CN116826121A - Vehicle HT-PEMFC system integrating MSR and ORC - Google Patents
Vehicle HT-PEMFC system integrating MSR and ORC Download PDFInfo
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- CN116826121A CN116826121A CN202310709227.2A CN202310709227A CN116826121A CN 116826121 A CN116826121 A CN 116826121A CN 202310709227 A CN202310709227 A CN 202310709227A CN 116826121 A CN116826121 A CN 116826121A
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- 239000001257 hydrogen Substances 0.000 claims abstract description 105
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 105
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 97
- 238000003860 storage Methods 0.000 claims abstract description 38
- 238000001179 sorption measurement Methods 0.000 claims abstract description 18
- 239000002828 fuel tank Substances 0.000 claims abstract description 15
- 210000001503 joint Anatomy 0.000 claims description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 66
- 239000000446 fuel Substances 0.000 abstract description 35
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 238000002407 reforming Methods 0.000 abstract description 6
- 238000006243 chemical reaction Methods 0.000 description 34
- 238000000034 method Methods 0.000 description 25
- 239000007789 gas Substances 0.000 description 16
- 239000002918 waste heat Substances 0.000 description 15
- 239000012530 fluid Substances 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 239000007788 liquid Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 150000002431 hydrogen Chemical class 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 4
- 238000001651 catalytic steam reforming of methanol Methods 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 238000010248 power generation Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000009440 infrastructure construction Methods 0.000 description 3
- MSSNHSVIGIHOJA-UHFFFAOYSA-N pentafluoropropane Chemical compound FC(F)CC(F)(F)F MSSNHSVIGIHOJA-UHFFFAOYSA-N 0.000 description 3
- 239000012495 reaction gas Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000004146 energy storage Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000003032 molecular docking Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- H01M8/0606—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
-
- 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
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
- H01M8/1231—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte with both reactants being gaseous or vaporised
-
- 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
- H01M8/22—Fuel cells in which the fuel is based on materials comprising carbon or oxygen or hydrogen and other elements; Fuel cells in which the fuel is based on materials comprising only elements other than carbon, oxygen or hydrogen
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Fuel Cell (AREA)
Abstract
The invention relates to the technical field of fuel cells, in particular to an automotive HT-PEMFC system integrating MSR and ORC, which comprises an MSR subsystem, an HT-PEMFC subsystem and an ORC subsystem; the MSR subsystem comprises a fuel tank, a first pump, a heat exchanger, a superheater, a reformer, a cooler, a separator, a pressure swing adsorption tower, a hydrogen storage tank, a first pressure regulator, a connecting pipe and a second pressure regulator; the first pump is communicated with the fuel tank, the heat exchanger is communicated with the first pump, the superheater is communicated with the heat exchanger, the reformer is respectively communicated with the superheater and the heat exchanger, the cooler is communicated with the heat exchanger, the separator is respectively communicated with the cooler and the fuel tank, the pressure swing adsorption tower is communicated with the separator, and the hydrogen storage tank is communicated with the pressure swing adsorption tower; the invention provides hydrogen for the fuel cell system through the hydrogen production by the methanol reforming, and solves the problems of hydrogen storage and transportation.
Description
Technical Field
The invention relates to the technical field of fuel cells, in particular to an automobile HT-PEMFC system integrating MSR and ORC.
Background
Proton Exchange Membrane Fuel Cells (PEMFCs) are considered as one of the most potential power sources for Fuel Cell Vehicles (FCV) because of their high energy conversion efficiency, high power density, zero emissions, low noise, and easy maintenance.
At present, due to the limitation of the working temperature (60-80 ℃) of a low-temperature proton exchange membrane fuel cell (LT-PEMFC), the generated liquid water can possibly cause membrane flooding, which can cause the transmission of reaction gas to be blocked and greatly influence the performance of the fuel cell; compared with LT-PEMFC, high temperature proton exchange membrane fuel cells (HT-PEMFC) operating at higher temperatures (120-200 ℃) have significant advantages: the reaction kinetics at the electrode is accelerated, the water and thermal management system is simplified, the tolerance of CO is improved, and the quality of the electric pile waste heat is improved; however, the existing pure hydrogen fuel cell vehicle still has the problems of higher manufacturing and operation cost of the battery, large investment of infrastructure, incomplete solution of basic technical problems such as preparation, transportation and storage of hydrogen, and the like, and severely restricts the development of the pure hydrogen fuel cell vehicle.
Disclosure of Invention
The invention aims to provide an automobile HT-PEMFC system integrating MSR and ORC, which provides hydrogen for a fuel cell system through hydrogen production by methanol reforming and solves the problems of hydrogen storage and transportation.
In order to achieve the above object, the present invention provides an in-vehicle HT-PEMFC system integrating MSR and ORC, comprising an MSR subsystem, an HT-PEMFC subsystem and an ORC subsystem;
the HT-PEMFC subsystem is arranged on one side of the MSR subsystem, and the ORC subsystem is arranged on one side of the HT-PEMFC subsystem; the MSR subsystem includes a fuel tank, a first pump, a heat exchanger, a superheater, a reformer, a cooler, a separator, a pressure swing adsorption column, a hydrogen storage tank, a first pressure regulator, a connecting pipe, and a second pressure regulator; the first pump is communicated with the fuel tank, the heat exchanger is communicated with the first pump, the superheater is communicated with the heat exchanger, the reformer is respectively communicated with the superheater and the heat exchanger, the cooler is communicated with the heat exchanger, the separator is respectively communicated with the cooler and the fuel tank, the pressure swing adsorption tower is communicated with the separator, the hydrogen storage tank is communicated with the pressure swing adsorption tower, the first pressure regulator is communicated with the pressure swing adsorption tower, the connecting pipe is communicated with the first pressure regulator, and the second pressure regulator is respectively communicated with the hydrogen storage tank and the connecting pipe.
Wherein the HT-PEMFC subsystem comprises a hydrogen compressor, an interfacing tube, an HT-PEMFC stack, an anode heat exchanger, a cathode heat exchanger, an air compressor and a second pump;
the hydrogen compressor is communicated with the connecting pipe, the butt joint pipe is communicated with the reformer, the HT-PEMFC galvanic pile is respectively communicated with the hydrogen compressor, the superheater and the butt joint pipe, the anode heat exchanger is respectively communicated with the connecting pipe and the HT-PEMFC galvanic pile, the cathode heat exchanger is respectively communicated with the HT-PEMFC galvanic pile and the anode heat exchanger, the air compressor is communicated with the cathode heat exchanger, and the second pump is communicated with the butt joint pipe.
Wherein the ORC subsystem comprises an evaporator, a turbine, a generator, a condenser, and a third pump;
the evaporator is respectively communicated with the second pump and the HT-PEMFC galvanic pile, the turbine is communicated with the evaporator, the generator is communicated with the turbine, the condenser is communicated with the turbine, and the third pump is respectively communicated with the evaporator and the condenser.
In the vehicle HT-PEMFC system integrating MSR and ORC, mixed liquid of methanol and water flowing out of a fuel tank is pressurized to a heat exchanger through a first pump to be preheated, preheated methanol aqueous solution is vaporized in a superheater, and then steam mixture flows into a reformer to react and generate hydrogen. The heat required for evaporation and reaction comes from the waste heat of the HT-PEMFC stack carried by the conduction oil (triethylene glycol). The mixture for generating the reaction gas comprises CO and CO besides hydrogen 2 Methanol gas and water vapor which are not completely reacted. The mixed gas releases heat through the heat exchanger, usingAfter preheating the incoming aqueous methanol solution, the gas mixture is cooled in a cooler. The two-phase gas-liquid mixture is separated in a separator, and methanol and aqueous solution are refluxed to an oil tank. The separated mixed gas flows into a Pressure Swing Adsorption (PSA) system to extract pure hydrogen, and the residual CO and CO 2 Into the environment. The extracted pure hydrogen is supplied to the HT-PEMFC subsystem for operation, and the redundant hydrogen flows into the hydrogen storage tank. During the start-up phase, the system may obtain hydrogen from a hydrogen tank. The first pressure regulator and the second pressure regulator may be adjusted according to the operating conditions of the FCV in operation. The hydrogen generated by the MSR subsystem flows into a hydrogen storage tank or is provided for an HT-PEMFC pile to perform oxidation-reduction reaction to generate electric energy; the generated hydrogen is preferentially provided for the HT-PEMFC subsystem to be used, and the redundant hydrogen flows into the gas storage tank to be stored; when the generated hydrogen is insufficient to meet the requirements of the HT-PEMFC galvanic pile, the hydrogen in the hydrogen storage tank flows out to be supplied, and the generated hydrogen and the hydrogen flowing out from the gas storage tank are respectively delivered to the first pressure regulator and the second pressure regulator to be regulated to the pressure required by the galvanic pile reaction. The heat required by the methanol steam reforming hydrogen production reaction in the MSR subsystem is derived from the waste heat generated by the electric pile, the waste heat generated by the HT-PEMFC electric pile is preferentially supplied to the MSR subsystem for producing hydrogen, and the surplus heat is supplied to the ORC subsystem for recovery work.
Equilibrium conversion of methanol in the MSR subsystemAnd hydrogen yield->Can be expressed as:
in the method, in the process of the invention,is the molar flow.
As shown in fig. 2, the CH reaches an equilibrium state 3 OH conversion with reaction temperature T reaction And H 2 O/CH 3 The molar ratio of OH increases gradually. When H is 2 O/CH 3 When the molar ratio of OH is greater than 1 and the reaction temperature is greater than 453K, the CH of the MSR subsystem 3 The OH conversion rate is above 95%.
As shown in FIG. 3, when H 2 O/CH 3 When the OH molar ratio is more than 1 and the hydrogen yield is higher than 95%, the reaction temperature has little influence on the hydrogen yield; since both the superheater and the reformer are heated by waste heat of the HT-PEMFC stack, the reaction temperature should be lower than the temperature of the stack outlet. Thus, to ensure a better output performance of the proposed system, H 2 O/CH 3 The molar ratio of OH should be greater than 1.2; at this point, the methanol equilibrium conversion and hydrogen yield of the MSR subsystem may be greater than 95% at a given reaction temperature. The invention adopts the methanol steam reforming, avoids the cost of hydrogen transportation and infrastructure construction, and improves the economy of the system.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of an in-vehicle HT-PEMFC system of the present invention that integrates MSR and ORC.
FIG. 2 is a schematic graph showing the effect of reaction temperature and water to alcohol molar ratio on methanol conversion for the MSR subsystem of the present invention.
FIG. 3 is a schematic diagram of the effect of reaction temperature and hydroalcoholic molar ratio on hydrogen yield for the MSR subsystem of the present invention.
FIG. 4 is a schematic diagram of the structure of the ORC subsystem of the present invention.
Fig. 5 is a temperature entropy diagram of an ORC subsystem of the present invention.
FIG. 6 is a schematic diagram of the effect of different organic agents of the ORC subsystem of the present invention on the output performance of the ORC subsystem.
Fig. 7 is a structural diagram of a fuel cell vehicle powertrain.
1-MSR subsystem, 2-HT-PEMFC subsystem, 3-ORC subsystem, 4-fuel tank, 5-first pump, 6-heat exchanger, 7-superheater, 8-reformer, 9-cooler, 10-separator, 11-pressure swing adsorption column, 12-hydrogen storage tank, 13-first pressure regulator, 14-connection pipe, 15-second pressure regulator, 16-hydrogen compressor, 17-connection pipe, 18-HT-PEMFC stack, 19-anode heat exchanger, 20-cathode heat exchanger, 21-air compressor, 22-second pump, 23-evaporator, 24-turbine, 26-generator, 27-condenser, 28-third pump.
Detailed Description
Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative and intended to explain the present invention and should not be construed as limiting the invention.
Referring to fig. 1 to 7, the present invention provides an automotive HT-PEMFC system integrating MSR and ORC, including an MSR subsystem 1, an HT-PEMFC subsystem 2, and an ORC subsystem 3;
the HT-PEMFC subsystem 2 is arranged on one side of the MSR subsystem 1, and the ORC subsystem 3 is arranged on one side of the HT-PEMFC subsystem 2; the MSR subsystem 1 includes a fuel tank 4, a first pump 5, a heat exchanger 6, a superheater 7, a reformer 8, a cooler 9, a separator 10, a pressure swing adsorption tower 11, a hydrogen storage tank 12, a first pressure regulator 13, a connecting pipe 14, and a second pressure regulator 15; the first pump 5 is communicated with the fuel tank 4, the heat exchanger 6 is communicated with the first pump 5, the superheater 7 is communicated with the heat exchanger 6, the reformer 8 is respectively communicated with the superheater 7 and the heat exchanger 6, the cooler 9 is communicated with the heat exchanger 6, the separator 10 is respectively communicated with the cooler 9 and the fuel tank 4, the pressure swing adsorption tower 11 is communicated with the separator 10, the hydrogen storage tank 12 is communicated with the pressure swing adsorption tower 11, the first pressure regulator 13 is communicated with the pressure swing adsorption tower 11, the connecting pipe 14 is communicated with the first pressure regulator 13, and the second pressure regulator 15 is respectively communicated with the hydrogen storage tank 12 and the connecting pipe 14.
In the present embodiment, the mixed liquid of methanol and water flowing out of the fuel tank 4 is pressurized by the first pump 5 to the heat exchanger 6 for preheating, the preheated aqueous methanol solution is vaporized in the superheater 7, and then the steam mixture flows into the reformer 8 for reaction and hydrogen generation. The heat required for evaporation and reaction comes from the waste heat of the HT-PEMFC stack 18 carried by the conduction oil (triethylene glycol). The mixture for generating the reaction gas comprises CO and CO besides hydrogen 2 Methanol gas and water vapor which are not completely reacted. The mixed gas releases heat through the heat exchanger 6 for preheating the incoming aqueous methanol solution, after which the gas mixture is cooled in the cooler 9. The two-phase gas-liquid mixture is separated in separator 10 and the methanol and aqueous solution are refluxed to the tank. The separated mixed gas flows into a Pressure Swing Adsorption (PSA) system to extract pure hydrogen, and the residual CO and CO 2 Into the environment. The extracted pure hydrogen is supplied to the HT-PEMFC subsystem operation, and the surplus hydrogen flows into the hydrogen tank 12. During the start-up phase, the system may obtain hydrogen from a hydrogen tank. The first pressure regulator 13 and the second pressure regulator 15 may be adjusted according to the operating conditions of the FCV in operation. The hydrogen generated by the MSR subsystem 1 flows into the hydrogen storage tank 12 or is provided for the HT-PEMFC stack 18 to perform oxidation-reduction reaction to generate electric energy; the generated hydrogen is preferentially provided for the HT-PEMFC subsystem 2 to be used, and the redundant hydrogen flows into a gas storage tank to be stored; when the generated hydrogen is insufficient to meet the requirements of the HT-PEMFC stack 18, the hydrogen in the hydrogen storage tank 12 flows out to be supplied, and the generated hydrogen and the hydrogen flowing out from the gas storage tank are respectively delivered to the first pressure regulator 13 and the second pressure regulator 15 to be regulated to the pressure required by the stack reaction. The heat required for the methanol steam reforming hydrogen production reaction in the MSR subsystem 1 comes fromThe waste heat generated by the electric pile and the waste heat generated by the HT-PEMFC electric pile 18 are preferentially supplied to the MSR subsystem 1 to produce hydrogen, and the surplus heat is supplied to the ORC subsystem 3 to perform recovery work.
Equilibrium conversion of methanol in the MSR subsystem 1And hydrogen yield->Can be expressed as:
in the method, in the process of the invention,is the molar flow.
As shown in fig. 2, the CH reaches an equilibrium state 3 OH conversion with reaction temperature T reaction And H 2 O/CH 3 The molar ratio of OH increases gradually. When H is 2 O/CH 3 When the molar ratio of OH is greater than 1 and the reaction temperature is greater than 453K, CH of MSR subsystem 1 3 The OH conversion rate is above 95%.
As shown in FIG. 3, when H 2 O/CH 3 When the OH molar ratio is more than 1 and the hydrogen yield is higher than 95%, the reaction temperature has little influence on the hydrogen yield; since both the superheater 7 and the reformer 8 are heated by waste heat of the HT-PEMFC stack 18, the reaction temperature should be lower than the temperature of the stack outlet. Thus, to ensure a better output performance of the proposed system, H 2 O/CH 3 The molar ratio of OH should be greater than 1.2; at this time, at a certain reaction temperature, the equilibrium conversion of methanol and the hydrogen yield of the MSR subsystem 1 may be greater than 95%. The invention adopts the steam reforming of methanol to avoidThe cost of hydrogen-free transportation and infrastructure construction improves the economy of the system.
Further, the HT-PEMFC subsystem 2 comprises a hydrogen compressor 16, a docking tube 17, an HT-PEMFC stack 18, an anode heat exchanger 19, a cathode heat exchanger 20, an air compressor 21 and a second pump 22;
the hydrogen compressor 16 is communicated with the connecting pipe 14, the butt joint pipe 17 is communicated with the reformer 8, the HT-PEMFC stack 18 is respectively communicated with the hydrogen compressor 16, the superheater 7 and the butt joint pipe 17, the anode heat exchanger 19 is respectively communicated with the connecting pipe 14 and the HT-PEMFC stack 18, the cathode heat exchanger 20 is respectively communicated with the HT-PEMFC stack 18 and the anode heat exchanger 19, the air compressor 21 is communicated with the cathode heat exchanger 20, and the second pump 22 is communicated with the butt joint pipe 17.
In this embodiment, the hydrogen entering the HT-PEMFC subsystem 2 is regulated to the working pressure by a pressure regulator; the hydrogen compressor 16 recovers the hydrogen gas that has not been completely reacted from the anode of the fuel cell and pressurizes it to the operating pressure. The recovered hydrogen is mixed with fresh hydrogen and then flows into the anode heat exchanger 19, and the mixed hydrogen is heated to the operating temperature. The air in the environment is pressurized and heated by the air compressor 21 and the cathode heat exchanger 20 to reach the working condition. Unreacted air and generated water in the HT-PEMFC stack 18 flow into the heat exchanger 6, providing heat to the inlet gas. The HT-PEMFC stack 18 generates electrical energy and heat during operation, the generated heat is carried away by the heat transfer oil, wherein a portion of the heat is provided to the MSR subsystem 1 for producing hydrogen and the remaining heat is provided to the ORC subsystem 3 for waste heat recovery to produce electrical power. The method combines a cooling system and a waste heat recovery technology, can maintain the working temperature of the HT-PEMFC stack 18 within a reasonable range, and simultaneously fully utilizes the waste heat generated by the stack to improve the system efficiency. The HT-PEMFC subsystem 2 preheats inlet hydrogen and oxygen with excess air and produced water at the cathode outlet, heats the hydrogen to the required operating temperature for the reaction in the anode heat exchanger 19, and heats the air to the required operating temperature for the reaction at the cathode heat exchanger 20; meanwhile, the hydrogen recycle compressor 25 is utilized to recover the incompletely reacted hydrogen, thereby improving the fuel utilization of the system.
Further, the ORC subsystem 3 includes an evaporator 23, a turbine 24, a generator 26, a condenser 27, and a third pump 28;
the evaporator 23 is respectively communicated with the second pump 22 and the HT-PEMFC stack 18, the turbine 24 is communicated with the evaporator 23, the generator 26 is communicated with the turbine 24, the condenser 27 is communicated with the turbine 24, and the third pump 28 is respectively communicated with the evaporator 23 and the condenser 27.
In the present embodiment, the heat transfer oil releases heat in the evaporator 23, and the organic working medium is vaporized. The superheated organic working medium steam flows into the turbine 24 to drive the generator 26 to generate electric energy; the organic working medium vapor is liquefied in the condenser 27 and flows into the third pump 28; the working fluid is pressurized to a desired pressure by the third pump 28 and then circulated. As shown in fig. 4, the process: the evaporator 23-turbine 24-condenser 27-third pump 28-the evaporator 23 is the thermodynamic cycle process of the organic rankine cycle of the present invention. As shown in fig. 5, the process: the evaporator 23-turbine 24 is an endothermic process of the working fluid under constant pressure, the organic working fluid fully absorbs heat in the cooling channel of the HT-PEMFC stack 18, gradually evaporates from a liquid state, and finally flows out of the stack in the form of superheated steam; the process comprises the following steps: the turbine 24-condenser 27 is in an isentropic expansion process, superheated organic working medium steam enters the expander to drive the generator 26 to generate power, and the superheated working medium is exothermic and condensed into a low-pressure liquid state at the condenser 27; the process comprises the following steps: the condenser 27-the third pump 28 is an isobaric condensation process, the organic working fluid is gradually liquefied from a superheated vapor state, and finally reaches a saturated liquid state; the process comprises the following steps: the third pump 28-evaporator 23 is an isentropic compression process. After the third pump 28 pressurizes the working fluid to a desired pressure, the liquid working fluid is circulated to the evaporator 23 by the working fluid pump to complete the entire cycle. From the ORC operating principle, it is known that the process evaporator 23-turbine 24 and the process condenser 27-third pump 28 are isobaric processes, while the process turbine 24-condenser 27 and the process third pump 28-evaporator 23 are isentropic processes. Mass flow rate of organic working fluidIt can be expressed that:
in the method, in the process of the invention,mass flow rate, Q eva Indicating the amount of heat evaporated by the evaporator 23 and indicating the enthalpy of the fluid.
Power W generated by the expander exp Can be expressed as:
wherein eta is exp Is the isentropic efficiency of the expander.
Heat Q from the organic working fluid diffusing into the environment in the condenser 27 cond Can be expressed as:
in ORC subsystem 3, the power W consumed by third pump 28 pump3 The method comprises the following steps:
on the premise that the system can be in a negative pressure environment, 5 working mediums are selected for numerical calculation: r245fa, R245ca, R134a, R123 and R11.
As illustrated in fig. 6, R245fa shows the best performance in ORC subsystem 3 for the different organic working fluids at the temperatures and pressures studied, with power and efficiency of 2.26kW and 18.6%, respectively. The ozone depletion potential value (Ozone Depletion Potential, ODP) value of R245fa is 0, so that the method is friendly to the environment; from the standpoint of output performance and environmental protection, R245fa is more suitable as an organic working fluid in a combined HT-PEMFC and ORC system.
As shown in fig. 7, the fuel cell system of the present invention is applied to an FCV power system, and drives a vehicle to travel by connecting a fuel cell and a battery in parallel (fc+b).
Since the output voltage of the fuel cell is not very stable during operation, a DC/DC converter is connected in series in the circuit to ensure that the output voltage can be a constant value when the input voltage fluctuates within its range; meanwhile, the storage battery is connected with a DC/DC converter in series, so that the maximum discharge power can be improved, the automobile has better starting performance, such as improving the temperature of a fuel cell system, increasing the air inlet pressure and the like, the high storage battery power can ensure that the motor can obtain enough and stable energy input, and the motor has high backup power during starting. The output voltage of the fuel cell system and the storage battery is driven by the motor to do work through the DC/AC converter; the fuel cell can charge the storage battery under low load, and the storage battery can also recover automobile braking energy.
The starting mode is as follows: the cold start performance of the fuel cell is poor, the power of the fuel cell system is unstable, the output power of the fuel cell system cannot be transmitted to the power system, and the storage battery provides all energy for driving the motor; the hydrogen starting mode of the fuel cell system is provided by the gas storage tank; the battery provides the power consumption required for the inlet hydrogen and oxygen warm-up of the HT-PEMFC stack 18, heating the fuel cell stack inlet gas until the fuel cell begins to operate.
In the normal operation mode: the fuel cell system starts to operate to generate electric energy to drive the vehicle to run, the waste heat generated by the HT-PEMFC stack 18 can provide the MSR subsystem 1 for reforming hydrogen production, the generated hydrogen provides the fuel cell system, and the surplus heat can be recovered by the ORC subsystem 3 to generate electric energy.
Under the low load working condition: the power generated by the fuel cell system charges the storage battery, redundant hydrogen generated by the MSR subsystem 1 can flow into the gas storage tank for storage, and the electric energy generated by the recovery of waste heat by the ORC subsystem 3 can charge the storage battery or heat the seat.
Under the high load working condition: the fuel cell system and the storage battery jointly provide the power required by the running of the automobile, and the storage battery discharges outwards.
According to the vehicle HT-PEMFC system integrating the MSR and the ORC, the methanol steam reforming hydrogen production subsystem is adopted, so that the transportation of hydrogen and the cost of infrastructure construction are avoided; the MSR subsystem 1 produces hydrogen in real time, and redundant hydrogen flows into the hydrogen storage tank 12, so that the waste of hydrogen is avoided; the methanol reforming hydrogen production fuel cell integrates two links of methanol reforming hydrogen production and hydrogen fuel cell power generation, and the energy storage density and energy storage economy of the power generation system are more superior to those of a pure hydrogen fuel cell in popularization. The HT-PEMFC stack 18 is adopted, so that the phenomenon of flooding of the LT-PEMFC is avoided, and the efficiency and the power density of the stack are improved. The waste heat of the fuel cell is used for providing heat for reforming the methanol steam, so that the energy utilization rate is improved, and the ORC cycle power generation is used for converting the heat into electric energy, so that the power generation efficiency is improved. The invention utilizes the hydrogen compressor 16 to recycle the hydrogen unreacted at the anode, and utilizes the separator 10 to recycle the unreacted methanol and the aqueous solution, thereby improving the fuel utilization rate. The hydrogen and the air entering the electric pile are preheated by using the excessive air and the generated water at the outlet of the cathode, so that the power consumption of auxiliary equipment is reduced, the system efficiency is improved, the electricity cost is saved, and the workload of air supply and the equipment cost are reduced.
The above disclosure is only a preferred embodiment of the present invention, and it should be understood that the scope of the invention is not limited thereto, and those skilled in the art will appreciate that all or part of the procedures described above can be performed according to the equivalent changes of the claims, and still fall within the scope of the present invention.
Claims (3)
1. An in-vehicle HT-PEMFC system integrating MSR and ORC, characterized in that,
comprises an MSR subsystem, an HT-PEMFC subsystem and an ORC subsystem;
the HT-PEMFC subsystem is arranged on one side of the MSR subsystem, and the ORC subsystem is arranged on one side of the HT-PEMFC subsystem; the MSR subsystem includes a fuel tank, a first pump, a heat exchanger, a superheater, a reformer, a cooler, a separator, a pressure swing adsorption column, a hydrogen storage tank, a first pressure regulator, a connecting pipe, and a second pressure regulator; the first pump is communicated with the fuel tank, the heat exchanger is communicated with the first pump, the superheater is communicated with the heat exchanger, the reformer is respectively communicated with the superheater and the heat exchanger, the cooler is communicated with the heat exchanger, the separator is respectively communicated with the cooler and the fuel tank, the pressure swing adsorption tower is communicated with the separator, the hydrogen storage tank is communicated with the pressure swing adsorption tower, the first pressure regulator is communicated with the pressure swing adsorption tower, the connecting pipe is communicated with the first pressure regulator, and the second pressure regulator is respectively communicated with the hydrogen storage tank and the connecting pipe.
2. The vehicle HT-PEMFC system integrated with MSR and ORC according to claim 1,
the HT-PEMFC subsystem comprises a hydrogen compressor, an interfacing tube, an HT-PEMFC stack, an anode heat exchanger, a cathode heat exchanger, an air compressor and a second pump;
the hydrogen compressor is communicated with the connecting pipe, the butt joint pipe is communicated with the reformer, the HT-PEMFC galvanic pile is respectively communicated with the hydrogen compressor, the superheater and the butt joint pipe, the anode heat exchanger is respectively communicated with the connecting pipe and the HT-PEMFC galvanic pile, the cathode heat exchanger is respectively communicated with the HT-PEMFC galvanic pile and the anode heat exchanger, the air compressor is communicated with the cathode heat exchanger, and the second pump is communicated with the butt joint pipe.
3. An in-vehicle HT-PEMFC system incorporating MSRs and ORCs as set forth in claim 2,
the ORC subsystem includes an evaporator, a turbine, a generator, a condenser, and a third pump;
the evaporator is respectively communicated with the second pump and the HT-PEMFC galvanic pile, the turbine is communicated with the evaporator, the generator is communicated with the turbine, the condenser is communicated with the turbine, and the third pump is respectively communicated with the evaporator and the condenser.
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| CN202310709227.2A CN116826121A (en) | 2023-06-15 | 2023-06-15 | Vehicle HT-PEMFC system integrating MSR and ORC |
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| CN202310709227.2A CN116826121A (en) | 2023-06-15 | 2023-06-15 | Vehicle HT-PEMFC system integrating MSR and ORC |
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