotate at a constant speed at a first speed.
If the preset signal is a power demand signal sent by the general controller, since the reaction gas starts to participate in the electrochemical reaction after entering the fuel cell stack, the time of the stage T2 is equivalent to the time of the stage T3, which is called equivalent time. If the equivalent time is greater than the duration of stage T1, the rotating blades are rotated at a constant speed at the second speed, otherwise, the rotating blades are rotated at a constant speed at the third speed.
The calculation formulas of the second speed and the third speed are as follows:
R2＝θ1/(T23*6)，
T23＝[(T2-T2′)+T3]*γ，
T2′＝l*Pout/S2*Pin，
S2＝f1/(w*h)，
wherein R is2Representing said second speed, T1Denotes the duration of the stage T1, T23Represents said equivalent time, T2Denotes the duration of the stage T2, T3The duration of the T3 stage is shown, gamma is the equivalent coefficient of simultaneous gas diffusion and electrochemical reaction, l is the length of the flow channel on the target fuel cell stack plate, and P isoutIs the target fuel cell stack outlet pressure, PinRepresents the target fuel cell stack inlet pressure, S2Indicating the target fuel cellFlow rate of reaction gas at the inlet of the stack, f1Representing the actual volume flow of the target fuel cell stack, w representing the width of a flow channel on the target fuel cell stack polar plate, and h representing the depth of the flow channel on the target fuel cell stack polar plate;
R2′＝θ1/(T1*6)，
wherein R is2′Representing the third speed.
And if the preset signal is a stop signal, the rotating blades are controlled to rotate at the first speed at a constant speed again.
On the basis of the above embodiment, preferably, the preset signal is that when the master controller sends a power demand signal, the rotating blade rotates between any two intake branches at a fourth speed, the fourth speed is determined according to an angle between any two intake branches and a gas distribution frequency of the target compressor at the maximum flow rate, and the gas distribution frequency of the target compressor at the maximum flow rate is determined according to the equivalent time and the duration of the T1 stage.
Specifically, when the preset signal is a power demand signal sent by the general controller, the reactant gas distribution frequency of each fuel cell stack needs to be determined, namely the fourth rotating speed when the rotating blades are positioned between the inlets of the two inlet branch pipes, and the determination method is as follows:
R3＝θ2*HCP/6，
HCP＝1/Δ(T23-T1)，
wherein R is3Representing said fourth speed, θ2Representing the angle, T, between two adjacent inlet manifolds23Represents said equivalent time, T1Indicating the duration of the T1 phase.
I.e. the rotating blades are dynamically changed between the second speed and the third and fourth speeds.
As a preferred embodiment, the fuel cell power system is provided with 4 proton exchange membrane fuel cell stacks FCs _1, FCs _2, FCs _3 and FCs _4 in total, and the rated output power of a single stack is 60 kW. 1 centrifugal electrically driven turbocharger ACMm and a controller ACMc thereof, the rated power is 17kW, and the maximum flow is 140 g/s. 1 set of fuel cell gas flow distribution device body ASMm and its controller ASMc, rated power 750W, equipped with circular arc opening rotating blades CP, equipped with 4 reaction gas inlet manifold joints and pipelines AIM _1, AIM _2, AIM _3, AIM _ 4.
In this embodiment, the maximum reactant gas consumption of the 60kW electric stack may be calculated according to the following formula:
(λ*M*P)/(4*F*v*ρ*φ)＝V0。
wherein, V0Represents the volume flow rate (L/s), rho represents the density (g/L) of the reaction gas, M represents the molar mass (g/mol) of the reaction gas, P represents the rated power (W) of the stack, V represents the calculated voltage (V) of the fuel cell unit, F represents the Faraday electromagnetic constant (C/mol), phi represents the volume fraction, and lambda represents the excess coefficient.
Calculating to obtain V054L/s, converted to a mass flow of 70 g/s.
It follows that, according to the prior art, a fuel cell power system consisting of 4 stacks is equipped with at least 2 compressors of this type, or 4 small compressors with a nominal power of 9kW and a maximum flow of 75 g/s. In the prior art, the system has a complex structure, the power consumption reaches 34kW and 36kW respectively, the power consumption accounts for 14.2 percent and 15 percent of the total power of the system respectively, and the system efficiency is low.
The embodiment of the invention adopts 1 large-flow compressor and is matched with a fuel cell gas flow distribution device, thereby realizing the function of providing reaction gas flow for 4 electric piles.
f0Indicating the target compressor maximum flow, f1、f2、f3、f4Actual volume flows of 4 stacks are respectively supplied to the compressors, and f0＜f1＝f2＝f3＝f4。
The time required for the reaction gas to pass through the AIM _1 to the inlet of FCs _1 is T1＝LAIM_1/S1*α，LAIM_1Is the length of the intake manifold, S1For the flow rate of the reaction gas, S1＝f1/(π*r2) And α is a path resistanceThe force coefficient. Taking the maximum required flow of the electric pile as an example: t is calculated when the intake manifold length is 1.5m, the diameter is 0.05m, and the manifold pressure P1 is 120kPa1＝0.266s。
FCs _1 at operating pressure P2, volume of reactive gas in the stack is V2The time T required for the reaction gas to fill the volume is known2＝V2/f2Beta and beta are diffusion coefficients selected according to the cross section of a flow passage in the electric pile, resistance and pressure drop.
V2The time required for the reaction gas to complete the electrochemical reaction is T3＝tv-tLim，tvMoment of starting to emit rated voltage for the pile, tLimThe voltage fluctuates after the electrochemical reaction rate is slowed down until the time point of reaching the limited voltage value.
Thus, FCs _1 is at f1Total time T required for the reaction gas to complete the reaction at flowT＝T1+T2+T3. The same applies to the remaining three stacks, which also have the same total reaction time.
The control target of the fuel cell gas flow distribution module ASM is at TTReasonably distributing gas flow in time when a certain pile enters T2At this stage, no gas flow is required to continue to the stack. And the gas flow is distributed to the rest of the electric pile to enter T1And (5) stage. When a certain pile has entered T3After a phase, consider T1Or T2The gas flow distribution device is controlled to supplement the reaction gas flow to the electric pile in time so as to enable the electric pile to enter the T again1And (5) stage.
Based on the control targets, two ASMc control strategies C1 and C2 are set.
The C1 control strategy is a fuel cell power system start-up and shut-down process control, i.e. where the preset signals are a start signal and a shut-down signal, in the C1 control strategy, the ASMc first detects the CP position at start-up and then drives the CP at the R rotation speed1At a constant speed, R1＝θ1/(T26), it is known that if the CP opening size is 210mm in the present embodiment, θ is1＝34.1°，T2R can be calculated for the time when the reactor volume is filled with the reaction gas1The value of (c).
FCc, i.e., the preset signal is the power demand signal, the ASMc control unit ends the C1 control strategy and starts to execute the C2 control strategy. Similarly, after FCc sends a shutdown signal, the ASMc control moves from the C2 strategy to the C1 strategy, and when the CP stops rotating, the ASMc will again check the CP position to ensure that it closes all AIM lines, until the C1 control strategy is completed.
The C2 control strategy is the control strategy when the fuel cell power system is in normal operation, and in the C2 control strategy, because gas starts to participate in the electrochemical reaction after the reaction gas enters the electric pile, T is2Phase time will be equivalent to T3Time, has T23＝[(T2-T2′)+T3]Gamma, wherein T2′＝l*Pout/S2*PinL is the length of the flow channel on the electrode plate of the pile, PoutIs the stack outlet pressure, PinIs the pressure at the inlet of the stack, S2Is the flow rate of the reaction gas at the inlet of the stack, S2＝f1And w is the width of the flow channel on the polar plate, and h is the depth of the flow channel on the polar plate. Therefore, under the C2 strategy, when T is23>T1Time CP rotation speed R2＝θ1/(T236) when T23≤T1Time CP rotation speed R2′＝θ1/(T1*6)。
Based on the above control objectives, the C2 strategy also determines the reactant gas distribution frequency of each stack, i.e., the rotation rate R when the CP opening is between the inlets of the AIM tubes3. Defined at the maximum flow f of the compressor0Lower gas distribution frequency HCP 1/Delta (T)23-T1) Then R is3＝θ2*HCP/6，θ2Is the angle between two adjacent AIM conduits, theta in this embodiment251.7. Finally, under the C2 strategy, CP speed is dynamically varied between R2 and R2' and R3.
In summary, embodiments of the present invention provide a fuel cell reactant gas distribution device and a control method thereof, which are necessary and feasible to utilize excess gas under the condition of ensuring the gas flow rate inside the stack participating in the electrochemical reaction. The device can fully utilize the compressed excessive reaction gas, and can realize the function of simultaneously providing gas supply and distribution for a plurality of galvanic piles by a single compressor, thereby greatly improving the system efficiency and the power grade of a fuel cell system.
The above-described embodiments of the apparatus are merely illustrative, and the units described as separate parts may or may not be physically separate, and parts displayed as units may or may not be physical units, may be located in one place, or may be distributed on a plurality of network units. Some or all of the modules may be selected according to actual needs to achieve the purpose of the solution of the present embodiment. One of ordinary skill in the art can understand and implement it without inventive effort.
Through the above description of the embodiments, those skilled in the art will clearly understand that each embodiment can be implemented by software plus a necessary general hardware platform, and certainly can also be implemented by hardware. With this understanding in mind, the above-described technical solutions may be embodied in the form of a software product, which can be stored in a computer-readable storage medium such as ROM/RAM, magnetic disk, optical disk, etc., and includes instructions for causing a computer device (which may be a personal computer, a server, or a network device, etc.) to execute the methods described in the embodiments or some parts of the embodiments.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.

Claims (10)

1. A fuel cell gas flow distribution device, comprising: intake manifold, a plurality of air inlet branch pipe, mass flow meter, pressure boost module, flow distribution module and total controller, wherein, intake manifold's one end and target compressor are connected, mass flow meter the pressure boost module with flow distribution module installs in proper order on the intake manifold, flow distribution module's exit end is connected with the one end of each air inlet branch pipe, and the other end and each fuel cell pile of each air inlet branch pipe are connected, wherein:
the mass flow meter is used for measuring the actual mass flow of the reaction gas in the gas inlet main pipe;
the pressurization module is used for increasing the pressure of the reaction gas in the gas inlet main pipe so that the reaction gas enters the flow distribution module;
the master controller is used for sending a preset signal to the flow distribution module;
the flow distribution module is used for determining a corresponding preset control strategy according to the preset signal, so that the flow distribution module is only communicated with one target air inlet branch pipe at a time, when the target fuel cell stack enters a stage T2, reactant gas is not required to be continuously provided for the target fuel cell stack, the reactant gas is distributed to any other fuel cell stack, any other fuel cell stack enters a stage T1, after the target fuel cell stack enters a stage T3, the reactant gas is supplemented for the target fuel cell stack, the target fuel cell stack enters a stage T1 again, the reaction of each fuel cell stack is divided into a stage T1, a stage T2 and a stage T3 according to the time sequence, and the stage T1 represents the process that the reactant gas passes through the target air inlet branch pipe to the target fuel cell stack, the stage T2 represents the process of the reactant gas filling the working volume in the target fuel cell stack, the stage T3 represents the process of the reactant gas completing the electrochemical reaction at the working volume, and the duration of the stage T1 is determined according to the actual mass flow.
2. The fuel cell gas flow distribution device according to claim 1, wherein the flow distribution module includes: the gas flow control device comprises a rotating blade, a driving motor, a rotating shaft, a rotating limiting groove, a gas flow distribution mechanism body and a gas flow control unit, wherein the rotating blade is arranged on the rotating shaft;
the driving motor is connected with the rotating shaft, the rotating shaft is also connected with the rotating blades, and the rotating limiting grooves are positioned on the outer sides of the rotating blades;
the rotating blade includes a hollow portion and a solid portion;
the gas flow distribution mechanism body comprises a plurality of gas distribution ports, each gas distribution port corresponds to each gas inlet branch pipe, and the gas distribution ports corresponding to the gas inlet branch pipes which are not communicated are sealed;
the gas flow control unit is used for controlling the driving motor according to the preset signal and driving a motor in the fuel cell gas flow distribution mechanism body so as to adjust the rotating speed and the stop position of the rotating blade, so that the flow distribution module is communicated with only one target gas inlet branch pipe at each time.
3. The fuel cell gaseous fluid distribution apparatus of claim 1, wherein the length of each inlet manifold is the same and the number of bends in the conduit is the same as the bend angle.
4. A control method of a fuel cell gas flow rate distribution device according to any one of claims 1 to 3, comprising:
measuring an actual mass flow of reactant gas in the inlet manifold by the mass flow meter;
increasing the pressure of the reaction gas in the gas inlet manifold through the pressurization module so that the reaction gas enters the flow distribution module;
sending a preset signal to the flow distribution module through the master controller;
determining a corresponding preset control strategy by the flow distribution module according to the preset signal, so that the flow distribution module is communicated with only one target air inlet branch pipe at a time, when the target fuel cell stack enters a stage T2, reactant gas is not required to be continuously provided for the target fuel cell stack, the reactant gas is distributed to any other fuel cell stack, any other fuel cell stack enters a stage T1, after the target fuel cell stack enters a stage T3, the target fuel cell stack is supplemented with reactant gas flow according to the time of the stage T1 or the time of the stage T2, the target fuel cell stack enters a stage T1 again, the reaction of each fuel cell stack is divided into a stage T1, a stage T2 and a stage T3 according to the time sequence, the stage T1 represents the process of the reactant gas passing through the target air inlet branch pipe to the target fuel cell stack, the stage T2 represents the process required for the reactant gas to fill the working volume within the target fuel cell stack, the stage T3 represents the process required for the reactant gas to complete the electrochemical reaction at the working volume, and the duration of the stage T1 is determined based on the actual mass flow rate.
5. The control method of a fuel cell gas flow distribution apparatus according to claim 4, wherein the preset control strategy includes:
if the preset signal is a starting signal, the rotating blade rotates at a constant speed at a first speed, and the first speed is determined according to the opening size of the rotating blade and the duration of the T2 stage;
if the preset signal is that the master controller sends a power demand signal and the equivalent time is longer than the duration of the stage T1, the rotating blades rotate at a second speed at a constant speed;
if the preset signal is that the master controller sends a power demand signal, and the equivalent time is less than the duration of a T1 stage, the rotating blades rotate at a third speed at a constant speed, wherein the equivalent time is determined according to the T2 stage time, the T2 equivalent time, the duration of the T3 stage and gamma, the gamma represents an equivalent coefficient for simultaneously performing gas diffusion and electrochemical reaction, the equivalent time is determined by the length of a flow channel on a fuel cell stack plate, the outlet pressure of the fuel cell stack, the pressure at the inlet of the fuel cell stack and the flow rate of reactant gas at the inlet of the fuel cell stack, the second speed is determined according to the opening size of the rotating blades and the equivalent time, and the third speed is determined according to the opening size of the rotating blades and the duration of the T1 stage;
and if the preset signal is a stop signal, the rotating blade rotates at the first speed at a constant speed.
6. The control method of the fuel cell gas flow distribution device according to claim 5, wherein the preset signal is that when the general controller sends a power demand signal, the rotary vane rotates between any two intake branches at a fourth speed, the fourth speed is determined according to an angle between any two intake branches and a gas distribution frequency of the target compressor at a maximum flow, and the gas distribution frequency of the target compressor at the maximum flow is determined according to the equivalent time and a duration of a period T1.
7. The control method of a gas flow distributing device of a fuel cell according to claim 4, wherein the duration of the period T1 for the target intake manifold is determined by:
T1＝LAIM_1/S1*α，
S1＝f1/(π*r2)，
wherein, T1Denotes the duration, L, of the T1 phaseAIM_1Indicates the length of the target intake manifold, S1Denotes the flow rate of the reaction gas, f1Representing an actual volume flow of the target fuel cell stack, r being a radius of the target intake manifold;
the duration of stage T2 is determined by:
T2＝V2/f2*β，
wherein, T2Denotes the duration, V, of the T2 phase2Representing the working volume of reactant gas in the target fuel cell stack, f2Representing an actual volumetric flow rate of the target fuel cell stack, β representing a diffusion coefficient of the target fuel cell stack;
the duration of stage T3 is determined by:
T3＝tv-tLim，
wherein, T3Denotes the duration, T, of the stage T3vIndicates the time at which the target fuel cell stack starts to emit the rated voltage, tLimIndicating the time when the voltage fluctuates after the electrochemical reaction rate is slowed down until the limited voltage value is reached.
8. The control method of a fuel cell gas flow rate distribution device according to claim 5, characterized in that the first speed is determined specifically according to the following formula:
R1＝θ1/(T2*6)，
wherein R is1Representing said first speed, θ1Denotes the size of the opening, T, of the rotating blade2Indicating the duration of the T2 phase.
9. The control method of a fuel cell gas flow rate distribution device according to claim 5, wherein the second speed and the third speed are determined specifically according to the following formulas:
R2＝θ1/(T23*6)，
T23＝[(T2-T2′)+T3]*γ，
T2′＝l*Pout/S2*Pin，
S2＝f1/(w*h)，
wherein R is2Representing said second speed, T1Denotes the duration of the stage T1, T23Represents said equivalent time, T2Indicating the T2 orderDuration of the segment, T3The duration of the T3 stage is shown, gamma is the equivalent coefficient of simultaneous gas diffusion and electrochemical reaction, l is the length of the flow channel on the target fuel cell stack plate, and P isoutIs the target fuel cell stack outlet pressure, PinRepresents the target fuel cell stack inlet pressure, S2Representing the target fuel cell stack inlet reactant gas flow rate, f1Representing the actual volume flow of the target fuel cell stack, w representing the width of a flow channel on the target fuel cell stack polar plate, and h representing the depth of the flow channel on the target fuel cell stack polar plate;
the third speed is specifically determined according to the following formula:
R2′＝θ1/(T1*6)，
wherein R is2′Representing the third speed.
10. The control method of a fuel cell gas flow rate distribution device according to claim 5, wherein the fourth speed is determined by the following formula:
R3＝θ2*HCP/6，
HCP＝1/Δ(T23-T1)，
wherein R is3Representing said fourth speed, θ2Representing the angle, T, between two adjacent inlet manifolds23Represents said equivalent time, T1Indicating the duration of the T1 phase.
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