Patent Application
20120040264
1. Field of the Invention
This invention relates generally to a hydrogen concentration sensor that determines the concentration of hydrogen in an anode sub-system of a fuel cell system and, more particularly, to a hydrogen concentration sensor that determines the concentration of hydrogen in an anode sub-system of a fuel cell system that employs anode exhaust gas recirculation, where the Nernst equation is used to determine the hydrogen partial pressure in the recirculation gas from the hydrogen concentration sensor voltage output and the hydrogen partial pressure is used to determine the hydrogen concentration in the recirculation gas.
2. Discussion of the Related Art
Hydrogen is a very attractive fuel because it is clean and can be used to efficiently produce electricity in a fuel cell. A hydrogen fuel cell is an electro-chemical device that includes an anode and a cathode with an electrolyte therebetween. The anode receives hydrogen gas and the cathode receives oxygen or air. The hydrogen gas is dissociated in the anode to generate free protons and electrons. The protons pass through the electrolyte to the cathode. The protons react with the oxygen and the electrons in the cathode to generate water. The electrons from the anode cannot pass through the electrolyte, and thus are directed through a load to perform work before being sent to the cathode.
Proton exchange membrane fuel cells (PEMFC) are a popular fuel cell for vehicles. The PEMFC generally includes a solid polymer electrolyte proton conducting membrane, such as a perfluorosulfonic acid membrane. The anode and cathode typically include finely divided catalytic particles, usually platinum (Pt), supported on carbon particles and mixed with an ionomer. The catalytic mixture is deposited on opposing sides of the membrane. The combination of the anode catalytic mixture, the cathode catalytic mixture and the membrane define a membrane electrode assembly (MEA). MEAs are relatively expensive to manufacture and require certain conditions for effective operation.
Several fuel cells are typically combined in a fuel cell stack to generate the desired power. For example, a typical fuel cell stack for a vehicle may have two hundred or more stacked fuel cells. The fuel cell stack receives a cathode input reactant gas, typically a flow of air forced through the stack by a compressor. Not all of the oxygen is consumed by the stack and some of the air is output as a cathode exhaust gas that may include water as a stack by-product. The fuel cell stack also receives an anode hydrogen reactant gas that flows into the anode side of the stack. The stack also includes flow channels through which a cooling fluid flows.
The fuel cell stack includes a series of bipolar plates positioned between several MEAs in the stack, where the bipolar plates and the MEAs are positioned between the two end plates. The bipolar plates include an anode side and a cathode side for adjacent fuel cells in the stack. Anode gas flow channels are provided on the anode side of the bipolar plates that allow the anode reactant gas to flow to the respective MEA. Cathode gas flow channels are provided on the cathode side of the bipolar plates that allow the cathode reactant gas to flow to the respective MEA. One end plate includes anode gas flow channels, and the other end plate includes cathode gas flow channels. The bipolar plates and end plates are made of a conductive material, such as stainless steel or a conductive composite. The end plates conduct the electricity generated by the fuel cells out of the stack. The bipolar plates also include flow channels through which a cooling fluid flows.
MEAs are permeable and thus allow nitrogen in the air from the cathode side of the stack to permeate through and collect in the anode side of the stack, referred to in the industry as nitrogen cross-over. Even though the anode side pressure may be higher than the cathode side pressure, the cathode side partial pressures will cause air to permeate through the membrane. Nitrogen in the anode side of the fuel cell stack dilutes the hydrogen such that if the nitrogen concentration increases beyond a certain percentage, such as 50%, the fuel cell stack becomes unstable and may fail. It is known in the art to provide a bleed valve at the anode exhaust gas output of the fuel cell stack to remove nitrogen from the anode side of the stack.
It is desirable to predict or estimate the amount of hydrogen in the anode and cathode of a fuel cell system during system start-up to allow the start-up strategy to meet emissions requirements while maximizing reliability and minimizing start time. It is further desirable to estimate the hydrogen concentration in the anode during normal operation, vehicle idle, and all other operating modes of the vehicle to better control the bleeds and maximize fuel efficiency while minimizing stack damage. It is generally desirable that the hydrogen concentration estimator be robust to shut-down and off time related functions and account for membrane permeation of gases as well as air intrusion from external sources. At the same time, the estimation algorithm must be simple enough to be provided in an automotive controller with the calculation sufficiently minimal so as to be completed without delaying the start-up.
Determining the hydrogen concentration in the anode and cathode of the fuel cell stack at start-up will allow the fastest possible start time because the system control does not need to provide excess dilution air when unnecessary. Further, knowing the hydrogen concentration provides a more reliable start because the amount of hydrogen in the anode that needs to be replenished will be known. This is especially relevant for start-ups from a stand-by state, or from the middle of a shut-down, where hydrogen concentrations can be relatively high.
Further, knowing the hydrogen concentration improves durability because when there is an unknown hydrogen concentration in the stack, typical start-up strategies assume the worst case percentage of hydrogen for injection purposes and 100% hydrogen for dilution purposes. In those situations, the initial anode flush with hydrogen could be slower than if the stack is known to be filled with air. The rate of corrosion is proportional to the initial hydrogen flow rate. Therefore, without accurately knowing the hydrogen concentration, each of these events will be more damaging than necessary.
Also, knowing the hydrogen concentration provides improved efficiency because a more accurate determination of hydrogen concentration in the anode and cathode prior to start-up will lead to more effective start-up decisions and potential reduction in hydrogen uses. For example, dilution air could be lowered if it is known that the stack is starting with no hydrogen in it. Further, knowing the hydrogen concentration provides more robust start-ups. In the event of a premature shut-down or a shut-down with a failed sensor, the algorithm can use physical limits to provide an upper and lower bound on the hydrogen in the cathode and anode.
An algorithm may be employed to model an online estimation of the hydrogen and/or nitrogen concentration in the anode during stack operation to know when to trigger the anode exhaust gas bleed. The algorithm may track the nitrogen concentration over time in the anode side of the stack based on the permeation rate from the cathode side to the anode side, and the periodic bleeds of the anode exhaust gas. When the algorithm calculates an increase in the nitrogen concentration above a predetermined threshold, for example 10%, it may trigger the bleed. This bleed is typically performed for a duration that allows multiple stack anode volumes to be bled, thus reducing the nitrogen concentration below the threshold. However, known hydrogen estimation models have typically been relatively inaccurate due to increases in gas cross-over rate as the stack ages.
It is known in the art to provide a hydrogen concentration sensor in an anode exhaust gas recirculation loop that measures the concentration of hydrogen in the anode exhaust to determine whether a bleed is necessary. However, known hydrogen sensors of this type are susceptible to water droplets, which require liquid water separators in the exhaust in order to allow the sensors to operate properly. Further, there is a measurement delay due to the volume the exhaust gas must travel to reach the sensor, which can be on the order of fifteen seconds.
One known hydrogen concentration sensor is known as a thermal conductivity detector (TCD) that uses the known thermal conductivity of gases to calculate the hydrogen concentration. The TCD needs to be calibrated in whatever environment it is being used in, here a hydrogen-nitrogen environment. The TCD also requires a very robust and efficient method for removing all of the water from the gas that is being detected before it is measured because water will cause the sensor to fail. This requires the use of significant plumbing and water separation devices that add volume to the system and generally provides an unacceptable time delay to the measurement.
These sensors also are fairly expensive where the system typically employs two sensors, one in the anode inlet manifold and one in the anode outlet manifold. Because the nitrogen buildup typically occurs very rapidly at high power transients, which may be limited in time, the delay in the sensor reading may cause the hydrogen concentration measurement to not be available during the power up-transient when the nitrogen concentration is the highest.
In accordance with the teachings of the present invention, a hydrogen concentration sensor is disclosed for measuring the hydrogen concentration in an anode sub-system of a fuel cell system. The hydrogen concentration sensor includes a membrane, a first catalyst layer on one side of the membrane and a second catalyst layer on an opposite side of the membrane where the sensor operates as a concentration cell. The first catalyst layer is exposed to fresh hydrogen for the anode side of a fuel cell stack and the second catalyst layer is exposed to an anode recirculation gas from an anode exhaust of the fuel cell stack. The voltage generated by the sensor allows the hydrogen partial pressure in the recirculation gas to be determined, from which the hydrogen concentration can be determined.
Additional features of the present invention will become apparent from the following description and appended claims, taken in conjunction with the accompanying drawings.
The following discussion of the embodiments of the invention directed to a hydrogen concentration sensor for a fuel cell system is merely exemplary in nature, and is in no way intended to limit the invention or its applications or uses.
The hydrogen concentration sensor assembly 28 receives a flow of the anode recirculation gas in the recirculation line 38 and the flow of fresh hydrogen from the source 36 before it is sent to the valve 32, and provides a measurement of the concentration of hydrogen gas in the anode sub-system, as will be discussed in detail below. A pressure sensor 44 provides a measurement of the pressure of the recirculation gas in the recirculation line 38. A temperature sensor 30 measures the temperature of the gas flowing in the anode sub-system, here specifically the recirculation line 38. Also, a relative humidity (RH) sensor 46 measures the relative humidity of the anode recirculation gas in the line 38. In alternate embodiments, the relative humidity of the anode recirculation gas can be obtained in other ways known to those skilled in the art. A controller 48 receives the various sensor measurements discussed herein, including a voltage measurement from the sensor assembly 28, pressure measurements from the pressure sensors 22 and 44, the temperature measurement from the temperature sensor 30 and the relative humidity measurement from the RH sensor 46, and calculates the concentration of hydrogen gas in the recirculation line 38 consistent with the discussion below.
The sensor array 54 is positioned between the flow paths 50 and 52 so that the catalyst layers 64 in all of the sensors 56 are exposed to the hydrogen flow through the flow path 50 and the catalyst layers 66 in all of the sensors 56 are exposed to the anode recirculation gas in the flow path 52. In this manner, one side of all of the sensors 56 is exposed to one of the flows and the other side of all of the sensors 56 is exposed to the other flow. The sensors 56 operate as hydrogen-hydrogen concentration cells where the cell potential of the cell is determined by the partial pressure of hydrogen on either side of the membrane. Particularly, the catalyst layers 64 and 66 electro-chemically react within the hydrogen gas in the flows so that a voltage potential is provided between the catalyst layer 64 and 66.
Because the concentration of the hydrogen gas flowing through the flow path 50 including the fresh hydrogen is greater than the concentration of the hydrogen gas flowing through the flow path 52 including the recirculation gas, the voltage for electro-chemical reaction will be greater on the fresh hydrogen side of the sensors 56 depending on the pressure. The voltage potential V is the voltage difference between the catalyst layers 64 and 66 that is used to determine the concentration of the hydrogen gas in the anode recirculation gas. Because the gas from the hydrogen source 36 is nearly pure hydrogen, the pressure sensor 22 provides a measurement of the hydrogen gas in the flow path 50. Using the measured voltage potential V, the pressure of the hydrogen gas in the flow path 50 and the known Nernst equation, shown as equation (1) below, the partial pressure of the hydrogen gas in the recirculation line 38 flowing through the flow path 52 can be determined. By knowing the hydrogen partial pressure in the recirculation line 38, the hydrogen gas concentration can be determined.
Where R is the universal gas constant 8.314 J/molK, z is electron exchange and is 2 in this calculation, F is Faraday's constant of 96485 C/mol, T is the temperature of the anode recirculation gas in K, AnPH, is the fresh hydrogen gas pressure and CaPH, is the hydrogen partial pressure in the recirculation gas with units of kPa. In this representation, the recirculation gas side of the sensor assembly 28 is referred to as the cathode (Ca) side because it has a lower hydrogen partial pressure.
The Nernst equation defines about a 35 V of cell voltage per decade of hydrogen partial pressure difference. To exaggerate this voltage difference, multiple sensors are employed as discussed that are connected in series resulting in an amplified voltage difference, where in one non-limiting embodiment, each sensor 56 has an active area less than a centimeter squared. Multiple sensors can also be placed in a parallel array to increase the robustness and reliability of the sensor against various disturbances from the system including, but not limited to, liquid water droplets.
Rearranging equation (1) allows the hydrogen partial pressure in the recirculation gas CaPH
The hydrogen concentration H2Conc in the recirculation gas can then be calculated as:
Where RH is the relative humidity of the recirculation gas, P is the total pressure of the recirculation gas and Psat is the saturation pressure of the recirculation gas calculated as:
P
sat=(1.45E−4·T3)−(6.11E−3·T2)+(1.60E−1·T)+(6.00E−1) (4)
At a relative humidity between 20% and 100% and temperatures between 30° C. and 80 C.° in the anode sub-system, there exists at least a 100 mV signal with respect to a 20% drop in the hydrogen gas concentration, which is easily recognized by software and usable as a trigger for an anode bleed as well as hydrogen concentration when the system is in park.
The foregoing discussion discloses and describes merely exemplary embodiments of the present invention. One skilled in the art will readily recognize from such discussion and from the accompanying drawings and claims that various changes, modifications and variations can be made therein without departing from the spirit and scope of the invention as defined in the following claims.
