CN106856245A - CLP and SOFC integrated power generation plant and operation method thereof - Google Patents
CLP and SOFC integrated power generation plant and operation method thereof Download PDFInfo
- Publication number
- CN106856245A CN106856245A CN201510961310.4A CN201510961310A CN106856245A CN 106856245 A CN106856245 A CN 106856245A CN 201510961310 A CN201510961310 A CN 201510961310A CN 106856245 A CN106856245 A CN 106856245A
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- Prior art keywords
- fuel cell
- solid
- oxide fuel
- chemical loop
- chamber
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Links
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000010248 power generation Methods 0.000 title abstract 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 184
- 239000000446 fuel Substances 0.000 claims abstract description 141
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 91
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 91
- 239000000126 substance Substances 0.000 claims abstract description 90
- 239000001257 hydrogen Substances 0.000 claims abstract description 74
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 74
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000007787 solid Substances 0.000 claims abstract description 19
- 239000007789 gas Substances 0.000 claims description 93
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 61
- 239000003085 diluting agent Substances 0.000 claims description 40
- 238000010438 heat treatment Methods 0.000 claims description 29
- 229910052757 nitrogen Inorganic materials 0.000 claims description 29
- 238000011017 operating method Methods 0.000 claims description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- 239000001301 oxygen Substances 0.000 claims description 10
- 229910052760 oxygen Inorganic materials 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 8
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 241000790917 Dioxys <bee> Species 0.000 claims description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 238000010943 off-gassing Methods 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 238000010025 steaming Methods 0.000 claims description 2
- 239000004408 titanium dioxide Substances 0.000 claims description 2
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 6
- 230000008569 process Effects 0.000 abstract description 5
- 229960004424 carbon dioxide Drugs 0.000 description 71
- 238000010586 diagram Methods 0.000 description 10
- 238000007254 oxidation reaction Methods 0.000 description 7
- 230000003647 oxidation Effects 0.000 description 6
- 238000006722 reduction reaction Methods 0.000 description 6
- 230000009467 reduction Effects 0.000 description 5
- 238000010790 dilution Methods 0.000 description 4
- 239000012895 dilution Substances 0.000 description 4
- 230000005611 electricity Effects 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 229910002090 carbon oxide Inorganic materials 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000002912 waste gas 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
-
- 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
-
- 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
- H01M8/124—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte characterised by the process of manufacturing or by the material of the electrolyte
- H01M8/1246—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte characterised by the process of manufacturing or by the material of the electrolyte the electrolyte consisting of oxides
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Life Sciences & Earth Sciences (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
A power plant and method of operating the same that integrates a chemical looping process with a solid oxide fuel cell. The power generation equipment comprises a cavity, a solid oxide fuel cell device and a chemical loop program device. The cavity is provided with a valve to divide the cavity into a first cavity and a second cavity, and the solid oxide fuel cell device is arranged in the first cavity. The chemical loop program device is arranged in the second chamber and can generate hydrogen and carbon dioxide, and the generated hydrogen is used as anode fuel of the solid oxide fuel cell device. The high-temperature carbon dioxide generated by the chemical loop program device can enter the first chamber by opening the valve so as to heat the solid oxide fuel cell device. The invention integrates the design of a chemical loop program and the solid oxide fuel cell into a whole, and is matched with the configuration of an operation interface, and the high-temperature steady-state operation of the solid oxide fuel cell is considered, so as to have the effects of carbon dioxide capture, high energy utilization rate and high power generation efficiency.
Description
Technical field
The invention relates to a kind of generating equipment, and in particular to a kind of integrated chemical loop program
(Chemical Looping Process, CLP) and solid-oxide fuel cell (solid oxide fuel cell,
SOFC generating equipment and its operating method).
Background technology
Solid oxide fuel cell system operation temperature about at 850 DEG C, due to this fuel cell need exist
Under hot environment just can steady running generate electricity, current system heats up or maintains system operation context temperature manner to lead to
Often meet the heat demand of system using gas heater.But warm mode is held using gas heater, belongs to consumption
The non-tool source benefit of energy, therefore, need to arrange in pairs or groups one and have the system alliance operating of high temperature aerogenesis, using its supply
Demand for fuel, and effectively reclaim the heat energy of high temperature source of the gas, then energy saving of system can be reached with the target for simplifying.
The content of the invention
The present invention provides the generating equipment of a kind of integrated chemical loop program and solid-oxide fuel cell, energy
Have the effect of carbon dioxide capture, high-energy source utilization rate and high generation efficiency concurrently.
The present invention separately provides a kind of integrated chemical loop program with the generating equipment of solid-oxide fuel cell
, can be recycled for used heat by operating method.
The generating equipment of integrated chemical loop program of the invention and solid-oxide fuel cell, including have
One valve is divided into the cavity of first and second chamber, the Solid oxide fuel in first chamber
Battery (solid oxide fuel cell, SOFC) device and the chemical loop program in second chamber
(chemical looping process, CLP) device.CLP devices can produce the hydrogen of high temperature and the dioxy of high temperature
Change carbon, wherein hydrogen as SOFC devices anode fuel, and unlatching by the first valve makes high temperature
Carbon dioxide enters first chamber, is used to heat SOFC devices.
Wherein, the first chamber is located at second chamber top.
Wherein, the first chamber also includes carbon dioxide outlet.
Wherein, the equipment also includes the second valve, is arranged at by the carbon dioxide outlet, out
Open or close the carbon dioxide outlet.
Wherein, the equipment also includes air distributor, is arranged in the first chamber and between described the
Between one valve and the solid-oxide fuel cell device.
Wherein, the air distributor is the flat board with several holes.
Wherein, the chemical loop timer includes being passed through the steam pipework of steam, is passed through fuel
Fuel conduit, the hydrogen pipeline for discharging hydrogen and the air pipe line for being passed through air.
Wherein, the solid-oxide fuel cell device includes being passed through the anode manifolds of anode fuel and leading to
Enter the cathode manifold of cathodic fuel, and the anode manifolds and the chemical loop timer the hydrogen
Air pipe is connected.
Wherein, the equipment also includes steam generator, is used to supply the chemical loop timer steam.
Wherein, the equipment also includes the first heating unit, is used to heat two from first chamber discharge
Carbonoxide, and it is sent to the steam generator.
Wherein, the equipment also includes the second heating unit, is used to heat from Solid oxide fuel electricity
The tail gas of pool device discharge, and it is sent to the steam generator.
Wherein, the equipment also includes that water helps Pu, is used to supply the water to the steam generator.
Wherein, the equipment also includes anode fuel feeding unit, is used to receive diluent gas and described in
The hydrogen that chemical loop timer is produced, and supplied to the solid-oxide fuel cell device.
Wherein, the anode fuel feeding unit includes：
First heat exchanger, is used to reduce the energy heats institute that the temperature of the hydrogen and application heat exchange are taken out
State diluent gas；
First flow divider, is used to shunt the hydrogen entered from the first heat exchanger；
Pumping side Pu, is used to extract the hydrogen by first flow divider；
First flowmeter, the flow of the hydrogen of the control from pumping side Pu；And
Blender, receives through the hydrogen of first flowmeter control flow and through first heat exchange
The diluent gas of device heating.
Wherein, the anode fuel feeding unit also includes hydrogen storage groove, is used to store by described first
The part hydrogen of flow divider, in chemical loop timer shutdown or failure as the solid-state
Oxid fuel cell device enters hydrogen source needed for shutdown procedure.
Wherein, the anode fuel feeding unit also include deduster, be arranged at the first heat exchanger with
Between first flow divider, the hydrogen after being used to cooling carries out dust removal step.
Wherein, the equipment also includes diluent gas feeding unit, is used to supply the diluent gas to described
Anode fuel feeding unit, and the diluent gas feeding unit includes：
Second flow divider, is used to shunt nitrogen and the carbon dioxide from first chamber discharge, described dilute
Outgassing body is selected from one of the nitrogen and described carbon dioxide；
Second heat exchanger, is used to heat the diluent gas by second flow divider；And
3rd flow divider, is arranged between second flow divider and the second heat exchanger, is used to institute
State diluent gas and bypass the second heat exchanger.
Wherein, the equipment also includes air supply unit, is used to supply air to the chemical loop respectively
Timer and the solid-oxide fuel cell device.
Wherein, the air supply unit includes：
Air helps Pu；
Second flowmeter, the air capacity needed for coordinating the solid-oxide fuel cell device, control comes from
The amount of the air at air side Pu；
3rd flowmeter, the air capacity needed for coordinating the chemical loop timer, control comes from the sky
The amount of the air at gas side Pu；And
4th flow divider, is used to shunt the air from the second flowmeter.
Wherein, the equipment also includes air intake conduit, be arranged in the second chamber and with the sky
Gas feeding unit is connected, and is heated by institute with the carbon dioxide produced by the chemical loop timer
State the 4th flow divider into the air in the air intake conduit.
Wherein, the equipment also includes hot tank, is used to heat by the air of the air intake conduit,
And transmit heated air to the solid-oxide fuel cell device.
Wherein, the chemical loop timer is to use carbon-based fuel with iron system oxygen carrier as reaction raw materials,
To produce the hydrogen with the carbon dioxide.
Operating method of the invention include supply fuel to a generating equipment CLP devices, with produce hydrogen with
Carbon dioxide, wherein generating equipment include being separated into by one first valve a cavity of first and second chamber,
And above-mentioned CLP devices are just arranged in second chamber.Then, above-mentioned first valve is opened, CLP is filled
The carbon dioxide for putting generation enters first chamber by the first valve opened, and first chamber is arranged on to heat
Interior SOFC devices.The hydrogen produced as CLP devices is then transported to SOFC devices, as
The anode fuel of SOFC devices.
Wherein, methods described also includes the valve opening of control first valve, with according to the solid oxide
The temperature of thing fuel-cell device, controls the carbon dioxide to enter the flow of the first chamber.
Wherein, methods described also includes the valve opening of the second valve of control, is fired with according to the solid-oxide
Expect the temperature of cell apparatus, control the carbon dioxide to discharge the flow of the first chamber, second valve
Door is arranged on the first chamber and discharges at the opening of the carbon dioxide.
Wherein, methods described is also included using the tail gas of the solid-oxide fuel cell device or described in
First chamber discharge the carbon dioxide as the chemical loop timer steam source.
Wherein, use the tail gas or from the first chamber discharge the carbon dioxide as the steaming
Before vapour thermal source, also including the heating tail gas or the carbon dioxide.
Wherein, methods described also includes entering the carbon dioxide discharged from the first chamber using nitrogen
Row heat exchange, to heat the nitrogen and reduce the temperature of the carbon dioxide, wherein, heated is described
Nitrogen is the source of diluent gas as the solid-oxide fuel cell device.
Wherein, methods described also includes using the carbon dioxide from first chamber discharge as described
The source of diluent gas of solid-oxide fuel cell device.
Wherein, methods described also includes the hydrogen using chemical loop timer generation to described
The source of diluent gas of solid-oxide fuel cell device carries out heat exchange, to heat the source of diluent gas simultaneously
Reduce the temperature of the hydrogen.
Wherein, methods described also includes one of the hydrogen that the storage chemical loop timer is produced
Point, it is supplied to the solid-oxide fuel cell with chemical loop timer shutdown or failure
Device, hydrogen source needed for shutdown procedure is entered as the solid-oxide fuel cell device.
Wherein, methods described also includes that the carbon dioxide produced by the chemical loop timer adds
Heat is arranged at the air in the air intake conduit in the second chamber, and is made with the heated air
It is the cathodic fuel of the solid-oxide fuel cell device.
Wherein, methods described also includes entering air using the tail gas of the solid-oxide fuel cell device
Row heat exchange, to heat air, and using the heated air as the solid-oxide fuel cell
The cathodic fuel of device.
Based on above-mentioned, the present invention can be integrally formed by chemical loop program and solid-oxide fuel cell
Design, and operating interface of arranging in pairs or groups configures and takes into account the operating of solid-oxide fuel cell High Temperature and Stable State, to have concurrently
The effect of carbon dioxide capture, high-energy source utilization rate and high generation efficiency.
Below in conjunction with the drawings and specific embodiments, the present invention will be described in detail, but not as to of the invention
Limit.
Brief description of the drawings
Fig. 1 is fired with solid-oxide according to a kind of integrated chemical loop program of the first embodiment of the present invention
Expect the sketch of the generating equipment of battery.
Fig. 2 is fired with solid-oxide according to a kind of integrated chemical loop program of the second embodiment of the present invention
Expect the schematic diagram of the generating equipment of battery.
Fig. 3 is fired with solid-oxide according to a kind of integrated chemical loop program of the third embodiment of the present invention
Expect the schematic diagram of the generating equipment of battery.
Fig. 4 is fired with solid-oxide according to a kind of integrated chemical loop program of the fourth embodiment of the present invention
Expect the schematic diagram of the generating equipment of battery.
Fig. 5 is fired with solid-oxide according to a kind of integrated chemical loop program of the fifth embodiment of the present invention
Expect the schematic diagram of the generating equipment of battery.
Fig. 6 is fired with solid-oxide according to a kind of integrated chemical loop program of the sixth embodiment of the present invention
Expect the schematic diagram of the generating equipment of battery.
Wherein, reference：
10、20：Integrate the generating equipment of CLP and SOFC
100、200：Cavity
102、202、210：Valve
104、204：First chamber
106、206：Second chamber
108、208：Solid-oxide fuel cell device
110：Chemical loop timer
212：Air distributor
214：Reduction reactor
216：Oxidation reactor
218：Burner
220：Cyclone separator
222：Fuel conduit
224：Steam pipework
226：Air pipe line
228：Gas exhaust piping
230：Hydrogen pipeline
232：Anode manifolds
234：Cathode manifold
300：Steam generator
302：First heating unit
304：Second heating unit
306、512：After burner
308、402、418、514：Heat exchanger
310：Water helps Pu
400：Anode fuel feeding unit
404、420、422、508、600：Flow divider
406：Pumping side Pu
408、504、506：Flowmeter
410：Blender
412：Hydrogen storage groove
414：Deduster
416：Diluent gas feeding unit
500：Air supply unit
502：Air helps Pu
510：Hot tank
Specific embodiment
Fig. 1 is according to a kind of integrated chemical loop program (CLP) of the first embodiment of the present invention and solid oxygen
The sketch of the generating equipment of compound fuel cell (SOFC).
Fig. 1 is refer to, the Major Systems in the generating equipment 10 of the present embodiment are all disposed within a cavity 100,
And there is cavity 100 valve 102 to be divided into first chamber 104 and second chamber 106, and generate electricity
Solid-oxide fuel cell (SOFC) device 108 and chemical loop program (CLP) device in equipment 10
110 are just separately positioned in first chamber 104 and second chamber 106.When fuel is provided to generating equipment
10 CLP devices 110, can produce the carbon dioxide of high temperature and the hydrogen of high temperature, and carbon dioxide temperature is about
More than 900 DEG C.For example, CLP devices 110 are to use carbon-based fuel as reaction raw materials, and iron
It is that oxygen carrier is then the offer source of source of oxygen in chemical reaction process, and so as to producing hydrogen and carbon dioxide.
Then, the carbon dioxide of high temperature by Open valve 102, can be made to enter first chamber 102, and then heating sets
Put the SOFC devices 108 in first chamber 102.Valve 102 in the present embodiment can be made according to demand
Different designs, for example there is the resistant to elevated temperatures plate washer of collocation in figure, but the present invention is not limited thereto, and for generating electricity
The valve 102 (with plate washer) of equipment 10 be preferably can more than 1000 DEG C of heatproof, its temperature resistant range for example exists
Between 1000 DEG C~1800 DEG C.The hydrogen produced as CLP devices 110 is then transported to SOFC devices 108,
As the anode fuel of SOFC devices 108.In the present embodiment, first chamber 104 is to be located at second
The top of chamber 106, but the present invention is not limited thereto, as long as the carbon dioxide of high temperature can be opened in valve 102
Enter in first chamber 102 afterwards, either by hot gas toward the principle for rising or by other pumping dresses
Auxiliary is put, can use that the effect above can be reached.
In the present embodiment, the high temperature carbon dioxide into first chamber 102 can heat SOFC devices 108,
Applicable operation temperature is reached, and can be by the temperature for measuring SOFC devices 108 (such as fuel cell pack)
Spend the degree to decide whether to continue to heat or heat.For example, can be according to SOFC devices 108
Temperature, the valve opening of control valve 102, whereby control carbon dioxide enter first chamber 102 flow.
" valve opening " so-called in text refers to the degree of valve opening, i.e. valve opening for 0 represents that valve is fully closed, valve
Aperture represents valve wide open, valve opening as 50% represents valves half open for 100%, and the rest may be inferred.
Fig. 2 is fired with solid-oxide according to a kind of integrated chemical loop program of the second embodiment of the present invention
Expect the schematic diagram of the generating equipment of battery.
Fig. 2 is refer to, the Major Systems in the generating equipment 20 of the present embodiment are arranged in a cavity 200,
And there is cavity 200 one first valve 202 to be divided into first chamber 204 and second chamber 206, and
Solid-oxide fuel cell (SOFC) device 208 and chemical loop program (CLP) dress in generating equipment 20
Put and be just separately positioned in first chamber 204 and second chamber 206.In the present embodiment, first chamber 204
There can be carbon dioxide outlet 200a, and one second valve is set by carbon dioxide outlet 200a
210, it is used to be turned on and off carbon dioxide outlet 200a.In addition, because of the temperature pole of carbon dioxide gas stream
Height, to avoid air-flow from disperseing inequality to cause the battery temperature skewness of SOFC devices 208 and then influence anti-
Efficiency is answered, therefore, the valve 202 of SOFC devices 208 and first, second that can be in first chamber 204
And between 210, add an air distributor 212.When the carbon dioxide gas stream of high temperature is intended to, into fashionable, to borrow
Air flow method is carried out by air distributor 212, with up to the flow field of a uniformly dispersing, wherein air distributor 212
Flat board or other suitable designs for example with several holes.
As for CLP devices can comprising reduction reactor 214, oxidation reactor 216, burner 218 and
Cyclone separator 220, its operation principle is that redox is carried out in chemical loop program using oxygen carrier is anti-
Should, fuel is (such as：Carbon-based fuel) first by being passed through in fuel conduit 222, carried out in reduction reactor 214
The carbon dioxide of chemical reaction generation high temperature, the carbon dioxide of high temperature will be discharged via gas exhaust piping 228, and
Oxygen carrier may proceed to fall into oxidation reactor 216, while also will be interior by steam pipe in oxidation reactor 216
Steam is passed through in road 224 to carry out second chemical reaction.Gas exhaust piping 228 is discharged except upward, also can be
Side is discharged, or top is emitted into second chamber 206 simultaneously with side, and the high temperature carbon dioxide discharged converges
Flow to the thermal source that first chamber 204 is preheated as SOFC devices 208 or holds temperature.Oxidation reaction will generate high
Warm hydrogen, and high-temperature hydrogen also will be by being emitted into hydrogen pipeline 230 in oxidation reactor 216.Now,
The complete oxygen carrier of unreacted will continue to fall into burner 218, and via being passed through sky in air pipe line 226
Gas is reacted to burner 218, and so as to the oxygen carrier of reduction reaction, subsequent oxygen carrier will be into whirlwind point
From device 220, this chemical loop response procedures is persistently carried out.SOFC devices 208 then may include to be passed through anode combustion
The anode manifolds 232 of material and the cathode manifold 234 for being passed through cathodic fuel, and anode manifolds 232 and CLP
The hydrogen pipeline 230 of device is connected, accordingly, it is capable to receive anode fuel of the hydrogen as SOFC devices 208.
In the present embodiment, the first valve 202 and the second valve 210 resistant to elevated temperatures baffle design that can arrange in pairs or groups go out
Current path, therefore, after the first valve 202 and the second valve 210 are opened, the carbon dioxide gas of high temperature
Stream can be by the first valve 202 and by air distributor 212 by air-flow uniformly dispersing, now SOFC dresses
The carbon dioxide gas stream that high temperature is spread around 208 is put, using this high temperature gas flow heating SOFC devices 208
After operation temperature needed for reaching, high temperature gas flow will enter the second valve by air distributor 212 once again
Door 210, subsequently departs from first chamber 204.And, can be determined by the temperature for measuring SOFC devices 208
It is fixed whether to proceed heating, then control the first valve 202 and the second valve 210 to continue to continue to heat
Open；If conversely, reached the operation temperature of SOFC devices 208, will close the first valve 202 with
Second valve 210, is turned on and off determining high temperature by the first valve 202 and the second valve 210
The flow that carbon dioxide gas stream enters in first chamber 204.Additionally, can also be by the second valve 210 of control
Valve opening come control carbon dioxide discharge first chamber 204 flow.For example, when SOFC is filled
208 are put in start temperature rise period, then the first valve 202 and the second valve 210 all standard-sized sheets；When SOFC dresses
208 are put holding thermophase, the first valve 202 and the second valve 210 also all standard-sized sheet；When SOFC devices 208
In load stage, then the first valve 202 and the second valve 210 are all fully closed；When SOFC devices 208 are being closed
Machine temperature-fall period, the first valve 202 and the second valve 210 are then all half-open.
Fig. 3 is fired with solid-oxide according to a kind of integrated chemical loop program of the third embodiment of the present invention
The schematic diagram of the generating equipment of battery is expected, wherein using with Fig. 2 identicals component symbol to represent identical or class
As component.
Fig. 3 is refer to, in the present embodiment in addition to the component of Fig. 2, SOFC devices 208 is it is also possible to use
Tail gas or from the carbon dioxide of the discharge of first chamber 204 as CLP devices steam source, and will be upper
Before gas is stated as steam source, above-mentioned tail gas or carbon dioxide can be also first heated.For example, aoxidize
Steam needed for reaction in reactor 216 can be produced by a steam generator 300, the institute of steam generator 300
The thermal source for needing is then via the first heating unit 302 (such as heat exchanger) heating from the two of the discharge of first chamber 204
Carbonoxide is provided；Also or, heating the tail discharged from SOFC devices 208 via the second heating unit 304
Gas is provided, wherein the dress that the second heating unit 304 is for example made up of after burner 306 and heat exchanger 308
Put, above-mentioned tail gas can be the tail gas after heat exchanger 308.Can as the water source needed for steam generator 300
There is provided by water side Pu 310, but the present invention is not limited thereto.Water source needed for steam generator 300 can also be adopted
With each heat exchanger condense collect and come water.
By taking the operation of SOFC devices 208 as an example, when SOFC devices 208 are in start temperature rise period, SOFC
The tail gas of device 208 and the carbon dioxide from the discharge of first chamber 204 are all not required to heat up；When SOFC devices
208 are holding thermophase, and the tail gas of SOFC devices 208 will with the carbon dioxide from the discharge of first chamber 204
Maintain high temperature；When SOFC devices 208 are in load stage, the tail gas of SOFC devices 208 with from the first chamber
The carbon dioxide of the discharge of room 204 will maintain high temperature；When SOFC devices 208 are in shutdown temperature-fall period, SOFC
The tail gas of device 208 and the carbon dioxide from the discharge of first chamber 204 are all not required to heat up.
Fig. 4 is fired with solid-oxide according to a kind of integrated chemical loop program of the fourth embodiment of the present invention
The schematic diagram of the generating equipment of battery is expected, wherein using with Fig. 2 identicals component symbol to represent identical or class
As component.
Fig. 4 is refer to, in the present embodiment in addition to the component of Fig. 2, anode fuel supply is may also include
Unit 400, is used to the hydrogen for receiving diluent gas and being produced from CLP devices, and fill supplied to SOFC
Put 208.Because the density of hydrogen of SOFC need not be too high, therefore, in the present embodiment can using nitrogen or
Carbon dioxide is used as the gas of above-mentioned dilution hydrogen, and the source of nitrogen may be from liquid nitrogen steel cylinder or
Nitrogen making machine.Above-mentioned anode fuel feeding unit 400 may include heat exchanger 402, flow divider 404, pumping side
Pu 406, flowmeter 408 and blender 410.For example, the high temperature generated in chemical loop program
Hydrogen gas stream, enters in heat exchanger 402 via in hydrogen pipeline 230.Heat exchanger 402 at least has
Two functions, first is the temperature of reduction high-temperature hydrogen, with sharp subsequent gases dust removal step；Second is application
The heat that heat exchange is taken out is used as heating diluent gas.Hydrogen is by that can be directly entered a deduster after cooling
Dust removal step is carried out in 414, flow divider 404 is entered back into；Or by fuel incoming fuel pipeline 222
Shi Xianyong screen clothes sieving removal powder therein, reaches dust removing effects, so the hydrogen after cooling also can be direct
Shunted into flow divider 404.The hydrogen partial that can also produce CLP devices in the process passes through
Flow divider 404 is shunted and stored to hydrogen storage groove 412, is shut down or during failure with CLP devices, as
SOFC devices 208 enter hydrogen source needed for shutdown procedure, also hydrogen partial directly can be conveyed into rear end
Technique producing line is learned, to process industry or people's livelihood chemicals.The hydrogen of another part then can be using pumping side Pu
The amounts of hydrogen in blender 410 is flowed into needed for 406 are pumped into pipeline, and application traffic meter 408 is controlled,
The function of blender 410 is mainly gas (diluent gas and the hydrogen for mixing SOFC devices 208 to be entered
Gas), when gas after the completion of this mixing therewith using in the anode manifolds 232 for entering SOFC devices 208 as
Fuel needed for anode.Above-mentioned flowmeter 408 can be mass flowmenter or mass flow controller (Mass flow
controller,MFC)。
The source of above-mentioned diluent gas can be nitrogen (N2) or from first chamber 204 discharge carbon dioxide.
Such as with nitrogen as diluent gas, nitrogen (N can be used2) carbon dioxide to being discharged from first chamber 204 enters
Row heat exchange, with heated nitrogen and reduces the temperature of carbon dioxide.And work as the gas flow temperature reduction of carbon dioxide
Afterwards, you can carry out carbon dioxide capture program.For example, a diluent gas feeding unit 416 can be set,
It is used to supply the heat exchanger 402 of diluent gas to anode fuel supply unit 400, and diluent gas is supplied
Unit 416 may include heat exchanger 418 and flow divider 420 and 422.
When flow divider 420 is selected with nitrogen as diluent gas, nitrogen subsequently enters flow divider 422, point
Stream valve 422 predominantly controls whether nitrogen needs to carry out nitrogen heat temperature raising by heat exchanger 418.Nitrogen
Gas is understood by two channel heat exchangers, i.e. heat exchanger 418 and heat exchanger 402 in whole generating equipment,
The thermal source of heat exchanger 402 is mainly the hydrogen generated in chemical loop program, via being carried after heat exchange
For carrying out heated nitrogen, is conveyed toward blender 410 after nitrogen is heated, but due to SOFC devices 208 in
Initial stage heats up to draw and do not needed when carrying temperature nitrogen too high, therefore, nitrogen can be bypassed using flow divider 422
Heat exchanger 418；Conversely, if the nitrogen temperature that heat exchanger 402 is heated is not up to required temperature,
Make nitrogen by heat exchanger 418 come the program of many one section of nitrogen heating application flow divider 422.It is hot herein
The heat energy of exchanger 418 is that the carbon dioxide by being discharged from first chamber 204 is obtained.Nitrogen after heating will
Mixed in blender 410 according to required ratio with hydrogen, in subsequently entering anode manifolds 232.
When flow divider 420 is selected using carbon dioxide as diluent gas, it can be flowed out by first chamber 204
High temperature carbon dioxide cooling obtain, after the high temperature carbon dioxide of outflow is through heat exchanger 418, by titanium dioxide
The temperature of carbon is down to trappable temperature, then, flows into flow divider 420, and control from flow divider 420
Carbon dioxide gas stream is set to enter flow divider 422, such as description of above-mentioned nitrogen, if the carbon dioxide of dilution is needed
Additionally to heat, then will make carbon dioxide by heat exchanger 418 using flow divider 422, come many one sections and add
Hot program；If the carbon dioxide of dilution is not required to extra heating, heat exchange will be bypassed using flow divider 422
Device 418.Carbon dioxide after heating will be mixed according to required ratio with hydrogen in blender 410,
In subsequently entering anode manifolds 232.
By taking the operation of SOFC devices 208 as an example, when SOFC devices 208 start the temperature rise period, then it is dilute
The obstructed over-heat-exchanger 418 of outgassing body, but can be through over-heat-exchanger 402；When SOFC devices 208 are holding temperature
Stage, diluent gas can will also pass through heat exchanger 402 by heat exchanger 418；When SOFC devices
208 in load stage, and diluent gas can be by heat exchanger 418 and heat exchanger 402；When SOFC devices
208 in shutdown temperature-fall period, the obstructed over-heat-exchanger 418 of diluent gas, but can be through over-heat-exchanger 402.
Fig. 5 is fired with solid-oxide according to a kind of integrated chemical loop program of the fifth embodiment of the present invention
The schematic diagram of the generating equipment of battery is expected, wherein using with Fig. 2 identicals component symbol to represent identical or class
As component.
Fig. 5 is refer to, in the present embodiment in addition to the component of Fig. 2, an air supply unit is may also include
500, it is used to supply air respectively to the burner 218 of CLP devices and is supplied to SOFC devices 208.
Above-mentioned air supply unit 500 may include air side Pu 502, flowmeter 504 and 506 and flow divider 508.
For example, the cathodic fuel of SOFC devices 208 is air, and its source can application air side Pu 502
To extract, wherein air side Pu 502 can also be replaced with large-scale air storage tank, air compressor or air blower.
The air draught of extraction will be divided into two parts and use, and a part makes as the cathodic fuel of SOFC devices 208
With another part is then used as the reaction air needed for burner 218 in chemical loop program.And flow
Meter 504 is the air capacity needed for coordinating SOFC devices 208, and the air capacity at Pu 502 is helped in control from air；
Flowmeter 506 is then the air capacity needed for coordinating CLP devices, and the air capacity at Pu 502 is helped in control from air.
When being used as the cathodic fuel of SOFC devices 208, first pass through the control flow of flowmeter 504 and go forward side by side
Enter flow divider 508, wherein flowmeter 504 can be connected mass flow control with large-scale air storage tank and in rear end
Device (MFC) replaces.Air can be divided into twice air-flow by above-mentioned flow divider 508, enter be arranged at the together
The air intake conduit 516 being connected in two chambers 206 and with air supply unit 500, another road is then made
For SOFC devices 208 heat up or temperature adjustment during load operation air.Above-mentioned air intake conduit
516 can be coiled and increase air preheat amount in the inwall mode of cavity 200, and pre- heat number can be coiled by pipeline and enclosed
Number is determined.When air air inlet air inlet pipeline 516, the air inside air intake conduit 516 is flowed through
Influenceed by the high temperature carbon dioxide that CLP devices are produced, and carried out first time heating.Then SOFC can be used
The tail gas of device 208 carries out heat exchange in hot tank 510 to above-mentioned air, to heat air, and with through adding
The air of heat is used as cathodic fuel.Specifically, if during SOFC 208 initial startups of device its air temperature
Du Taigao, in being intended to be needed into before hot tank 510 elder generation to mix with the air of temperature adjustment and enter back into hot tank 510.
Two units, respectively after burner 512 and heat exchanger 514, wherein after burner 512 are included in hot tank 510
The unreacted tail gas that will can burn is burnt again, and heat exchange heat removal is carried out followed by via heat exchanger 514,
Give carries out second heating and uses by the air of air intake conduit 516, immediately into SOFC devices
208 cathode manifold 234.
If the air from air side Pu 502 is used as the reaction needed for burner 218 in chemical loop program
During air, then application traffic meter 506 is controlled that the flow of burner need to be entered.Such as quality of flowmeter 506
Flowmeter, or large-scale air storage tank can be used, and in rear end be connected mass flow controller (MFC) and replace.
It is when SOFC devices 208 are in the start temperature rise period, then empty by taking the operation of SOFC devices 208 as an example
Gas is heated in air intake conduit 516, but the not start of after burner 512；When SOFC devices 208 are being held
Thermophase, air is heated in air intake conduit 516, is also heated through after burner 512；When SOFC dresses
208 are put in load stage, air is heated in air intake conduit 516 and after burner 512；Work as SOFC
In shutdown temperature-fall period, air is heated device 208 in air intake conduit 516, but after burner 512 is not
Start.
Fig. 6 is fired with solid-oxide according to a kind of integrated chemical loop program of the sixth embodiment of the present invention
The schematic diagram of the generating equipment of battery is expected, wherein using with Fig. 2 to Fig. 5 identicals component symbol to represent phase
Same or similar component.
In figure 6, can simultaneously as the supply thermal source of steam generator 300 for heating the hot tank 510 of air
The second heating unit (such as the 304 of Fig. 3), such as after burner 512 in hot tank 510 and heat exchanger 514
Configuration is constant, on the premise of air intake conduit 516 can provide the pre- heat of enough gas, hot tank 510
Produced high-temp waste gas heat can turn supply steam generator 300 to produce sufficient steam to supply chemical loop
The oxidation reactor 216 of program produces hydrogen.
Conduct can also add simultaneously as for heating the heat exchanger 302 of the thermal source needed for steam generator 300
The heat exchanger (such as the 418 of Fig. 4) of heat dilution gas；That is, through the dioxy after heat exchanger 302
Change carbon air-flow, can be shunted by current divider 600.Now to application carbon dioxide as diluent gas, then
Can control to make carbon dioxide gas stream enter in flow divider 420 from flow divider 600；To carbon dioxide is made
Thermal source for needed for steam generator 300, then can control to provide carbon dioxide gas stream from flow divider 600
To steam generator 300.Additionally, by the low-temperature carbon dioxide discharged through steam generator 300, can also return
The position of flow divider 420 is delivered to, as the source of diluent gas.
In sum, the present invention, can by integrated chemical loop program and solid oxide fuel cell system
Electronic type gas heater is not used to provide hot operation environment, and can make all used heat in generating equipment
It is recycled, therefore can reach the effect for having carbon dioxide capture, high-energy source utilization rate and high generation efficiency concurrently.
Certainly, the present invention can also have other various embodiments, in the feelings without departing substantially from spirit of the invention and its essence
Under condition, those of ordinary skill in the art can make various corresponding changes and deformation, but this according to the present invention
A little corresponding changes and deformation should all belong to the protection domain of the claims in the present invention.
Claims (33)
1. a kind of generating equipment of integrated chemical loop program and solid-oxide fuel cell, its feature exists
In, including：
Cavity, with the first valve, the cavity is separated into first chamber and second by first valve
Chamber；
Solid-oxide fuel cell device, in the first chamber；And
Chemical loop timer, in the second chamber, the chemical loop timer can be produced
Hydrogen and carbon dioxide, the hydrogen as the solid-oxide fuel cell device anode fuel, and
The carbon dioxide is entered the first chamber by the unlatching of first valve, be used to heat described solid
State oxid fuel cell device.
2. the hair of integrated chemical loop program according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that the first chamber is located at second chamber top.
3. the hair of integrated chemical loop program according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that the first chamber also includes carbon dioxide outlet.
4. the hair of integrated chemical loop program according to claim 3 and solid-oxide fuel cell
Electric equipment, it is characterised in that also including the second valve, is arranged at by the carbon dioxide outlet, is used to
It is turned on and off the carbon dioxide outlet.
5. the hair of integrated chemical loop program according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that also including air distributor, is arranged in the first chamber and between described
Between first valve and the solid-oxide fuel cell device.
6. the hair of integrated chemical loop program according to claim 5 and solid-oxide fuel cell
Electric equipment, it is characterised in that the air distributor is the flat board with several holes.
7. the hair of integrated chemical loop program according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that the chemical loop timer includes being passed through the steam pipework of steam, leads to
Enter the fuel conduit of fuel, discharge the hydrogen pipeline of hydrogen and be passed through the air pipe line of air.
8. the hair of integrated chemical loop program according to claim 7 and solid-oxide fuel cell
Electric equipment, it is characterised in that the solid-oxide fuel cell device includes being passed through the sun of anode fuel
Pole pipe road and the cathode manifold for being passed through cathodic fuel, and the anode manifolds fill with the chemical loop program
The hydrogen pipeline connection put.
9. the hair of integrated chemical loop program according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that also including steam generator, is used to supply the chemical loop timer steaming
Vapour.
10. the hair of integrated chemical loop program according to claim 9 and solid-oxide fuel cell
Electric equipment, it is characterised in that also including the first heating unit, is used to heat from first chamber discharge
Carbon dioxide, and it is sent to the steam generator.
The hair of 11. integrated chemical loop programs according to claim 9 and solid-oxide fuel cell
Electric equipment, it is characterised in that also including the second heating unit, is used to heat from the Solid oxide fuel
The tail gas of cell apparatus discharge, and it is sent to the steam generator.
The hair of 12. integrated chemical loop programs according to claim 9 and solid-oxide fuel cell
Electric equipment, it is characterised in that also help Pu including water, be used to supply the water to the steam generator.
The hair of 13. integrated chemical loop programs according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that also including anode fuel feeding unit, is used to receive diluent gas and from institute
The hydrogen of chemical loop timer generation is stated, and is filled supplied to the solid-oxide fuel cell
Put.
14. integrated chemical loop programs according to claim 13 and solid-oxide fuel cell
Generating equipment, it is characterised in that the anode fuel feeding unit includes：
First heat exchanger, is used to reduce the energy heats institute that the temperature of the hydrogen and application heat exchange are taken out
State diluent gas；
First flow divider, is used to shunt the hydrogen entered from the first heat exchanger；
Pumping side Pu, is used to extract the hydrogen by first flow divider；
First flowmeter, the flow of the hydrogen of the control from pumping side Pu；And
Blender, receives through the hydrogen of first flowmeter control flow and through first heat exchange
The diluent gas of device heating.
15. integrated chemical loop programs according to claim 14 and solid-oxide fuel cell
Generating equipment, it is characterised in that the anode fuel feeding unit also includes hydrogen storage groove, is used to store
By the part hydrogen of first flow divider, in chemical loop timer shutdown or failure
Enter hydrogen source needed for shutdown procedure as the solid-oxide fuel cell device.
16. integrated chemical loop programs according to claim 14 and solid-oxide fuel cell
Generating equipment, it is characterised in that the anode fuel feeding unit also includes deduster, is arranged at described the
Between one heat exchanger and first flow divider, the hydrogen after being used to cooling carries out dust removal step.
17. integrated chemical loop programs according to claim 13 and solid-oxide fuel cell
Generating equipment, it is characterised in that also including diluent gas feeding unit, is used to supply the diluent gas extremely
The anode fuel feeding unit, and the diluent gas feeding unit includes：
Second flow divider, is used to shunt nitrogen and the carbon dioxide from first chamber discharge, described dilute
Outgassing body is selected from one of the nitrogen and described carbon dioxide；
Second heat exchanger, is used to heat the diluent gas by second flow divider；And
3rd flow divider, is arranged between second flow divider and the second heat exchanger, is used to institute
State diluent gas and bypass the second heat exchanger.
The hair of 18. integrated chemical loop programs according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that also including air supply unit, is used to supply air to the chemistry time respectively
Road timer and the solid-oxide fuel cell device.
19. integrated chemical loop programs according to claim 18 and solid-oxide fuel cell
Generating equipment, it is characterised in that the air supply unit includes：
Air helps Pu；
Second flowmeter, the air capacity needed for coordinating the solid-oxide fuel cell device, control comes from
The amount of the air at air side Pu；
3rd flowmeter, the air capacity needed for coordinating the chemical loop timer, control comes from the sky
The amount of the air at gas side Pu；And
4th flow divider, is used to shunt the air from the second flowmeter.
20. integrated chemical loop programs according to claim 19 and solid-oxide fuel cell
Generating equipment, it is characterised in that also including air intake conduit, be arranged in the second chamber and with institute
State air supply unit to be connected, heated with the carbon dioxide produced by the chemical loop timer
The air entered in the air intake conduit by the 4th flow divider.
21. integrated chemical loop programs according to claim 20 and solid-oxide fuel cell
Generating equipment, it is characterised in that also including hot tank, is used to heat by described in the air intake conduit
Air, and transmit heated air to the solid-oxide fuel cell device.
The hair of 22. integrated chemical loop programs according to claim 1 and solid-oxide fuel cell
Electric equipment, it is characterised in that the chemical loop timer is to use carbon-based fuel with iron system oxygen carrier work
It is reaction raw materials, to produce the hydrogen with the carbon dioxide.
The operation side of the generating equipment of a kind of 23. integrated chemical loop programs and solid-oxide fuel cell
Method, it is characterised in that the generating equipment includes cavity, the cavity has the first valve, described first
Valve is divided into first chamber and second chamber, and in being provided with solid-oxide in the first chamber
Fuel-cell device, in chemical loop timer is provided with the second chamber, the operating method includes：
The chemical loop timer in supply fuel to the second chamber, to produce hydrogen and dioxy
Change carbon；
First valve is opened, makes the carbon dioxide that the chemical loop timer is produced by opening
First valve for opening enters the first chamber, to heat the solid-oxide fuel cell device；
And
Convey the hydrogen that the chemical loop timer produces to the solid-oxide fuel cell
Device, as the anode fuel of the solid-oxide fuel cell device.
24. operating methods according to claim 23, it is characterised in that also including controlling described the
The valve opening of one valve, with the temperature according to the solid-oxide fuel cell device, controls the dioxy
Change the flow that carbon enters the first chamber.
25. operating methods according to claim 23, it is characterised in that also including controlling the second valve
The valve opening of door, with the temperature according to the solid-oxide fuel cell device, controls the carbon dioxide
The flow of the first chamber is discharged, second valve is arranged on the first chamber and discharges the titanium dioxide
At the opening of carbon.
26. operating methods according to claim 23, it is characterised in that also including using described solid
The tail gas of state oxid fuel cell device or from the first chamber discharge the carbon dioxide as institute
State the steam source of chemical loop timer.
27. operating methods according to claim 26, it is characterised in that using the tail gas or
It is also described including heating before the carbon dioxide discharged from the first chamber is as the steam source
Tail gas or the carbon dioxide.
28. operating methods according to claim 23, it is characterised in that also including using nitrogen pair
Heat exchange is carried out from the carbon dioxide of first chamber discharge, to heat the nitrogen and reduce described
The temperature of carbon dioxide, wherein, the heated nitrogen is filled as the solid-oxide fuel cell
The source of diluent gas put.
29. operating methods according to claim 23, it is characterised in that also including using described in
First chamber discharge the carbon dioxide as the solid-oxide fuel cell device diluent gas
Source.
30. operating methods according to claim 23, it is characterised in that also including using describedization
Learn the diluent gas of the hydrogen to the solid-oxide fuel cell device of loop program device generation
Source carries out heat exchange, to heat the source of diluent gas and reduce the temperature of the hydrogen.
31. operating methods according to claim 23, it is characterised in that also including storage describedization
Learn a part for the hydrogen that loop program device is produced, shutting down in the chemical loop timer or
The solid-oxide fuel cell device is supplied to during failure, is filled as the solid-oxide fuel cell
Put into hydrogen source needed for shutdown procedure.
32. operating methods according to claim 23, it is characterised in that also including by describedization
Learn the air inlet that the carbon dioxide heating of loop program device generation is arranged in the second chamber
Air in pipeline, and using the heated air as the moon of the solid-oxide fuel cell device
Pole fuel.
33. operating methods according to claim 23, it is characterised in that also including using described solid
The tail gas of state oxid fuel cell device carries out heat exchange to air, to heat air, and with heated
The air as the solid-oxide fuel cell device cathodic fuel.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| TW104141065A TWI557981B (en) | 2015-12-08 | 2015-12-08 | Power generation apparatus integrated clp and sofc and operation method thereof |
| TW104141065 | 2015-12-08 |
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| CN106856245A true CN106856245A (en) | 2017-06-16 |
| CN106856245B CN106856245B (en) | 2020-08-25 |
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| CN201510961310.4A Active CN106856245B (en) | 2015-12-08 | 2015-12-18 | Power plant integrating chemical loop program means with SOFC and method of operating same |
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| Country | Link |
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| CN (1) | CN106856245B (en) |
| AU (1) | AU2016269456B2 (en) |
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| JP7213217B2 (en) * | 2020-10-30 | 2023-01-26 | 三菱重工業株式会社 | Fuel cell power generation system and control method for fuel cell power generation system |
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| US20040023085A1 (en) * | 2002-08-05 | 2004-02-05 | Lightner Gene E. | Prodoction of electricity from fuel cells depending on gasification of carbonatious compounds |
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- 2015-12-08 TW TW104141065A patent/TWI557981B/en active
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| US20060115691A1 (en) * | 2002-12-10 | 2006-06-01 | Aker Kvaemer Engineering & Technology | Method for exhaust gas treatment in a solid oxide fuel cell power plant |
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| TW201721949A (en) | 2017-06-16 |
| CN106856245B (en) | 2020-08-25 |
| AU2016269456A1 (en) | 2017-06-22 |
| TWI557981B (en) | 2016-11-11 |
| AU2016269456B2 (en) | 2018-05-10 |
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