CN112803039A - Combined heat and power device and method - Google Patents
Combined heat and power device and method Download PDFInfo
- Publication number
- CN112803039A CN112803039A CN202011615866.5A CN202011615866A CN112803039A CN 112803039 A CN112803039 A CN 112803039A CN 202011615866 A CN202011615866 A CN 202011615866A CN 112803039 A CN112803039 A CN 112803039A
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- fuel cell
- exchange device
- reactor
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims description 31
- 239000000446 fuel Substances 0.000 claims abstract description 176
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 162
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 109
- 239000012528 membrane Substances 0.000 claims abstract description 106
- 239000003345 natural gas Substances 0.000 claims abstract description 71
- 229910001868 water Inorganic materials 0.000 claims abstract description 71
- 239000001257 hydrogen Substances 0.000 claims abstract description 66
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 66
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000002918 waste heat Substances 0.000 claims abstract description 33
- 238000002407 reforming Methods 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims description 78
- 238000002485 combustion reaction Methods 0.000 claims description 55
- 238000006243 chemical reaction Methods 0.000 claims description 45
- 239000000498 cooling water Substances 0.000 claims description 20
- 238000003487 electrochemical reaction Methods 0.000 claims description 19
- 238000000629 steam reforming Methods 0.000 claims description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 17
- 230000006835 compression Effects 0.000 claims description 16
- 238000007906 compression Methods 0.000 claims description 16
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 230000009466 transformation Effects 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 4
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 21
- 239000003570 air Substances 0.000 abstract description 2
- 238000003860 storage Methods 0.000 abstract description 2
- 239000002828 fuel tank Substances 0.000 abstract 1
- 230000015572 biosynthetic process Effects 0.000 description 11
- 238000003786 synthesis reaction Methods 0.000 description 11
- 230000000052 comparative effect Effects 0.000 description 9
- 238000010992 reflux Methods 0.000 description 9
- 239000008367 deionised water Substances 0.000 description 8
- 229910021641 deionized water Inorganic materials 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 238000010248 power generation Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000001991 steam methane reforming Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- 238000003541 multi-stage reaction Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007792 addition Methods 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
- F22B31/08—Installation of heat-exchange apparatus or of means in boilers for heating air supplied for combustion
-
- 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
-
- 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
-
- 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
- H01M8/04029—Heat exchange using liquids
-
- 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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Organic Chemistry (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- General Engineering & Computer Science (AREA)
- Fuel Cell (AREA)
Abstract
The invention provides a combined heat and power device, which comprises a fuel processing module, a proton exchange membrane fuel cell module, a fuel storage battery, a fuel tank, a fuel; the combined heat and power device also comprises a waste heat utilization module and an exhaust steam utilization module which are arranged in the fuel processing module and the proton exchange membrane fuel cell module; the waste heat utilization module and the dead steam utilization module can fully utilize waste heat and dead steam, so that the energy utilization rate is improved; the device outputs electric energy and multilevel heat energy by inputting natural gas, air and water, realizes multilevel and high-efficiency cogeneration and heat energy utilization, obtains domestic water with utilization value, and forms a clean and high-efficiency cogeneration household energy router system based on natural gas reforming hydrogen production and a fuel cell.
Description
Technical Field
The invention relates to the technical field of energy supply, in particular to a combined heat and power device and a method.
Background
The natural gas reforming hydrogen production technology comprises various modes such as steam methane reforming, autothermal oxidation reforming, partial oxidation, direct natural gas cracking and the like, wherein the steam reforming is a hydrogen production method widely applied at present, the process is mature, the device is reliable in operation, energy is saved, the environment is protected, and the method is the simplest and most economical hydrogen production method; however, the hydrogen production by steam reforming is a strong endothermic reaction, the heat supply of a required external heat source is usually completed by burning natural gas, and the combustion process can generate a large amount of high-temperature waste heat besides the reaction heat required by steam reforming, and the waste heat has high grade, and if the waste heat can be utilized, the utilization efficiency of energy is improved.
The proton exchange membrane fuel cell is used as a new generation energy system, and has the advantages of energy conservation, environmental protection, small occupied area, similar thermoelectric ratio and thermoelectric demand structure, quick start and high power generation efficiency, however, one of the raw materials required by the fuel cell, pure hydrogen limits the scale of the fuel cell to a certain extent due to the limitations of price, safety, storage, transportation and the like in various aspects, in particular to the application of household fuel cells; on the other hand, in practical application, the comprehensive utilization rate of fuel of the power generation system of the proton exchange membrane fuel cell is not high, mainly because the power generation efficiency of the proton exchange membrane fuel cell is influenced by various operation parameters, and simultaneously, a large amount of heat is generated in the power generation process, the waste heat of the part has low grade and is difficult to use, but the energy is larger and occupies about 40 to 60 percent of the total energy.
Scientific and technological workers at home and abroad carry out various researches on heat management and waste heat utilization of fuel cells, and main technical routes comprise waste heat heating, system preheating, waste heat refrigerating and the like. The technology of reforming the natural gas to produce hydrogen is combined with the power generation of the fuel cell, and a new mode of application and popularization of the fuel cell at the present stage is developed. Natural gas of a natural gas pipe network of cities and towns is used as a raw material to carry out reforming hydrogen production, hydrogen is directly supplied to a fuel cell system, various problems faced by pure hydrogen in practical use can be avoided, the natural gas and electric power have a peak regulation effect, the natural gas and the electric power are praised as fourth generation power generation following firepower, water power and nuclear power, and the natural gas and the electric power are particularly concerned by numerous scholars at home and abroad in the fields of distributed power generation, household cogeneration, mobile power supplies, traffic and the like, and have high use value and commercial value at present.
Therefore, it is necessary to develop a cogeneration device and method that can fully utilize the waste heat and the tail gas.
Disclosure of Invention
In view of the problems in the prior art, the invention provides a combined heat and power device, and particularly provides a combined heat and power household energy router based on natural gas reforming hydrogen production and a fuel cell, according to the principle of waste heat recovery and cascade utilization, working medium water is heated step by utilizing heat released by compression of an air compressor, waste heat of a proton exchange membrane fuel cell, and heat released in the processes of two-stage methanation reaction and water-vapor conversion reaction, and the combined heat and power household energy router based on natural gas reforming hydrogen production and the fuel cell is provided, so that heat in various links such as steam methane reforming reaction heat, waste heat of the proton exchange membrane fuel cell, waste heat of combustion tail gas and the like is scientifically, fully and efficiently exploited, the comprehensive utilization efficiency of energy is further improved, economic benefits are increased, and waste heat pollution is reduced.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the present invention provides a cogeneration apparatus, said cogeneration apparatus comprising a fuel processing module and a proton exchange membrane fuel cell module; the combined heat and power device also comprises a waste heat utilization module and an exhaust steam utilization module which are arranged in the fuel processing module and the proton exchange membrane fuel cell module; the dead steam utilization module comprises: and the anode outlet of the proton exchange membrane fuel cell module is connected with the pipeline of the fuel processing module.
The combined heat and power device provided by the invention is a combined heat and power household energy router based on natural gas reforming hydrogen production and fuel cells, natural gas directly comes from the existing urban gas supply pipe network, the self-heating of the system is realized through the oxidation reaction of methane, namely combustion coupling steam methane reforming, the hydrogen for the fuel cell is produced through the water-vapor transformation reaction and the two-stage methanation reaction, and electrochemically reacts with the processed air in the proton exchange membrane fuel cell stack to output electric power, simultaneously, the waste heat of the system is utilized to produce hot water, the cogeneration is realized, the heat released by the combustion tail gas and the multistage reaction is fully utilized as the energy source of natural gas, air, working medium water preheating and domestic hot water, the heat of the system is utilized in multiple stages, waste heat is collected and utilized as much as possible, and the heat pollution is reduced while the energy utilization efficiency is improved and resources are saved.
The natural gas enters the household through a city pipe network and is controlled by a valve to enter the combustion device, the natural gas is used as a fuel source of the combustion device to provide heat for the steam reforming reactor, meanwhile, the combustion device also receives anode exhaust gas from a proton exchange membrane fuel cell to participate in combustion, and the reactions of the formulas (1) and (2) are carried out:
CH4+2O2→CO2+2H2O (1)
H2+1/2O2→H2O (2)
preferably, the fuel processing module comprises a combustion unit and a natural gas reforming unit connected in series.
Preferably, the combustion unit comprises a combustion device.
Preferably, the combustion device is connected with the first natural gas conveying pipeline.
Preferably, the combustion device is connected to a first air delivery conduit.
Preferably, the natural gas reforming unit includes a first reactor, a second reactor and a third reactor connected in sequence.
Preferably, the first reactor is connected to the outlet of the combustion device.
Preferably, the first reactor is a steam reforming reactor.
Preferably, the second reactor is a water-gas shift reactor.
Preferably, the third reactor is a methanation reactor, preferably a two-stage methanation reactor.
Hydrogen of the proton exchange membrane fuel cell is derived from steam methane reforming, a raw material is provided based on the existing urban natural gas pipe network, a part of methane is combusted to generate a large amount of heat to be provided for steam reforming reaction, water vapor is simultaneously prepared, fuel gas obtained by the other part of methane after the steam reforming reaction is subjected to water vapor shift reaction and two-stage methanation reaction, so that the content of carbon monoxide in the mixed gas is reduced to 10ppm, even below 1ppm, hydrogen-rich gas meeting the technical requirements of the fuel cell is obtained, and a hydrogen source is provided for the proton exchange membrane fuel cell.
The steam reforming reaction takes place in the reaction of formula (3):
CH4+H2O→CO+3H2 (3)
the water-gas shift reaction is to reduce the content of CO, the synthesis gas comprises hydrogen, carbon monoxide, methane, carbon dioxide, water vapor and nitrogen, and the reaction formula is shown as (4):
CO+H2O→H2+CO2 (4)
the CO content in the synthesis gas after the water-vapor shift reaction still does not meet the requirements of the proton exchange membrane fuel cell, the synthesis gas enters the two-stage methanation reactor after being cooled to a certain temperature to generate a (5) type reaction, the CO is further removed, the CO concentration is controlled to be 10ppm or even below 1ppm, and hydrogen-rich gas meeting the technical requirements of the fuel cell is obtained and comprises hydrogen, carbon monoxide, methane, carbon dioxide, water vapor and nitrogen:
CO+3H2→CH4+H2O (5)
preferably, a first heat exchange device is arranged between the first reactor and the second reactor.
Preferably, a second heat exchange device is arranged between the second reactor and the third reactor.
Preferably, the outlet of the third reactor is connected with a third heat exchange device.
Preferably, the first medium outlet of the third heat exchange device is connected with a proton exchange membrane fuel cell module.
Preferably, the natural gas reforming unit further comprises a steam generation unit disposed before the first reactor.
Preferably, the steam generating unit comprises a steam generating device and a fourth heat exchanging device connected with an outlet of the steam generating device.
Preferably, the inlet of the steam generating device is connected to the first water conveying pipe.
Preferably, the inlet of the steam generating device is connected with the heat exchange medium outlet of the first reactor.
Preferably, the outlet of the steam generating device is connected to the reaction mass inlet of the first reactor.
Preferably, the first medium inlet of the fourth heat exchange device is connected with a steam generating device.
Preferably, the first medium outlet of the fourth heat exchange device is connected with a fifth heat exchange device.
Preferably, the second medium inlet of the fourth heat exchange device is connected with a second natural gas conveying pipeline.
Preferably, the second medium outlet of the fourth heat exchange device is connected with the first reactor.
Preferably, the first medium inlet of the fifth heat exchange device is connected with the heat exchange medium outlet of the first heat exchange device.
Preferably, the second medium inlet of the fifth heat exchange device is connected with the fourth heat exchange device.
Preferably, the proton exchange membrane fuel cell module comprises a proton exchange membrane fuel cell.
And (3) allowing hydrogen-rich gas to enter the proton exchange membrane fuel cell and carrying out electrochemical reaction, wherein the formula (6) is as follows:
H2→2H++2e- (6)
preferably, the proton exchange membrane fuel cell is provided with an anode inlet, an anode outlet, a cathode inlet, a cathode outlet, a cooling water inlet and a cooling water outlet.
Preferably, the anode inlet of the proton exchange membrane fuel cell is connected with the second medium outlet of the third heat exchange device.
Preferably, the anode outlet of the proton exchange membrane fuel cell is connected with the anode inlet through an anode return device.
The dead steam at the anode outlet of the proton exchange membrane fuel cell is connected with the anode inlet through an anode reflux device (generally a reflux pump), so that the reflux and the reutilization of the anode gas are realized.
Preferably, the anode outlet is also connected to a combustion device.
Preferably, the anode outlet is also connected with a gas release valve.
Preferably, the proton exchange membrane fuel cell module further comprises a sixth heat exchange device connected with the proton exchange membrane fuel cell.
Preferably, the first medium inlet of the sixth heat exchange device is connected with the second water conveying pipeline.
Preferably, the first medium outlet of the sixth heat exchange device is connected with the first medium inlet of the third heat exchange device.
Preferably, the second medium inlet of the sixth heat exchange device is connected with the cooling water outlet of the proton exchange membrane fuel cell.
Preferably, the second medium outlet of the sixth heat exchange device is connected with the cooling water inlet of the proton exchange membrane fuel cell.
In order to maintain the optimal working temperature to ensure the normal operation of the fuel cell system, the heat generated by the electrochemical reaction needs to be released in time, and the waste heat is recovered, the sixth heat exchange device exchanges heat with the deionized water, so that the requirement of the initial temperature when the deionized water is used as the cooling water of the pile can be met, the heated deionized water can be cooled, and after the heat exchange of the sixth heat exchange device, the heat is used for heating the air introduced into the fuel cell in the seventh heat exchange device through the circulation of the working medium water.
Preferably, the proton exchange membrane fuel cell module further comprises a humidifier connected to the proton exchange membrane fuel cell.
Preferably, the humidifier is a proton exchange membrane humidifier, and other humidification methods such as bubbling humidification and spraying can also be selected.
Preferably, the steam exhaust inlet of the humidifier is connected with the cathode outlet of the proton exchange membrane fuel cell.
Preferably, the gas inlet of the humidifier is connected with a gas compression device.
Preferably, seventh heat exchange means is provided between the humidifier and the gas compression means.
After the air is heated through the gas compression device and the seventh heat exchange device, the air is mixed with tail gas of the cathode reaction of the proton exchange membrane fuel cell through the humidifier, so that the air humidity is improved, and wet air enters the cathode side of the proton exchange membrane fuel cell to generate electrochemical reaction, as shown in formula (7):
O2+4H++4e-→2H2O (7)
preferably, the first medium inlet of the seventh heat exchange device is connected with the first medium outlet of the sixth heat exchange device.
Preferably, the first medium outlet of the seventh heat exchange device is connected with the first medium inlet of the third heat exchange device.
Preferably, the second medium inlet of the seventh heat exchange device is connected with the gas compression device, and the second medium outlet is connected with the gas inlet of the humidifier.
Preferably, the humidifier is provided with a gas outlet.
Preferably, the gas outlet of the humidifier is connected to the cathode inlet of the proton exchange membrane fuel cell.
Preferably, the waste heat utilization module comprises a heat exchange medium conveying pipeline which is sequentially connected with a sixth heat exchange device, a seventh heat exchange device, a third heat exchange device, a second heat exchange device, a first heat exchange device and a fifth heat exchange device.
The waste heat utilization module comprises: energy level matching and energy gradient utilization among reactors in the fuel processing module; heat exchange between the domestic water and the air compressor, the cooling water of the proton exchange membrane fuel cell and the combustion tail gas of the fuel processing unit; specifically, water from outside the system is heated to hot water with a certain temperature through the sixth heat exchange device, the seventh heat exchange device, the third heat exchange device, the second heat exchange device, the first heat exchange device and the fifth heat exchange device, and the hot water is used for providing domestic hot water and hot water for heating; the water is utilized to play a role in cooling, the temperature requirement of step-by-step reaction is met, meanwhile, the self reaction energy of the collecting system is used for heating working medium water step by step, hot water is generated and used for heating and domestic hot water, compared with the traditional domestic hot water supply method, the energy consumption can be reduced, the waste heat in the reaction process of the collecting system is used, and the comprehensive efficiency of system energy is equivalently improved.
Preferably, the heat exchange medium conveying pipeline is respectively connected with a first medium inlet and a first medium outlet of a sixth heat exchange device, a seventh heat exchange device, a third heat exchange device, a second heat exchange device, a first heat exchange device and a fifth heat exchange device in sequence.
Preferably, the dead steam utilization device further comprises: a return pipeline connected with the anode outlet and the anode inlet, and an anode return device.
In a second aspect, the present invention provides a cogeneration method, which is performed using the cogeneration apparatus of the first aspect.
Preferably, the method comprises: in the fuel processing module, natural gas and air are mixed and combusted to generate heat energy, and simultaneously, the generated carbon dioxide and water are sequentially subjected to steam reforming, water-vapor conversion and methanation to obtain a gas phase containing hydrogen.
And the gas phase containing the hydrogen enters a proton exchange membrane fuel cell module for electrochemical reaction to generate electric energy.
And tail gas generated by the proton exchange membrane fuel cell module enters the fuel processing module for tail gas utilization.
Preferably, the method comprises the steps of:
(1) the natural gas and air enter a combustion device for mixed combustion, the generated carbon dioxide and water sequentially enter a first reactor for steam reforming reaction, enter a second reactor for steam-water transformation reaction and enter a third reactor for methanation reaction, and hydrogen-rich gas meeting the requirements of proton exchange membrane fuel is obtained;
(2) the gas phase containing hydrogen enters the proton exchange membrane fuel cell from the anode inlet, air enters the proton exchange membrane fuel cell from the cathode inlet to perform electrochemical reaction to generate electric energy, and deionized water enters the proton exchange membrane fuel cell from the cooling water inlet;
and (3) enabling a first part of the anode exhaust generated by the electrochemical reaction in the step (2) to enter a combustion device to be subjected to mixed combustion with the natural gas and the air in the step (1).
Preferably, the working medium water in the step (1) enters a steam generating device for steam generation.
Preferably, the heat exchange medium subjected to heat exchange in the first reactor in the step (1) enters a steam generating device for steam generation.
Preferably, a first part of the steam generated in step (1) enters the first reactor, and a second part exchanges heat with the natural gas through a fourth heat exchange device.
Preferably, the air in the step (2) enters the proton exchange membrane fuel cell from the cathode inlet after being compressed by the air compression device, heat exchanged by the seventh heat exchange device and humidified by the humidifier in sequence.
Preferably, the effluent generated by the electrochemical reaction in the step (2) is subjected to heat exchange by a sixth heat exchange device and then is circulated to the proton exchange membrane fuel cell from a cooling water inlet.
Preferably, the second portion of the electrochemically generated anode exhaust of step (2) is recycled to the anode inlet for electrochemical reaction.
Preferably, the electrochemically generated third portion of the anode exhaust of step (2) is directly exhausted.
Preferably, the electrochemically generated cathode exhaust steam in the step (2) enters a humidifier to humidify air.
Preferably, the heat exchange medium sequentially passes through the sixth heat exchange device, the seventh heat exchange device, the third heat exchange device, the second heat exchange device, the first heat exchange device and the fifth heat exchange device to perform gradual heat exchange.
As a preferable technical scheme of the invention, the method comprises the following steps:
(1) when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the fuel processing module starts to work, natural gas enters the combustion device and is mixed with air to be combusted as a fuel source of the combustion device, and heat is provided for the first reactor, namely the steam reforming reactor; the exhaust steam discharged from the first reactor enters a steam generating device, the heat of the exhaust steam discharged from the first reactor converts water into water steam, and the residual exhaust steam is preheated by a fourth heat exchange device and enters the natural gas of the first reactor;
after being heated by the fourth heat exchange device, the natural gas is mixed with the water vapor generated by the steam generation device and enters the first reactor to react to generate synthesis gas;
the synthesis gas is cooled by the first heat exchange device and then enters a second reactor, namely a water-vapor shift reactor, so that a water-vapor shift reaction is carried out, the CO content is reduced, and the hydrogen content is increased;
after the water-vapor shift reaction, the temperature is reduced by a second heat exchange device, and then the water-vapor shift reaction enters a third reactor, namely a two-stage methanation reactor, so that CO is further removed; after the discharge of the third reactor is cooled by a third heat exchange device, hydrogen enters a proton exchange membrane fuel cell to carry out electrochemical reaction;
(2) when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the proton exchange membrane fuel cell module starts to work, and air is introduced into the proton exchange membrane fuel cell to supply oxygen for electrochemical reaction after being compressed by the gas compression device, heated by the seventh heat exchange device and humidified by the humidifier in sequence; reacting oxygen with the hydrogen introduced into the proton exchange membrane fuel cell from the third heat exchange device in the step (1), wherein the hydrogen and the oxygen provide electric energy after the reaction;
(3) when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the waste heat utilization module starts to work, the water supply pipeline is connected with the sixth heat exchange device to cool the deionized water, then the working medium has two paths of water, one path of water is connected with the seventh heat exchange device, and the air is primarily heated by the seventh heat exchange device; the other path of the water is connected with a third heat exchange device, sequentially passes through a third reactor, a second heat exchange device, a second reactor, a first heat exchange device and a fifth heat exchange device, and working medium water is used as cooling water to cool each reactor and is heated step by step at the same time, and finally, the working medium water is supplied to domestic water through the fifth heat exchange device;
deionized water independently circulates in the corresponding pipeline, is cooled by the sixth heat exchange device, is introduced into the proton exchange membrane fuel cell to cool the proton exchange membrane fuel cell, flows out of the proton exchange membrane fuel cell and enters the sixth heat exchange device to exchange heat and cool;
(4) when the cogeneration device based on natural gas reforming hydrogen production and the fuel cell starts to operate, the dead steam utilization module starts to work, as shown in fig. 2, the dead steam exhausted from the proton exchange membrane fuel cell is divided into three parts, wherein one part of the dead steam generated by the anode is mixed with hydrogen-rich gas led to the anode inlet through the anode reflux device and then enters the anode of the fuel cell again to provide hydrogen, and the second part is led into the combustion device through the exhaust outlet to participate in combustion; the third part is discharged through a vent valve connected with the anode outlet;
and tail gas generated by the cathode is exhausted after the air communicated to the cathode of the proton exchange membrane fuel cell is heated and humidified by the humidifier.
Compared with the prior art, the invention has at least the following beneficial effects:
(1) the combined heat and power device provided by the invention can be used for inputting natural gas, air and water, outputting multi-quality electric power and thermal products such as electric power, hot water and hot steam and the like, and realizing combined heat and power;
(2) the cogeneration device provided by the invention utilizes the existing town natural gas pipe network, combines the water-steam transformation reaction, the methanation reaction and the exothermic oxidation reaction on the basis of the water-steam reforming technology to produce the hydrogen-rich gas, solves the bottleneck problems that the price of pure hydrogen is high, the transportation is difficult and the like which restrict the wide application of the proton exchange membrane fuel cell, and promotes the cogeneration of the fuel cell to the family for use, so that the energy supply of the family is free, integrated and energy-saving;
(3) the cogeneration device provided by the invention heats working medium water step by utilizing the waste heat of the proton exchange membrane fuel cell and the energy emitted in the processes of two-stage methanation reaction and water-vapor transformation reaction according to the principle of waste heat recovery and cascade utilization, fully collects and utilizes the heat of each link, and further improves the comprehensive utilization efficiency of energy;
(4) the combined heat and power device provided by the invention fully collects the waste heat of the proton exchange membrane fuel cell by utilizing the anode reflux device and the humidifier, and the exhaust steam is used as a humidifying source and a heating source, so that the device is a simple and practical self-humidifying mode of the proton exchange membrane fuel cell, is respectively mixed with the hydrogen and the air introduced into the fuel cell, and recycles the exhaust steam, so that the hydrogen in the mixed gas is fully utilized, and potential safety hazards caused by directly discharging the hydrogen contained in the exhaust steam are avoided;
(5) the combined heat and power method provided by the invention fully utilizes the heat released by combustion tail gas and multistage reaction as the energy source of natural gas, air, working medium water preheating and domestic hot water, and performs multistage utilization on the heat of the system, collects and utilizes waste heat as much as possible, improves the energy utilization efficiency, saves resources and reduces heat pollution at the same time.
Drawings
Fig. 1 is a schematic diagram of a fuel processing module in a cogeneration apparatus according to embodiment 1 of the present invention.
Fig. 2 is a schematic view of a proton exchange membrane fuel cell module in the cogeneration apparatus according to example 1 of the present invention.
Fig. 3 is an overall schematic view of the cogeneration device according to embodiment 1 of the present invention.
In the figure: 1011-a first air delivery duct; 1012-a second air delivery conduit; 1021-a first natural gas delivery pipeline; 1022-a second natural gas transportation pipeline; 1031-a first water delivery conduit; 1032-a second water delivery conduit; 104-a steam exhaust water supply pipeline; 11-a combustion device; 12-a first reactor; 13-a second reactor; 14-a third reactor; 15-a steam generating device; 21-proton exchange membrane fuel cell; 22-a gas compression device; 23-a humidifier; 24-anode return means; 31-first heat exchange means; 32-second heat exchange means; 33-third heat exchange means; 34-fourth heat exchange means; 35-a fifth heat exchange means; 36-a sixth heat exchange means; 37-seventh heat exchange means.
Detailed Description
The technical scheme of the invention is further explained by the specific implementation mode in combination with the attached drawings.
The present invention is described in further detail below. The following examples are merely illustrative of the present invention and do not represent or limit the scope of the claims, which are defined by the claims.
First, examples and comparative examples
Example 1
The present embodiment provides a cogeneration device, as shown in fig. 1 to 3, the cogeneration device includes a fuel processing module and a proton exchange membrane fuel cell module;
the cogeneration device also comprises a waste heat utilization module and an exhaust steam utilization module which are arranged in the fuel processing module and the proton exchange membrane fuel cell module.
The fuel processing module comprises a combustion unit and a natural gas reforming unit which are sequentially connected; the combustion unit comprises a combustion device 11; the combustion device 11 is connected with a first natural gas conveying pipeline 1021; the combustion device 11 is connected with a first air conveying pipeline 1011; the natural gas reforming unit comprises a first reactor 12, a second reactor 13 and a third reactor 14 which are connected in sequence; the first reactor 12 is connected with the outlet of the combustion device 11; the first reactor 12 is a steam reforming reactor; the second reactor 13 is a water-gas shift reactor; the third reactor 14 is a two-stage methanation reactor; a first heat exchange device 31 is arranged between the first reactor 12 and the second reactor 13; a second heat exchange device 32 is arranged between the second reactor 13 and the third reactor 14; the outlet of the third reactor 14 is connected with a third heat exchange device 33. And a first medium outlet of the third heat exchange device 33 is connected with the proton exchange membrane fuel cell module.
The natural gas reforming unit further comprises a steam generation unit disposed before the first reactor 12; the steam generating unit comprises a steam generating device 15 and a fourth heat exchanging device 34 connected with an outlet of the steam generating device 15; the inlet of the steam generating device 15 is connected with a first water delivery pipe 1031; the inlet of the steam generating device 15 is connected with the heat exchange medium outlet of the first reactor 12; the outlet of the steam generating device 15 is connected with the reaction material inlet of the first reactor 12; the first medium inlet of the fourth heat exchange device 34 is connected with the steam generating device 15; a fifth heat exchange device 35 is connected to a first medium outlet of the fourth heat exchange device 34; a second medium inlet of the fourth heat exchange device 34 is connected with a second natural gas conveying pipeline 1022; a second medium outlet of the fourth heat exchange device 34 is connected with the first reactor 12; the first medium inlet of the fifth heat exchange device 35 is connected with the heat exchange medium outlet of the first heat exchange device 31; a second medium inlet of the fifth heat exchange device 35 is connected with the fourth heat exchange device 34, and a second medium outlet of the fifth heat exchange device 35 is connected with the waste steam water supply pipeline 104.
The proton exchange membrane fuel cell module includes a proton exchange membrane fuel cell 21; the proton exchange membrane fuel cell 21 is provided with an anode inlet, an anode outlet, a cathode inlet, a cathode outlet, a cooling water inlet and a cooling water outlet; the anode inlet of the proton exchange membrane fuel cell 21 is connected with the second medium outlet of the third heat exchange device 33; the anode outlet of the proton exchange membrane fuel cell 21 is connected with the anode inlet; an anode return device 24 is arranged between the anode outlet and the anode inlet; the anode reflux device 24 is a reflux pump, and the anode outlet is also connected with the combustion device 11; and the outlet of the anode is also connected with a deflation valve.
The proton exchange membrane fuel cell module further comprises a sixth heat exchange device 36 connected with the proton exchange membrane fuel cell 21; the first medium inlet of the sixth heat exchange device 36 is connected with a second water conveying pipeline 1032; the first medium outlet of the sixth heat exchange device 36 is connected with the first medium inlet of the third heat exchange device 33; a second medium inlet of the sixth heat exchange device 36 is connected with a cooling water outlet of the proton exchange membrane fuel cell 21; the second medium outlet of the sixth heat exchange device 36 is connected with the cooling water inlet of the proton exchange membrane fuel cell 21.
The proton exchange membrane fuel cell module further comprises a humidifier 23 connected with the proton exchange membrane fuel cell 21; the exhaust steam inlet of the humidifier 23 is connected with the cathode outlet of the proton exchange membrane fuel cell 21; a gas inlet of the humidifier 23 is connected with a gas compression device 22; a seventh heat exchange device 37 is arranged between the humidifier 23 and the gas compression device 22; the first medium inlet of the seventh heat exchange device 37 is connected with the first medium outlet of the sixth heat exchange device 36; the first medium outlet of the seventh heat exchange device 37 is connected with the first medium inlet of the third heat exchange device 33; a second medium inlet of the seventh heat exchange device 37 is connected with the gas compression device 22, and a second medium outlet is connected with a gas inlet of the humidifier 23; the humidifier 23 is provided with a gas outlet; the gas outlet of the humidifier 23 is connected with the cathode inlet of the proton exchange membrane fuel cell 21; a second air delivery conduit 1012 is connected to the humidifier 23.
The waste heat utilization module comprises a heat exchange medium conveying pipeline which is sequentially connected with a sixth heat exchange device 36, a seventh heat exchange device 37, a third heat exchange device 33, a second heat exchange device 32, a first heat exchange device 31 and a fifth heat exchange device 35; the heat exchange medium conveying pipeline is respectively connected with a first medium inlet and a first medium outlet of a sixth heat exchange device 36, a seventh heat exchange device 37, a third heat exchange device 33, a second heat exchange device 32, a first heat exchange device 31 and a fifth heat exchange device 35 in sequence.
Example 2
This example provides a cogeneration device which is the same as that of example 1 except that the anode outlet is not connected to the anode inlet and an anode return device is not provided therebetween.
Example 3
This example provides a cogeneration device, which is the same as that of example 1 except that the inlet of the steam generator is not connected to the outlet of the heat exchange medium of the first reactor.
Example 4
The embodiment provides a cogeneration device, which is the same as the embodiment 1 except that the fourth heat exchange device is not arranged and the outlet of the steam generating device is directly connected with the fifth heat exchange device.
Comparative example 1
This comparative example provides a cogeneration unit which is the same as that of example 1 except that the anode outlet is not connected to the combustion apparatus.
Second, application example and application comparative example
Application example 1
The application example provides a cogeneration method, which is performed by using the cogeneration device provided in embodiment 1, and specifically includes the following steps:
(1) when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the fuel processing module starts to work, natural gas enters the combustion device and is mixed with air to be combusted as a fuel source of the combustion device, and heat is provided for the first reactor, namely the steam reforming reactor; the exhaust steam discharged from the first reactor enters a steam generating device, the heat of the exhaust steam discharged from the first reactor converts water into water steam, and the residual exhaust steam is preheated by a fourth heat exchange device and enters the natural gas of the first reactor;
after being heated by the fourth heat exchange device, the natural gas is mixed with the water vapor generated by the steam generation device and enters the first reactor to react to generate synthesis gas;
the synthesis gas is cooled by the first heat exchange device and then enters a second reactor, namely a water-vapor shift reactor, so that a water-vapor shift reaction is carried out, the CO content is reduced, and the hydrogen content is increased;
after the water-vapor shift reaction, the temperature is reduced by a second heat exchange device, and then the water-vapor shift reaction enters a third reactor, namely a two-stage methanation reactor, so that CO is further removed; after the discharge of the third reactor is cooled by a third heat exchange device, hydrogen enters a proton exchange membrane fuel cell to carry out electrochemical reaction;
(2) when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the proton exchange membrane fuel cell module starts to work, and air is introduced into the proton exchange membrane fuel cell to supply oxygen for electrochemical reaction after being compressed by the gas compression device, heated by the seventh heat exchange device and humidified by the humidifier in sequence; reacting oxygen with the hydrogen introduced into the proton exchange membrane fuel cell from the third heat exchange device in the step (1), wherein the hydrogen and the oxygen provide electric energy after the reaction;
(3) when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the waste heat utilization module starts to work, the water supply pipeline is connected with the sixth heat exchange device to cool the deionized water, then the working medium has two paths of water, one path of water is connected with the seventh heat exchange device, and the air is primarily heated by the seventh heat exchange device; the other path of the water is connected with a third heat exchange device, sequentially passes through a third reactor, a second heat exchange device, a second reactor, a first heat exchange device and a fifth heat exchange device, and working medium water is used as cooling water to cool each reactor and is heated step by step at the same time, and finally, the working medium water is supplied to domestic water through the fifth heat exchange device;
deionized water independently circulates in the corresponding pipeline, is cooled by the sixth heat exchange device, is introduced into the proton exchange membrane fuel cell to cool the proton exchange membrane fuel cell, flows out of the proton exchange membrane fuel cell and enters the sixth heat exchange device to exchange heat and cool;
(4) when the cogeneration device based on natural gas reforming hydrogen production and the fuel cell starts to operate, the dead steam utilization module starts to work, and the dead steam exhausted from the proton exchange membrane fuel cell is divided into three parts, wherein one part of the dead steam generated by the anode is mixed with hydrogen-rich gas led to the anode inlet through the anode reflux device and then enters the anode of the fuel cell again to provide hydrogen, and the second part of the dead steam is led into the combustion device through the exhaust outlet to participate in combustion; the third part is discharged through a vent valve connected with the anode outlet;
and tail gas generated by the cathode is exhausted after the air communicated to the cathode of the proton exchange membrane fuel cell is heated and humidified by the humidifier.
Application example 2
The application example provides a combined heat and power method, which is implemented by adopting the combined heat and power device provided in the embodiment 2, specifically, the method only divides the dead steam exhausted from the proton exchange membrane fuel cell in the step (3) into two parts, and the first part is introduced into a combustion device through an exhaust outlet to participate in combustion; the second part was discharged through a purge valve connected to the anode outlet, and the rest was the same as in application example 1.
Application example 3
The application example provides a combined heat and power method, the method is carried out by adopting the combined heat and power device provided by the embodiment 3, and concretely, the method is the same as the application example 1 except that the dead steam discharged by the first reactor in the step (1) does not enter the steam generating device.
Specifically, step (1): when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the fuel processing module starts to work, natural gas enters the combustion device and is mixed with air to be combusted as a fuel source of the combustion device, and heat is provided for the first reactor, namely the steam reforming reactor; preheating natural gas entering the first reactor by exhaust steam discharged from the first reactor through a fourth heat exchange device;
after being heated by the fourth heat exchange device, the natural gas is mixed with the water vapor generated by the steam generation device and enters the first reactor to react to generate synthesis gas;
the synthesis gas is cooled by the first heat exchange device and then enters a second reactor, namely a water-vapor shift reactor, so that a water-vapor shift reaction is carried out, and the content of CO is reduced;
after the water-vapor shift reaction, the temperature is reduced by a second heat exchange device, and the water-vapor shift reaction enters a third reactor, namely a two-stage methanation reactor, so that CO is further removed, and hydrogen is generated; and after the discharged material of the third reactor is cooled by the third heat exchange device, hydrogen enters the proton exchange membrane fuel cell to carry out electrochemical reaction.
Application example 4
The present application example provides a cogeneration method, which is performed by using the cogeneration device provided in example 4, and the rest is the same as in application example 1, specifically, step (1):
when the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell starts to operate, the fuel processing module starts to work, natural gas enters the combustion device and is mixed with air to be combusted as a fuel source of the combustion device, and heat is provided for the first reactor, namely the steam reforming reactor; the dead steam discharged from the first reactor enters a steam generating device, the heat of the dead steam discharged from the first reactor converts water into water steam, and the residual dead steam provides domestic water through a fifth heat exchange device;
the natural gas directly enters the first reactor, is mixed with the water vapor generated by the steam generating device and enters the first reactor, and reacts to generate synthesis gas;
the synthesis gas is cooled by the first heat exchange device and then enters a second reactor, namely a water-vapor shift reactor, so that a water-vapor shift reaction is carried out, and the content of CO is reduced;
after the water-vapor shift reaction, the temperature is reduced by a second heat exchange device, and the water-vapor shift reaction enters a third reactor, namely a two-stage methanation reactor, so that CO is further removed, and hydrogen is generated; and after the discharged material of the third reactor is cooled by the third heat exchange device, hydrogen enters the proton exchange membrane fuel cell to carry out electrochemical reaction.
Application comparative example 1
The application comparative example provides a combined heat and power method, the method is carried out by adopting the combined heat and power device provided by the comparative example 1, the rest is the same as the application example 1, and specifically, the step (4):
when the cogeneration device based on natural gas reforming hydrogen production and the fuel cell starts to operate, the dead steam utilization module starts to work, the dead steam exhausted from the proton exchange membrane fuel cell is divided into two parts, wherein one part of the dead steam generated by the anode is mixed with hydrogen-rich gas led to the anode inlet through the anode reflux device and then enters the anode of the fuel cell again to provide hydrogen; the second part is discharged through a vent valve connected with the anode outlet;
and tail gas generated by the cathode is exhausted after the air communicated to the cathode of the proton exchange membrane fuel cell is heated and humidified by the humidifier.
It can be seen from the comprehensive application example 1 and the application comparative example 1 that the exhaust gas can be fully utilized to burn in the application example 1, and the exhaust gas can be used as an energy source for preheating natural gas, air and working medium water and domestic hot water, so that compared with the application comparative example 1, the energy utilization efficiency is improved, resources are saved, and meanwhile, heat pollution can be reduced.
It can be seen from the comprehensive application examples 1 and 2 that the anode exhaust steam in the application example 1 can be partially circulated and effectively utilized as a hydrogen source, while the heat of the anode exhaust steam in the application example 2 cannot be fully utilized, and the potential safety hazard caused by directly discharging hydrogen contained in the exhaust steam is also avoided in the application example 1.
It can be seen from the combination of application example 1 and application example 3 that, compared with application example 3, application example 1 is more beneficial to fully utilizing the heat of the high-grade exhaust steam generated in the first reactor, and the energy utilization efficiency is higher.
It can be seen from the comprehensive application examples 1 and 4 that the dead steam discharged by the steam generator in the application example 1 can be fully utilized, while the dead steam discharged by the steam generator in the application example 4 is directly supplied to domestic water, which is more favorable for realizing reasonable utilization of high-grade heat in the application example 1.
In conclusion, the cogeneration device based on the natural gas reforming hydrogen production and the fuel cell provided by the invention has the advantages of high energy utilization efficiency, energy conservation, improvement of system economy and degree of freedom while eliminating thermal pollution and wide application prospect.
The applicant declares that the present invention illustrates the detailed structural features of the present invention through the above embodiments, but the present invention is not limited to the above detailed structural features, that is, it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be understood by those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, additions of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.
Claims (10)
1. A cogeneration apparatus, said cogeneration apparatus comprising a fuel processing module and a proton exchange membrane fuel cell module;
the combined heat and power device also comprises a waste heat utilization module and an exhaust steam utilization module which are arranged in the fuel processing module and the proton exchange membrane fuel cell module;
the dead steam utilization module comprises: and the anode outlet of the proton exchange membrane fuel cell module is connected with the pipeline of the fuel processing module.
2. The cogeneration device of claim 1, wherein said fuel processing module comprises a combustion unit and a natural gas reforming unit connected in series;
preferably, the combustion unit comprises a combustion device;
preferably, the combustion device is connected with a first natural gas conveying pipeline;
preferably, the combustion device is connected with a first air conveying pipeline;
preferably, the natural gas reforming unit comprises a first reactor, a second reactor and a third reactor which are connected in sequence;
preferably, the first reactor is connected to the outlet of the combustion device;
preferably, the first reactor is a steam reforming reactor;
preferably, the second reactor is a water-gas shift reactor;
preferably, the third reactor is a methanation reactor, preferably a two-stage methanation reactor;
preferably, a first heat exchange device is arranged between the first reactor and the second reactor;
preferably, a second heat exchange device is arranged between the second reactor and the third reactor;
preferably, the outlet of the third reactor is connected with a third heat exchange device;
preferably, the first medium outlet of the third heat exchange device is connected with a proton exchange membrane fuel cell module.
3. The cogeneration device of claim 2, wherein said natural gas reforming unit further comprises a steam generation unit disposed before the first reactor;
preferably, the steam generating unit comprises a steam generating device and a fourth heat exchanging device connected with an outlet of the steam generating device;
preferably, the inlet of the steam generating device is connected with a first water conveying pipeline;
preferably, the inlet of the steam generating device is connected with the heat exchange medium outlet of the first reactor;
preferably, the outlet of the steam generating device is connected with the reaction material inlet of the first reactor;
preferably, the first medium inlet of the fourth heat exchange device is connected with a steam generating device;
preferably, a first medium outlet of the fourth heat exchange device is connected with a fifth heat exchange device;
preferably, a second medium inlet of the fourth heat exchange device is connected with a second natural gas conveying pipeline;
preferably, the second medium outlet of the fourth heat exchange device is connected with the first reactor;
preferably, the first medium inlet of the fifth heat exchange device is connected with the heat exchange medium outlet of the first heat exchange device;
preferably, the second medium inlet of the fifth heat exchange device is connected with the fourth heat exchange device.
4. The cogeneration device of any one of claims 1 to 3, wherein said PEM fuel cell module comprises a PEM fuel cell;
preferably, the proton exchange membrane fuel cell is provided with an anode inlet, an anode outlet, a cathode inlet, a cathode outlet, a cooling water inlet and a cooling water outlet;
preferably, an anode inlet of the proton exchange membrane fuel cell is connected with a second medium outlet of the third heat exchange device;
preferably, the anode outlet of the proton exchange membrane fuel cell is connected with the anode inlet through an anode return device;
preferably, the anode outlet is also connected with a combustion device;
preferably, the anode outlet is also connected with a gas release valve.
5. The cogeneration device according to any one of claims 1 to 4, wherein said PEM fuel cell module further comprises a sixth heat exchange device connected to a PEM fuel cell;
preferably, the first medium inlet of the sixth heat exchange device is connected with a second water conveying pipeline;
preferably, the first medium outlet of the sixth heat exchange device is connected with the first medium inlet of the third heat exchange device;
preferably, the second medium inlet of the sixth heat exchange device is connected with the cooling water outlet of the proton exchange membrane fuel cell;
preferably, the second medium outlet of the sixth heat exchange device is connected with the cooling water inlet of the proton exchange membrane fuel cell.
6. The cogeneration device according to any one of claims 1 to 5, wherein said PEM fuel cell module further comprises a humidifier connected to the PEM fuel cell;
preferably, the steam exhaust inlet of the humidifier is connected with the cathode outlet of the proton exchange membrane fuel cell;
preferably, a gas inlet of the humidifier is connected with a gas compression device;
preferably, a seventh heat exchange device is arranged between the humidifier and the gas compression device;
preferably, the first medium inlet of the seventh heat exchange device is connected with the first medium outlet of the sixth heat exchange device;
preferably, the first medium outlet of the seventh heat exchange device is connected with the first medium inlet of the third heat exchange device;
preferably, the second medium inlet of the seventh heat exchange device is connected with the gas compression device, and the second medium outlet is connected with the gas inlet of the humidifier;
preferably, the humidifier is provided with a gas outlet;
preferably, the gas outlet of the humidifier is connected to the cathode inlet of the proton exchange membrane fuel cell.
7. The cogeneration device according to any one of claims 1 to 6, wherein the waste heat utilization module comprises a heat exchange medium conveying pipeline which is sequentially connected with a sixth heat exchange device, a seventh heat exchange device, a third heat exchange device, a second heat exchange device, a first heat exchange device and a fifth heat exchange device;
preferably, the heat exchange medium conveying pipeline is respectively connected with a first medium inlet and a first medium outlet of a sixth heat exchange device, a seventh heat exchange device, a third heat exchange device, a second heat exchange device, a first heat exchange device and a fifth heat exchange device in sequence.
8. A cogeneration method, characterized in that said method is carried out using the cogeneration apparatus according to any one of claims 1 to 7.
9. The method of claim 8, wherein the method comprises: in the fuel processing module, natural gas and air are mixed and combusted to generate heat energy, and simultaneously, the generated carbon dioxide and water are sequentially subjected to steam reforming, water-vapor conversion and methanation to obtain a gas phase containing hydrogen;
the gas phase containing the hydrogen enters a proton exchange membrane fuel cell module to carry out electrochemical reaction to generate electric energy;
and tail gas generated by the proton exchange membrane fuel cell module enters the fuel processing module for tail gas utilization.
10. The method according to claim 8, characterized in that it comprises the steps of:
(1) the method comprises the following steps that natural gas and air enter a combustion device for mixed combustion, generated carbon dioxide and water sequentially enter a first reactor for steam reforming reaction, enter a second reactor for steam-water transformation reaction and enter a third reactor for methanation reaction, and hydrogen is obtained;
(2) the gas phase containing hydrogen enters the proton exchange membrane fuel cell from the anode inlet, air enters the proton exchange membrane fuel cell from the cathode inlet, and water enters the proton exchange membrane fuel cell from the cooling water inlet to perform electrochemical reaction to generate electric energy;
enabling a first part of anode exhaust gas generated by the electrochemical reaction in the step (2) to enter a combustion device to be subjected to mixed combustion with the natural gas and the air in the step (1);
preferably, the working medium water in the step (1) enters a steam generating device for steam generation;
preferably, the heat exchange medium subjected to heat exchange in the first reactor in the step (1) enters a steam generating device for steam generation;
preferably, a first part of the steam generated in the step (1) enters the first reactor, and a second part exchanges heat with the natural gas through a fourth heat exchange device;
preferably, after being compressed by the gas compression device, heat exchanged by the seventh heat exchange device and humidified by the humidifier in sequence, the air in the step (2) enters the proton exchange membrane fuel cell from the cathode inlet;
preferably, effluent generated by the electrochemical reaction in the step (2) is subjected to heat exchange by a sixth heat exchange device and then is circulated into the proton exchange membrane fuel cell from a cooling water inlet;
preferably, the second portion of the electrochemically generated anode exhaust of step (2) is recycled to the anode inlet for electrochemical reaction;
preferably, the electrochemically generated third portion of the anode exhaust of step (2) is directly exhausted;
preferably, the electrochemically generated cathode exhaust steam in the step (2) enters a humidifier to humidify air;
preferably, the heat exchange medium sequentially passes through the sixth heat exchange device, the seventh heat exchange device, the third heat exchange device, the second heat exchange device, the first heat exchange device and the fifth heat exchange device to perform gradual heat exchange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011615866.5A CN112803039A (en) | 2020-12-30 | 2020-12-30 | Combined heat and power device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011615866.5A CN112803039A (en) | 2020-12-30 | 2020-12-30 | Combined heat and power device and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112803039A true CN112803039A (en) | 2021-05-14 |
Family
ID=75804821
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011615866.5A Pending CN112803039A (en) | 2020-12-30 | 2020-12-30 | Combined heat and power device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112803039A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113594516A (en) * | 2021-07-29 | 2021-11-02 | 上海空间电源研究所 | Distributed biomass power generation system and power generation method of plasma-assisted hydrogen production-fuel cell |
| CN115072662A (en) * | 2022-07-20 | 2022-09-20 | 山东省科学院能源研究所 | Proton exchange membrane fuel cell cogeneration system and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101373839A (en) * | 2007-08-20 | 2009-02-25 | 北京科技大学 | Method and apparatus for removing CO, electrification method and system for fuel battery with proton exchange film |
| CN207134431U (en) * | 2017-08-24 | 2018-03-23 | 中海石油气电集团有限责任公司 | A kind of natural gas hydrogen preparation and the skid-mounted type integrating device with Proton Exchange Membrane Fuel Cells integrated thermal electric cold triple supply |
| WO2019161776A1 (en) * | 2018-02-24 | 2019-08-29 | 北京联力源科技有限公司 | Fuel chemical looping hydrogen production system and method |
| CN110544785A (en) * | 2019-06-13 | 2019-12-06 | 华电电力科学研究院有限公司 | natural gas self-heating reforming proton exchange membrane fuel cell distributed cogeneration system and method |
| CN111211338A (en) * | 2020-03-19 | 2020-05-29 | 吉林大学 | High-pressure proton exchange membrane fuel cell power system |
-
2020
- 2020-12-30 CN CN202011615866.5A patent/CN112803039A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101373839A (en) * | 2007-08-20 | 2009-02-25 | 北京科技大学 | Method and apparatus for removing CO, electrification method and system for fuel battery with proton exchange film |
| CN207134431U (en) * | 2017-08-24 | 2018-03-23 | 中海石油气电集团有限责任公司 | A kind of natural gas hydrogen preparation and the skid-mounted type integrating device with Proton Exchange Membrane Fuel Cells integrated thermal electric cold triple supply |
| WO2019161776A1 (en) * | 2018-02-24 | 2019-08-29 | 北京联力源科技有限公司 | Fuel chemical looping hydrogen production system and method |
| CN110544785A (en) * | 2019-06-13 | 2019-12-06 | 华电电力科学研究院有限公司 | natural gas self-heating reforming proton exchange membrane fuel cell distributed cogeneration system and method |
| CN111211338A (en) * | 2020-03-19 | 2020-05-29 | 吉林大学 | High-pressure proton exchange membrane fuel cell power system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113594516A (en) * | 2021-07-29 | 2021-11-02 | 上海空间电源研究所 | Distributed biomass power generation system and power generation method of plasma-assisted hydrogen production-fuel cell |
| CN115072662A (en) * | 2022-07-20 | 2022-09-20 | 山东省科学院能源研究所 | Proton exchange membrane fuel cell cogeneration system and method |
| CN115072662B (en) * | 2022-07-20 | 2024-02-13 | 山东省科学院能源研究所 | Combined heat and power generation system and method for proton exchange membrane fuel cell |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110544785B (en) | Natural gas autothermal reforming proton exchange membrane fuel cell distributed cogeneration system and method | |
| CN108005742B (en) | Solid oxide fuel cell driven combined cooling, heating and power system capable of being partially recycled | |
| CN113540541B (en) | SOFC (solid oxide Fuel cell) using ammonia water as fuel, and cascade power generation system and operation method thereof | |
| Hou et al. | Thermodynamic performance study of the integrated MR-SOFC-CCHP system | |
| JPH09129255A (en) | Power generating system for combined cycle of indirect combustion gas turbine and doubled fuel cell | |
| CN102544549A (en) | Combined heat and power (CHP) supply system based on fuel cell | |
| CN205222680U (en) | Methanol -water reformation hydrogen production system that zero carbon discharged and fuel cell car thereof | |
| CN109004244A (en) | Solid oxide fuel cell association system based on solar energy preparing hydrogen by reforming methanol | |
| CN107359361A (en) | A kind of natural gas hydrogen preparation and skid-mounted type integrating device and method with Proton Exchange Membrane Fuel Cells integrated thermal electric cold triple supply | |
| KR20110029963A (en) | Molten carbonate fuel cell system with hydrocarbon reactor | |
| CN207134431U (en) | A kind of natural gas hydrogen preparation and the skid-mounted type integrating device with Proton Exchange Membrane Fuel Cells integrated thermal electric cold triple supply | |
| CN109361001A (en) | A kind of integral coal gasification solid oxide fuel cell power generating system and technique | |
| CN210516883U (en) | Natural gas self-heating reforming proton exchange membrane fuel cell distributed cogeneration system | |
| CN111477914A (en) | Energy recycling system and method for fuel cell system | |
| CN113889648B (en) | MW-level combined heat and power supply fuel cell power station | |
| CN208589494U (en) | Solid oxide fuel cell association system based on solar energy preparing hydrogen by reforming methanol | |
| CN112803039A (en) | Combined heat and power device and method | |
| CN201985204U (en) | Heat-power co-generation system based on fuel cell | |
| CN110676493A (en) | Photovoltaic coupling solid oxide fuel cell cold-hot electric system and energy supply method | |
| CN109119660A (en) | Thermoelectricity hydrogen polygenerations systeme based on city gas | |
| CN114955997B (en) | Distributed natural gas hydrogen production system | |
| CN114526158B (en) | Energy and substance conversion system and method based on carbon dioxide hydrogenation | |
| CN113937320B (en) | Combined cooling heating and power system and method for low-temperature proton exchange membrane fuel cell | |
| JPH11238520A (en) | Fuel cell power generating apparatus | |
| KR102602831B1 (en) | Hybrid system of fuel cell |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |