CN1326277C - System and method for management of gas and water in fuel cell system - Google Patents
System and method for management of gas and water in fuel cell system Download PDFInfo
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- CN1326277C CN1326277C CNB038226847A CN03822684A CN1326277C CN 1326277 C CN1326277 C CN 1326277C CN B038226847 A CNB038226847 A CN B038226847A CN 03822684 A CN03822684 A CN 03822684A CN 1326277 C CN1326277 C CN 1326277C
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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
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
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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
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
- H01M8/04126—Humidifying
- H01M8/04141—Humidifying by water containing exhaust gases
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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
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
- H01M8/04156—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying with product water removal
- H01M8/04164—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying with product water removal by condensers, gas-liquid separators or filters
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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
- H01M2250/00—Fuel cells for particular applications; Specific features of fuel cell system
- H01M2250/20—Fuel cells in motive systems, e.g. vehicle, ship, plane
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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
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04097—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with recycling of the reactants
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- 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
Abstract
A fuel cell system has: a fuel cell having a first reactant inlet, a first reactant outlet, a second reactant inlet, a second reactant outlet, and optionally a coolant inlet and coolant outlet. A first reactant supply subsystem supplies a first reactant incoming stream to the first reactant inlet of the fuel cell. A second reactant supply subsystem supplies a second reactant incoming stream to the second reactant inlet of the fuel cell. A first reactant recirculation subsystem recirculates at least a portion of the first reactant exhaust stream from the first reactant outlet to a regenerative dryer subsystem in which one portion of the heat and moisture in first reactant exhaust stream is transferred to one of the first reactant incoming stream in the first reactant supply subsystem and the second reactant incoming stream in the second reactant supply subsystem. Another portion of the heat and moisture is transferred to the other stream. A method of controlling reactant and water in a fuel cell system is also disclosed.
Description
Technical field
The present invention relates in general to a kind of apparatus and method of handling the process gas (processgases) of fuel cell system.More particularly, the present invention relates to a kind of humidity, temperature and mobile apparatus and method of controlling fuel cell process gases.
Background technology
Compare with traditional generation technology, fuel cell system is counted as promising substitute technology because of it has low emission, high efficiency and easy-operating characteristics.During fuel cell operation chemical energy is transformed into electric energy.Proton Exchange Membrane Fuel Cells comprises an anode, a negative electrode and the selective electrolysis plasma membrane between two electrodes.In catalytic reaction, fuel (for example hydrogen) is at oxidized formation cation of anode (proton) and electronics.Amberplex promotes the migration of proton from the anode to the negative electrode.Electronics can not pass through this exchange membrane, thereby is forced to flow through external circuit and electric current is provided.At negative electrode, oxygen forms anion at catalyst layer with the electron reaction of returning from circuit.Form aqueous water in negative electrode anion that forms and the proton reaction of passing exchange membrane and produce tide as reaction.
Proton exchange membrane needs a wet surface to be beneficial to the conduction of proton from the anode to the negative electrode, helps keeping the conductivity of this exchange membrane in other words.Studies show that each proton by exchange membrane carries two to three hydrones (U.S.Patent 5,996,976) at least.U.S.Patent 5,786, and 104 have described a kind of crying " pump action of water " mechanism of action (waterpumping) more qualitatively, and this mechanism of action makes cation (proton) pass through exchange membrane with hydrone.When current density increases, by the also increase thereupon of hydrone number of exchange membrane.Finally the water flux density that is carried by exchange membrane by proton stream has surpassed the water that is replenished by diffusion.At this moment exchange membrane begins to become dry (being like this in anode one side at least), and its internal resistance increases.Will be appreciated that this mechanism of action makes current direction negative electrode one side, the water through reacting generation is also in negative electrode one side.But, may be enough to remove these water by the air-flow of negative electrode one side, make negative electrode one side become dry equally.Therefore, the surface of exchange membrane must keep moist at any time.Therefore, for guaranteeing enough efficient, process gas must have needed suitable humidity of system and temperature when entering fuel cell.
Another consideration is that people increase day by day to the interest of fuel cell in the application of traffic and similar field, for example with its normal power as car, bus even the more large-scale vehicles.Application on motor vehicle is very different with application at a lot of fixed-sites.For example, in the application of fixed-site, fuel battery (fuel cell stack) is used as power supply usually and only requires that it moves a period of time down at metastable power level (power level).On the contrary, in automotive environment, the excursion of the electric power that the fuel battery actual needs provides can be very big.And fuel battery need be made quick response to the variation of electricity needs simultaneously keeping high efficiency, and no matter this demand increases electric power or reduces.In addition, when being applied to automotive field, wish that fuel battery all can move under extreme ambient temperature and damp condition.
All these require all quite harsh, and these require to make and guarantee the efficient operation of fuel battery in all possible operating condition scope difficulty that becomes.At this moment, crucial problem is will guarantee that fuel battery can continue the power level that provides high expeditiously and guarantee that simultaneously it has long useful life, therefore, must accurately control the interior humidity level of fuel battery to satisfy these requirements.More particularly, the humidity level of necessary controlled oxidation agent and fuel gas stream.There is defective in most of known humidifying technology designs, can not make response to the quick variation of temperature and conditions of similarity.A lot of known systems can provide insufficient humidity level, and may have high thermal inertia and/or big dead volume (deadvolume), make them not make quick response to the variation of condition.
The common unsettled U.S. Patent application U.S.Patent ApplicationNo.09/801 of applicant, 916, a kind of apparatus and method of controlling temperature and humidity in the fuel cell system are disclosed.This method comprises: with fuel cell process gas flow humidification under first temperature, make process gas flow contain excessive moisture, be lower than this process gas flow of cooling under second temperature of first temperature, make excessive condensate moisture, remove the excess water that is condensed in the process gas flow and under a known temperature, transmit this process gas flow, determine the relative humidity of process gas flow thus according to the ratio of saturated vapor pressure under second temperature and the above-mentioned known temperature.Particularly, this method comprises in the process gas that discharges from fuel cell and reclaims moisture, and with the moisture of this recovery one of at least humidification to fuel and oxidant stream.Yet this method needs a large amount of assemblies, thereby has reduced the overall efficiency of fuel cell system.
U.S.Patent No.6,013,385 discloses another method.A kind of fuel cell gas management system is disclosed in this patent.This system comprises: one first reactant humidification subsystem, be used for providing first reactant feed flow to first reactant entrance of fuel cell, and receive the first reactant effluent streams from the outlet of first reactant of fuel cell, the described first reactant humidification subsystem comprises enthalpy wheel (enthalpy wheel), is used for collecting moisture and the part of collected moisture is passed to first reactant feed flow from first reactant (oxidant) effluent streams; One second reactant (fuel) humidity keeps subsystem, comprise that a recirculation loop-be used for collects excessive second reactant, second reactant source mixing arrangement and the power set from second reactant outlet of fuel cell, the described second reactant source mixing arrangement is used in the future, and second reactant in autoreaction thing source mixes with second reactant of collecting from second reactant outlet of fuel cell, described power set are used to make second reactant to circulate in described recirculation loop, and second reactant is caused second reactant entrance.Yet this patent does not still have to make full use of used heat and the moisture in the fuel cell exhaust thing.
For fuel cell gas management system, also need it can provide to the temperature of fuel cell process gases charging and dynamically controlling fast of relative humidity.More particularly, such system all should be efficiently for oxidant and fuel system, and can provide enough humidity for these two systems in a wide flow rates.
The invention brief introduction
According to an aspect of the present invention, the present invention proposes a kind of fuel cell system, comprising:
A fuel cell is provided with one first reactant entrance, first reactant outlet, second reactant entrance, second reactant outlet, a coolant entrance and a coolant outlet;
One first reactant supply subsystem is used for providing first reactant feed flow to first reactant entrance of fuel cell;
One second reactant supply subsystem is used for providing second reactant feed flow to second reactant entrance of fuel cell;
One first reactant recirculation subsystem, be used for making at least a portion of the first reactant effluent streams to enter a regenerative dryer subsystem from first reactant outlet recirculation, wherein, at least a portion heat in described at least a portion first reactant effluent streams and moisture be delivered in first reactant feed flow in first reactant supply subsystem and second reactant feed flow in second reactant supply subsystem one of at least.
Preferably, the regenerative dryer subsystem comprises one first regenerative dryer and one second regenerative dryer, and first regenerative dryer is used for giving first reactant feed flow in first reactant supply subsystem with at least a portion heat in the first reactant effluent streams in the first reactant recirculation subsystem and moisture transmission; Second regenerative dryer is used for supplying second reactant feed flow of subsystem for second reactant at least a portion heat and moisture transmission in the first reactant effluent streams of the first reactant recirculation subsystem.
More preferably, fuel cell system also comprises one second reactant recirculation subsystem, be used for making at least a portion of the second reactant effluent streams to enter second reactant supply subsystem, make at least a portion of the second reactant effluent streams mix with second reactant feed flow from second reactant outlet recirculation.
According to another aspect of the present invention, the invention provides a kind of reactant in the fuel cell system and method for water controlled, this fuel cell is provided with one first reactant entrance, first reactant outlet, second reactant entrance, second reactant outlet, a coolant entrance and a coolant outlet, and described method comprises:
(a) provide first reactant feed flow to first reactant entrance;
(b) provide second reactant feed flow to second reactant entrance;
(c) export at least a portion of collecting the first reactant effluent streams from first reactant;
(d) at least a portion heat at least a portion first reactant effluent streams and moisture transmission are given in first reactant feed flow and second reactant feed flow one of at least.
Preferably, in step (d): give first reactant feed flow and second reactant feed flow with at least a portion heat at least a portion first reactant effluent streams and moisture transmission.
More preferably, this method also comprises: at least a portion of collecting the second reactant effluent streams from the outlet of second reactant; And at least a portion of the second reactant effluent streams mixed with second reactant feed flow.
The present invention has several advantages over the prior art.The interior carrying object (onboard fluid) of battery unique among the present invention is a cooling agent.All are used for all self being produced by fuel cell 12 for the water of fuel and oxidant humidification.This has reduced the weight and the quantity of assembly in the system, makes whole system compact and efficient.Native system has the ability that electricity needs is responded fast.All these features all are to need especially in the vehicular applications.
Description of drawings
In order to understand the present invention better, and be illustrated more clearly in how to implement the present invention, will be by the mode quoted figures of example, description of drawings an embodiment preferred of the present invention, wherein:
Fig. 1 shows the flow chart according to fuel cell G﹠W treatment system first embodiment of the present invention;
Fig. 2 shows a conversion scheme according to fuel cell G﹠W treatment system first embodiment of the present invention, wherein only shows a cool cycles;
Fig. 3 shows the part flow chart according to second embodiment of fuel cell G﹠W treatment system of the present invention, and this embodiment is under high pressure moved;
Fig. 4 shows a part of flow chart according to fuel cell G﹠W treatment system of the present invention, a plurality of forward pressure regulator shown in it (forward pressureregulators);
Fig. 5 a and 5b show the part flow chart according to fuel cell G﹠W treatment system of the present invention, the connection between two regenerative dryer shown in it;
Fig. 6 shows the part flow chart according to fuel cell G﹠W treatment system of the present invention, a kind of pressure balance mechanism shown in it.
Embodiment
At first referring to Fig. 1, this figure is the flow chart of first embodiment of fuel cell gas management system 10 of the present invention.Fuel cell gas management system 10 comprises a fuel supply lines 20, oxidant supply line 30, a cathode exhaust recirculation line 40 and an anode effluent recirculation line 60, and all pipelines all are connected with fuel cell 12.It should be understood that fuel cell 12 can comprise a plurality of or single fuel cell.For the sake of simplicity, fuel cell described herein 12 adopts hydrogen to act as a fuel, and air is as oxidant, and can be a proton exchange membrane (PEM) fuel cell.But the present invention is not limited to such fuel cell, can also be applied to the fuel cell of other type.
Fuel cell cathode exhaust stream contains the water of excessive air, generation and the water of coming from anode one side migration, and air wherein is rich in nitrogen owing to wherein at least a portion oxygen is consumed in fuel cell 12.Cathode exhaust stream is carried out recirculation by the cathode exhaust recirculation line 40 that the cathode outlet with fuel cell 12 links to each other.At first by hydrogen humidifier 90, heat and moisture are delivered to the dry feed hydrogen in the fuel supply lines 20 to moist cathode exhaust stream therein.Hydrogen humidifier 90 can be any suitable humidifier, for example can be by Perma Pure Inc, the humidifier that Toms River, NJ buy.It also can be the humidifier of film humidifier or other type, and no matter its saturation efficiency is high or low.In fact, hydrogen humidifier 90 also can be a regenerative dryer, still, considers the different of gas in anode logistics and the negative electrode logistics, can not adopt the regenerative dryer or the miscellaneous equipment that allow to take place between two kinds of logistics remarkable mass exchange.
As mentioned above, fuel cell cathode exhaust stream 40 continue to flow and by regenerative dryer 80 from hydrogen humidifier 90 along recirculation line.When the cathode exhaust passes of humidity is passed through regenerative dryer 80, heat wherein and moisture are deposited in the porous paper or fiber material of regenerative dryer 80, when the switching device of regenerative dryer 80 with the connection status of regenerative dryer 80 when cathode exhaust stream is adjusted into air feed stream, heat that these are retained and moisture are delivered to the dry air incoming flow of flowing through regenerative dryer 80 through oxidant supply line 30.Cathode exhaust stream continues to flow to effluent streams separator 100 along recirculation line 40 then, and therein, the excess water that is not delivered to feed hydrogen and air stream in the effluent streams is separated from effluent streams with liquid form once more.Effluent streams is discharged in the environment by discharge pipe line 50 then.
On recirculation line 40, close on the place of fuel battery negative pole outlet, a cathode outlet flowing line 42 can optionally be set, be used for any aqueous water residual or that condensation goes out is discharged.Cathode outlet flowing line 42 can be designed to suitable dimensions, so that the bubble in this flowing line can maintain the moisture in the cathode outlet flowing line, and substantially regularly water is discharged automatically, thereby avoid adopting normally used draining valve when draining from air-flow.This flowing line can be used in any place that aqueous water need be discharged from air-flow in system.Pressure increases along with the increase of gas flow rate and conventional water that generate or condensation usually, and the gas of low flow velocity can not cause damage to for example cathode exhaust passes separator and cathode outlet flowing line 42 etc.
Flow to anode water separator 95 from the hydrogen behind the humidification in the hydrogen humidifier 90 along fuel supply lines 20, excessive therein water was separated before hydrogen enters fuel cell 12.Similarly, flow to cathode water separator 85 from the air behind the humidification of regenerative dryer 80 along oxidant supply line 30, excessive therein aqueous water was separated before air enters fuel cell 12.
Under the effect of recirculation pump 64, the anode of fuel cell emission that contains the excessive hydrogen G﹠W carries out recirculation along the anode recirculation line 60 that links to each other with fuel cell 12 anode exports.Anode recirculation line 60 is connected with fuel supply lines 20 at first node 62 places that are positioned at anode water separator 95 upstreams.Excess hydrogen and steam recirculation together not only can farthest utilize hydrogen, and prevent that aqueous water from blocking to reaction site supply of hydrogen reactant, and owing to the steam in the hydrogen of recirculation will from the feed hydrogen humidification of hydrogen humidifier 90 realized fuel stream from humidification.This design is in demand, because this arrangement makes the hydrogen humidifier 90 that uses in native system not need to have very high efficient, thereby makes the selection of hydrogen humidifier 90 that very big flexibility can be arranged.By selecting suitable hydrogen gas recycle flow velocity, hydrogen humidifier 90 needed efficient can be minimized.For example, suppose that fuel cell 12 needs the hydrogen of a unit, the hydrogen of three units can be provided from sources of hydrogen, the hydrogen of two wherein excessive units is with steam recirculation.Can adjust recycled hydrogen shared ratio in the hydrogen mixture in first node 62 downstreams by the speed that changes recirculation pump 64.Select the speed of stoichiometric relationship and recirculation pump 64 can finally cause omitting hydrogen humidifier 90.
In practice, owing to use air, have been found that nitrogen may take place enters the situation of anode one side from fuel battery negative pole one side, for example passes the exchange membrane of PEM fuel cell as oxidant.Therefore, in fact anode effluent comprises some nitrogen and other possible impurity.The recirculation of anode effluent may cause the accumulation of nitrogen and fuel cell is poisoned.Preferably, hydrogen cleaning (purge) pipeline 70 is told from fuel recycle pipeline 60 at breakout 74 places of closing on the fuel battery negative pole outlet.Cleaning control device 72 is arranged on hydrogen and cleans on the pipeline 70, is used to clean the part from the anode effluent of recirculation line 60.The frequency of cleaning operation and flow velocity depend on the power of fuel cell 12 operations.When fuel cell 12 high power operations, need to clean more a high proportion of anode effluent.Cleaning control device 72 can be solenoid valve or other suitable device.
Hydrogen cleans pipeline 70 and extends to Section Point 92 from breakout 74, and here combines with cathode exhaust recirculation line 40.Then, the hydrogen that is cleaned with from the mixture of the cathode exhaust passes of regenerative dryer 80 by emission separator 100.In separator 100, water is condensed out, and remaining admixture of gas is discharged in the environment by discharge pipe 50.Perhaps, cathode exhaust recirculation line 40 or cleaning pipeline 70 are directly connected on the separator 100.Those of ordinary skills know, the hydrogen that is cleaned, or from the cathode exhaust passes of regenerative dryer 80 also can not condensation wherein water and discharge respectively.
Preferably, for discharging by the water of separating in anode water separator 95, cathode water separator 85 and the emission separator 100, enter a generation water receptacle 97 but reclaim along anode inlet flowing line 96, cathode inlet flowing line 84 and effluent flowing line 94 respectively, be used for various processing step.For this reason, container 97 comprises and is used for the pipeline 98 and the drainage pipe 99 that are connected with other processing steps.
As known to persons of ordinary skill in the art, first cooling circuit 14 passes fuel cell 12.First cooling medium pump 13 is arranged in first cooling circuit 14, is used for making cooling agent to circulate.Cooling agent can be any cooling agent that is generally used for this area, for example any non-conductive water, ethylene glycol etc.Can use one first expansion vessel 11 in known manner.One first heat exchanger 15 is set in first cooling circuit 14, is used for cool stream to cross the cooling agent of fuel cell 12, to keep cooling agent in suitable temperature range.
Fig. 1 illustrates a kind of conversion scheme, and second cooling circuit 16 wherein comprises one second cooling medium pump 17, so that second cooling agent circulates.The temperature that one second heat exchanger 18 (for example radiator) keeps cooling agent in second cooling circuit is set, if desired, one second container 19 is set again.Can use the cooling agent of any kind in second cooling circuit 16, because first and second cooling circuits 14 and 16 do not mix.
It should be understood, however, that independently second cooling circuit is not essential.On the contrary, as shown in Figure 2, the temperature that a radiator keeps cooling agent in first cooling circuit 14 is set in first cooling circuit 14.In this case, second cooling circuit 16 can be omitted.Should be appreciated that required in may using as some, the heat exchanger 15 among Fig. 1 also can be isolated copper coin formula (brazed) heat exchanger, is arranged in the cooling circuit of " open (open) ".That is to say that second cooling circuit 16 can be an open cooling circuit, cooling agent wherein for example obtains in atmosphere, the ocean etc. and turns back in this cooling agent storehouse and go from a cooling agent storehouse.
When water is used as the cooling agent of above any conversion scheme, because the water from separator 95,85,100 is the generation water of fuel cell, therefore pure and non-conductive, can and import in expansion vessel 11,19 or the cooling agent storehouse cooling agent when acting as a fuel battery operation with its collection.
Preferably, a flow rate adjustment device 22 is arranged on the supply of fuel line 20, and is in the upstream of hydrogen humidifier 90.This flow rate adjustment device or valve 22 can respond the flow velocity that flows to the hydrogen of fuel cell 12 from sources of hydrogen 21 to the pressure drop the fuel supply lines 20.This flow rate adjustment device 22 can be a forward pressure regulator with set point, and this adjuster provides hydrogen in fuel cell 12 when making pressure in the fuel supply lines 20 be lower than set point because of the consumption of hydrogen in fuel cell 12.This forward pressure regulator is avoided needing expensive mass flow controller, and response faster and the control of more accurate flow velocity are provided.Referring to Fig. 4, for bigger control flexibility is provided, flow rate adjustment device 22 can comprise a plurality of pre-set forward pressure regulators arranged that are connected in parallel, and wherein, each forward pressure regulator all has a different set point.For example, the first forward pressure regulator 22a can be made as 10Psig with set point, and the second forward pressure regulator 22b can be set at 20Psig, and the 3rd forward pressure regulator 22c can be set at 30Psig, or the like.This make can with different pressure with under each pressure, provide fuel to fuel cell 12 with different speed, and do not need the operation of interrupts fuel battery and change the set point of forward pressure regulator.
It should be understood that in the present embodiment, though cathode exhaust passes at first is used for being the feed hydrogen humidification, is the feeding air humidification then, and this order is not essential.On the contrary, cathode exhaust passes can at first be used for being the feeding air humidification, is the feed hydrogen humidification then.The another kind of selection shown in Fig. 5 a, hydrogen humidifier 90 and regenerative dryer 80 can be in parallel in cathode exhaust recirculation line 60 rather than be connected in series, so that be hydrogen and air wetting simultaneously.Another selection is, shown in Fig. 5 b, the operating condition of fuel cell 12 is when adopting the series connection humidification, can also select to provide again a by-pass line 82 to walk around hydrogen humidifier 90, make the part of cathode exhaust stream not flow to regenerative dryer 80 by hydrogen humidifier.
But, preferably at first be the hydrogen gas stream humidification in practice because expectation anode dew point temperature is higher than the negative electrode dew point temperature, this be since the water in fuel cell 12 can be naturally from anode to the negative electrode transmission.In fuel cell 12, the relative humidity of the hydrogen of expectation also often is higher than the relative humidity of air, so that do not have too much water in the fuel cell 12.Therefore, preferably make cathode exhaust stream at first flow heat-shift and moisture with hydrogen feed.
Various transducers can be set in known manner, be used for measuring the parameter of the fuel stream, oxidant stream and the cooling agent logistics that provide to fuel cell 12.Another aspect of the present invention depends on the temperature of measurement reactant and determines humidity according to known temperature-humidity characteristic curve,, does not directly measure humidity that is.
Can figure out, in the present invention, before process gas enters fuel cell 12, needn't earlier the process gas humidification be arrived supersaturation, again water condensation is gone out to obtain 100% relative humidity, make it be in a certain temperature obtaining required relative humidity then, and at the common pending application U.S.Patent of applicant Application No.09/801, but do like this in 916.Native system can be applied in fuel stream wherein and oxidant stream has or do not have in the fuel cell system of 100% relative humidity.When fuel cell 12 can not move, the humidity of an anode dew point heat exchanger and negative electrode dew point heat exchanger control fuel and oxidant can be set under fuel and oxidant have the condition of 100% relative humidity.Yet this depends on the characteristic of fuel cell 12 fully, for example the service conditions of proton exchange membrane.
First embodiment that should also be understood that this fuel cell system of the present invention is moved under ambient pressure or the condition near ambient pressure.Referring now to Fig. 3,, it has expressed second cooling circuit that embodiment adopted of fuel cell system of the present invention, and this loop under high pressure promptly, is higher than under the atmospheric condition and moves.
In second embodiment, similar assembly is represented with identical numeral, for the purpose of brief, no longer is repeated in this description these assemblies.
In second embodiment, on oxidant supply line 30 and the place that is positioned at regenerative dryer 80 upstreams a high pressure compressor 105 is set, be used for compressing feeding air from air cleaner 32.A second cooling heat exchanger 110 is set between compressor 105 and regenerative dryer 80, is used for the compressed air that chilling temperature raises.Therefore, except first cooling circuit 14 that is used for fuel cell 12, one the 3rd cooling circuit 114 is set also, it comprises the secondary heat exchanger 110 with the water-water heat exchanger form.The 3rd cooling circuit 114 can also and be used for the mains switch plate 108 of compressor 105 by compressor motor 106, compressor motor controller 107, to cool off these assemblies.Cooling agent in the first and the 3rd cooling circuit 14 and 114 is all driven by first cooling medium pump 13.The same with the radiator 18 in second cooling circuit, the radiator 116 of a powered fan is set in the 3rd cooling circuit 114; Other of heat exchanger 15 selects equally also to be applicable to radiator 116.
Regardless of the pressure of operation of fuel cell system, common preferably build-up pressure balance between the fuel stream of fueling battery 12 and oxidant stream.This has guaranteed can not have significant barometric gradient in fuel cell 12, and thereby prevented the damage of the fuel cell that causes owing to barometric gradient, and prevent that reactant and cooling agent from flowing on undesirable direction.And this has also guaranteed to offer the fuel that fuel cell 12 is used to react and the suitable stoichiometric relationship of oxidant.
In the present invention, as shown in Figure 6, this point realizes by a balanced pressure regulator 22 ' and a pressure-equalizing line 25 are provided between fuel supply lines 10 and oxidant supply line 30.The mode that pressure-equalizing line 25 is communicated with by fluid be arranged on the fuel supply lines 20 and be positioned at the balanced pressure regulator 22 ' of hydrogen humidifier 90 upstreams, and the 3rd node 102 that is positioned at regenerative dryer 80 upstreams on the oxidant supply line 30 is connected.Balanced pressure regulator 22 ' can be forward pressure regulator equally.Yet, it must be suitable for two kinds of fluids work and can balance two fluid streams between pressure.At the common pending application U.S.Patent of applicant Application No.09/961, an example of this balanced pressure regulator 22 ' is disclosed in 092, this patent application mode is by reference included this specification in.Usually, this balanced pressure regulator 22 ' is regulated flowing of hydrogen according to the pressure of the air logistics that pressure-equalizing line 25 is introduced, and is adjusted to acquisition mechanical balance when equating with the pressure of air logistics up to the pressure with hydrogen gas stream.
Can figure out, pressurizer can be arranged on the oxidant supply line 30, thereby can regulate the pressure of air logistics according to hydrogen gas stream pressure.Yet mode is by selecting air blast or compressor proper speed or capacity to come the pressure of setting air logistics easily in practice, and changes the pressure of hydrogen gas stream in view of the above.Therefore, the pressure that preferably makes hydrogen gas stream changes with the variation of the pressure of air logistics.In some systems, the pressure balance between two reactant feed flows is provided with by manual or controller.Yet design of the present invention has automatically guaranteed the balance of pressure.
The present invention compared with prior art has lot of advantages.All water that are used for to fuel and oxidant humidification all are that fuel cell 12 self produces.This has reduced the weight and the quantity of assembly in the system, makes whole system compact and efficient.Native system can be made quick response to electricity needs.All these features all need in vehicular applications especially.
Though above explanation has constituted embodiment preferred, should be realized that, under the condition of the reasonable intension of the proper range that does not depart from claims, can adjust or change the present invention.For example, the present invention can be applied in the dissimilar fuel cells, includes but not limited to soild oxide, alkalescence, fused carbonate (molton-carbonate) and phosphoric acid fuel cell.Particularly, the present invention can be applied to the fuel cell that moves under suitable high-temperature.Can understand as those of ordinary skills, the demand of humidification depends on the electrolyte of use and the operating temperature and the pressure of fuel cell to a great extent.Therefore, be understandable that perhaps the present invention is not that the fuel cell to number of different types all is suitable for.
Claims (38)
1. fuel cell system comprises:
(a) fuel cell is provided with one first reactant entrance, first reactant outlet, second reactant entrance, second reactant outlet, a coolant entrance and a coolant outlet;
(b) one first reactant supply subsystem is used for providing first reactant feed flow to first reactant entrance of fuel cell;
(c) one second reactant supply subsystem is used for providing second reactant feed flow to second reactant entrance of fuel cell;
(d) regenerative dryer subsystem, comprise one first regenerative dryer and one second regenerative dryer, wherein, first regenerative dryer is used at least a portion of heat in the first reactant effluent streams and moisture is passed to first reactant feed flow that first reactant is supplied subsystem, and second regenerative dryer is used at least a portion of heat in the first reactant effluent streams and moisture is passed to second reactant feed flow that second reactant is supplied subsystem;
(e) one first reactant recirculation subsystem, be used for making at least a portion of the first reactant effluent streams to enter a regenerative dryer subsystem, give first reactant feed flow of first reactant supply subsystem and second reactant feed flow of second reactant supply subsystem heat and moisture transmission from first reactant outlet recirculation;
Wherein first and second regenerative dryer connect with series system in the regenerative dryer subsystem, make heat and moisture in the reactant effluent streams of winning at first pass to second reactant feed flow, pass to first reactant feed flow by the first regenerative dryer equipment then by second regenerative dryer; And
The drying system of wherein regenerating also comprises a by-pass line of walking around second regenerative dryer, makes a part first reactant effluent streams in the reactant recirculation subsystem of winning directly flow to the first regenerative dryer equipment without the second regenerative dryer equipment.
2. according to the fuel cell system of claim 1, also comprise one second reactant recirculating system, be used for making at least a portion of the second reactant effluent streams to enter second reactant supply subsystem, so that at least a portion of the second reactant effluent streams is mixed with second reactant feed flow from second reactant outlet recirculation.
3. according to the fuel cell system of claim 2, wherein second reactant supply subsystem comprises a flow rate adjustment device, is used for regulating the flow velocity of second reactant feed flow that second reactant entrance to fuel cell provides.
4. according to the fuel cell system of claim 3, wherein flow rate adjustment device is at least one forward pressure regulator.
5. according to the fuel cell system of claim 4, wherein flow rate adjustment device comprises a plurality of forward pressure regulator that are connected in parallel, and each adjuster all has a different set point.
6. according to each fuel cell system in the claim 2～5, wherein closing on the first reactant exit in the first reactant recirculation subsystem provides a drainage arrangement, is used for discharging at least a portion of the water in the first reactant recirculation subsystem.
7. according to the fuel cell system of claim 6, wherein drainage arrangement comprises a cathode outlet flowing line, it is designed and sized to the bubble that makes in this flowing line can maintain moisture in the cathode outlet flowing line, so that water can be discharged along the cathode outlet flowing line automatically and termly.
8. according to each fuel cell system in the claim 2～5, wherein second reactant supply subsystem comprises one second reactants water separation device, is used at second reactant feed flow by separating at least a portion of water wherein behind the second regenerative dryer equipment.
9. according to the fuel cell system of claim 8, wherein second reactants water separation device is located in second reactant supply subsystem, so that divide dried up from following mixture: this mixture is from least a portion of the second reactant effluent streams of the second reactant recirculation subsystem and the mixture of second reactant feed flow.
10. according to the fuel cell system of claim 9, wherein first reactant supply subsystem comprises one first reactants water separation device, is used at first reactant feed flow by separating at least a portion of water wherein behind the first regenerative dryer equipment.
11. according to the fuel cell system of claim 10, comprise that also one second reactant cleans subsystem, this subsystem cleans at least a portion from the second reactant effluent streams of second reactant outlet.
12. according to the fuel cell system of claim 11, wherein second reactant cleaning subsystem comprises a cleaning control device, is used for controlling at least a portion of cleaning the second reactant effluent streams.
13. according to the fuel cell system of claim 12, wherein the cleaning control device is selected from solenoid valve, proportional solenoid valve and Venturi tube.
14. according to the fuel cell system of claim 13, wherein the regenerative dryer subsystem has an outlet, is used for after the first reactant effluent streams is passed through the regenerative dryer subsystem its discharge; This fuel cell system also comprises a discharging subsystem, is used for mixing with the second reactant effluent streams of cleaning subsystem from second reactant from the first reactant emission of regenerative dryer subsystem outlet, and this mixture is discharged.
15., wherein discharge subsystem and comprise that is divided a dried up emission separator from described mixture according to the fuel cell system of claim 14.
16. according to the fuel cell system of claim 15, also comprise first cooling circuit that has coolant container, wherein cooling agent returns this coolant container then from this coolant container fuel cell of flowing through.
17. fuel cell system according to claim 16, also comprise one second cooling circuit, and being arranged at one first heat exchanger between first and second cooling circuits, this heat exchanger is realized the heat exchange between the cooling agent in first and second cooling circuits in the mode of non-mixing.
18. according to the fuel cell system of claim 17, wherein second cooling circuit is an open cycle system, the cooling agent in this circulatory system from and return a cooling agent storehouse.
19. according to the fuel cell system of claim 17 or 18, wherein isolated water is led to coolant container from first reactants water separation device, second reactants water separation device and emission separator.
20. fuel cell system according to claim 16, wherein first reactant supply subsystem also is equipped with a compression set in the place that is positioned at the first regenerative dryer equipment upstream, is used for compressing first reactant and offers first reactant entrance and the second cooling heat exchanger of fuel cell; And wherein this fuel cell system also comprises one the 3rd cooling circuit, and compression set and second cooling heat exchanger are run through in this loop, with first reactant flow after cooled compressed device and the compression.
21. according to each fuel cell system in the claim 2～5, wherein the second reactant recirculating system comprises a recirculation pump that variable velocity is arranged, and is used to make at least a portion of the second reactant effluent streams to export to second reactant supply subsystem with different flow velocitys from second reactant and carries out recirculation.
22. according to each fuel cell system in the claim 2～5, also comprise a pressure equaliser, this device is suitable for the pressure of first reactant feed flow in balance first reactant supply subsystem and the pressure of second reactant feed flow in second reactant supply systems.
23. fuel cell system according to claim 22, wherein pressure equaliser comprises a balanced pressure regulator and a pressure-equalizing line, balanced pressure regulator is arranged in one of first reactant and second reactant supply subsystem, and is positioned at the upstream of corresponding regenerative dryer equipment; The mode that pressure-equalizing line is communicated with by fluid is connected between in described balanced pressure regulator and first reactant and second reactant supply subsystem another, the junction is positioned at the upstream of corresponding regenerative dryer, and described balanced pressure regulator is regulated the pressure of another reactant feed flow according to the pressure of a reactant feed flow in first reactant and second reactant and both are equated.
24. according to the fuel cell system of claim 23, wherein balanced pressure regulator is located in second reactant supply subsystem, the mode that pressure-equalizing line is communicated with by fluid connects balanced pressure regulator and first reactant supply subsystem.
25. control the reactant in the fuel cell system and the method for water for one kind, this fuel cell is provided with one first reactant entrance, first reactant outlet, second reactant entrance, second reactant outlet, described method comprises:
(a) provide first reactant feed flow to first reactant entrance;
(b) provide second reactant feed flow to second reactant entrance;
(c) make at least a portion of the first reactant effluent streams of collecting from first reactant outlet carry out recirculation by first and second regenerative dryer;
(d) in first regenerative dryer, at least a portion of heat in the first reactant effluent streams and moisture is passed to first reactant feed flow, and the another part with heat in the first reactant effluent streams and moisture in second regenerative dryer passes to second reactant feed flow;
Wherein step (d) comprises at first and to give second reactant feed flow with a part of heat and the moisture transmission of the described first reactant effluent streams, and another part heat that then will the described first reactant effluent streams and moisture transmission are to first reactant feed flow; And
Wherein at least a portion of the first reactant effluent streams is flowed through and is flowed to the first regenerative dryer equipment behind the by-pass line of walking around second regenerative dryer.
26. the method according to claim 25 also comprises:
(e) export at least a portion of collecting the second reactant effluent streams from second reactant;
(f) at least a portion of the second reactant effluent streams is mixed with second reactant feed flow;
27. according to the method for claim 26, wherein step (b) comprises that the needs of fuel cell regulate the flow velocity of second reactant feed flow, with dynamic provisioning second reactant feed flow.
28. according to the method for claim 27, wherein step (f) also comprises: from the mixture of at least a portion of the second reactant effluent streams and second reactant feed flow, divide dried up.
29. according to the method for claim 28, wherein step (d) comprises that also branch is dried up from first reactant feed flow.
30. according to the method for claim 29, wherein step (e) also comprises: clean at least a portion from the second reactant effluent streams of second reactant outlet.
31. the method according to claim 30 also comprises:
(g) after the part of the described first reactant effluent streams and another part are given first reactant feed flow and second reactant feed flow with its heat and moisture transmission, the first reactant effluent streams is mixed with the second reactant effluent streams after the cleaning;
(h) mixture is discharged.
32. according to the method for claim 31, wherein step (g) comprises that also branch is dried up from mixture.
33., also comprise with the cooling agent that flows through a cooling circuit and come the cooled fuel cell group according to each method in the claim 25～32.
34. according to each method in the claim 25～32, wherein step (a) comprises compression first reactant feed flow.
35. according to the method for claim 34, wherein step (a) also comprises first reactant feed flow after the cooled compressed.
36. according to each method in the claim 25～32, wherein step (e) comprises that at least a portion that makes from the second reactant effluent streams of second reactant outlet carries out recirculation with variable flow velocity.
37. according to each method in the claim 25～32, step (a) and (b) comprise the pressure of balance first and second reactant feed flows wherein.
38. according to the method for claim 37, step (a) and (b) comprise the pressure of regulating second reactant feed flow according to the pressure of first reactant feed flow wherein.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA002404685A CA2404685A1 (en) | 2002-04-15 | 2002-09-23 | System and method for management of gas and water in fuel cell system |
| CA2,404,685 | 2002-09-23 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1685549A CN1685549A (en) | 2005-10-19 |
| CN1326277C true CN1326277C (en) | 2007-07-11 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB038226847A Expired - Fee Related CN1326277C (en) | 2002-09-23 | 2003-06-18 | System and method for management of gas and water in fuel cell system |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP1543576A2 (en) |
| JP (1) | JP2006500737A (en) |
| CN (1) | CN1326277C (en) |
| AU (1) | AU2003245138A1 (en) |
| WO (1) | WO2004027908A2 (en) |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006024123A1 (en) * | 2004-08-30 | 2006-03-09 | Hydrogenics Corporation | Method and apparatus for removing heat from a radiator of an electrochemical cell stack by evaporation of water |
| RU2379794C1 (en) * | 2005-12-12 | 2010-01-20 | Тойота Дзидося Кабусики Кайся | Fuel element cooling system and method |
| JP2007280927A (en) * | 2005-12-12 | 2007-10-25 | Toyota Motor Corp | Cooling system for fuel cell |
| US8639903B2 (en) | 2010-05-13 | 2014-01-28 | Micron Technology, Inc. | Staggered programming for resistive memories |
| DE102014018230B4 (en) * | 2014-12-04 | 2016-10-27 | Mann + Hummel Gmbh | Accumulator arrangement for a vehicle |
| SG10201912064YA (en) * | 2016-06-29 | 2020-02-27 | Nat Univ Singapore | A toxicant monitoring system |
| CN106410243B (en) * | 2016-11-29 | 2019-03-22 | 北京建筑大学 | A kind of fuel cell experimental bench looped system and its working method |
| JP2019114485A (en) * | 2017-12-26 | 2019-07-11 | トヨタ自動車株式会社 | Fuel cell system, mobile body, and method for controlling exhaust gas discharge |
| CN109786790B (en) * | 2019-03-27 | 2024-02-23 | 佛山市清极能源科技有限公司 | Fuel cell system capable of being started and stopped at low temperature and control method thereof |
| CN110600771A (en) * | 2019-09-20 | 2019-12-20 | 东方电气(成都)氢燃料电池科技有限公司 | Fuel cell system and control method thereof |
| JP2022108688A (en) * | 2021-01-13 | 2022-07-26 | 本田技研工業株式会社 | Vehicle temperature control system |
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| JP3244912B2 (en) * | 1994-02-15 | 2002-01-07 | 三菱重工業株式会社 | Fuel cell system |
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2003
- 2003-06-18 EP EP03737767A patent/EP1543576A2/en not_active Withdrawn
- 2003-06-18 AU AU2003245138A patent/AU2003245138A1/en not_active Abandoned
- 2003-06-18 CN CNB038226847A patent/CN1326277C/en not_active Expired - Fee Related
- 2003-06-18 WO PCT/CA2003/000901 patent/WO2004027908A2/en active Application Filing
- 2003-06-18 JP JP2004536707A patent/JP2006500737A/en active Pending
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| US5786104A (en) * | 1996-12-31 | 1998-07-28 | The Dow Chemical Company | Method and apparatus for humidification of incoming fuel cell process gases |
| US6013385A (en) * | 1997-07-25 | 2000-01-11 | Emprise Corporation | Fuel cell gas management system |
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| DE19902219C1 (en) * | 1999-01-21 | 2000-06-08 | Daimler Chrysler Ag | Process for operating a fuel cell system comprises removing moisture from a waste air stream of a fuel cell, desorbing the water and recycling |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1685549A (en) | 2005-10-19 |
| WO2004027908A2 (en) | 2004-04-01 |
| JP2006500737A (en) | 2006-01-05 |
| EP1543576A2 (en) | 2005-06-22 |
| WO2004027908A3 (en) | 2005-01-06 |
| AU2003245138A1 (en) | 2004-04-08 |
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