CN112864432B - System and method for generating power by using synthesis gas high-temperature fuel cell - Google Patents
System and method for generating power by using synthesis gas high-temperature fuel cell Download PDFInfo
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- CN112864432B CN112864432B CN201911185183.8A CN201911185183A CN112864432B CN 112864432 B CN112864432 B CN 112864432B CN 201911185183 A CN201911185183 A CN 201911185183A CN 112864432 B CN112864432 B CN 112864432B
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- 239000000446 fuel Substances 0.000 title claims abstract description 113
- 238000000034 method Methods 0.000 title claims abstract description 28
- 230000015572 biosynthetic process Effects 0.000 title claims description 55
- 238000003786 synthesis reaction Methods 0.000 title claims description 55
- 239000007789 gas Substances 0.000 claims abstract description 128
- 238000010248 power generation Methods 0.000 claims abstract description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 238000002485 combustion reaction Methods 0.000 claims abstract description 38
- 239000001257 hydrogen Substances 0.000 claims abstract description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 36
- 239000002737 fuel gas Substances 0.000 claims description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 18
- 239000001569 carbon dioxide Substances 0.000 claims description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 230000005611 electricity Effects 0.000 claims description 4
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 239000007787 solid Substances 0.000 description 14
- 239000003345 natural gas Substances 0.000 description 8
- 239000002994 raw material Substances 0.000 description 7
- 238000002407 reforming Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—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
-
- 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
-
- 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
- H01M8/0625—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 in a modular combined reactor/fuel cell structure
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
- H01M8/0668—Removal of carbon monoxide or carbon dioxide
-
- 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
Abstract
The invention relates to the field of battery power generation, and discloses a synthetic gas fuel cell power generation system which comprises a synthetic gas source, a heat exchange device, a fuel cell and a combustion device, wherein the synthetic gas source is used for providing synthetic gas; the heat exchange device comprises a heat exchange conversion device, a first heat exchange device and a second heat exchange device; the heat exchange conversion device is connected with the anode of the fuel cell through a first heat exchange device; the cathode of the fuel cell is connected with the combustion device; the combustion device is connected with the cathode of the fuel cell through a second heat exchange device. The power generation system of the synthetic gas fuel cell provided by the invention has simple flow, improves the hydrogen partial pressure, reduces the heat productivity of the synthetic gas fuel cell in the power generation process, reasonably utilizes the heat of the system and improves the power generation efficiency of the fuel cell when the system is used for power generation.
Description
Technical Field
The invention relates to the field of battery power generation, in particular to a synthesis gas high-temperature fuel cell power generation system and a method thereof.
Background
A Solid Oxide Fuel Cell (SOFC) power generation system is a clean and efficient energy conversion system, which uses gaseous hydrocarbons such as natural gas or hydrogen, carbon monoxide and the like as raw materials and can convert chemical energy in Fuel into electric energy. By means of a natural gas pipe network which is widely distributed, the SOFC power generation system can be integrated into a distributed power station which takes natural gas as a raw material in a large scale, so that the power demand of buildings, plants, communities and the like is met, and the commercial prospect is good.
In the prior art, a solid oxide fuel cell generally uses natural gas as a raw material, and generates gas such as hydrogen, carbon monoxide gas and the like through reforming, the gas enters an anode of a cell stack, cathode air enters a cathode of the cell stack, and under a certain condition, the anode gas and the cathode gas react to generate water and generate electricity. To accomplish these processes, various kit components such as a reformer, a start-up burner, an anode tailgas burner, a heat exchanger, etc. are required. The components need to be well combined to form an organic whole so that the flow of material and energy flows can be performed. For example, CN106784940A discloses a solid oxide fuel cell power generation system, which includes a hot zone, a reformer, a start-up burner, an anode tail gas burner, a mixer, and a heat exchange component, wherein the hot zone includes a stack array and corresponding gas distribution pipelines, the reformer, the heat exchange component and the hot zone are separately disposed and connected to each other through pipelines, the heat exchange component includes a reforming feed preheater, an air primary preheater, an air secondary preheater, a gasifier and a condenser, and a reforming reserved air inlet is disposed on the mixer. The invention separately sets each main component instead of concentrating in the hot area, reduces the difficulty of combining each component, is convenient for overall layout, reduces the possibility of mutual cross influence, and is convenient for each component to stably exert the function; the solid oxide fuel cell power generation system has the advantages of reasonable structural layout, convenience in assembly, convenience in disassembly, appropriate layout, stable function, reasonable heat exchange and the like, and is suitable for building a single hundred kilowatt-level solid oxide fuel cell power generation system.
However, the conventional solid oxide fuel cell power generation system mainly uses natural gas as a raw material, and requires a methane reformer or the like, and thus cannot be applied to an inexpensive synthesis gas.
Disclosure of Invention
The invention aims to solve the problem of low power generation efficiency of a solid oxide fuel cell power generation system used for synthesis gas in the prior art, and provides a synthesis gas fuel cell power generation system and a synthesis gas fuel cell power generation method.
In order to achieve the above object, a first aspect of the present invention provides a synthesis gas fuel cell power generation system, which includes a synthesis gas source, a heat exchange device, a fuel cell, and a combustion device, wherein the synthesis gas source is used for providing synthesis gas; the heat exchange device comprises a heat exchange conversion device, a first heat exchange device and a second heat exchange device; the heat exchange conversion device is connected with the anode of the fuel cell through a first heat exchange device; the cathode of the fuel cell is connected with the combustion device; the combustion device is connected with the cathode of the fuel cell through a first heat exchange device.
A second aspect of the invention provides a method of generating electricity from a syngas fuel cell, wherein the method comprises the steps of:
mixing synthesis gas provided by a synthesis gas source with steam, preheating the mixture to a first temperature by a heat exchange conversion device, and then carrying out water gas conversion reaction to prepare mixed fuel gas containing hydrogen and carbon monoxide;
the mixed fuel gas is heated to a second temperature by the first heat exchange device, enters the anode of the fuel cell, reacts with air which is heated by the second heat exchange device and enters the cathode of the fuel cell, and generates power to respectively generate anode tail gas and cathode tail gas;
and the cathode tail gas enters a combustion device to be combusted to generate combustion tail gas.
Through the technical scheme, the synthesis gas fuel cell power generation system and the power generation method provided by the invention have the following beneficial effects:
the battery power generation system provided by the invention does not need cooling, condensation and dehydration, is directly mixed and combusted with high-temperature cathode air at a higher temperature, ensures the combustion stability, and simultaneously does not need to be additionally provided with a starting burner, thereby simplifying the system flow.
To achieve efficient syngas generation. The invention converts CO in the synthesis gas into H through water gas shift reaction 2 Meanwhile, carbon dioxide is separated and then is sent into the high-temperature fuel cell for power generation, so that the hydrogen partial pressure in the power generation process of the synthetic gas fuel cell is improved, the heat productivity in the power generation process of the synthetic gas fuel cell is reduced, the system heat is reasonably utilized, and the power generation efficiency of the fuel cell is improved.
Drawings
FIG. 1 is a syngas fuel cell power generation system according to the present invention.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and these ranges or values should be understood to encompass values close to these ranges or values. For numerical ranges, each range between its endpoints and individual point values, and each individual point value can be combined with each other to give one or more new numerical ranges, and such numerical ranges should be construed as specifically disclosed herein.
The invention provides a synthesis gas fuel cell power generation system, which comprises a synthesis gas source, a heat exchange device, a fuel cell and a combustion device, wherein the synthesis gas source is used for providing synthesis gas; the heat exchange device comprises a heat exchange conversion device, a first heat exchange device and a second heat exchange device; the heat exchange conversion device is connected with the anode of the fuel cell through a first heat exchange device; the cathode of the fuel cell is connected with the combustion device; the combustion device is connected with the cathode of the fuel cell through a second heat exchange device.
In the invention, the inventor researches and discovers that because the carbon-hydrogen ratio in the synthesis gas is far larger than that of the natural gas, the heat generated in the power generation process of the solid oxide fuel cell is higher than that of the natural gas by more than 50%, so that the power generation efficiency of the solid oxide fuel cell system taking the natural gas as the raw material gas is low when the solid oxide fuel cell system is directly applied to the synthesis gas.
The invention takes the synthesis gas as raw material gas, improves the solid oxide fuel cell system and provides the solid oxide fuel cell system suitable for the synthesis gas. In the solid oxide fuel cell system provided by the invention, a starting burner is not required to be additionally arranged, and the flow of the system is greatly simplified.
According to the invention, the heat exchange device further comprises a third heat exchange device which is respectively connected with the second heat exchange device and the heat exchange conversion device and used for supplying low-pressure steam to the heat exchange conversion device.
According to the invention, the heat exchange conversion device is internally provided with a conversion reaction catalyst for converting carbon monoxide in the synthesis gas into hydrogen.
Because the shift reaction of the synthesis gas can generate a large amount of heat, the invention carries out the shift reaction in the heat exchange shift device before the synthesis gas enters the anode of the fuel cell, and releases the heat generated by the shift reaction of the synthesis gas outside the fuel cell in advance, thereby obviously reducing the heat release of the fuel cell, simultaneously reducing the air input of the cathode of the fuel cell and obviously improving the power generation power of the fuel cell.
In the invention, the synthesis gas is subjected to water gas shift reaction to convert CO in the synthesis gas into H 2 And meanwhile, the heat generated by the reaction is utilized to further realize the heating treatment of the gas, and compared with the prior art, the load and the cost of a heat exchange device in the synthesis gas fuel cell power generation system are reduced.
According to the invention, the system further comprises CO 2 A separator connected with the heat exchange conversion device and the first heat exchange device respectively for reducing CO in the anode feed gas 2 The content of (a).
According to the invention, the third heat exchange device is a steam generator.
A second aspect of the invention provides a method of generating electricity from a syngas fuel cell, wherein the method comprises the steps of:
mixing synthetic gas provided by a synthetic gas source with steam, preheating the mixture to a first temperature by a heat exchange conversion device, and carrying out water gas conversion reaction to prepare mixed fuel gas containing hydrogen and carbon monoxide;
the mixed fuel gas is heated to a second temperature by the first heat exchange device, enters the anode of the fuel cell, reacts with air which is heated by the second heat exchange device and enters the cathode of the fuel cell, and generates power to respectively generate anode tail gas and cathode tail gas;
and the cathode tail gas enters a combustion device to be combusted to generate combustion tail gas.
In the fuel cell, the anode tail gas generated at the anode of the fuel cell by the chemical reaction of the mixed fuel gas and the air does not need to be subjected to the steps of cooling, condensation, dehydration and the like, and can be directly mixed and combusted with high-temperature cathode air at higher temperature, so that the combustion stability is ensured, and the system flow is greatly simplified.
In the invention, the water gas shift reaction is carried out on the synthesis gas to convert CO in the synthesis gas into H 2 The partial pressure of hydrogen in the anode gas entering the fuel cell is obviously improved, compared with the prior art, the power generation efficiency of the fuel cell can be improved, meanwhile, the risk of carbon deposition of the fuel cell is reduced, and the service life of the fuel cell is further prolonged.
According to the invention, the anode tail gas sequentially enters the first heat exchange device and the heat exchange conversion device to be used for heating the mixed fuel gas and the synthesis gas, and then enters the combustion device to be combusted.
According to the invention, the combustion tail gas enters the second heat exchange device and the third heat exchange device in sequence to heat air and water so as to obtain high-temperature air and water vapor.
According to the invention, the steam is mixed with the synthesis gas and then enters the heat conversion device.
According to the present invention, the mixed fuel gas further contains carbon dioxide.
According to the invention, the method further comprises passing the mixed fuel gas throughOver CO 2 A separator to remove carbon dioxide from the mixed fuel gas.
In the invention, the amount of carbon dioxide entering the anode of the fuel cell is strictly controlled through the step of removing the carbon dioxide in the mixed fuel gas, and researches show that when the molar content of the carbon dioxide in the mixed fuel gas is less than 30%, the power generation efficiency of the carbon dioxide to the fuel cell can be obviously reduced, the risk of carbon deposition of the fuel cell can be obviously reduced, and the service life of the fuel cell is prolonged.
Further, the molar content of carbon dioxide in the mixed fuel gas is less than 15%.
According to the invention, the first temperature is 100-400 ℃, preferably 200-300 ℃;
according to the invention, the second temperature is 500-800 ℃, preferably 600-700 ℃;
according to the invention, the temperature of the anode tail gas is 600-900 ℃, preferably 700-800 ℃;
according to the invention, the temperature of the cathode tail gas is 600-900 ℃, preferably 700-800 ℃;
according to the invention, the working temperature of the fuel cell is 500-900 ℃, preferably 600-800 ℃;
according to the invention, the operating pressure of the fuel cell is between 0.05 and 0.5MPa, preferably between 0.1 and 0.2 MPa.
According to the invention, the molar ratio of hydrogen to carbon monoxide in the synthesis gas is between 0.2 and 6, preferably between 0.5 and 4.
According to the invention, the molar ratio of water vapor to CO is between 0.2 and 2.5, preferably between 0.5 and 1.5.
According to the invention, the temperature of the combustion tail gas is 700-1000 ℃, and preferably 800-900 ℃.
According to the invention, the temperature of the combustion tail gas is reduced to 400 ℃ below zero (100-.
Mode for carrying out the invention
Mixing synthesis gas provided by a synthesis gas source with steam, preheating the mixture to a first temperature by a heat exchange conversion device, and carrying out water gas conversion reaction to prepare mixed fuel gas containing hydrogen and carbon monoxide;
the mixed fuel gas is heated to a second temperature by the first heat exchange device, enters the anode of the fuel cell, and chemically reacts with air which is heated by the second heat exchange device and enters the cathode of the fuel cell to respectively generate anode tail gas containing carbon dioxide and water and cathode tail gas containing nitrogen and oxygen;
after the anode tail gas sequentially passes through the first heat exchange device and the heat exchange conversion device and is used for heating mixed fuel gas and synthesis gas, the tail gas enters the combustion device and is mixed with cathode tail gas from the cathode of the fuel cell for combustion;
combustion tail gas generated by combustion sequentially passes through the second heat exchange device and the third heat exchange device to be used for heating air and water so as to obtain high-temperature air and water vapor;
the high-temperature air enters the cathode of the fuel cell;
and the steam and the synthesis gas are mixed and then enter the heat exchange conversion device.
The present invention will be described in detail below by way of examples. In the following examples of the present invention, the following examples,
the battery power generation power parameter is measured by a battery voltage and battery current method;
the fuel utilization rate parameter is measured by a fuel flow and cell current method, and the specific calculation formula is as follows:
fuel utilization,% [ current (a) × 3600 ] number of cells of the stack]/[96485 × 2 electric stack inlet fuel flow (Nm) 3 /h)/0.0224]×100％。
The raw materials used in the examples and comparative examples are all commercially available products.
Example 1
In a set of MW th A staged syngas fuel cell power generation system is exemplified:
290Nm 3 synthesis gas (H)/H 2 Molar ratio to CO 1.68) to 103Nm 3 H steam mixing, wherein the molar ratio of the steam to the CO is 1: 1. Preheating to 220 ℃ by a heat exchange conversion device, carrying out water gas conversion reaction,70% conversion of CO to H 2 And the outlet temperature reaches 400 ℃ to obtain mixed fuel gas containing hydrogen and carbon monoxide, wherein the content of carbon dioxide in the mixed fuel gas is 20 percent, the mixed fuel gas is further preheated to 700 ℃ through a first heat exchange device and enters a solid oxide fuel cell for anode reaction, the fuel utilization rate is 85 percent, the power generation power is 550kW, the temperature of tail gas at the outlet of the anode is 800 ℃, the mixed fuel gas and the synthesis gas which sequentially pass through the first heat exchange device and a heat exchange conversion device and are used for heating the anode feeding mixture fuel gas and the synthesis gas are reduced to 450 ℃, the mixed fuel gas is sent into a gas burner to be mixed with the cathode tail gas (800 ℃) for combustion, the temperature of the combustion tail gas is controlled by fresh air, and the temperature of the cathode feeding air is heated (the flow rate is 5700Nm & lt/m & gt) 3 Heating to 700 deg.C, cooling to 300 deg.C, generating 0.5MPa steam by steam generator, supplying to anode, cooling to 200 deg.C, and discharging.
Example 2
The procedure is as in example 1, except that: the molar ratio of hydrogen to carbon monoxide in the synthesis gas was 0.5. The fuel utilization rate of the fuel cell was 80%, and the power generation power was 500 kW.
Example 3
The procedure is as in example 1, except that: the molar ratio of hydrogen to carbon monoxide in the synthesis gas was 3. The fuel utilization of the fuel cell was 90%, and the power generation power was 600 kW.
Example 4
The procedure is as in example 1, except that: the molar ratio of hydrogen to carbon monoxide in the synthesis gas was 0.2. The fuel utilization of the fuel cell was 70%, and the generated power was 450 kW.
Example 5
The procedure is as in example 1, except that: the molar ratio of water vapor to CO was 1.5. The fuel utilization of the fuel cell was 85%, and the power generation power was 530 kW.
Example 6
The procedure is as in example 1, except that: the molar ratio of water vapor to CO was 0.5, the fuel utilization of the fuel cell was 83%, and the power generation power was 520 kW.
Example 7
The procedure is as in example 1, except that: the molar ratio of water vapor to CO was 2.5. The fuel utilization of the fuel cell was 85%, and the generated power was 520 kW.
Example 8
The procedure is as in example 1, except that: the carbon dioxide content in the fuel mixed gas was 45%. The fuel utilization of the fuel cell was 65%, and the power generation power was 400 kW.
Example 9
The procedure is as in example 1, except that: in the first preheating device, the mixed fuel gas containing hydrogen and carbon monoxide obtained by the water gas shift reaction is subjected to CO 2 A separator to remove carbon dioxide from the mixed fuel gas. After the separation treatment, the content of carbon dioxide in the mixed fuel gas is 5%. The fuel utilization of the fuel cell was 90%, and the generated power was 600 kW.
Comparative example 1
The procedure is as in example 1, except that: the synthesis gas directly enters the anode of the fuel cell after secondary heating without carrying out water gas change reaction. The carbon dioxide content in the fuel mixed gas was 45%. The fuel utilization of the fuel cell was 65%, and the power generation power was 400 kW.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (13)
1. A synthesis gas fuel cell power generation system comprises a synthesis gas source, a heat exchange device, a fuel cell and a combustion device, wherein the synthesis gas source is used for providing synthesis gas; the heat exchange device comprises a heat exchange conversion device, a first heat exchange device and a second heat exchange device; the heat exchange conversion device is connected with the anode of the fuel cell through a first heat exchange device; the cathode of the fuel cell is connected with the combustion device; the combustion device is connected with the cathode of the fuel cell through a second heat exchange device;
in the system, a method of generating electricity using a syngas fuel cell includes the steps of: mixing synthesis gas provided by a synthesis gas source with steam, preheating the mixture to a first temperature by a heat exchange conversion device, and then carrying out water gas conversion reaction to prepare mixed fuel gas containing hydrogen and carbon monoxide;
the mixed fuel gas is heated to a second temperature by the first heat exchange device, enters the anode of the fuel cell, reacts with air which is heated by the second heat exchange device and enters the cathode of the fuel cell, and generates power to respectively generate anode tail gas and cathode tail gas;
the cathode tail gas enters a combustion device to be combusted to generate combustion tail gas;
wherein the molar ratio of hydrogen to carbon monoxide in the synthesis gas is in the range of 1.68 to 6;
the mixed fuel gas also comprises carbon dioxide, and the molar content of the carbon dioxide is less than 30%.
2. The syngas fuel cell power plant of claim 1, wherein the heat exchange means further comprises a third heat exchange means connected to the second heat exchange means and the heat exchange reformer means, respectively, for providing a low pressure steam feed to the heat exchange reformer means.
3. The syngas fuel cell power generation system of claim 2, wherein the heat exchange shift unit houses a shift reaction catalyst for converting carbon monoxide in the syngas to hydrogen;
the system further comprises CO 2 A separator connected with the heat exchange conversion device and the first heat exchange device respectively for reducing CO in the anode feed gas 2 The content of (a);
the third heat exchange device is a steam generator.
4. The system of claim 1, wherein the anode tail gas enters the first heat exchange device and the heat exchange conversion device in sequence for heating the mixed fuel gas and the synthesis gas, and then enters the combustion device for combustion.
5. The system of claim 2, wherein combustion exhaust gas generated by the combustion enters the second heat exchange device and the third heat exchange device in sequence for heating air and water to obtain high-temperature air and water vapor;
and/or the water vapor and the synthesis gas are mixed and then enter a heat exchange conversion device.
6. The system of claim 1 or 4, wherein the method further comprises passing the mixed fuel gas through CO 2 A separator to remove carbon dioxide from the mixed fuel gas.
7. The system of claim 1 or 4, wherein the molar content of carbon dioxide in the mixed fuel gas is less than 15%.
8. The system of claim 1 or 4, wherein the first temperature is 100-400 ℃;
and/or, the second temperature is 500-;
and/or the temperature of the anode tail gas is 600-900 ℃;
and/or the temperature of the cathode tail gas is 600-900 ℃;
and/or the working temperature of the fuel cell is 500-900 ℃;
and/or the working pressure of the fuel cell is 0.05-0.5 MPa.
9. The system of claim 1 or 4, wherein the first temperature is 200-300 ℃;
and/or, the second temperature is 600-700 ℃;
and/or the temperature of the anode tail gas is 700-800 ℃;
and/or the temperature of the cathode tail gas is 700-800 ℃;
and/or the working temperature of the fuel cell is 600-800 ℃;
and/or the working pressure of the fuel cell is 0.1-0.2 MPa.
10. The system of claim 1 or 4, wherein the molar ratio of water vapor to CO is 0.2-2.5.
11. The system of claim 1 or 4, wherein the molar ratio of water vapor to CO is from 0.5 to 1.5.
12. The system as claimed in claim 1 or 4, wherein the temperature of the combustion exhaust gas is 700-1000 ℃;
and/or after the combustion tail gas passes through the second heat exchange device, the temperature is reduced to 100-400 ℃.
13. System according to claim 1 or 4, wherein the temperature of the combustion exhaust gas is 800-900 ℃;
and/or after the combustion tail gas passes through the second heat exchange device, cooling to 200-300 ℃.
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| CN114639843A (en) * | 2022-03-09 | 2022-06-17 | 上海电力大学 | Fuel cell and double-gas turbine coupling system |
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