CN114024009A - Fuel cell power generation system - Google Patents
Fuel cell power generation system Download PDFInfo
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- CN114024009A CN114024009A CN202111193376.5A CN202111193376A CN114024009A CN 114024009 A CN114024009 A CN 114024009A CN 202111193376 A CN202111193376 A CN 202111193376A CN 114024009 A CN114024009 A CN 114024009A
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- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
- H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
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- H—ELECTRICITY
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- 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
- H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
- H01M8/04022—Heating by combustion
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- 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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- 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
- H01M8/04201—Reactant storage and supply, e.g. means for feeding, pipes
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- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04305—Modeling, demonstration models of fuel cells, e.g. for training purposes
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- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
- H01M8/0438—Pressure; Ambient pressure; Flow
- H01M8/04395—Pressure; Ambient pressure; Flow of cathode reactants at the inlet or inside the fuel cell
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- H—ELECTRICITY
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- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
- H01M8/04746—Pressure; Flow
- H01M8/04753—Pressure; Flow of fuel cell reactants
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
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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
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Abstract
A fuel cell power generation system includes a fuel cell stack, an anode circulation circuit, a combustor, and a cathode gas supply unit. The fuel cell stack includes an anode and a cathode. The anode recycle loop includes a fuel reformer and a recycler coupled between the fuel reformer and the anode to form an anode recycle loop. The combustor is connected with the fuel cell stack and used for combusting tail gas generated by the fuel cell stack to generate heat energy. The cathode gas supply unit is connected to the cathode and the burner, respectively, so that the cathode gas supply unit supplies the heated gas to the cathode. In the fuel cell power generation system provided by the embodiment of the application, the unreacted fuel in the anode can be circulated and returned to the fuel reformer through the anode circulation loop to realize the utilization rate of the supplied fuel, and the steam with heat can be introduced into the fuel reformer to participate in the reaction, so that the structure of the power generation system is simplified and the net efficiency of the system is improved.
Description
Technical Field
The application relates to the technical field of fuel cell power generation, in particular to a fuel cell power generation system.
Background
A fuel cell is a power generation device that directly converts chemical energy of a fuel into electric energy, and generally includes an electrolyte, an anode, a cathode, and a connector or bipolar plate, wherein the anode side is continuously fed with a fuel (such as hydrogen, carbon monoxide, methane, etc.), the fuel is adsorbed by the surface of the anode having a catalytic function, and diffuses the fuel to the interface between the anode and the electrolyte through the porous structure of the anode, the cathode side is continuously fed with an oxidant (such as air), the oxidant is also adsorbed by the surface of the cathode having a porous structure, so that the oxidant obtains electrons, the oxidant obtaining electrons reaches the interface between the electrolyte and the anode due to diffusion caused by a concentration gradient, reacts with the fuel, and the lost electrons return to the cathode through an external circuit, thereby forming an electric current.
However, the fuel in the anode contains a large amount of heat and, at the same time, a large amount of insufficiently reacted fuel, and direct combustion causes fuel and heat losses.
Disclosure of Invention
The present application provides a fuel cell power generation system that can efficiently utilize the fuel and heat that is not fully reacted in the anode to provide a net system efficiency of the power generation system.
An embodiment of the present application provides a fuel cell power generation system, including:
a fuel cell stack comprising an anode and a cathode;
an anode circulation loop, which comprises a fuel reformer and a circulation device, wherein the circulation device is connected between the fuel reformer and an anode to form an anode circulation loop, and the circulation device can convey tail gas containing fuel and water vapor in the anode into the fuel reformer, wherein the water vapor in the anode tail gas is conveyed into the fuel reformer to participate in reforming reaction, and the fuel in the anode tail gas is mixed with gas generated in the fuel reformer and then conveyed into the anode;
the combustor is connected with the fuel cell stack and used for combusting tail gas generated by the fuel cell stack to generate heat energy;
and a cathode gas supply unit connected to the cathode and the burner, respectively, such that the cathode gas supply unit supplies the heated gas to the cathode.
In the fuel cell power generation system provided by the embodiment of the application, the unreacted fuel in the anode can be circulated and returned to the fuel reformer through the anode circulation loop to realize the utilization rate of the supplied fuel, and the steam with heat can be introduced into the fuel reformer to participate in the reaction, so that the structure of the power generation system is simplified and the net efficiency of the system is improved.
In some embodiments of the present application, a gas supply unit is further included, the gas supply unit being connected to the fuel reformer.
In some embodiments of the present application, the burner is in heat exchange connection with the air supply unit such that the air supply unit provides heated gas to the fuel reformer.
In some embodiments of the present application, the gas supply unit includes a first gas flow meter and a first heat exchanger, the gas flow meter being connected between the first heat exchanger and the fuel reformer.
In some embodiments of the present application, the cathode gas supply unit includes a blower, a second heat exchanger connected to the blower, and a second gas flow meter connected to the second heat exchanger, the second heat exchanger being further connected to the cathode and the burner, respectively.
In some embodiments of the present application, further comprising:
a flow pump having a pump inlet and a pump outlet for conveying a hydrocarbon-containing feedstock;
and the preheater is respectively connected with the pump outlet and the fuel reformer and is used for providing heated raw materials for the fuel reformer.
In some embodiments of the present application, further comprising:
and the modeling simulation unit is used for calculating the system net efficiency of the fuel cell power generation system according to the oxygen-carbon ratio in the fuel reformer and the circulation ratio in the circulating device. The net system efficiency of the fuel cell power generation system can be obtained in real time through the modeling simulation unit, and the oxygen-carbon ratio and the circulation ratio are adjusted in time to improve the net system efficiency.
In some embodiments of the present application, further comprising:
and the control unit is respectively connected with the circulating device and the flow pump and is used for controlling the opening degrees of the circulating device and the flow pump.
In some embodiments of the present application, the fuel cell stack is a high temperature fuel cell stack. The high-temperature fuel cell has the advantages of simplified hydrothermal management system, strong catalyst poison resistance, high reaction kinetics speed, wide fuel selection range and the like.
In some embodiments of the present application, the high temperature fuel cell stack is a solid oxide fuel cell stack. The solid oxide fuel cell has excellent performances of high efficiency, no pollution, all-solid structure, wide adaptability to various fuel gases and the like, so that the solid oxide fuel cell is widely applied.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present application and together with the description, serve to explain the principles of the application.
FIG. 1 is a schematic diagram of a fuel cell power generation system according to some embodiments of the present application;
FIG. 2 is a graph of stack fuel utilization versus net system efficiency, stack efficiency, and tail gas exhaust temperature for a fuel cell power generation system according to some embodiments of the present disclosure;
FIG. 3 is a graph of air preheat temperature versus net system efficiency, stack efficiency, and exhaust stack temperature for a fuel cell power generation system according to some embodiments of the present disclosure;
FIG. 4 is a graph of stack air utilization versus net system efficiency, stack efficiency, and tail gas exhaust temperature for a fuel cell power generation system according to some embodiments of the present disclosure;
FIG. 5 is a graph of the oxygen to carbon ratio versus the net system efficiency, stack efficiency, and tail gas exit temperature for a fuel cell power generation system according to some embodiments of the present disclosure;
FIG. 6 is a graph of cycle ratio versus net system efficiency, stack efficiency, and exhaust stack temperature for a fuel cell power generation system according to some embodiments of the present application;
fig. 7 is a bar graph of reforming efficiency, stack efficiency and net system efficiency for a fuel cell power generation system of example 1 of the present application versus a power generation system of comparative example 1.
Description of reference numerals:
10-a fuel cell power generation system;
11-a combustion cell stack;
12-an anode recycle loop;
121-a fuel reformer;
122-a circulation device;
123-a first heat exchanger;
13-a burner;
14-a cathode gas supply unit;
15-a flow pump;
16-a preheater;
17-a blower;
18-a draught fan;
19-a heat sink;
20-heat dissipation fan.
With the above figures, there are shown specific embodiments of the present application, which will be described in more detail below. These drawings and written description are not intended to limit the scope of the inventive concepts in any manner, but rather to illustrate the inventive concepts to those skilled in the art by reference to specific embodiments.
Detailed Description
The embodiments or implementation schemes are described in a progressive mode in the specification, each embodiment focuses on differences from other embodiments, and the same parts and the similar parts among the embodiments are referred to each other.
In the description herein, references to the description of the terms "one embodiment," "some embodiments," "an illustrative embodiment," "an example," "a specific example," or "some examples" or the like mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present application. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present application, "plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
The fuel cell comprises an electrolyte, an anode, a cathode and a connector or bipolar plate, wherein fuel (such as hydrogen, carbon monoxide, methane and the like) is continuously introduced into one side of the anode, the fuel is adsorbed by the surface of the anode with catalytic action, the fuel is diffused to the interface of the anode and the electrolyte through the porous structure of the anode, oxidant (such as air) is continuously introduced into one side of the cathode, the oxidant is also adsorbed by the surface of the cathode with the porous structure, electrons are obtained, the oxidant for obtaining the electrons reaches the interface of the electrolyte and the anode due to diffusion caused by concentration gradient and reacts with the fuel, and the lost electrons return to an air electrode through an external circuit to form current. However, the fuel in the anode contains a large amount of heat and, at the same time, a large amount of insufficiently reacted fuel, and direct combustion causes fuel and heat losses.
In order to solve the above technical problems, embodiments of the present application provide a fuel cell power generation system, which not only can recycle unreacted fuel in an anode back to a fuel reformer through an anode recycle loop to achieve a utilization rate of supplied fuel, but also can introduce steam with heat into the fuel reformer to participate in a reaction to simplify a structure of the power generation system and improve a net efficiency of the system.
Referring to fig. 1, a fuel cell power generation system 10 according to an embodiment of the present application includes a fuel cell stack 11, an anode circulation circuit 12, a combustor 13, and a cathode gas supply unit 14. The fuel cell stack 11 includes an anode and a cathode, a fuel and an oxidant are respectively introduced from the anode and the cathode of the fuel cell stack, the fuel emits electrons on the anode, the electrons are conducted to the cathode through an external circuit and combined with the oxidant to generate ions, and the ions migrate to the anode through an electrolyte under the action of an electric field to react with the fuel to form a loop to generate current, thereby realizing power generation. The anode circulation circuit 12 includes a fuel reformer 121 and a circulation device 122, the circulation device 122 is connected between the fuel reformer 121 and the anode to form the anode circulation circuit 12, the circulation device 122 is capable of transporting a tail gas containing the fuel in the anode into the fuel reformer 121, and the fuel in the anode tail gas is transported into the anode after being mixed with the gas generated in the fuel reformer 121. The combustor 13 is connected to the fuel cell stack 11 for combusting the off-gas generated by the fuel cell stack 11 to generate heat energy. The cathode gas supply unit 14 is connected to the cathode and the burner 13, respectively, so that the cathode gas supply unit 14 supplies the heated gas to the cathode.
In the embodiment provided by the present application, the anode off-gas in the fuel cell stack 11 contains a large amount of fuel which is not fully reacted and a large amount of heat, and the circulation device 122 can deliver part of the combustion which is not fully reacted and the heat and steam carried by the combustion into the fuel reformer 121, so that not only the temperature of the reaction in the fuel reformer 121 can be maintained, but also the water can be returned to the fuel reformer 121 in the form of steam without using a condenser, a water pump or the like, thereby reducing the manufacturing cost of the power generation system and simplifying the structure of the power generation system. In addition, another part of the insufficiently combusted fuel in the anode tail gas flows into the combustor 13 to be combusted to generate heat to heat the air required by the fuel reformer 121 and the fuel cell stack 11, so that the heat of the fuel in the tail gas is fully utilized to simplify a heat management system in the power generation system, and the structure of the power generation system is further simplified.
In summary, the circulation device 122 in the anode circulation loop 12 delivers part of the unreacted fuel, the carried heat and the water vapor in the anode tail gas to the fuel reformer 121, which not only can improve the output rate of the fuel, but also can mix the generated fuel with part of the fuel in the anode tail gas and then feed the mixed fuel into the anode again for reaction, so that the fuel utilization rate of the stack is greatly improved.
Referring to fig. 2, both the net system efficiency and the stack efficiency increase with increasing stack fuel utilization. Under the condition of keeping the fuel flow at the inlet of the system unchanged, the fuel utilization rate of the electric pile is improved, which means that the output power of the electric pile is increased, so that the net efficiency of the system and the efficiency of the electric pile are both increased. Along with the promotion of galvanic pile fuel utilization ratio, tail gas temperature reduces, this is because after galvanic pile fuel utilization ratio promotes, the gaseous partial pressure of fuel of galvanic pile export reduces for among the non-circulating anode tail gas, gaseous fuel reduces, therefore the fuel of burning significantly reduces, and the tail gas temperature reduces greatly. This also indicates that the energy carried in the anode tail gas is greatly reduced, which can promote an increase in the net efficiency of the system. The calculation formulas of reforming efficiency, galvanic pile efficiency and system net efficiency are shown as formulas (1), (2) and (3).
1) Reforming efficiency: the ratio of the lower heating value of the fuel entering the anode of the stack to the system fuel;
wherein eta isATRRepresents reforming efficiency in%; m isH2Represents the mass flow of hydrogen in the anode fuel in kg/s, LHVH2Represents the lower calorific value of hydrogen, and the unit is kJ/kg; m isCH4Represents the mass flow rate of methane in the anode fuel in kg/s, LHVCH4The lower calorific value of methane is expressed in kJ/kg; m isCORepresents the mass flow of carbon monoxide in the anode fuel in kg/s, LHVCORepresents the lower calorific value of carbon monoxide in kJ/kg; m isfuelRepresents the mass flow of the fuel of the system with the unit of kg/s and LHVfuelRepresenting the lower heating value of the system fuel, with the unit of kJ/kg.
2) The efficiency of the galvanic pile: the ratio of the output electric energy of the electric pile to the low heating value of the fuel gas entering the anode of the electric pile;
wherein eta isSOFCRepresents the stack efficiency in%; welecThe unit of electric power output by the electric pile is kW; m isH2Represents the mass flow of hydrogen in the anode fuel in kg/s, LHVH2Represents the lower calorific value of hydrogen, and the unit is kJ/kg; m isCH4Represents the mass flow rate of methane in the anode fuel in kg/s, LHVCH4The lower calorific value of methane is expressed in kJ/kg; m isCORepresents the mass flow of carbon monoxide in the anode fuel in kg/s, LHVCORepresents the lower calorific value of carbon monoxide in kJ/kg;
3) net efficiency η of the systemsystem: net electric power W output by the systemelec，netThe net electric power of the system is the net output power of the total power of the electric pile minus the parasitic power and the DC/DC conversion loss power, and the loss of the parasitic power and the loss of the DC/DC conversion loss power is converted into loss factors, wherein the loss factors of the parasitic power and the DC/DC are eta respectivelyparasitic89% and ηdc/dc92 percent; the parasitic power includes losses of a parasitic resistance in addition to losses of a flow pump and the like.
ηparasiticηdc/dc≈82％
It should be noted that the raw material of the fuel cell power generation system 10 in the embodiment of the present application may be fossil energy, such as natural gas, gasoline or diesel oil, methanol, etc., or a mixed raw material of natural gas, gasoline, diesel oil, etc., which is well known to those skilled in the art. In the example provided herein, the feedstock used by the fuel cell power generation system 10 is diesel fuel.
In some embodiments of the present application, the fuel cell power generation system 10 further includes a gas supply unit connected to the fuel reformer 121 to supply the reaction gas to the fuel reformer 121.
Further, in some embodiments of the present application, the burner 13 is in heat exchange connection with the air supply unit such that the air supply unit provides the heated gas to the fuel reformer 121. Specifically, the off-gas in the fuel cell stack 11 flows into the combustor 13 to be combusted, the heat generated during the combustion flows into the gas supply unit to heat the reaction gas therein, and the heated reaction gas has a certain temperature and is delivered to the fuel reformer 121 to react with the hydrocarbon, so that the reaction rate in the fuel reformer 121 can be increased.
In some embodiments of the present application, the gas supply unit may include a gas flow meter and the first heat exchanger 123, wherein the gas flow meter is connected between the first heat exchanger 123 and the fuel reformer 121 to control the flow rate of the heating gas into the fuel reformer 121 to adjust the oxygen-to-carbon ratio, further improving the system net efficiency of the power generation system.
In some embodiments of the present application, the cathode gas supply unit 14 includes a second heat exchanger, which is respectively connected to the cathode and the burner 13 to heat the cathode gas in the second heat exchanger by the heat energy generated in the burner 13, and the heated cathode gas is delivered to the cathode for reaction.
Referring to fig. 3, as the preheat temperature of the air entering the fuel reformer 121 increases, both the net system efficiency and the stack efficiency increase linearly. Firstly, the temperature of air entering reforming is increased due to the increase of the air preheating temperature, so that the hydrogen yield is increased, and the output power of a galvanic pile is increased; second, as the air temperature of the fuel cell stack increases, the energy lost by the fuel reformer 121 and the fuel cell stack for thermal insulation decreases, and thus both the net system efficiency and the stack efficiency increase. And the temperature of the off-gas of the fuel cell stack decreases as the preheating temperature of the air increases because the energy of the preheated air is recovered from the off-gas.
In some embodiments of the present application, the fuel cell power generation system further includes a blower 17 connected to the air inlets of the first heat exchanger 123 and the second heat exchanger, respectively, to rapidly input air into both.
Referring to fig. 4, stack efficiency and net system efficiency increase as stack air utilization increases. First, an increase in the stack air utilization rate can be understood as a decrease in the amount of air entering the fuel cell power generation system 10, and therefore the power required by the blower decreases and the power consumed decreases. Secondly, air is preheated to 700 ℃ and enters the fuel cell stack, and the fuel cell stack works at 850 ℃, and the increase of the air utilization rate of the stack can be understood as that the air quantity for cooling the stack is reduced, and the stack can keep higher temperature without losing more output energy for heat preservation. The exhaust temperature of the fuel cell power generation system 10 decreases with an increase in the air utilization rate because most of the exhaust gas is the unused air, the fuel utilization rate increases, the unused air decreases, the mass flow rate of the exhaust gas decreases accordingly, and the temperature decrease range is large after heat exchange.
In some embodiments of the present application, the fuel cell power generation system further comprises a flow pump 15 and a preheater 16, the flow pump 15 having a pump inlet and a pump outlet for transporting the hydrocarbon containing feedstock. The preheater 16 is connected to the pump outlet and the fuel reformer 121, respectively, for providing heated feedstock to the fuel reformer.
In some embodiments of the present application, a modeling simulation unit is further included for calculating a system net efficiency of the fuel cell power generation system based on the oxygen to carbon ratio in the fuel reformer 121 and/or the recycle ratio in the recycle device 122. The net system efficiency of the fuel cell power generation system can be obtained in real time through the modeling simulation unit, and the oxygen-carbon ratio and the circulation ratio are adjusted in time to improve the net system efficiency. The oxygen-carbon ratio herein refers to the ratio of the amount of oxygen molecules to the total amount of carbon contained in the carbon-containing compound in the fuel reformer, and the recycle ratio refers to the mass ratio of the tail gas recovered in the recycle device to the anode tail gas.
In some embodiments of the present application, the modeling simulation unit performs simulation calculations using ASPEN PLUS software.
Referring to fig. 5, as the oxygen to carbon ratio increases, the net efficiency of the system increases and the stack efficiency is nearly constant. This is primarily due to the increased oxygen, increased ratio of partial oxidation to total oxidation within the fuel reformer 121, and more heat released to support downstream steam reforming, resulting in increased hydrogen yield, increased reforming efficiency, and, therefore, increased system net efficiency. In addition, as the oxygen-to-carbon ratio increases, the temperature of the exhaust gas increases, mainly due to the increased oxidation reaction rate, and more CO is generated2And H2O, and the heat capacities of these two are large, thus resulting in an increase in the exhaust gas temperature, but the exhaust gas temperature is still at a low level.
In some embodiments of the present application, controlling the oxygen to carbon ratio within the fuel reformer 11 in the range of 0.05 to 0.2 may be beneficial in improving the net efficiency of the system.
Referring to fig. 6, as the cycle ratio increases, the stack efficiency increases. This is because the increase of the circulation ratio recovers fuel and heat in the anode off-gas, so that the output power of the stack increases, and the loss holding power decreases, thereby increasing the stack efficiency. However, when the recycle ratio exceeds 0.68, the stack efficiency decreases with the increase of the recycle ratio because the recovered anode off-gas contains a large amount of CO2The increase in fuel flow is not significant despite the increase in recycle ratio, and CO2Obviously increased, thereby causing the partial pressure of the fuel gas at the inlet of the galvanic pile to be reduced, and CO2The partial pressure is increased, so that the output power of the electric pile is reduced, and the performance of the whole electric pile is reduced. At this point, the net efficiency of the system increases slowly and then decays slowly as the recycle ratio increases. The net efficiency of the system increases primarily because of the increased fuel that increases the stack efficiency. However, when the recycle ratio exceeds 0.68, the net efficiency of the system does not significantly decrease as the efficiency of the stack decreases, primarily because the recycle ratio increasesLarge, the reason for the increased reforming efficiency.
In some embodiments of the present application, the circulation ratio in the circulation device 122 is in the range of 0.65-0.75, which can ensure that the net system efficiency of the power generation system is above 47%.
In some embodiments of the present application, the flow pump 15 controls the flow rate of the raw material to be 0.63kg/h, the gas flow meter controls the flow rate of the air to be 0.77kg/h, and the circulation ratio in the circulation device 122 is 0.69, at which time, the net system efficiency of the power generation system provided by the present application can reach about 48%.
In some embodiments of the present application, the fuel cell power generation system further includes a control unit connected to the circulation device 122 and the flow pump 15, respectively, for controlling the opening degrees of the circulation device 122 and the flow pump 15.
In the embodiments provided herein, the circulation device 122 can regulate the flow of fuel in the anode circulation loop 12 into the fuel reformer 121 to further improve the system net efficiency of the power generation system.
In some embodiments of the present application, the circulation device 122 may be a fan or a pump. When diesel oil is used as the raw material, the reaction temperature of the diesel oil in the fuel reformer 121 is high, and the temperature of the fuel that is not sufficiently reacted in the anode is also about 800 ℃, so that the circulating device 122 needs to use a high-temperature-resistant pump or fan.
In some embodiments of the present application, the fuel cell stack is a high temperature fuel cell stack. The high-temperature fuel cell has the advantages of simplified hydrothermal management system, strong catalyst poison resistance, high reaction kinetics speed, wide fuel selection range and the like.
In some embodiments of the present application, the high temperature fuel cell stack is a solid oxide fuel cell stack. The solid oxide fuel cell has excellent performances of high efficiency, no pollution, all-solid structure, wide adaptability to various fuel gases and the like, so that the solid oxide fuel cell is widely applied.
In some embodiments of the present application, the burner 13 is also connected to the tail gas port of the cathode, so as to further utilize the heat of the tail gas of the cathode.
In some embodiments of the present application, the fuel cell power generation system further includes an induced draft fan 18, and the induced draft fan 18 is connected to the air outlet of the first heat exchanger 123 and the air outlet of the second heat exchanger, respectively, so as to rapidly discharge the excess air.
Further, in some embodiments of the present application, a radiator 19 is installed between the induced draft fan 18 and the first heat exchanger 123 and the second heat exchanger. Furthermore, the radiator 19 is also connected with a radiator fan, so as to further accelerate the reduction rate of the temperature of the tail gas.
Example 1
Boosting the pressure of diesel oil to 200kPa by a pump, exchanging heat with anode tail gas, vaporizing and entering a fuel reformer; the air entering the fuel cell power generation system is divided into two parts after being compressed to 120kPa, one part is used for reforming reaction in the fuel reformer, the other part is used in the electric pile and the combustor, and the air is heated to 700 ℃ through the heat exchanger before entering the fuel reformer, the electric pile and the combustor. The feed material reacts in the fuel reformer to produce reformate, which enters the stack anode. The reacted anode tail gas is divided into two parts by a separator, one part directly enters a combustor, and the other part returns to a fuel reformer after passing through a circulating device. One part of the heated air directly enters the electric reactor for reaction, the other part of the heated air directly enters the combustor through the separator to be used as an oxidant, and the combusted tail gas is discharged after three-stage heat exchange.
Comparative example 1
Boosting the pressure of diesel oil to 200kPa by a pump, exchanging heat with anode tail gas, vaporizing and entering a fuel reformer; the air entering the system is compressed to 120kPa and then divided into two parts, one part is used for reforming, the other part is used for the electric pile and the combustor, and the air is heated to 700 ℃ by combustion tail gas before entering the reactor; the water enters the reformer after the heat exchange of the combustion tail gas reaches 300 ℃. The feed material reacts in the reformer to produce reformate, which enters the stack anode. One part of the heated air directly enters the electric reactor for reaction, the other part of the heated air directly enters the combustor through the separator to be used as an oxidant, and the combusted tail gas is discharged after three-stage heat exchange.
Referring to fig. 7, the reforming efficiency, stack efficiency and net system efficiency of the fuel cell power generation system in example 1 are significantly superior to those of comparative example 1.
Finally, it should be noted that: the above embodiments are only used for illustrating the technical solutions of the present application, and not for limiting the same; although the present application has been described in detail with reference to the foregoing embodiments, it should be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present application.
Claims (10)
1. A fuel cell power generation system characterized by comprising:
a fuel cell stack comprising an anode and a cathode;
an anode circulation loop comprising a fuel reformer and a circulation device connected between the fuel reformer and the anode to form the anode circulation loop, wherein the circulation device is capable of delivering a tail gas containing fuel and water vapor in the anode into the fuel reformer, wherein the water vapor in the anode tail gas is delivered into the fuel reformer to participate in a reforming reaction, and the fuel in the anode tail gas is mixed with the gas generated in the fuel reformer and then delivered into the anode;
the combustor is connected with the fuel cell stack and is used for combusting tail gas generated by the fuel cell stack to generate heat energy;
and a cathode gas supply unit connected to the cathode and the burner, respectively, such that the cathode gas supply unit supplies the heated gas to the cathode.
2. The fuel cell power generation system according to claim 1, further comprising an air supply unit connected to the fuel reformer.
3. A fuel cell power generation system according to claim 2, wherein the burner is in heat exchange connection with the air supply unit such that the air supply unit provides heated gas to the fuel reformer.
4. The fuel cell power generation system according to claim 3, wherein the gas supply unit includes a first gas flow meter and a first heat exchanger, the gas flow meter being connected between the first heat exchanger and the fuel reformer.
5. The fuel cell power generation system according to claim 1, wherein the cathode gas supply unit includes a blower, a second heat exchanger connected to the blower, and a second gas flow meter connected to the second heat exchanger, the second heat exchangers being further connected to the cathode and the combustor, respectively.
6. The fuel cell power generation system according to claim 1, further comprising:
a flow pump having a pump inlet and a pump outlet for conveying a hydrocarbon-containing feedstock;
a preheater respectively connected with the pump outlet and the fuel reformer for providing the heated raw material to the fuel reformer.
7. The fuel cell power generation system according to claim 6, further comprising:
and the modeling simulation unit is used for calculating the system net efficiency of the fuel cell power generation system according to the oxygen-carbon ratio in the fuel reformer and/or the circulation ratio in the circulating device.
8. The fuel cell power generation system according to claim 7, characterized by further comprising:
and the control unit is respectively connected with the circulating device and the flow pump and is used for controlling the opening degrees of the circulating device and the flow pump.
9. The fuel cell power generation system of claim 1, wherein the fuel cell stack is a high temperature fuel cell stack.
10. The fuel cell power generation system according to claim 9, wherein the high-temperature fuel cell stack is a solid oxide fuel cell stack.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114665120A (en) * | 2022-03-10 | 2022-06-24 | 南京航空航天大学 | SOFC-GT hybrid power generation system based on multi-type fuel |
| CN115939470A (en) * | 2023-03-02 | 2023-04-07 | 哈尔滨工业大学(深圳)(哈尔滨工业大学深圳科技创新研究院) | Anode tail gas double-reflux solid oxide fuel cell system and operation method thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080292922A1 (en) * | 2007-05-22 | 2008-11-27 | Fischer Bernhard A | Method and apparatus for fueling a solid oxide fuel cell stack assembly |
| CN104124462A (en) * | 2013-04-25 | 2014-10-29 | 中国科学院宁波材料技术与工程研究所 | Solid oxide fuel cell system for recycling of electric pile anode tail gas |
| CN105594045A (en) * | 2013-07-09 | 2016-05-18 | 塞瑞斯知识产权有限公司 | Improved fuel cell systems and methods |
| CN109686998A (en) * | 2019-02-18 | 2019-04-26 | 广东索特能源科技有限公司 | Association circulating power generation system based on the cooling fuel cell of gas turbine |
| CN111952642A (en) * | 2020-08-21 | 2020-11-17 | 清华大学 | High-efficiency low-vibration noise fuel cell power generation system |
| CN112290055A (en) * | 2020-10-28 | 2021-01-29 | 中国科学技术大学 | Self-humidifying anode fuel circulation system and method of fuel cell system |
-
2021
- 2021-10-13 CN CN202111193376.5A patent/CN114024009A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080292922A1 (en) * | 2007-05-22 | 2008-11-27 | Fischer Bernhard A | Method and apparatus for fueling a solid oxide fuel cell stack assembly |
| CN104124462A (en) * | 2013-04-25 | 2014-10-29 | 中国科学院宁波材料技术与工程研究所 | Solid oxide fuel cell system for recycling of electric pile anode tail gas |
| CN105594045A (en) * | 2013-07-09 | 2016-05-18 | 塞瑞斯知识产权有限公司 | Improved fuel cell systems and methods |
| CN109686998A (en) * | 2019-02-18 | 2019-04-26 | 广东索特能源科技有限公司 | Association circulating power generation system based on the cooling fuel cell of gas turbine |
| CN111952642A (en) * | 2020-08-21 | 2020-11-17 | 清华大学 | High-efficiency low-vibration noise fuel cell power generation system |
| CN112290055A (en) * | 2020-10-28 | 2021-01-29 | 中国科学技术大学 | Self-humidifying anode fuel circulation system and method of fuel cell system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114665120A (en) * | 2022-03-10 | 2022-06-24 | 南京航空航天大学 | SOFC-GT hybrid power generation system based on multi-type fuel |
| CN114665120B (en) * | 2022-03-10 | 2024-01-30 | 南京航空航天大学 | SOFC-GT hybrid power generation system based on multi-type fuel |
| CN115939470A (en) * | 2023-03-02 | 2023-04-07 | 哈尔滨工业大学(深圳)(哈尔滨工业大学深圳科技创新研究院) | Anode tail gas double-reflux solid oxide fuel cell system and operation method thereof |
| CN115939470B (en) * | 2023-03-02 | 2023-06-13 | 哈尔滨工业大学(深圳)(哈尔滨工业大学深圳科技创新研究院) | Anode tail gas double-reflux solid oxide fuel cell system and operation method thereof |
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