CN114566675A - Medium-temperature solid oxide fuel cell thermal management system and method - Google Patents
Medium-temperature solid oxide fuel cell thermal management system and method Download PDFInfo
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—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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- 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
The invention provides a thermal management system and a method for an intermediate-temperature solid oxide fuel cell, which adopts a connection structure among a first control valve, a second control valve, a pre-burner, a first mixing valve, an oxidation reforming system and a post-burner; the gas pipeline of the POX can be switched from cathode waste gas to tail gas of the post combustor through the arranged post combustor, so that the transition problem of heat dissipation to heat supply of the POX is solved; by the aid of the arranged first control valve, a small part of natural gas is directly introduced into the post-combustor as supplementary fuel, so that fresh fuel and air entering the POX are not preheated any more, and energy supply of reforming reaction under a high AOGR rate is guaranteed; under the above measures, in order to realize the stable operation of the system at the time of low AOGR rate so as to complete the switching of the AOGR rate from low to high, a pre-burner is arranged so as to maintain the minimum temperature required by the POX fuel inlet.
Description
Technical Field
The invention belongs to the technical field of battery heat pipes, and particularly relates to a thermal management system and method for an intermediate-temperature solid oxide fuel cell.
Background
At present, Solid Oxide Fuel Cells (SOFC) are mainly applied to a fixed power generation module, and the application of the SOFC to a vehicle-mounted or portable mobile power supply is still limited by two factors, namely the characteristics of a pile and a peripheral system; wherein, aiming at the restriction problem of peripheral system factors, the problem can be solved only by the continuous optimization of a heat management system (BOP); one feasible way is to use Partial Oxidation Reforming (POX) instead of Steam Reforming (Steam Reforming, SR) to form a POX-aogr (anode off Gas recycle) system, thereby eliminating complex Steam generation and superheating devices and simplifying the structure of the thermal management system; however, the lower hydrogen yield of oxidative reforming relative to steam reforming results in a reduction in system electrical efficiency, and therefore a large proportion of anode exhaust gas cycles (AOGR) need to be coupled to mitigate this effect.
The inventor finds that the application of the POX-AOGR system has the following problems that along with the increase of the circulation rate of anode waste gas, the reforming reaction in the POX is gradually transited from heat release to heat absorption, and the prior BOP system cannot well realize the transition from heat release to heat supply of the POX; along with the improvement of the circulation rate of anode waste gas, the anode waste gas flowing into the post combustor is reduced, the temperature of tail gas of the post combustor is reduced, and sufficient heat cannot be provided for reforming reaction; measures for reducing the inlet temperature of the POX fuel, such as not preheating fresh air and fuel entering the POX, are beneficial to expanding the operation range of the SOFC system under the high AOGR rate and improving the system efficiency, but such measures can cause the POX inlet temperature to be too low under the low AOGR rate and even lead the reforming reaction to be gradually extinguished.
Disclosure of Invention
The invention provides a heat management system and a method for a medium-temperature solid oxide fuel cell, aiming at solving the transition problem of POX from heat dissipation to heat supply, a gas pipeline of the POX is switched from cathode waste gas to tail gas of a post-combustor; in order to ensure the energy supply of the reforming reaction under the high AOGR rate, a small part of natural gas is directly introduced into a post-combustor as a supplementary fuel, and fresh fuel and air entering POX are not preheated any more; under the measures, in order to realize the stable operation of the system when the AOGR rate is low so as to complete the switching of the AOGR rate from low to high, the pre-burner is arranged to maintain the minimum temperature of 400 ℃ required by the POX fuel inlet.
In order to achieve the above object, in a first aspect, the present invention provides an intermediate-temperature solid oxide fuel cell thermal management system, which adopts the following technical solutions:
an intermediate-temperature solid oxide fuel cell thermal management system comprises a first control valve, a second control valve, a pre-burner, a first mixing valve, an oxidation reforming system and a post-burner;
the first control valve comprises two outlets which are respectively communicated with a first inlet of the after burner and an inlet of the second control valve; the first control valve is configured to deliver at least a portion of the received natural gas to the post combustor;
the second control valve comprises two outlets which are respectively communicated with the natural gas inlet of the precombustor and the first inlet of the first mixing valve; the second control valve is configured to deliver at least a portion of the provided natural gas received in the first control valve to the preburner and another portion of the natural gas to the first mixing valve; the pre-burner is configured to burn natural gas for heating;
the first mixing valve further comprises a second inlet, and the outlet of the pre-burner is communicated with the second inlet of the first mixing valve; the outlet of the first mixing valve is communicated with the first inlet of the oxidation reforming system; the first mixing valve is configured to mix natural gas from the second control valve with the heated fluid from the pre-burner and input the mixed gas to the oxidative reforming system;
the afterburner further comprises a second inlet and a third inlet; the second inlet of the post-combustor is configured to receive anode exhaust gas of the intermediate-temperature solid oxide fuel cell to be managed, and the third inlet of the post-combustor is configured to receive cathode exhaust gas of the intermediate-temperature solid oxide fuel cell to be managed;
the oxidation reforming system also comprises a second inlet and a third inlet which are respectively communicated with the outlet of the after-burner and the cathode of the intermediate-temperature solid oxide fuel cell to be managed.
Further, an ejector is further arranged between the second control valve and the first mixing valve.
Further, a third control valve is arranged between the anode of the intermediate-temperature solid oxide fuel cell to be managed and the second inlet of the after-burner; and the third control valve is provided with two outlets which are respectively communicated with the second inlet of the post combustor and the inlet of the ejector.
Further, the oxidation reforming system comprises a first outlet and a second outlet, and the first outlet of the oxidation reforming system is communicated with an anode inlet of the intermediate-temperature solid oxide fuel cell to be managed.
Further, a first heat exchanger is arranged between the first outlet of the oxidation reforming system and the anode inlet of the intermediate-temperature solid oxide fuel cell to be managed.
Further, a second outlet of the oxidation reforming system is sequentially communicated with a third heat exchanger, the first heat exchanger and the second heat exchanger.
Further, a second mixing valve and a third mixing valve are sequentially arranged between a second outlet of the oxidation reforming system and the third heat exchanger, and the second mixing valve and the third mixing valve are both provided with two inlets; a fourth control valve is arranged between the after burner and the oxidation reforming system, two outlets of the fourth control valve are respectively communicated with a second inlet of the oxidation reforming system and one inlet of the second mixing valve, and the other inlet of the second mixing valve is communicated with a second outlet of the oxidation reforming system;
a sixth control valve is arranged between the third inlet of the oxidation reforming system and the cathode of the intermediate-temperature solid oxide fuel cell to be managed; the sixth control valve comprises two outlets which are respectively communicated with the third inlet of the post combustor and the third inlet of the oxidation reforming system; a seventh control valve is arranged between the sixth control valve and the third inlet of the oxidation reforming system; the seventh control valve includes two outlets respectively communicating with the third inlet of the oxidation reforming system and one inlet of the third mixing valve.
The system further comprises an air compressor, wherein an outlet of the air compressor is communicated with a fifth control valve, the fifth control valve comprises two outlets, and one outlet is communicated with a cathode inlet of the intermediate-temperature solid oxide fuel cell to be managed; and a communication pipeline between the fifth control valve and the cathode inlet of the intermediate-temperature solid oxide fuel cell to be managed sequentially passes through the second heat exchanger and the third heat exchanger.
Further, another outlet of the fifth control valve communicates with an air inlet of the pre-burner; an eighth control valve is arranged between the fifth control valve and the pre-burner;
the eighth control valve comprises two outlets, one outlet communicating with the air inlet of the pre-burner; a fourth mixing valve is further arranged between the second inlet of the first mixing valve and the pre-burner, and the fourth mixing valve comprises two inlets which are respectively communicated with the outlet of the pre-burner and the other outlet of the eighth control valve.
In order to achieve the above object, in a second aspect, the present invention further provides a thermal management method for an intermediate-temperature solid oxide fuel cell, which adopts the following technical scheme:
a method for thermal management of an intermediate-temperature solid oxide fuel cell, which employs the thermal management system for an intermediate-temperature solid oxide fuel cell as described in the first aspect, and comprises:
when the anode off-gas circulation rate is a first value:
at least one part of the normal-temperature natural gas enters the pre-burner to be combusted under the action of the second control valve, and the combusted tail gas enters the first mixing valve after passing through the fourth mixing valve; the other part of the natural gas is gradually merged with the recirculated anode exhaust gas at the ejector and the tail gas of the pre-burner at the first mixing valve, and then enters a fuel channel of an oxidation reforming system for reforming reaction; the reformed gas enters an anode channel of the intermediate-temperature solid oxide fuel cell to be managed through a first heat exchanger to carry out electrochemical reaction; the anode waste gas is divided into two paths by a third control valve, one path of the anode waste gas enters the ejector, and the other path of the anode waste gas directly enters the afterburner; the tail gas of the post combustor directly bypasses to the second mixing valve through a fourth control valve and is converged with the cathode waste gas radiated by the oxidation reforming system; the mixed waste gas flows through a third mixing valve and then sequentially enters a third heat exchanger, a first heat exchanger and a second heat exchanger for waste heat utilization, and finally is discharged out of the system;
normal temperature air enters a fifth control valve through an air compressor, and is divided into two paths at the fifth control valve, wherein one path of the normal temperature air serves as an oxidant and enters an eighth control valve, and the other path of the normal temperature air successively passes through a second heat exchanger and a third heat exchanger and then enters a cathode channel of the intermediate temperature solid oxide fuel cell to be managed; the air entering the eighth control valve is divided into two paths, wherein one path enters the precombustor, and the other path enters the fourth mixing valve; the cathode waste gas is divided into two paths by a sixth control valve, one path of the cathode waste gas enters the afterburner, and the other path of the cathode waste gas flows to the oxidation reforming system by a seventh control valve to dissipate heat for the reforming reaction;
when the anode exhaust gas circulation rate value is transited from low to high:
when the temperature at the fuel inlet of the oxidation reforming system continuously rises, the amount of the natural gas flowing to the pre-burner at the second control valve is continuously reduced, and the amount of the natural gas is reduced to zero when the temperature of the fuel inlet of the oxidation reforming system exceeds a preset value; when the reforming reaction heat is neutral, the tail gas of the post combustor is continuously bypassed to the second mixing valve through the fourth control valve, and the cathode waste gas is directly bypassed to the third mixing valve through the seventh control valve; when the reforming reaction absorbs heat, the tail gas of the post combustor flows into a gas channel of the oxidation reforming system through the fourth control valve, and the cathode waste gas is continuously bypassed to the third mixing valve through the seventh control valve;
when the anode waste gas circulation rate is a second value, the second value is larger than the first value, and when the reforming reaction absorbs heat and the energy of the post combustor is insufficient:
the first control valve provides a portion of the natural gas directly to the afterburner as supplemental fuel.
Compared with the prior art, the invention has the beneficial effects that:
in the invention, in order to solve the transition problem of heat dissipation to heat supply of the POX, a post-combustor is arranged and a gas pipeline of the POX is switched from cathode waste gas to tail gas of the post-combustor; in order to ensure the energy supply of the reforming reaction under the high AOGR rate, a small part of natural gas can be directly introduced into a post-combustor as supplementary fuel through the action of a first control valve, and fresh fuel and air entering POX are not preheated any more; under the above measures, in order to realize the stable operation of the system at the time of low AOGR rate so as to complete the switching of the AOGR rate from low to high, a pre-burner is arranged so as to maintain the minimum temperature required by the POX fuel inlet.
Drawings
The accompanying drawings, which form a part hereof, are included to provide a further understanding of the present embodiments, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the present embodiments and together with the description serve to explain the present embodiments without unduly limiting the present embodiments.
FIG. 1 is a schematic structural view of example 1 of the present invention;
the system comprises a natural gas supply end 1, a natural gas supply end 2, a first control valve 3, a second control valve 4, an ejector 5, a first mixing valve 6, an oxidation reforming system 7, a first heat exchanger 8, an intermediate-temperature solid oxide fuel cell to be managed 9, a third control valve 10, a post combustor 11, a fourth control valve 12, a second mixing valve 13, a third mixing valve 14 and an air supply end; 15. the air compressor 16, the fifth control valve 17, the pre-burner 18, the second heat exchanger 19, the third heat exchanger 20, the sixth control valve 21, the seventh control valve 22, the eighth control valve 23 and the fourth mixing valve.
The specific implementation mode is as follows:
the invention is further described with reference to the following figures and examples.
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
The terms "first," "second," and the like, herein do not denote any order, quantity, or importance, but rather are used to denote different elements.
Example 1:
as a novel energy utilization method, the fuel cell can directly convert chemical energy in fuel into electric energy through electrochemical reaction. Because the device is not limited by Carnot cycle and does not have the phenomenon of high-temperature combustion, the device has the advantages of high energy conversion rate, less harmful emissions and low noise. Among the many types of fuel cells, Solid Oxide Fuel Cells (SOFC) have some advantages over other types of fuel cells due to their high operating temperatures and lack of noble metal catalysts. Firstly, the SOFC works at 600-1000 ℃, and the high working temperature enables the waste gas to have high-grade heat energy, thereby being beneficial to waste heat recovery. If the SOFC is coupled with thermal equipment for cogeneration, the efficiency can reach 90 percent. Secondly, the use of the nickel-based catalyst reduces the production and manufacturing costs of the SOFC on one hand; on the other hand, the tolerance to the fuel impure degree is improved, so that the fuel utilization form of the SOFC is more flexible, and natural gas, biomass gas, methanol and the like can be used as fuels. Therefore, the SOFC has a good development prospect.
At present, the application of the SOFC is also mainly focused on a stationary power generation module, and the application of the SOFC to a vehicle-mounted or portable mobile power supply is still limited by two factors, namely the characteristics of the stack and the peripheral system. Conventional electrolyte-supported and anode-supported SOFCs use ceramic materials as the matrix. The ceramic material has low mechanical strength due to the specific brittleness of the ceramic material; due to the low heat conductivity coefficient of the ceramic material, the temperature distribution of the electric pile is uneven in the preheating process, and thermal stress is easy to generate. Therefore, the conventional SOFC has strict limits on the temperature rise rate, the temperature difference between the preheated gas and the stack, and the temperature difference inside the stack in the preheating process, and cannot realize quick start. Furthermore, the sealing problem between ceramic materials further weakens the reliability of the SOFC under cold and hot shock. The metal-supported SOFC effectively solves the problems, and due to the high heat conductivity coefficient of the metal matrix, the galvanic pile is uniformly heated and has small thermal stress in the preheating process, and in addition, the application of metal welding can ensure the good tightness of the galvanic pile under the cold and hot circulation, so the starting time is greatly shortened. The second problem can only be solved by relying on continuous optimization of the thermal management system (BOP). One possible approach is to use partial oxidation reforming (POX) instead of Steam Reforming (SR) to eliminate the complex steam generation and superheating equipment and simplify the BOP structure. However, the lower hydrogen yield of POX relative to SR results in reduced system electrical efficiency, and therefore a large proportion of anode exhaust gas cycles (AOGR) need to be coupled to mitigate this effect.
In the application process of AOGR, on one hand, hydrogen and carbon monoxide in anode exhaust gas can be directly utilized by electrochemical reaction; on the other hand, the heat energy of the exhaust gas can increase the fuel inlet temperature of the POX; in addition, with the introduction of a large amount of carbon dioxide and water, the demand for oxygen decreases, and the reforming reaction in POX gradually transitions from exothermic to endothermic. Therefore, the first problem to be solved by the application of the POX-AOGR system is how to realize the transition from heat dissipation to heat supply for the POX. Secondly, with the increase of the AOGR rate, the anode waste gas flowing into the post-combustor is reduced, the tail gas temperature of the post-combustor is reduced, and sufficient heat cannot be provided for the reforming reaction; meanwhile, the temperature of the fuel at the inlet of the POX rises, the temperature difference between the fuel and the tail gas of the post-combustor is reduced, and the heat exchange in the POX is more difficult. Therefore, the second problem to be solved by the application of the POX-AOGR system is how to guarantee the energy supply of the reforming reaction at the high AOGR rate. Finally, measures for reducing the inlet temperature of the POX fuel, such as not preheating fresh air and fuel entering the POX, are beneficial to expanding the operation range of the SOFC system under the high AOGR rate and improving the system efficiency. However, such measures cause the POX inlet temperature to be too low at low AOGR rates, and even cause the reforming reaction to gradually quench. Therefore, the third problem to be solved by the application of the POX-AOGR system is how to realize the smooth transition from low AOGR rate to high AOGR rate while ensuring the high efficiency of the system.
Currently, research on SOFC focuses on cogeneration, and an SR coupling system is generally selected to obtain a higher hydrogen concentration. But for the vehicle-mounted or portable mobile power supply only considering the electric efficiency, the POX-AOGR system with simple structure and compact volume is obviously more suitable. The current research on POX-AOGR is still rare, on one hand, the energy flow of a system with the structure is more complex and the control is more difficult, and on the other hand, the three problems of the transition from heat dissipation to heat supply of POX, the energy supply of reforming reaction under high AOGR rate and the smooth transition under different AOGR rates are still unsolved.
In order to solve the above problems, the present embodiment provides an intermediate-temperature solid oxide fuel cell thermal management system, which includes a first control valve 2, a second control valve 3, a pre-burner 17, a first mixing valve 5, an oxidation reforming system 6, and a post-burner 10;
the first control valve 2 comprises two outlets which are respectively communicated with a first inlet of the after-burner 10 and an inlet of the second control valve 3; the first control valve 2 may be configured to deliver at least a portion of the received natural gas to the post combustor; in this embodiment, the first control valve 2 may be connected to a natural gas supply end 1, and the natural gas supply end 1 and the after burner 10 may be implemented by existing burner equipment or conventional arrangements, but the specific structure is not limited thereto;
the second control valve 3 comprises two outlets, respectively communicating with the natural gas inlet of the pre-burner 17 and the first inlet of the first mixing valve 5; the second control valve 3 is configured to deliver at least a part of the natural gas provided in the first control valve 2 to the pre-burner 17 and the other part of the natural gas to the first mixing valve 5; the pre-burner 17 is configured to burn natural gas; the pre-burner 17 may be implemented by existing burner equipment or conventional arrangements, but is not limited to its specific structure;
the first mixing valve 5 further comprises a second inlet, the outlet of the pre-burner 17 being in communication with the second inlet of the first mixing valve 5; the outlet of the first mixing valve 5 is communicated with the first inlet of the oxidation reforming system 6; the first mixing valve 5 is configured to mix the natural gas from the second control valve 3 with the heated fluid from the pre-burner 17 and to input the mixed gas to the oxidation reforming system 6; the oxidative reforming system 6 may be implemented by existing burner equipment or conventional arrangements, but is not limited to its specific structure;
the afterburner 10 further comprises a second inlet and a third inlet; the second inlet of the post-combustor 10 is configured to receive the anode off-gas of the intermediate-temperature solid oxide fuel cell 8 to be managed, and the third inlet of the post-combustor 10 is configured to receive the cathode off-gas of the intermediate-temperature solid oxide fuel cell 8 to be managed;
the oxidation reforming system 6 further comprises a second inlet and a third inlet which are respectively communicated with the outlet of the after-burner 10 and the cathode of the intermediate-temperature solid oxide fuel cell 8 to be managed;
by the intermediate-temperature solid oxide fuel cell thermal management system provided in the present embodiment, and the connection structure among the first control valve 2, the second control valve 3, the pre-burner 17, the first mixing valve 5, the oxidation reforming system 6, and the post-burner 10; the gas pipeline of the POX can be switched from cathode waste gas to tail gas of the post combustor through the arranged post combustor, so that the transition problem of heat dissipation to heat supply of the POX is solved; by the aid of the first control valve, a small part of natural gas is directly introduced into the afterburner as supplementary fuel, fresh fuel and air entering the POX are not preheated any more, and energy supply of reforming reaction under the high AOGR rate is guaranteed; under the above measures, in order to realize the stable operation of the system at the time of low AOGR rate so as to complete the switching of the AOGR rate from low to high, a pre-burner is arranged so as to maintain the minimum temperature required by the POX fuel inlet.
In this embodiment, an ejector 4 is further disposed between the second control valve 2 and the first mixing valve 5; the ejector; the ejector utilizes a device that one high-speed high-energy flow (liquid flow, air flow or other material flow) ejects another low-speed low-energy flow, and the jet flows into a mixing chamber through a convergent nozzle, and the periphery of the mixing chamber is ejected flow.
In the present embodiment, a third control valve 9 is arranged between the anode of the intermediate-temperature solid oxide fuel cell 8 to be managed and the second inlet of the after-burner 10; the third control valve 9 has two outlets which are respectively communicated with the second inlet of the after burner 10 and the inlet of the ejector 4.
In the present embodiment, the oxidation reforming system 6 comprises a first outlet and a second outlet, the first outlet of the oxidation reforming system 6 is communicated with the anode inlet of the intermediate-temperature solid oxide fuel cell 8 to be managed; specifically, a first heat exchanger 7 may be disposed between the first outlet of the oxidation reforming system 6 and the anode inlet of the intermediate-temperature solid oxide fuel cell 8 to be managed; a second outlet of the oxidation reforming system 6 is sequentially communicated with a third heat exchanger 19, the first heat exchanger 7 and a second heat exchanger 18; the heat exchanger may be implemented by existing burner equipment or conventional arrangements, but is not limited to its specific structure.
In this embodiment, a second mixing valve 12 and a third mixing valve 13 are sequentially disposed between the second outlet of the oxidation reforming system 6 and the third heat exchanger 19, and both the second mixing valve 12 and the third mixing valve 13 are provided with two inlets; a fourth control valve 11 is arranged between the post-combustor 10 and the oxidation reforming system 6, two outlets of the fourth control valve 11 are respectively communicated with a second inlet of the oxidation reforming system 6 and one inlet of the second mixing valve 12, and the other inlet of the second mixing valve 12 is communicated with a second outlet of the oxidation reforming system 6;
a sixth control valve 20 is arranged between the third inlet of the oxidation reforming system 6 and the cathode of the intermediate-temperature solid oxide fuel cell 8 to be managed; the sixth control valve 20 includes two outlets respectively communicating the third inlet of the post-combustor 10 and the third inlet of the oxidation reforming system 6; a seventh control valve 21 is further arranged between the sixth control valve 20 and the third inlet of the oxidation reforming system 6; the seventh control valve 21 includes two outlets that communicate with the third inlet of the oxidation reforming system 6 and one inlet of the third mixing valve 13, respectively.
In the embodiment, the device further comprises an air compressor 15, an outlet of the air compressor 15 is communicated with a fifth control valve 16, the fifth control valve 16 comprises two outlets, and one outlet is communicated with a cathode inlet of the intermediate-temperature solid oxide fuel cell 8 to be managed; a communication pipeline between the fifth control valve 16 and the cathode inlet of the intermediate-temperature solid oxide fuel cell 8 to be managed sequentially passes through the second heat exchanger 18 and the third heat exchanger 19; the inlet of the air compressor 15 is communicated with an air supply end 14, and the air supply end 14 can be realized by existing burner equipment or conventional arrangement, but the specific structure is not limited.
In the present embodiment, the other outlet of the fifth control valve 16 communicates with the air inlet of the preburner 17; an eighth control valve 22 is arranged between the fifth control valve 16 and the pre-burner 17;
the eighth control valve 22 comprises two outlets, one outlet communicating with the air inlet of the pre-burner 17; a fourth mixing valve 23 is further arranged between the second inlet of the first mixing valve 5 and the pre-burner 17, the fourth mixing valve 23 comprising two inlets communicating with the outlet of the pre-burner 17 and the other outlet of the eighth control valve 22, respectively.
The working process or principle of the embodiment is as follows:
low AOGR rate, exothermic reforming reaction, POX inlet temperature below 400 deg.C:
the normal-temperature natural gas in the natural gas supply end flows to the second control valve 3 through the first control valve 2 and is divided into two paths at the second control valve 3; a small part of natural gas is combusted in the pre-combustor 17, and high-temperature tail gas of the natural gas is merged into a main fuel flow line through the fourth mixing valve 23 and the first mixing valve 5, so that the inlet temperature of POX fuel is maintained to be stable at 400 ℃; most of natural gas is gradually merged with the recirculated anode exhaust gas at the ejector 4 and the pre-burner tail gas at the first mixing valve 5, and then enters a fuel passage of the oxidation reforming system 6 for reforming reaction; after the temperature of the reformed gas is controlled to be 500 ℃ by the first heat exchanger 7, the reformed gas enters an anode channel of the intermediate-temperature solid oxide fuel cell 8 to be managed for electrochemical reaction; the working temperature of the intermediate-temperature solid oxide fuel cell 8 to be managed is 600 ℃, so the outlet temperature of the anode waste gas is 600 ℃; the anode waste gas is divided into two paths by the third control valve 9, one path of the anode waste gas is subjected to AOGR circulation and enters the ejector 4, the other path of the anode waste gas directly enters the post-combustor 10, and the tail gas of the post-combustor directly bypasses the second mixing valve 12 (a dotted line part in the figure) through the fourth control valve 11 and is converged with the cathode waste gas participating in the heat dissipation of POX; the mixed exhaust gas flows through the third mixing valve 13 and then sequentially enters the third heat exchanger 19, the first heat exchanger 7 and the second heat exchanger 18 for waste heat utilization, and finally is discharged out of the system.
Normal temperature air in the air supply end 14 enters the fifth control valve 16 after being pressurized by the air compressor 15, and is divided into two paths at the fifth control valve 16, wherein one path is taken as an oxidant and enters the eighth control valve 22, and the other path is preheated to 300 ℃ by the second heat exchanger 18, preheated to 500 ℃ by the third heat exchanger 19, and then enters a cathode channel of the intermediate temperature solid oxide fuel cell 8 to be managed; the eighth control valve 22 is also divided into two paths, one path enters the pre-burner 17 to ensure that the excess air coefficient of the pre-burner is 3.5, and the other path enters the fourth mixing valve 23 to meet the oxygen requirement of the reforming reaction; the outlet temperature of the cathode waste gas is 600 ℃, the cathode waste gas is divided into two paths by the sixth control valve 20, one path enters the post combustor 10 to ensure the excess air coefficient 12 of the post combustor, the other path flows to the oxidation reforming system 6 (the dotted line part in the figure) by the seventh control valve 21, and the heat is dissipated for the reforming reaction to ensure the outlet temperature of the reformed gas is 700 ℃.
When the low AOGR rate is transited to the high AOGR rate:
with the increase of the AOGR rate, two transition working conditions gradually appear; firstly, the temperature at the inlet of the POX fuel is continuously increased, at the moment, the amount of the natural gas flowing to the pre-burner 17 at the position of the second control valve 3 is continuously reduced, and the amount of the natural gas is reduced to zero after the temperature at the inlet of the POX fuel exceeds 400 ℃; secondly, the reforming reaction is gradually transited from heat release to heat neutrality until the reforming reaction is converted into heat absorption, when the reforming reaction is heat neutrality, the tail gas of the post combustor 10 is continuously and directly bypassed to the second mixing valve 12 through the fourth control valve 11, and the cathode waste gas is directly bypassed to the third mixing valve 13 through the seventh control valve 21; when the reforming reaction is endothermic, the whole exhaust gas of the post-combustor 10 flows into the gas passage of the oxidation reforming system 6 through the fourth control valve 11, and the cathode exhaust gas continues to bypass the third mixing valve 13 directly from the seventh control valve 21.
Under the high AOGR rate, when the reforming reaction absorbs heat and the energy of the post combustor is insufficient:
the first control valve 2 directly provides partial natural gas as supplementary fuel for the post combustor 10, so that the phenomena that the anode waste gas flowing into the post combustor 10 is too little and the temperature difference between the fuel and the waste gas in the oxidation reforming system 6 is too small are solved, and the heat exchange is difficult, and the problem that the endothermic reforming reaction cannot be maintained due to insufficient energy of the tail gas of the post combustor is solved.
The embodiment has the advantages that: POX is used for replacing SR, so that the BOP system structure is simplified, and the SOFC is favorably applied to the direction of a vehicle-mounted or portable mobile power supply; the BOP system is coupled with the AOGR cycle, so that the negative influence caused by low POX hydrogen yield can be eliminated, and the high system electrical efficiency is maintained; fresh fuel and air entering the POX are not preheated, the lowest fuel inlet temperature of the POX can be maintained at the expense of combustion of a small part of natural gas in the pre-combustor under the low AOGR rate, the transition of a system to the high AOGR rate is ensured, the temperature difference between the fuel and waste gas in the POX is favorably expanded under the high AOGR rate, and the conversion of the heat energy of the waste gas to the chemical energy of the fuel is promoted; the fuel supplementing route of the after-burner is designed, the problem that the energy of the after-burner is insufficient under the high AOGR rate can be effectively solved, the application upper limit of the AOGR rate is expanded, and the system electrical efficiency is improved within a certain range.
Example 2:
the embodiment provides a thermal management method for an intermediate-temperature solid oxide fuel cell, which adopts the thermal management system for the intermediate-temperature solid oxide fuel cell as described in embodiment 1, and includes:
when the anode off-gas circulation rate is a first value:
at least one part of the normal-temperature natural gas enters the pre-burner 17 to be burned under the action of the second control valve 3, and the burned tail gas enters the first mixing valve 5 after passing through the fourth mixing valve 23; the other part of the natural gas is gradually merged with the recirculated anode exhaust gas at the ejector 4 and the tail gas of the pre-burner at the first mixing valve 5, and then enters a fuel channel of an oxidation reforming system 6 for reforming reaction; the reformed gas enters an anode channel of an intermediate-temperature solid oxide fuel cell 8 to be managed through a first heat exchanger 7 to carry out electrochemical reaction; the anode waste gas is divided into two paths by a third control valve 9, one path of the anode waste gas enters the ejector 4, and the other path of the anode waste gas directly enters the afterburner 10; the tail gas of the post combustor directly bypasses to a second mixing valve 12 through a fourth control valve 11 and is converged with the cathode waste gas radiated by the oxidation reforming system 6; the mixed waste gas flows through a third mixing valve 13 and then sequentially enters a third heat exchanger 19, a first heat exchanger 7 and a second heat exchanger 18 for waste heat utilization, and finally is discharged out of the system;
after passing through an air compressor 15, the normal temperature air enters a fifth control valve 16 and is divided into two paths at the fifth control valve 16, wherein one path is used as an oxidant and enters an eighth control valve 22, and the other path successively passes through a second heat exchanger 18 and a third heat exchanger 19 and then enters a cathode channel of the intermediate temperature solid oxide fuel cell 8 to be managed; the air entering the eighth control valve 22 is divided into two paths, one path enters the precombustor 17, and the other path enters the fourth mixing valve 23; the cathode waste gas is divided into two paths by a sixth control valve 20, one path enters the post combustor 10, and the other path flows to the oxidation reforming system by a seventh control valve 21 to dissipate heat for the reforming reaction;
when the anode exhaust gas circulation rate value is transited from low to high:
when the temperature at the fuel inlet of the oxidation reforming system continuously rises, the amount of the natural gas flowing to the pre-burner at the second control valve 3 is continuously reduced, and the amount of the natural gas is reduced to zero when the temperature of the fuel inlet of the oxidation reforming system 6 exceeds a preset value; when the reforming reaction is thermally neutral, the tail gas of the post combustor is continuously bypassed to the second mixing valve 12 through the fourth control valve 11, and the cathode waste gas is bypassed to the third mixing valve 13 through the seventh control valve 21; when the reforming reaction absorbs heat, the tail gas of the post-combustor 10 flows into the gas channel of the oxidation reforming system 6 through the fourth control valve 11, and the cathode waste gas is continuously bypassed to the third mixing valve 13 through the seventh control valve 21;
when the anode exhaust gas circulation rate is a second value, the second value is larger than the first value, and when the reforming reaction absorbs heat and the energy of the after-burner 10 is insufficient:
the first control valve 2 supplies part of the natural gas directly to the post combustor 10 as supplementary fuel.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and those skilled in the art can make various modifications and variations. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present embodiment should be included in the protection scope of the present embodiment.
Claims (10)
1. The intermediate-temperature solid oxide fuel cell thermal management system is characterized by comprising a first control valve, a second control valve, a pre-burner, a first mixing valve, an oxidation reforming system and a post-burner;
the first control valve comprises two outlets which are respectively communicated with a first inlet of the after burner and an inlet of the second control valve;
the second control valve comprises two outlets which are respectively communicated with the natural gas inlet of the pre-burner and the first inlet of the first mixing valve; the first mixing valve further comprises a second inlet, and the outlet of the pre-burner is communicated with the second inlet of the first mixing valve; the outlet of the first mixing valve is communicated with the first inlet of the oxidation reforming system;
the afterburner further comprises a second inlet and a third inlet; the second inlet of the post-combustor is configured to receive anode exhaust gas of the intermediate-temperature solid oxide fuel cell to be managed, and the third inlet of the post-combustor is configured to receive cathode exhaust gas of the intermediate-temperature solid oxide fuel cell to be managed;
the oxidation reforming system also comprises a second inlet and a third inlet which are respectively communicated with the outlet of the after-burner and the cathode of the intermediate-temperature solid oxide fuel cell to be managed.
2. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 1, wherein an ejector is further provided between said second control valve and said first mixing valve.
3. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 2, characterized in that a third control valve is arranged between the anode of the intermediate-temperature solid oxide fuel cell to be managed and the second inlet of the after-burner; and the third control valve is provided with two outlets which are respectively communicated with the second inlet of the after burner and the inlet of the ejector.
4. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 1, characterized in that said oxidation reforming system comprises a first outlet and a second outlet, said first outlet of said oxidation reforming system being in communication with an anode inlet of the intermediate-temperature solid oxide fuel cell to be managed.
5. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 4, characterized in that a first heat exchanger is arranged between the first outlet of the oxidation reforming system and the anode inlet of the intermediate-temperature solid oxide fuel cell to be managed.
6. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 5, wherein a third heat exchanger, the first heat exchanger and a second heat exchanger are sequentially communicated with a second outlet of the oxidation reforming system.
7. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 6, wherein a second mixing valve and a third mixing valve are sequentially arranged between the second outlet of the oxidation reforming system and the third heat exchanger, and both the second mixing valve and the third mixing valve are provided with two inlets; a fourth control valve is arranged between the post combustor and the oxidation reforming system, two outlets of the fourth control valve are respectively communicated with a second inlet of the oxidation reforming system and one inlet of the second mixing valve, and the other inlet of the second mixing valve is communicated with a second outlet of the oxidation reforming system;
a sixth control valve is arranged between the third inlet of the oxidation reforming system and the cathode of the intermediate-temperature solid oxide fuel cell to be managed; the sixth control valve comprises two outlets which are respectively communicated with the third inlet of the post combustor and the third inlet of the oxidation reforming system; a seventh control valve is arranged between the sixth control valve and the third inlet of the oxidation reforming system; the seventh control valve includes two outlets respectively communicating with the third inlet of the oxidation reforming system and one inlet of the third mixing valve.
8. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 6, characterized by further comprising an air compressor, wherein an outlet of the air compressor is communicated with a fifth control valve, the fifth control valve comprises two outlets, and one outlet is communicated with a cathode inlet of the intermediate-temperature solid oxide fuel cell to be managed; and a communication pipeline between the fifth control valve and the cathode inlet of the intermediate-temperature solid oxide fuel cell to be managed sequentially passes through the second heat exchanger and the third heat exchanger.
9. An intermediate-temperature solid oxide fuel cell thermal management system according to claim 8, characterized in that the other outlet of the fifth control valve communicates with the air inlet of the pre-burner; an eighth control valve is arranged between the fifth control valve and the pre-burner;
the eighth control valve comprises two outlets, one outlet communicating with the air inlet of the pre-burner; a fourth mixing valve is further arranged between the second inlet of the first mixing valve and the pre-burner, and the fourth mixing valve comprises two inlets which are respectively communicated with the outlet of the pre-burner and the other outlet of the eighth control valve.
10. An intermediate-temperature solid oxide fuel cell thermal management method, which is characterized in that the intermediate-temperature solid oxide fuel cell thermal management system according to any one of claims 1 to 9 is adopted, and the method comprises the following steps:
when the anode off-gas circulation rate is a first value:
at least one part of the normal-temperature natural gas enters the pre-burner to be combusted under the action of the second control valve, and the combusted tail gas enters the first mixing valve after passing through the fourth mixing valve; the other part of the natural gas is gradually merged with the recirculated anode exhaust gas at the ejector and the tail gas of the pre-burner at the first mixing valve, and then enters a fuel channel of an oxidation reforming system for reforming reaction; the reformed gas enters an anode channel of the intermediate-temperature solid oxide fuel cell to be managed through a first heat exchanger to carry out electrochemical reaction; the anode waste gas is divided into two paths by a third control valve, one path of the anode waste gas enters the ejector, and the other path of the anode waste gas directly enters the afterburner; the tail gas of the post combustor directly bypasses to the second mixing valve through a fourth control valve and is converged with the cathode waste gas radiated by the oxidation reforming system; the mixed waste gas flows through a third mixing valve and then sequentially enters a third heat exchanger, a first heat exchanger and a second heat exchanger for waste heat utilization, and finally is discharged out of the system;
normal temperature air enters a fifth control valve through an air compressor, and is divided into two paths at the fifth control valve, wherein one path of the normal temperature air serves as an oxidant and enters an eighth control valve, and the other path of the normal temperature air successively passes through a second heat exchanger and a third heat exchanger and then enters a cathode channel of the intermediate temperature solid oxide fuel cell to be managed; the air entering the eighth control valve is divided into two paths, wherein one path enters the precombustor, and the other path enters the fourth mixing valve; the cathode waste gas is divided into two paths by a sixth control valve, one path of the cathode waste gas enters the afterburner, and the other path of the cathode waste gas flows to the oxidation reforming system by a seventh control valve to dissipate heat for the reforming reaction;
when the anode exhaust gas circulation rate value is transited from low to high:
when the temperature at the fuel inlet of the oxidation reforming system continuously rises, the amount of the natural gas flowing to the pre-burner at the second control valve is continuously reduced, and the amount of the natural gas is reduced to zero when the temperature of the fuel inlet of the oxidation reforming system exceeds a preset value; when the reforming reaction heat is neutral, the tail gas of the post combustor is continuously bypassed to the second mixing valve through the fourth control valve, and the cathode waste gas is directly bypassed to the third mixing valve through the seventh control valve; when the reforming reaction absorbs heat, the tail gas of the post combustor flows into a gas channel of the oxidation reforming system through the fourth control valve, and the cathode waste gas is continuously bypassed to the third mixing valve through the seventh control valve;
when the anode waste gas circulation rate is a second value, the second value is larger than the first value, and when the reforming reaction absorbs heat and the energy of the post combustor is insufficient:
the first control valve provides a portion of the natural gas directly to the afterburner as supplemental fuel.
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| CN102473948A (en) * | 2009-07-30 | 2012-05-23 | 日产自动车株式会社 | Fuel cell system and control method thereof |
| CN102593547A (en) * | 2011-01-18 | 2012-07-18 | 上海鼎研智能科技有限公司 | Low-temperature charging heating and protecting method for secondary battery pack |
| KR20150035268A (en) * | 2013-09-27 | 2015-04-06 | 주식회사 엘지화학 | Device for detecting inner pressure of secondary battery, and method for detecting inner pressure of secondary battery by using the same |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102473948A (en) * | 2009-07-30 | 2012-05-23 | 日产自动车株式会社 | Fuel cell system and control method thereof |
| CN102593547A (en) * | 2011-01-18 | 2012-07-18 | 上海鼎研智能科技有限公司 | Low-temperature charging heating and protecting method for secondary battery pack |
| KR20150035268A (en) * | 2013-09-27 | 2015-04-06 | 주식회사 엘지화학 | Device for detecting inner pressure of secondary battery, and method for detecting inner pressure of secondary battery by using the same |
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