CN216213576U - Power generation system of molten carbonate fuel cell - Google Patents
Power generation system of molten carbonate fuel cell Download PDFInfo
- Publication number
- CN216213576U CN216213576U CN202122677466.3U CN202122677466U CN216213576U CN 216213576 U CN216213576 U CN 216213576U CN 202122677466 U CN202122677466 U CN 202122677466U CN 216213576 U CN216213576 U CN 216213576U
- Authority
- CN
- China
- Prior art keywords
- outlet
- heat exchanger
- inlet
- power generation
- cathode
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000010248 power generation Methods 0.000 title claims abstract description 101
- 239000000446 fuel Substances 0.000 title claims abstract description 45
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 title claims abstract description 39
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 42
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000001257 hydrogen Substances 0.000 claims abstract description 28
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 28
- 230000003197 catalytic effect Effects 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 23
- 239000007789 gas Substances 0.000 claims description 72
- 238000010521 absorption reaction Methods 0.000 claims description 56
- 238000003795 desorption Methods 0.000 claims description 52
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 52
- 239000007788 liquid Substances 0.000 claims description 50
- 239000003546 flue gas Substances 0.000 claims description 45
- 238000010992 reflux Methods 0.000 claims description 28
- 239000002904 solvent Substances 0.000 claims description 23
- 238000005262 decarbonization Methods 0.000 claims description 16
- 239000003245 coal Substances 0.000 claims description 6
- 238000005868 electrolysis reaction Methods 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 abstract description 12
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 2
- 230000007547 defect Effects 0.000 abstract 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 88
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 33
- 239000001569 carbon dioxide Substances 0.000 description 15
- 238000003860 storage Methods 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 238000007084 catalytic combustion reaction Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000003487 electrochemical reaction Methods 0.000 description 7
- 238000007906 compression Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 239000003792 electrolyte Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000006073 displacement reaction Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 238000011033 desalting Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000009919 sequestration Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- -1 Carbonate ions Chemical class 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000010349 cathodic reaction Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- 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
- Fuel Cell (AREA)
Abstract
The utility model provides a power generation system of a molten carbonate fuel cell, belongs to the field of low-carbon and carbon-emission-free power generation, and overcomes the defect of CO (carbon monoxide) in the power generation system in the prior art2The discharge amount of (2) is high. The power generation system of the molten carbonate fuel cell comprises a hydrogen production device and CO2Collection device and MCFC, a power generation unit and a catalytic combustor; the hydrogen production device comprises a power generation device and an electrolytic cell, wherein the electrolytic cell is provided with H2Outlet and O2An outlet, an anode inlet of the MCFC power generation unit and H of the electrolytic cell2Outlet connection, cathode inlet of which is connected to O of the electrolytic cell2An outlet and the CO2The air outlet of the trapping device is connected. The utility model realizes low-carbon emission power generation.
Description
Technical Field
The utility model belongs to the field of low-carbon and carbon-emission-free power generation, and particularly relates to a molten carbonate fuel cell power generation system for coupling hydrogen production and flue gas of a coal-fired power plant.
Background
The Molten Carbonate Fuel Cell (MCFC) is a high-temperature Fuel Cell working at about 650 ℃, has the advantages of no need of noble metal as a catalyst, wide Fuel source, low noise, nearly zero emission of pollutants, high power generation efficiency, long service life of more than 4 ten thousand hours, realization of combined heat and power supply and the like, is suitable for distributed power stations or fixed power stations of hundreds of kilowatts to megawatts, and has good development prospect.
The molten carbonate fuel cell operates at 650 deg.c, and the structure of MCFC can be divided into three parts, cathode, electrolyte and anode, where the electrolyte is molten carbonate. During operation, air and CO are introduced into the cathode2At the electrode of the cathode, a reaction occurs
Generating carbonate ions; the carbonate ions pass through the electrolyte to the anode electrode; at the anode electrode H2Electrochemically reacting with carbonate ions
Generation of H2O and CO2And is andat the same time, the electrons pass from the anode to the cathode through an external circuit, and perform an external electric work. As can be seen from the power generation principle of MCFC, MCFC will consume CO at the cathode when it works2Carbonate ions generated by the cathode can migrate to the anode to electrochemically react with the anode fuel to release CO2And generate electric energy, CO in MCFC2For reduction of greenhouse gases (mainly CO)2) The discharge of the waste water has important environmental protection significance.
Chinese patent CN112864438A discloses a high-temperature fuel cell coupled power generation system and method capable of realizing carbon dioxide capture, carbon-containing fuel participates in the reaction at the anode of a Solid Oxide Fuel Cell (SOFC) and a Molten Carbonate Fuel Cell (MCFC), the anode product enters the cathode reaction of the MCFC after catalytic combustion, and CO is enriched at the cathode outlet of the MCFC2. Patent CN108417876A discloses a high-temperature fuel cell coupled power generation system and method, which also adopts the Solid Oxide Fuel Cell (SOFC) and Molten Carbonate Fuel Cell (MCFC) power generation coupled mode to generate power and enrich CO as in patent CN112864438A2. The two methods both adopt carbon-containing fuel, consume fossil energy and bring CO2The problem of emissions.
Therefore, in the context of carbon neutralization, there is a great need to investigate how to reduce CO2The power generation system with low carbon and even no carbon emission is provided.
SUMMERY OF THE UTILITY MODEL
Therefore, the technical problem to be solved by the present invention is to overcome the CO of the power generation system in the prior art2The emission is high, thereby providing a molten carbonate fuel cell power generation system which couples renewable energy sources for hydrogen production and flue gas of a coal-fired power plant.
From the principle of electricity generation of molten carbonate fuel cells, MCFC has the capacity to absorb H2、O2And CO2And from CO2From the flow footprint of CO2Can be enriched at the anode of the MCFC by electrochemical reaction from the cathode, and can realize CO2The trapping function of (1). Therefore, CO in the flue gas of the existing coal-fired power plant can be fully utilized2And can be regeneratedH generated by electric energy hydrogen production during wind and light abandoning of energy2And O2Integrating these resources with an MCFC power generation system, generating electrical energy and performing CO2To achieve CO concentration and capture2Low carbon emission.
Therefore, the utility model provides the following technical scheme.
The utility model discloses a power generation system of a molten carbonate fuel cell, which comprises a hydrogen production device and CO2The hydrogen production device comprises a power generation device and an electrolytic cell, wherein the electrolytic cell is provided with H2Outlet and O2Outlet, CO2The trapping device is used for trapping CO in the flue gas2An anode inlet of the MCFC power generation unit and H of the electrolytic cell2Outlet connection, cathode inlet of which is connected to O of the electrolytic cell2An outlet and the CO2The air outlet of the trapping device is connected.
Further, the hydrogen production device is a renewable energy hydrogen production device; and/or the flue gas is flue gas generated by coal burning.
Further, said CO2The trapping device comprises a fan, an absorption tower, a lean-rich heat exchanger and a desorption tower, wherein the air inlet of the absorption tower is connected with the fan used for conveying flue gas into the absorption tower, and the liquid inlet of the absorption tower is used for inputting CO in the absorbed flue gas into the absorption tower2The lean-rich heat exchanger of the decarbonization solvent is connected; the absorption tower is characterized in that a rich solution outlet of the absorption tower is connected with a cold end inlet of the lean-rich heat exchanger through a rich solution pump, a cold end outlet of the lean-rich heat exchanger is connected with a rich solution inlet of the desorption tower, a lean solution outlet of the desorption tower is connected with a hot end inlet of the lean-rich heat exchanger through a lean solution pump, and a hot end outlet of the lean-rich heat exchanger is connected with a liquid inlet of the absorption tower.
Further, a condenser and a reflux tank are connected between the desorption tower and the MCFC power generation unit;
the gas outlet of the desorption tower is connected with the inlet of the reflux tank through the condenser, the liquid outlet of the reflux tank is connected with the reflux inlet of the desorption tower, and the gas outlet of the reflux tank is connected with the MCFC power generation unit.
Further, said CO2The trapping device also comprises a reboiler, a gas-water separator and a desalted water tank, and the catalytic combustor is also connected with a combustor heat exchanger;
a liquid outlet of the gas-water separator, a desalted water tank, a cold end inlet of the burner heat exchanger, a cold end outlet of the burner heat exchanger, a hot end inlet of the reboiler, a hot end outlet of the reboiler and an inlet of the gas-water separator are sequentially connected; preferably, the gas outlet of the gas-water separator is connected with a steam pipeline between the outlet of the cold end of the burner heat exchanger and the inlet of the hot end of the reboiler.
Further, the device also comprises an anode heat exchanger and a cathode heat exchanger; h of the electrolytic cell2The outlet is connected with the anode inlet through the cold end inlet of the anode heat exchanger and the cold end outlet of the anode heat exchanger in sequence, and the O of the electrolytic cell2An outlet and the CO2The air outlets of the trapping devices are connected with the cold end inlet of the cathode heat exchanger, and the cold end outlet of the cathode heat exchanger is connected with the cathode inlet;
the anode outlet is connected with the inlet of the catalytic combustor sequentially through the hot end inlet of the anode heat exchanger and the hot end outlet of the anode heat exchanger; and the cathode outlet is connected with the inlet of the catalytic combustor sequentially through the hot end inlet of the cathode heat exchanger and the hot end outlet of the cathode heat exchanger.
Further, a direct current-direct current power supply converter is arranged between the power generation device and the electrolytic cell.
Further, the outlet of the catalytic combustor is also connected with CO2Compression liquefaction plant, preferably catalytic combustor outlet with CO through combustor heat exchanger2The compression liquefaction device is connected.
The technical scheme of the utility model has the following advantages:
1. the power generation system of the molten carbonate fuel cell comprises a hydrogen production device and CO2The hydrogen production device comprises a power generation device and an electrolytic cell, wherein the electrolytic cell is provided with H2Outlet and O2An outlet, an anode inlet of the MCFC power generation unit and H of the electrolytic cell2Outlet connection, cathode inlet of which is connected to O of the electrolytic cell2An outlet and the CO2The air outlet of the trapping device is connected.
The carbon dioxide in the flue gas is captured, so that carbon dioxide gas with higher concentration can be obtained, the gas can be directly input into the cathode of the MCFC power generation unit together with oxygen obtained by the hydrogen production device to generate electrochemical reaction, and the CO in the flue gas is avoided2Atmospheric pollution and greenhouse effect caused by direct emission, and utilization of carbon dioxide gas, thereby remarkably reducing CO2Discharge, improve the energy utilization rate and reduce the energy consumption.
The research of the prior art finds that CO in the desulfurized flue gas of the coal-fired power plant2The concentration is very low, only 11-12%, if the desulfurized flue gas of the coal-fired power plant is directly introduced into the molten carbonate fuel cell, the concentration of the reaction gas in the cathode is too low, the generation of carbonate is influenced, the efficiency of the cell is influenced, and the generated cathode tail gas contains a large amount of N2Waste a large amount of heat energy, resulting in CO in the tail gas2Difficult to separate and can only be emptied. Therefore, the utility model leads CO to enter the MCFC power generation unit before the desulfurized flue gas of the coal-fired power plant enters the MCFC power generation unit2Trapping and concentrating to reduce N2The influence on the subsequent battery and system performance realizes the reduction of CO2The purpose of the discharge amount. The utility model passes CO2The concentration of carbon dioxide gas obtained after the capture device captures the flue gas is high, cathode tail gas generated by electrochemical reaction mainly comprises carbon dioxide gas and water, carbon dioxide in the cathode tail gas is convenient to separate, and a compression liquefying device can be adopted to generate liquid CO2Oil displacement or geological sequestration is carried out, thereby reducing CO2And (5) discharging.
2. The molten carbonate fuel cell power generation system provided by the utility model has the advantages that the hydrogen production device is a renewable energy hydrogen production device, and the hydrogen is produced by electrolyzing the electric energy generated by renewable energy power generation devices such as wind power photovoltaic devices and the like to produce H2And O2Renewable energy sources such as light energy, wind energy and the like in the nature can be converted into electric energy. Water electrolysis into H by adopting electric energy during wind and light abandoning period2And O2Instead of the naturalCarbon emission caused by electricity generation of carbon-containing fuels such as gas, coal gas and methane in the MCFC is solved, and storage and application of renewable energy sources are realized.
The overall reaction of a molten carbonate fuel cell is:
in the formula, CO2，cCO as cathode2，CO2，aCO as anode2. Anodic reaction requires H2The cathodic reaction requires O2And CO2，H2And CO2Is in a 1:1 relationship, H2And O2Is in a 2:1 relationship. H obtained by electrolytic hydrogen production2And O2In a molar ratio exactly corresponding to the MCFC anode H2And cathode O2Does not require additional H2And O2And (4) source.
CO from flue gas emissions from coal combustion2To achieve the purposes of trapping, concentrating and recovering, and finally achieving CO2The utility model achieves the aim of hydrogen energy storage on one hand and CO on the other hand2Concentrating and recovering to achieve the purpose of carbon emission reduction.
3. The molten carbonate fuel cell power generation system provided by the utility model is CO2The trapping device comprises a fan, an absorption tower, a lean-rich heat exchanger and a desorption tower, wherein the air inlet of the absorption tower is connected with the fan used for conveying flue gas into the absorption tower, and the liquid inlet of the absorption tower is used for inputting CO in the absorbed flue gas into the absorption tower2The lean-rich heat exchanger of the decarbonization solvent is connected; the absorption tower is characterized in that a rich solution outlet of the absorption tower is connected with a cold end inlet of the lean-rich heat exchanger through a rich solution pump, a cold end outlet of the lean-rich heat exchanger is connected with a rich solution inlet of the desorption tower, a lean solution outlet of the desorption tower is connected with a hot end inlet of the lean-rich heat exchanger through a lean solution pump, and a hot end outlet of the lean-rich heat exchanger is connected with a liquid inlet of the absorption tower.
Flue gas from factories such as coal-fired power plants and the like is conveyed into an absorption tower through a fan, carbon dioxide in the flue gas is absorbed by a decarburization solvent in the absorption tower to obtain a rich solution, the rich solution enters a desorption tower after heat exchange through a lean-rich heat exchanger, and the temperature is raised in the desorption tower for desorption to release the carbon dioxide, so that the capture of the carbon dioxide is realized.
Preferably, a booster fan is adopted to boost the pressure of the desulfurization flue gas of the coal-fired power plant, so that the desulfurization flue gas is fully contacted with the decarbonization solvent in the absorption tower. The absorption tower can remove CO in the desulfurized flue gas2Absorbing CO with decarbonizing solvent2The solution becomes rich liquid, and other gas components which are not absorbed are discharged to the atmosphere from a gas outlet at the top of the absorption tower; the rich liquid pump can convey rich liquid to a rich liquid inlet at the upper part of the desorption tower; the lean-rich liquid heat exchanger can heat the rich liquid from the absorption tower and reduce the temperature of the lean liquid from the desorption tower to the inlet temperature of the absorption tower.
4. The utility model provides a power generation system of a molten carbonate fuel cell, wherein a condenser and a reflux tank are also connected between a desorption tower and an MCFC power generation unit; the top gas outlet of the desorption tower is connected with the inlet of the reflux tank through a condenser, the liquid outlet of the reflux tank is sequentially connected with the reflux inlet at the upper part of the desorption tower, and the gas outlet of the reflux tank is connected with the MCFC power generation unit.
The condenser can desorb CO2Condensing the decarbonization solvent carried by the gas into liquid and flowing into a reflux tank; the reflux tank returns the condensed and recovered decarbonization solvent to the desorption tower; the decarbonization solvent is circulated in the absorption tower and the desorption tower and is used for continuous power generation, the energy utilization rate is improved, and the system efficiency is improved.
5. The molten carbonate fuel cell power generation system of the present invention, the CO2The trapping device also comprises a reboiler, a gas-water separator and a desalted water tank, and the catalytic combustor is also connected with a combustor heat exchanger; a liquid outlet of the gas-water separator, a desalted water tank, a cold end inlet of the burner heat exchanger, a cold end outlet of the burner heat exchanger, a hot end inlet of the reboiler, a hot end outlet of the reboiler and an inlet of the gas-water separator are sequentially connected; preferably, the gas outlet of the gas-water separator is connected with the outlet of the cold end of the burner heat exchanger and reboiledThe steam pipeline between the hot end inlets of the devices is connected.
The gas-water separator can condense the water in the steam after heat exchange into liquid and flow into the desalting water tank; the desalted water tank has the function of storing desalted water; the steam generated is heated by the reboiler as CO2CO in rich liquid in trapping process2The heat source required by desorption reduces the consumption of steam and improves the efficiency of the system. And the combustor heat exchanger recovers waste heat of high-temperature gas generated by catalytic combustion of MCFC cathode and anode tail gases, and the temperature of the high-temperature gas is reduced to below 120 ℃.
6. The power generation system of the molten carbonate fuel cell comprises an anode heat exchanger and a cathode heat exchanger, wherein H of the electrolytic cell2An outlet is connected with the anode inlet sequentially through the cold end inlet of the anode heat exchanger and the cold end outlet of the anode heat exchanger, and a gas outlet of the gas mixer is connected with the cathode inlet sequentially through the cold end inlet of the cathode heat exchanger and the cold end outlet of the cathode heat exchanger; the anode outlet is connected with the inlet of the catalytic combustor sequentially through the hot end inlet of the anode heat exchanger and the hot end outlet of the anode heat exchanger; and the cathode outlet is connected with the inlet of the catalytic combustor sequentially through the hot end inlet of the cathode heat exchanger and the hot end outlet of the cathode heat exchanger. The efficiency of the system is improved while the energy consumption is reduced.
The anode heat exchanger can be fed with H into the anode2Heating to the temperature of 400-500 ℃ at the inlet of the MCFC anode, and reducing the temperature of the high-temperature tail gas at the outlet of the MCFC anode to 100-120 ℃. The cathode heat exchanger being able to pass O in the cathode2And CO2Heating to the temperature of 400-500 ℃ at the cathode inlet of the MCFC, and reducing the temperature of the high-temperature tail gas at the cathode outlet to 100-120 ℃.
7. The power generation system of the molten carbonate fuel cell provided by the utility model also comprises a direct current-direct current power converter between the power generation device and the electrolytic cell, wherein the direct current-direct current power converter can convert direct current generated by the renewable energy power generation device into direct current with stable output.
The power generation system of the molten carbonate fuel cell also comprises a direct current power inverter, wherein the direct current power inverter can convert direct current generated by the MCFC power generation unit into alternating current and transmit the alternating current to a power grid or a user.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a process flow diagram of a specific example of a molten carbonate fuel cell power generation system in example 1 of the present invention.
Reference numerals:
1-power generation device, 2-DC power converter, 3-electrolytic cell, 4-H2Storage tank, 5-O2Storage tank, 61-H2Pressure reducing valve, 62-O2Pressure reducing valve, 63-CO2The system comprises a pressure reducing valve, a 7-blower, an 8-absorption tower, a 9-rich liquid pump, a 10-lean rich liquid heat exchanger, an 11-lean liquid pump, a 12-desorption tower, a 13-condenser, a 14-reflux tank, a 15-reboiler, a 16-gas-water separator, a 17-desalted water tank, a 18-desalted water pump, a 19-gas mixer, a 20-anode heat exchanger, a 21-MCFC power generation unit, a 22-direct current power inverter, a 23-cathode heat exchanger, a 24-catalytic combustor and a 25-combustor heat exchanger.
Detailed Description
The following examples are provided to further understand the present invention, not to limit the scope of the present invention, but to provide the best mode, not to limit the content and the protection scope of the present invention, and any product similar or similar to the present invention, which is obtained by combining the present invention with other prior art features, falls within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In addition, the technical features involved in the different embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
Example 1
A molten carbonate fuel cell power generation system, as shown in FIG. 1, comprises a hydrogen production device and CO2A trapping device, an MCFC power generation unit 21 and a catalytic burner 24, wherein the hydrogen production device comprises a power generation device 1 and an electrolytic cell 3, and H is arranged on the electrolytic cell 32Outlet and O2Outlet, CO2The trapping device is used for trapping CO in the flue gas2Inlet of anode of MCFC power generation unit 21 and H of electrolytic cell 32Outlet connection, cathode inlet of which is connected to O of the electrolytic cell 32Outlet and CO2The air outlet of the trapping device is connected. The power generation device 1 provides electric energy for the electrolytic cell 3, and water is electrolyzed in the electrolytic cell 3 to prepare H2And O2，H2The electrochemical reaction occurs in the anode of the MCFC power generation cell 21. O is2And CO2CO trapped by the trap2And the cathode is led into the MCFC power generation unit 21 to generate electrochemical reaction.
In order to further reduce carbon emission, the hydrogen production device is an existing renewable energy hydrogen production device, and the flue gas is flue gas generated by coal. Specifically, the power generation device 1 is a renewable energy power generation device, and optionally, the renewable energy power generation device is an existing photovoltaic power generation device or wind energy power generation device.
In particular, CO2The trapping device comprises a fan 7, an absorption tower 8, a lean-rich heat exchanger 10 and a desorption tower 12, wherein the air inlet of the absorption tower 8 is connected with the fan 7 used for conveying flue gas into the absorption tower 8, the liquid inlet of the absorption tower 8 is used for inputting CO in the absorbed flue gas into the absorption tower 82The lean-rich heat exchanger 10 of the decarbonization solvent is connected; a rich liquid outlet of the absorption tower 8 is connected with a cold end inlet of the lean-rich heat exchanger 10 through a rich liquid pump 9, a cold end outlet of the lean-rich heat exchanger 10 is connected with a rich liquid inlet of the desorption tower 12, a lean liquid outlet of the desorption tower 12 is connected with a hot end inlet of the lean-rich heat exchanger 10 through a lean liquid pump 11, and a hot end outlet of the lean-rich heat exchanger 10 is connected with a liquid inlet of the absorption tower 8. Specifically, an air inlet of the absorption tower 8 is arranged at the lower part of the absorption tower 8, a liquid inlet is arranged at the upper part of the absorption tower 8, a rich liquid outlet is arranged at the bottom of the absorption tower 8, and the top of the absorption tower 8 is also provided with a device for discharging decarbonized solvent to remove CO2The gas outlet of (3). A rich liquid inlet of the desorption tower 12 is arranged at the upper part of the desorption tower 12, and a lean liquid outlet is arranged at the bottom of the desorption tower 12.
The fan 7 conveys the flue gas into the absorption tower 8, the carbon dioxide in the flue gas is absorbed by the decarbonization solvent in the absorption tower 8 to obtain a rich solution, the rich solution enters the desorption tower 12 after heat exchange through the lean-rich heat exchanger 10, the rich solution after temperature rise is desorbed in the desorption tower 12 to release the carbon dioxide, thereby realizing the capture of the carbon dioxide and obtaining the carbon dioxide gas with higher concentration, the gas can be directly input into the cathode of the MCFC power generation unit 21 together with the oxygen obtained by the hydrogen production device to generate electrochemical reaction, and the CO in the flue gas is avoided2Atmospheric pollution and greenhouse effect caused by direct emission, and utilization of carbon dioxide gas, thereby remarkably reducing CO2Discharge, improve the energy utilization rate and reduce the energy consumption.
Preferably, the fan 7 is a booster fan, and the booster fan can boost the pressure of the desulfurization flue gas of the coal-fired power plant, so that the desulfurization flue gas is fully contacted with the decarburization solvent in the absorption tower 8.
In order to remove unreacted H in cathode and anode tail gases of the MCFC power generation unit 212And O2The cathode outlet and the anode outlet of the MCFC power generation unit 21 are both connected to the catalytic combustor 24. O not reacted in the cathode2With CO2Mixing the gas with H from the anode outlet2、H2O、CO2The mixed gas enters a catalytic combustor 24 for catalytic combustion, and unreacted H in tail gas at the outlet of the anode2And unreacted O in the cathode outlet tail gas2The molar ratio is 2:1, H2And O2All react to form H2O, without introducing additional H2Or O2。
For removing desorbed CO2Gas-borne decarbonizing solvent to increase the CO fed to the cathode of the MCFC power generation unit 212A condenser 13 and a reflux drum 14 are connected between the desorption tower 12 and the MCFC power generation unit 21. Wherein, the gas outlet of the desorption tower 12 is connected with the inlet of the reflux tank 14 through the condenser 13, the liquid outlet of the reflux tank 14 is connected with the reflux liquid inlet of the desorption tower 12, the gas outlet of the reflux tank 14 is connected with the MCFC power generation unit 21, and is specifically connected with the cathode inlet of the MCFC power generation unit 21. Specifically, the gas outlet of the desorption tower 12 is arranged at the top of the desorption tower 12, and the reflux inlet is arranged at the upper part of the desorption tower 12. The condenser 13 is capable of desorbing CO2The decarbonizing solvent carried by the gas is condensed into liquid and flows into the reflux tank 14; the reflux drum 14 returns the condensed and recovered decarbonization solvent to the desorption tower 12; the decarbonization solvent is circulated in the absorption tower 8 and the desorption tower 12 for continuous power generation, so that the energy utilization rate is improved, and the system efficiency is improved.
In order to further increase the CO in the desorption tower 122To reduce energy consumption, to increase system efficiency, CO2The trapping device also comprises a reboiler 15, a gas-water separator 16 and a desalted water tank 17, and the catalytic combustor 24 is also connected with a combustor heat exchanger 25; a decarbonization solvent outlet at the lower part of the desorption tower 12, a cold end inlet of a reboiler 15, a cold end outlet of the reboiler 15 and a decarbonization solvent inlet of the desorption tower 12 are sequentially connected. A liquid outlet of the gas-water separator 16, a desalted water tank 17, a cold end inlet of the combustor heat exchanger 25, a cold end outlet of the combustor heat exchanger 25, a hot end inlet of the reboiler 15, a hot end outlet of the reboiler 15 and an inlet of the gas-water separator 16 are connected in sequence; preferably, the gas outlet of the gas-water separator 16 is connected with a steam pipeline between the outlet of the cold end of the burner heat exchanger 25 and the inlet of the hot end of the reboiler 15. The gas-water separator 16 can condense the water in the steam after heat exchange into liquid and flow into the desalting water tank 17; the desalted water tank 17 has a function of storing desalted water; the desalted water is delivered to a burner heat exchanger 25 for heat exchange and temperature rise, and the generated steam is heated by a reboiler 15 and used as CO2CO in rich liquid in trapping process2Further desorbing the required heat source. The rich liquid is stripped in a stripper 12 to desorb part of the CO by stripping2Then enters a reboiler 15 to be heated so as to lead CO in the water to be2Further desorption is carried out. The burner heat exchanger 25 recovers the waste heat of the high-temperature gas generated by the MCFC cathode and anode tail gas catalytic combustion, and reduces the temperature of the high-temperature gas to below 120 ℃.
In order to enable the pressure of the desalted water to meet the application requirements of various distances or height differences between the desalted water tank 17 and the cold-end inlet of the burner heat exchanger 25, a desalted water pump 18 is further arranged between the desalted water tank 17 and the cold-end inlet of the burner heat exchanger 25.
In order to reduce energy consumption and improve system efficiency, the system also comprises an anode heat exchanger 20 and a cathode heat exchanger 23; h of the electrolytic cell 32The outlet is connected with the anode inlet through the cold end inlet of the anode heat exchanger 20 and the cold end outlet of the anode heat exchanger 20 in sequence, and the O of the electrolytic cell 32An outlet and the CO2The air outlets of the trapping devices are connected with the cold end inlet of the cathode heat exchanger 23, and the cold end outlet of the cathode heat exchanger 23 is connected with the cathode inlet; the anode outlet is connected with the inlet of the catalytic combustor 24 through the hot end inlet of the anode heat exchanger 20 and the hot end outlet of the anode heat exchanger 20 in sequence; the cathode outlet is connected with the inlet of the catalytic combustor 24 through the hot end inlet of the cathode heat exchanger 23 and the hot end outlet of the cathode heat exchanger 23 in sequence. Using the heat of the anode tail gas as H to be introduced into the anode2Heating, the anode heat exchanger 20 can be brought to H in the anode2Heating to the temperature of 400-500 ℃ at the inlet of the MCFC anode, and reducing the temperature of the high-temperature tail gas at the outlet of the MCFC anode to 100-120 ℃. The heat of the cathode tail gas is adopted as O to be introduced into the cathode2And CO2Heating, the cathode heat exchanger 23 being able to pass O in the cathode2And CO2Heating to the temperature of 400-500 ℃ at the cathode inlet of the MCFC, and reducing the temperature of the high-temperature tail gas at the cathode outlet to 100-120 ℃.
To add O to2And CO2Mixing is carried out before the cathode is introduced, and a gas mixer 19 is also included. O of the electrolytic cell 32An outlet and the CO2The gas outlets of the trapping devices are all connected with a gas mixer 19, the outlet of the gas mixer 19 is connected with the cathode inlet of the MCFC power generation unit 21, and O2And CO2Mixed uniformly in the gas mixer 19 and then introduced into the cathode of the MCFC power generation unit 21. Gas mixer 19 mixes CO2And O2And uniformly mixing to reach a molar ratio of 2: 1.
Further, a dc-dc power converter 2 is provided between the power generation apparatus 1 and the electrolytic cell 3. The dc-dc power converter 2 can convert the dc power generated by the power generation device 1 into a dc power of stable output.
Further, the power supply device also comprises a direct current power supply inverter 22, wherein the direct current power supply inverter 22 is electrically connected with the MCFC power generation unit 21 and can convert direct current generated by the MCFC power generation unit 21 into alternating current to be transmitted to a power grid or a user.
Further, the outlet of the catalytic combustor 24 is connected with CO2A compression liquefaction unit for compressing CO2And (4) oil displacement or texture sealing after compression and liquefaction. For convenience of CO2The tail gas at the outlet of the catalytic combustor 24 is cooled, and specifically, the outlet of the catalytic combustor 24 passes through a combustor heat exchanger 25 and CO2The compression liquefying device is connected, so that water in the tail gas can be conveniently removed after the temperature of the tail gas is reduced, and CO is improved2Purity, reduced consumption and waste of system energy.
In one embodiment of the utility model, the hydrogen plant further comprises H2Storage tank 4 and O2Storage tank 5, H2Outlet and O2The outlet is respectively connected with H2Storage tank 4 and O2Tank 5 is connected, H2The outlet of the storage tank 4 is provided with H2Pressure reducing valve 61, O2The outlet of the storage tank 5 is provided with O2A pressure relief valve 62. Electrolysis of water into H2And O2Into H2Storage tank 4 and O2Tank 5, through H2Pressure reducing valves 61 and O2 Pressure reducing valve 62 will discharge H2And O2To the use pressure of the MCFC power generation unit 21.
In one embodiment of the utility model, the gas outlet of the reflux drum 14 is provided with CO2A pressure reducing valve 63 for introducing CO2Is adjusted to the MCFC usage pressure.
As an alternative embodiment, the flue gas is a coal fired power plant flue gas, preferably a coal fired power plant desulphurised flue gas. In particular, the flue gas can be flue gas of a supercritical power plant, an ultra supercritical power plant or a natural gas combined cycle power plant.
Example 2
The embodiment provides a power generation method of a molten carbonate fuel cell power generation system, which adopts the molten carbonate fuel cell power generation system provided by the embodiment 1 to generate power, and specifically comprises the following steps:
direct current from a photovoltaic power generation hydrogen production device is converted into stable direct current through a direct current-direct current converter 2 and is led to an electrolytic cell 3, and water in the electrolytic cell 3 is electrolyzed into H with the pressure of 3MPa and the temperature of 40 DEG C2And O2And are respectively stored in H2Storage tank 4 and O2In the tank 5. Desulfurized flue gas from a coal-fired power plant with the temperature of 40 ℃ is boosted to 0.5MPa by a booster fan 7 and then is sent into an absorption tower, the flue gas flows from bottom to top, and CO in the flue gas flows from top to bottom2The decarbonized solvent ethanolamine solution is contacted and absorbed, and the unabsorbed gas is discharged into the atmosphere from the top of the absorption tower 8. Absorption of CO2The rich liquid is sent to a lean-rich liquid heat exchanger 10 from the bottom of an absorption tower 8 through a rich liquid pump 9, and is sent to a desorption tower 12 after absorbing heat and raising the temperature. CO desorbed at 97.5 deg.C2Cooling the product together with the steam in a condenser 13, separating and removing the decarbonization solvent in a reflux tank 14 to obtain the product CO with the purity of more than 99.5 percent (dry basis)2Gas, temperature 40 ℃. The decarbonization solvent separated by condensation is sent to a desorption tower 12 at 96 DEG CThe rich solution enters from a rich solution inlet at the middle upper part of the desorption tower 12, and partial CO is desorbed by stripping2Then enters a reboiler 15 at the temperature of 110 ℃ to ensure that CO in the liquid2Further desorbing to desorb CO2The lean solution at 110 deg.C flows out from the bottom of the desorption tower 12, and is heat exchanged by the lean and rich solution heat exchanger 10, the temperature is reduced to 40 deg.C, and is sent to the absorption tower 8 by the lean solution pump 11, and the decarbonization solvent circulates back and forth to form continuous absorption and desorption CO2The process of (1).
From H2H of tank 42Warp H2The pressure reducing valve 61 reduces the pressure to 0.2Mpa, sends the pressure to the anode heat exchanger 20, and enters the anode of the MCFC power generation unit 21 after the temperature is raised to 400 ℃; from CO2CO of the trap2And from O2O of tank 52Reducing pressure to 0.2Mpa, regulating CO2Flow rate of (1) and H2The flow rate is the same, and CO is adjusted2And O2After the molar ratio of (2) to (1), adding CO2And O2The mixture is introduced into a gas mixer 19 and is sent into a cathode heat exchanger 23 to be preheated to 400 ℃ and then enters the cathode of the MCFC power generation unit 21. H entering the anodes of the MCFC power generation units 21 respectively2And CO entering the cathode2And O2Electrochemical reactions occur in the MCFC power generation unit 21 to generate electric power and heat, and the generated direct current is converted into alternating current by the direct current power inverter 22 to be sent to the grid or the user.
The temperature of the tail gas at the anode outlet and the cathode outlet is 650 ℃, and the temperature is reduced to 120 ℃ after heat exchange is respectively carried out by the anode heat exchanger 20 and the cathode heat exchanger 23. At the cathode of the MCFC power generation unit 21, about 70% of CO2And O2Carbonate generated by the reaction, the carbonate moves to about 70% of H between the anode and the cathode in the electrolyte layer2Reaction to form H2O and CO2The anode tail gas contains 30% of unreacted H2And 70% CO from the cathode2The tail gas of the cathode of the MCFC power generation unit 21 contains 30% of unreacted CO2And O2. Unreacted H in cathode tail gas and anode tail gas of MCFC power generation unit 212、O2、CO2Enters the catalytic combustor 24 to recover the remaining small amount of H2Of catalytic combustion products containing only H2O and CO2Introducing catalytic combustion tail gas into a combustor heat exchanger 25 at the temperature of 1000 ℃, pressurizing normal-temperature desalted water to 0.9Mpa by a desalted water pump 18, sending the normal-temperature desalted water to the combustor heat exchanger 25 to recover heat and generate low-pressure steam of 0.8Mpa and 179 ℃, cooling the catalytic combustion tail gas to the normal temperature, and sending the catalytic combustion tail gas to CO2Compressing liquefaction plant to produce liquid CO2And performing oil displacement or geological sequestration.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications of the utility model may be made without departing from the spirit or scope of the utility model.
Claims (7)
1. A power generation system of a molten carbonate fuel cell is characterized by comprising a hydrogen production device and CO2The device comprises a trapping device, an MCFC power generation unit and a catalytic combustor;
the hydrogen production device comprises a power generation device and an electrolytic cell, wherein the electrolytic cell is provided with H2Outlet and O2An outlet; the CO is2The trapping device is used for trapping CO in the flue gas2(ii) a The anode inlet of the MCFC power generation unit and the H of the electrolytic cell2Outlet connection, cathode inlet of which is connected to O of the electrolytic cell2An outlet and the CO2The air outlet of the trapping device is connected.
2. The molten carbonate fuel cell power generation system of claim 1, wherein the hydrogen generation assembly is a renewable energy hydrogen generation assembly; and/or the flue gas is flue gas generated by coal burning.
3. The molten carbonate fuel cell power generation system of claim 1 or 2, wherein the CO is present in the fuel cell system2The trapping device comprises a fan, an absorption tower, a lean-rich heat exchanger and a desorption tower, wherein an air inlet of the absorption tower and the fan used for conveying flue gas into the absorption towerThe liquid inlet of the absorption tower is connected with a liquid inlet used for inputting CO in the absorption flue gas to the absorption tower2The lean-rich heat exchanger of the decarbonization solvent is connected; the absorption tower is characterized in that a rich solution outlet of the absorption tower is connected with a cold end inlet of the lean-rich heat exchanger through a rich solution pump, a cold end outlet of the lean-rich heat exchanger is connected with a rich solution inlet of the desorption tower, a lean solution outlet of the desorption tower is connected with a hot end inlet of the lean-rich heat exchanger through a lean solution pump, and a hot end outlet of the lean-rich heat exchanger is connected with a liquid inlet of the absorption tower.
4. The molten carbonate fuel cell power generation system according to claim 3, wherein a condenser and a reflux drum are further connected between the desorption tower and the MCFC power generation unit;
the gas outlet of the desorption tower is connected with the inlet of the reflux tank through the condenser, the liquid outlet of the reflux tank is connected with the reflux inlet of the desorption tower, and the gas outlet of the reflux tank is connected with the MCFC power generation unit.
5. The molten carbonate fuel cell power generation system of claim 3, wherein the CO is present in the fuel cell system2The trapping device also comprises a reboiler, a gas-water separator and a desalted water tank, and the catalytic combustor is also connected with a combustor heat exchanger;
a liquid outlet of the gas-water separator, a desalted water tank, a cold end inlet of the burner heat exchanger, a cold end outlet of the burner heat exchanger, a hot end inlet of the reboiler, a hot end outlet of the reboiler and an inlet of the gas-water separator are sequentially connected; the gas outlet of the gas-water separator is connected with a steam pipeline between the outlet of the cold end of the burner heat exchanger and the inlet of the hot end of the reboiler.
6. The molten carbonate fuel cell power generation system of claim 3, further comprising an anode heat exchanger and a cathode heat exchanger; h of the electrolytic cell2The outlet is connected with the anode inlet through the cold end inlet of the anode heat exchanger and the cold end outlet of the anode heat exchanger in sequence, and the O of the electrolytic cell2An outlet and the CO2The air outlets of the trapping devices are all cooled with the cathode heat exchangerThe cold end outlet of the cathode heat exchanger is connected with the cathode inlet;
the anode outlet is connected with the inlet of the catalytic combustor sequentially through the hot end inlet of the anode heat exchanger and the hot end outlet of the anode heat exchanger; and the cathode outlet is connected with the inlet of the catalytic combustor sequentially through the hot end inlet of the cathode heat exchanger and the hot end outlet of the cathode heat exchanger.
7. The molten carbonate fuel cell power generation system according to claim 1 or 2, further comprising a dc-dc power converter between the power generation means and the electrolysis cell.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122677466.3U CN216213576U (en) | 2021-11-03 | 2021-11-03 | Power generation system of molten carbonate fuel cell |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122677466.3U CN216213576U (en) | 2021-11-03 | 2021-11-03 | Power generation system of molten carbonate fuel cell |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216213576U true CN216213576U (en) | 2022-04-05 |
Family
ID=80902259
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122677466.3U Active CN216213576U (en) | 2021-11-03 | 2021-11-03 | Power generation system of molten carbonate fuel cell |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216213576U (en) |
-
2021
- 2021-11-03 CN CN202122677466.3U patent/CN216213576U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101427408B (en) | Integrated high efficiency fossil fuel power plant/fuel cell system with co2 emissions abatement | |
| CN109301283B (en) | With CO 2 Captured integrated gasification fuel cell system | |
| CN113350989A (en) | Carbon dioxide capture method and system for coal-fired power generation coupled with renewable energy power generation | |
| CN104196582B (en) | Based on CO in MCFC electrochemical process trapping IGCC system 2combined power system | |
| KR20160114632A (en) | Reformer-electrolyzer-purifier(rep) assembly for hydrogen production, systems incorporating same and method of producing hydrogen | |
| CN112864438B (en) | High-temperature fuel cell coupling power generation system and method capable of realizing carbon dioxide capture | |
| CN108321416A (en) | CO2The integral coal gasification fuel cell generation and method of near-zero release | |
| EP2719008A1 (en) | Fuel cell and reciprocating gas/diesel engine hybrid system | |
| CN116435559A (en) | Methanation of anode off-gas to enhance carbon dioxide capture | |
| CN209374564U (en) | A kind of integral coal gasification fuel cell system of band CO2 trapping | |
| CN115763883B (en) | Zero-carbon-emission solid oxide fuel cell power generation system integrated with oxygen permeable membrane | |
| CN109473702A (en) | A kind of solid oxide fuel cell exhaust treatment system and processing method | |
| KR20120014840A (en) | Combined power generation system of thermal power plants with co2 capture and storage equipments and molten carbonate fuel cell power plants with hydrocarbon generation equipments | |
| CN109659590A (en) | A kind of integral coal gasification solid oxide fuel cell power generating system and method | |
| CN113921863A (en) | Power generation system and method for molten carbonate fuel cell | |
| CN114526158B (en) | Energy and substance conversion system and method based on carbon dioxide hydrogenation | |
| CN216213576U (en) | Power generation system of molten carbonate fuel cell | |
| JP2004171802A (en) | Fuel cell system | |
| CN214411263U (en) | Zero-carbon-emission distributed energy supply system | |
| CN115354345A (en) | Photovoltaic photo-thermal coupling co-electrolysis combined garbage power generation comprehensive energy system and process method thereof | |
| CN116262614A (en) | Carbon-based product preparation system and method for preparing carbon-based product | |
| CN110661014B (en) | Efficient low-concentration gas power generation system and control method thereof | |
| CN109638331B (en) | Fuel cell hybrid power generation system based on methanol | |
| CN207538871U (en) | A kind of near-zero release coal gasification power generation system with pollutant catabolic gene | |
| CN113594522B (en) | Molten carbonate fuel cell power generation system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |