CN221783255U - Anode subsystem of fuel cell and fuel cell - Google Patents

Abstract

The application relates to a fuel cell anode subsystem and a fuel cell, wherein the fuel cell comprises a pile with an anode and a cathode, and the anode subsystem comprises: an anode gas supply line supplying hydrogen gas to the anode inlet; an anode exhaust line for partially recycling the anode medium discharged from the anode outlet back to the anode gas supply line, a water separator being provided on the anode exhaust line to separate liquid water in the anode medium; a cooling device and a heating device are also arranged along the anode exhaust pipeline, and the cooling device is arranged between the anode outlet and the water separator to cool the anode medium passing through the cooling device so as to condense water vapor in the anode medium; and a heating device is arranged at the downstream of the water separator to heat the separated anode medium so as to convert liquid water remained in the separated anode medium into water vapor. By adopting the technical scheme of the application, the separation efficiency of the water separator can be improved, the hydrogen circulating pump is protected, and the hydrogen which is circulated into the fuel cell stack is ensured to have proper humidity.

Description

Anode subsystem of fuel cell and fuel cell

Technical Field

The present utility model relates to the technical field of fuel cells, and in particular, to an anode subsystem of a fuel cell and a fuel cell including the anode subsystem.

Background

With the popularity of electric vehicles, fuel cells are becoming increasingly popular as a very important component thereof, in proton exchange membrane fuel cells, the anode subsystem thereof is used to supply hydrogen to the stack anode of the fuel cell and to recycle the anode medium discharged from the stack anode outlet. The anode medium comprises saturated gas composed of residual hydrogen after reaction, a small amount of nitrogen from air and water vapor generated by reaction, and the saturated gas is recycled through a hydrogen circulating pump in the anode subsystem so that the hydrogen is reused. In addition to the saturated gases, a portion of the liquid water produced by the reaction at the stack cathode of the fuel cell during the reaction also permeates through the proton exchange membrane to exit the anode outlet of the stack as a portion of the anode media. In order to reduce the influence of water vapor in saturated gas and the above-mentioned liquid water on the fuel cell, a water separator is generally provided in the fuel cell to separate the liquid water therein.

However, in the actual working process, the humidity of the anode supply of the electric pile of the fuel cell needs to be controlled within the range of 40% -70% RH, and the saturation degree of water vapor in the saturated gas coming out of the outlet of the anode is high, so that in the case that the water vapor and the liquid water flowing from the cathode can not be effectively separated, on one hand, the failure of the hydrogen circulating pump can be caused, and on the other hand, the gas with relatively high humidity can be caused to circulate into the anode of the electric pile of the fuel cell, which causes flooding, blocking of the gas flow channel and increase of concentration polarization, thereby greatly reducing the performance of the fuel cell.

Accordingly, there remains a need for improvements in the anode subsystem of existing fuel cells to reduce the moisture content of saturated gases exiting the anode of the fuel cell stack, to improve the efficiency of the water separator to protect the hydrogen circulation pump, and to moderate the humidity of the gases recirculated into the fuel cell stack, thereby improving the performance of the fuel cell.

It should be noted that the "background" section is only for aiding in understanding the present utility model, and thus the disclosure in the "background" section may contain some of the prior art that does not form part of the knowledge of one skilled in the art. The matters disclosed in the "background" section are not representative of the matters or problems to be solved by one or more embodiments of the present utility model, and are known or recognized by those skilled in the art prior to the application of the present utility model.

Disclosure of utility model

The utility model aims to provide an anode subsystem of a fuel cell, which can collect more liquid water formed by condensation from saturated gas from an anode outlet of a cell stack of the fuel cell, and improve the efficiency of a water separator to protect a hydrogen circulating pump. In addition, the anode subsystem of the fuel cell of the present utility model also enables the humidity of the gas recirculated into the fuel cell stack to be moderate, thereby enhancing the performance of the fuel cell.

According to one aspect of the present utility model there is provided an anode subsystem for a fuel cell comprising a stack having an anode and a cathode, the anode of the stack having an anode inlet and an anode outlet, the anode subsystem comprising:

An anode gas supply line for supplying hydrogen to the anode inlet;

An anode exhaust line for partially recycling anode media discharged from the anode outlet back to the anode gas supply line, a water separator being provided on the anode exhaust line for separating liquid water in the anode media;

wherein a cooling device and a heating device are also provided along the anode exhaust line, the cooling device being disposed between the anode outlet and the water separator to cool the anode medium passing therethrough to condense water vapor in the anode medium; and the heating device is arranged at the downstream of the water separator to heat the separated anode medium so as to convert liquid water remained in the separated anode medium into water vapor.

Preferably, the cooling device is a first heat exchanger, the heat exchange medium of which is air from the external environment, the air flowing in from one end of the first heat exchanger to reduce the temperature of the anode medium and being discharged from the other end of the first heat exchanger to the external environment.

Optionally, the cooling device is a first heat exchanger, the heat exchange medium of which is a cooling liquid, the cooling liquid is stored in a reservoir, and flows in from one end of the first heat exchanger to reduce the temperature of the anode medium, and flows out from the other end of the first heat exchanger and flows back to the reservoir for recycling.

Preferably, the heating means is a second heat exchanger, the heat exchange medium of which is a portion of the compressed air supplied to the cathodes of the stacks, which portion of the compressed air is re-supplied to the cathodes of the stacks after flowing through the second heat exchanger.

Optionally, the heating device is a hydrogen heat exchanger provided on an anode gas supply line, and the anode medium separated by the water separator and the hydrogen gas from the hydrogen reservoir are subjected to temperature raising treatment at the hydrogen heat exchanger to be supplied to the anode inlet via the anode gas supply line.

Optionally, the heating device is a resistive heater.

Preferably, an ejector pump is arranged on the anode gas supply line, and the anode medium heated by the heating device is conveyed to the ejector pump to be mixed with the hydrogen from the hydrogen storage device, and then is supplied to the anode inlet through the anode gas supply line.

Optionally, a hydrogen circulation pump is arranged downstream of the heating device along the anode exhaust line for delivering the warmed anode medium to the ejector pump.

Optionally, the anode subsystem further comprises a drain line connected to the water separator for draining liquid water separated by the water separator to an external environment.

According to another aspect of the present utility model, there is provided a fuel cell comprising:

A galvanic pile having an anode and a cathode;

An air supply system for supplying air to the cathodes of the stacks; and

An anode subsystem according to the preceding claim, wherein hydrogen is supplied to the anodes of the stack via an anode gas supply line of the anode subsystem, and anode medium after electrochemical reaction between the air and the hydrogen is discharged from the anode outlet and partly recycled back to the anode gas supply line.

Drawings

The foregoing and other aspects of the utility model will be more fully understood and appreciated in conjunction with the following drawings. It is to be understood that the drawings are provided for purposes of illustration only and depict only typical or exemplary embodiments. These drawings are provided to facilitate an understanding of the concepts disclosed herein and should not be considered limiting of the breadth, scope, or applicability of these concepts. It should be noted that for clarity and ease of illustration, the drawings are not necessarily drawn to scale. Wherein:

FIG. 1 is a schematic diagram of an anode subsystem of a fuel cell according to the prior art, with system components for hydrogen supply in the anode gas supply line omitted for clarity;

FIG. 2 is a schematic view of an anode sub-system according to a first embodiment of the utility model, with system components for hydrogen supply in the anode gas supply line omitted for clarity;

Fig. 3 is a schematic view of an anode sub-system according to a second embodiment of the utility model, showing system components for hydrogen supply in the anode gas supply line.

Detailed Description

In the drawings, wherein like structural or functional features are represented by like reference numerals throughout the several views, the drawings are not necessarily to scale, but are exaggerated for clarity.

Referring to fig. 1, which shows a partial schematic view of an anode sub-system of a fuel cell according to the related art, a part of system components for supplying hydrogen in the anode sub-system are omitted for clarity (omitted parts may be seen in fig. 3). As shown, the fuel cell includes a stack 10, the stack 10 having an anode 101 and a cathode 102, the anode 101 of the stack 10 having an anode inlet 1011 and an anode outlet 1012. It should be noted that the placement of the anode inlet and anode outlet in fig. 1 is illustrative only and not limiting. It can be understood that the anode inlet and the anode outlet can be flexibly arranged at the end of the anode of the electric pile according to actual needs. Further, the anode subsystem comprises an anode gas supply line 11 for supplying hydrogen to the anode inlet 1011 and an anode exhaust line 12, wherein the anode exhaust line 12 is adapted to partially recycle anode medium after reaction and discharged from the anode outlet 1012 back to the anode gas supply line 11. During operation of the fuel cell, hydrogen from the hydrogen supply system is supplied to the anode 101 of the stack 10 by means of a jet pump 13 provided on the anode supply line 11 and air is supplied to the cathode 102 of the stack 10 via an air supply system (i.e. a cathode supply line in the cathode subsystem of the fuel cell, not shown in the figure). The hydrogen molecules entering the anode 101 are adsorbed by the catalyst and undergo oxidation reaction to be ionized into hydrogen ions and electrons, the hydrogen ions are transferred from the anode 101 to the cathode 102 via the proton exchange membrane in the stack 10, and the electrons flow to the cathode 102 through an external circuit to form an electric current. In addition, the hydrogen ions traveling to the cathode 102 undergo a reduction reaction with oxygen from the fuel cell stack cathode 102, thereby generating liquid water, most of which is discharged from a cathode outlet (not shown in the figure) as a "cathode medium" together with the remaining gas in the air.

On the other hand, a saturated gas composed of hydrogen remaining after the reaction, a small amount of nitrogen from the air, water vapor generated by the reaction, and part of liquid water generated at the cathode 102 of the stack and permeated back through the proton exchange membrane are discharged together as the above-mentioned "anode medium" from the anode outlet 1012, and supplied to the anode gas supply line 11 via the anode exhaust line 12 for circulation supply of anode gas. As can be seen from fig. 1, the anode exhaust line 12 communicates with a jet pump 13 provided on the anode gas supply line 11 and an anode outlet 1012 of the stack 10, and a water separator 14 for separating liquid water in the above-mentioned "anode medium" is further provided on the anode exhaust line 12. Depending on the amount of hydrogen circulation, a hydrogen circulation pump 15 may optionally be provided on the anode exhaust line 12 downstream of the water separator 14 for assisting in circulating the "anode medium" after separation of the liquid water into the anode supply line 11 to be supplied to the anodes 101 of the stack 10 together with hydrogen from the hydrogen supply system. It should be noted that the terms "upstream" and "downstream" are defined herein with respect to the position where the anode medium passes sequentially along the anode exhaust line after exiting the anode outlet.

As described in the background section, the saturated water vapor and liquid water in the "anode medium" described above cannot be sufficiently separated only by the existing water separator 14, which may cause more liquid water to enter the hydrogen circulation pump 15, possibly causing malfunction of the hydrogen circulation pump. Even if a hydrogen circulation pump is not provided on the anode exhaust line 12, hydrogen with high water content circulates into the stack anode 101 through the anode gas supply line 11, which reduces the reaction efficiency at the stack anode 101, reduces the working efficiency of the entire fuel cell, and even causes flooding of the stack, thereby causing failure of the fuel cell and shortening the service life.

To solve the above-mentioned technical problems, the present utility model is directed to an anode subsystem of the fuel cell shown in fig. 1. Referring to fig. 2, a schematic diagram of an anode sub-system according to a first embodiment of the utility model is shown. In this embodiment, the arrangement relationship of the stack 10, the anode gas supply line 11, and the anode gas exhaust line 12 of the fuel cell, and the parts of the ejector pump 13, the water separator 14, the hydrogen circulation pump 15, and the like, which are provided on the corresponding lines, respectively, are identical to those described above in connection with fig. 1, and thus will not be described in detail. The main difference of the present utility model compared to the prior art is that additional cooling means and heating means are provided along the anode exhaust line 12. In this embodiment the cooling means takes the form of a first heat exchanger 100 and the heating means takes the form of a second heat exchanger 200. Wherein the first heat exchanger 100 is disposed between the anode outlet 1012 and the water separator 14 (in other words, upstream of the water separator 14 along the anode exhaust line 12) for cooling the anode medium discharged from the anode outlet 1012 to condense water vapor in the anode medium to form more liquid water; the second heat exchanger 200 is disposed between the water separator 14 and the ejector pump 13 of the anode gas supply line 11 (in other words, downstream of the water separator 14 along the anode exhaust line 12), and is used for heating the anode medium separated by the water separator 14, so as to convert the liquid water remaining in the separated anode medium into water vapor. As shown, after the anode medium discharged from the anode outlet 1012 of the stack 10 is subjected to a temperature reduction treatment by the first heat exchanger 100, more liquid water is condensed from the saturated water vapor, and this liquid water is separated by the water separator 14 together with the liquid water originally contained in the anode medium and having permeated from the stack cathode 102. Here, since the separation efficiency of the water separator 14 cannot reach 100%, not all the liquid water is separated. Further as shown, a drain line 16 is connected to the water separator 14 and is configured to drain the liquid water separated by the water separator 14 to the external environment by opening a drain valve 17. Next, the anode medium separated by the water separator 14 (including the hydrogen remaining from the reaction, a small amount of nitrogen from the air, and a part of water vapor and liquid water not completely separated by the water separator 14) is continuously transferred downstream along the anode exhaust line 12, and is further passed through the second heat exchanger 200 to heat the anode medium so that the remaining liquid water therein is converted into water vapor, whereby the heated anode medium (including the hydrogen remaining from the reaction, a small amount of nitrogen from the air, and a certain amount of saturated water vapor) is fed into the hydrogen circulation pump 15 located downstream of the second heat exchanger 200, is pumped through the hydrogen circulation pump 15 into the ejector pump 13 provided on the anode exhaust line 11 to be mixed with the hydrogen from the hydrogen supply system, Thereby humidifying the hydrogen gas before it enters the anode inlet 1011 of the stack 10. The humidified hydrogen can avoid the increase of the internal resistance of the cell caused by the decrease of the proton conductivity of the proton exchange membrane in the fuel cell stack due to the evaporation of water. It will be appreciated that to prevent the warmed anode media from cooling to condense, the tubing between the second heat exchanger 200 and the jet pump 13 and between the jet pump 13 and the anode inlet 1011 needs to be insulated.

For the first heat exchanger 100, conventional air cooling and liquid cooling may be used to cool the anode medium exiting the anode outlet 1012. For example, ambient air or a cooling liquid may be used as a heat exchange medium, as indicated by arrows in fig. 2, to flow in from one end of the first heat exchanger 100, through heat exchange tubes therein, and to be discharged from the other end of the first heat exchanger 100. Depending on the nature of the heat exchange medium itself, a separate storage vessel may be provided for it. For example, when the heat exchange medium is a cooling fluid (e.g., water, ethanol, ethylene glycol, etc.), a separate reservoir may be provided, and the cooling fluid discharged from the first heat exchanger 100 may flow back to the reservoir for recycling. When air is used as the heat exchange medium, air from the external environment can be directly drawn into the first heat exchanger 100 and discharged from the other end to the external environment without providing a special storage container.

The heat exchange medium of the second heat exchanger 200 is a part of the compressed air supplied to the cathode 102 of the stack 10. As will be appreciated by those skilled in the art, the air supplied to the stack cathode 102 thereof during the reaction of the fuel cell is subjected to compression treatment by the air compressor before entering the stack cathode 102, and a part of the compressed air may be supplied to the second heat exchanger 200, for example, through a bypass line (not shown) provided in the cathode subsystem of the fuel cell, and the high-temperature compressed air may flow in from one end of the second heat exchanger 200, flow through a heat exchange tube therein, and be discharged from the other end of the second heat exchanger 200 as indicated by an arrow in fig. 2. It will be appreciated that the compressed air described above may continue to be supplied to the stack cathode 102 of the fuel cell after being discharged from the second heat exchanger 200 to participate in the electrochemical reaction therein.

On the other hand, an existing hydrogen heat exchanger in the hydrogen supply system of the fuel cell may also be utilized as the second heat exchanger. Referring to fig. 3, there is shown a schematic diagram of an anode sub-system according to a second embodiment of the utility model, in which the components provided by the anode gas supply line 11 are fully shown. As shown, hydrogen from the refill station is maintained in the hydrogen reservoir 110, and in use hydrogen is supplied from the hydrogen reservoir 110 along the anode supply line 11 to the stack anode 101 of the fuel cell via the hydrogen heat exchanger 120 and shut-off valve 18. In this case, the hydrogen heat exchanger 120 may still be considered as a heating device arranged downstream of the water separator 14. Similarly to the foregoing embodiment, the hydrogen heat exchanger 120 serves as a second heat exchanger to heat the anode medium separated by the water separator 14 so that the remaining liquid water therein is converted into water vapor, and the heated anode medium (including the hydrogen remaining from the reaction, a small amount of nitrogen from the air, and a certain amount of saturated water vapor) is fed into the ejector pump 13 on the anode gas supply line 11 via the additional feed line 12 '(this feed line 12' may be regarded as an extension of the anode gas discharge line 12 downstream of the hydrogen heat exchanger 120), thereby achieving the purpose of humidifying the hydrogen gas before it enters the anode inlet 1011 of the stack 10. It is to be understood that the hydrogen heat exchanger 120 may also use compressed air as the heat exchange medium in the previous embodiments, and will not be described herein.

In practical operation, the stack anode supply humidity of the fuel cell is typically controlled in the range of 40% -70% rh. For example, under the following specific conditions: in the case where the hydrogen nitrogen mixture is discharged from the anode outlet of the stack at a flow rate of 450L/min and contains 1.9g/s of liquid water, the separation efficiency of the water separator is assumed to be 90%, and then with the prior art anode subsystem, 0.19g/s of liquid water will be circulated back to the anode inlet of the stack. Compared with the prior art, by utilizing the technical scheme of the utility model, after the hydrogen-nitrogen mixed gas passes through the first heat exchanger (cooling device), the temperature is reduced to 45 ℃ after heat exchange with the cold heat exchange medium, 0.9g/s of liquid water is condensed and separated from saturated water vapor, the part of liquid water and the original 1.9g/s of liquid water in the anode medium pass through the water separator with the separation efficiency of 90%, 0.28g/s of liquid water is contained in the hydrogen-nitrogen mixed gas after passing through the second heat exchanger (heating device), the temperature of the mixed gas is controlled to 65 ℃ after the temperature rising treatment of the mixed gas, the liquid water with the temperature of 0.18g/s is gasified into water vapor in the process, the dew point temperature is approximately 55 ℃ at the moment, the humidity is approximately 62% RH, the calculated water separator efficiency after the gasified liquid water is subtracted is 94.7%, and the separation efficiency is improved by 4.7% compared with the scheme in the prior art. It will be appreciated that the increase in water separator efficiency will depend on the magnitude of the temperature drop after passing through the first heat exchanger, with a theoretical increase in water separation efficiency being greater as the drop is greater. However, it should be noted that the temperature drop across the first heat exchanger should not be excessive, since as the condensed liquid water increases, meaning that relatively more of the remaining liquid water after separation by the water separator needs to be warmed from a lower temperature to a temperature suitable for transport in the anode gas supply line, this increases the work load and energy consumption of the second heat exchanger. In other words, in the present utility model, it is preferable to control the temperature decrease width of the cooling means in the form of the first heat exchanger and the temperature increase width of the heating means in the form of the second heat exchanger within relatively reasonable ranges, so that the anode medium discharged from the anode outlet of the stack precipitates enough liquid water while passing through the cooling means, while ensuring that enough remaining liquid water is gasified into steam while passing through the heating means later and ensuring that the mixture gas circulated into the anode gas supply line has a proper temperature and humidity. Referring to fig. 3, it can be seen that a temperature sensor T and a pressure sensor P (preferably, an additional humidity sensor may be further provided) are provided along the anode gas supply line at the inlet of the ejector pump to monitor the hydrogen parameter entering the ejector pump, and it is also preferable that similar temperature sensors, pressure sensors and humidity sensors are also provided at the stack anode inlet 1011 for data monitoring, and based on the comparison of the monitored data with desired data, it is determined whether the cooling power of the cooling unit and the heating power of the heating unit are required to be controlled so that hydrogen satisfying the appropriate pressure, temperature and humidity is circulated into the stack anode of the fuel cell.

The utility model is not limited to the embodiments described above, but may be modified. For example, while the principles of the present utility model have been described in the above embodiments by taking the first heat exchanger and the second heat exchanger as examples, respectively, it is to be understood that the cooling means provided between the anode outlet and the water separator and the heating means provided downstream of the water separator are not limited to the form of heat exchangers only. In the case of no consideration of the possibility of excessive energy consumption, it is conceivable to use a cooling device using, for example, electric energy or a resistance heater, as long as the cooling and heating of the anode medium can be achieved accordingly.

In addition, although a hydrogen circulation pump is shown in the embodiment of fig. 2 as being disposed downstream of the second heat exchanger (i.e., the heating device) along the anode exhaust line, the hydrogen circulation pump is not required. In other words, the hydrogen circulating pump can be omitted according to the actual working condition, for example, the anode medium which is subjected to cooling treatment and then heating treatment can be circularly conveyed to the stack anode of the fuel cell by means of the ejector pump in the working range of the ejector pump; and in a low-power area where the ejector pump does not work, the hydrogen circulation can be realized by arranging the hydrogen circulation pump. In addition, although in the embodiment of fig. 2, the ejector pump and the hydrogen circulation pump are operated cooperatively in a serial manner (i.e., the anode medium sequentially passes through the hydrogen circulation pump and the ejector pump along the anode exhaust line), it is envisioned that the ejector pump may also be operated cooperatively in a parallel manner with the hydrogen circulation pump (i.e., the ejector pump and the hydrogen circulation pump are respectively provided with branch lines, and the anode medium is selectively circulated from the anode exhaust line to the anode supply line through different branch lines based on the circulation amount of the anode medium), thereby realizing the recycling of hydrogen.

In summary, the utility model improves the anode subsystem of the existing fuel cell by arranging corresponding cooling devices and heating devices along the anode exhaust line at the upstream and downstream of the water separator respectively, on the one hand, more condensed water formed by condensation can be collected from saturated gas from the anode outlet of the cell stack of the fuel cell, and the efficiency of the water separator is improved to protect the hydrogen circulating pump; and on the other hand, the humidity of the gas recycled into the fuel cell stack can be moderate, so that the performance of the fuel cell is improved.

The utility model has been described in detail with reference to specific embodiments thereof. It will be apparent that the embodiments described above and shown in the drawings are to be understood as illustrative and not limiting of the utility model. It will be apparent to those skilled in the art that the embodiments described in this specification can be used in combination with each other and that the various components of the utility model can be combined in any desired manner, unless such a combination would violate the objectives of the utility model or is otherwise unrealizable. The utility model in its broader aspects is therefore not limited to the specific details, representative structures, and illustrative examples shown and described.

Claims (10)

1. An anode subsystem of a fuel cell, the fuel cell comprising a stack (10) having an anode (101) and a cathode (102), the anode (101) of the stack (10) having an anode inlet (1011) and an anode outlet (1012), the anode subsystem comprising:

an anode gas supply line (11) for supplying hydrogen to the anode inlet (1011);

An anode exhaust line (12) for partially recycling anode medium discharged from the anode outlet (1012) back to the anode gas supply line (11), a water separator (14) being provided on the anode exhaust line (12) for separating liquid water in the anode medium;

The method is characterized in that:

-further cooling means and heating means are provided along the anode exhaust line (12), said cooling means being arranged between the anode outlet (1012) and the water separator (14) to cool the anode medium passing therethrough, thereby condensing water vapor in the anode medium; and the heating device is arranged downstream of the water separator (14) to heat the separated anode medium, thereby converting liquid water remaining in the separated anode medium into water vapor.

2. The anode subsystem of a fuel cell according to claim 1, characterized in that the cooling means is a first heat exchanger (100) whose heat exchange medium is air from the external environment, which air flows in from one end of the first heat exchanger (100) to reduce the temperature of the anode medium and is discharged from the other end of the first heat exchanger (100) to the external environment.

3. The anode subsystem of a fuel cell according to claim 1, characterized in that the cooling means is a first heat exchanger (100) whose heat exchange medium is a cooling liquid, which cooling liquid is stored in a reservoir, flows in from one end of the first heat exchanger (100) to reduce the temperature of the anode medium and is discharged from the other end of the first heat exchanger (100) and flows back to the reservoir for recycling.

4. -The anode subsystem of a fuel cell according to any one of claims 1 to 3, characterized in that the heating means is a second heat exchanger (200), the heat exchange medium of the second heat exchanger (200) being a part of the compressed air supplied towards the cathode (102) of the stack (10), which part of the compressed air is re-supplied to the cathode (102) of the stack (10) after flowing through the second heat exchanger (200).

5. An anode subsystem of a fuel cell according to any one of claims 1-3, characterized in that the heating means is a hydrogen heat exchanger (120) arranged on an anode gas supply line (11), the anode medium separated by a water separator (14) and the hydrogen from the hydrogen reservoir (110) being subjected to a temperature raising treatment at the hydrogen heat exchanger (120) to be supplied to the anode inlet (1011) via the anode gas supply line (11).

6. An anode sub-system of a fuel cell according to any one of claims 1 to 3, wherein the heating means is a resistive heater.

7. -An anode sub-system of a fuel cell according to any of claims 1 to 3, characterized in that an ejector pump (13) is provided on the anode gas supply line (11), the anode medium warmed up via the heating means being fed to the ejector pump (13) to be mixed with hydrogen from a hydrogen reservoir (110) and to be supplied to the anode inlet (1011) via the anode gas supply line (11).

8. Anode subsystem of a fuel cell according to claim 7, characterized in that a hydrogen circulation pump (15) is arranged along the anode exhaust line (12) downstream of the heating means for delivering warmed anode medium to the ejector pump (13).

9. An anode sub-system of a fuel cell according to any of claims 1-3, further comprising a drain line (16) connected to the water separator (14) for draining liquid water separated by the water separator (14) to the external environment.

10. A fuel cell, characterized by comprising:

a galvanic pile (10) having an anode (101) and a cathode (102);

an air supply system for supplying air to the cathodes (102) of the stacks (10); and

The anode subsystem according to any one of claims 1 to 9, wherein hydrogen is supplied to an anode (101) of the stack (10) via an anode gas supply line (11) of the anode subsystem, and anode medium after electrochemical reaction between the air and the hydrogen is discharged from the anode outlet (1012) and partly recycled back to the anode gas supply line (11).